JP7663168B2 - Method for cleaning instruments, raw liquid treatment device, and method for operating raw liquid treatment device - Google Patents

Description

The present invention relates to a method for cleaning instruments, a raw liquid treatment device, and a method for operating the raw liquid treatment device. More specifically, the present invention relates to a raw liquid treatment device and a method for operating the raw liquid treatment device that obtains a treatment liquid to be administered intravenously by filtering or concentrating raw liquids such as pleural and abdominal fluids accumulated in cancerous pleural peritonitis, liver cirrhosis, etc., and waste plasma from plasma exchange therapy, and also to a method for cleaning instruments used in the raw liquid treatment device and the raw liquid treatment device.

In cases of cancerous pleural and peritoneal effusion, liver cirrhosis, etc., pleural and ascites fluid may accumulate in the thoracic and abdominal cavities, causing problems such as the fluid compressing the surrounding organs. To alleviate such problems, the pleural and ascites fluid may be drained by puncture.

On the other hand, pleural and ascites fluids contain some or all of the plasma components that have leaked out of the blood, and this plasma contains major proteins (such as albumin and globulin). Although the above symptoms can be improved by draining the pleural and ascites fluid, proteins and other components that are useful to the human body are lost along with the fluid. For this reason, it is necessary to replenish the lost components by administering albumin preparations, globulin preparations, etc. intravenously.

Although it is possible to replenish certain components by administering albumin preparations or globulin preparations intravenously, the preparations are expensive, leading to high treatment costs.
Furthermore, since certain lost components can only be supplied in limited amounts, problems such as malnutrition and susceptibility to infection may occur.

A treatment method known as Cell-free and Concentrated Ascites Reinfusion Therapy (CART) has been developed in which pleural or ascites fluid (hereinafter sometimes referred to as the original fluid) removed from the pleural or abdominal cavity is treated and then administered intravenously. With CART, most of the active components other than the cellular components contained in the pleural or ascites fluid can be returned to the patient's body, so components lost from the blood can be effectively supplied to the patient without being limited to specific components. Furthermore, even if the concentrated fluid is administered, the missing components can be supplemented with a preparation in the amount that is lacking, so the amount of albumin preparations and the like used can be minimized, and treatment costs can be reduced.

In CART, the treated fluid to be returned to the patient's body is produced by filtering and concentrating pleural fluid or ascites. In a treatment device that produces such treated fluid, raw fluid such as pleural fluid or ascites is supplied to a filter having a filtering member such as a hollow fiber membrane or a plate-shaped permeable membrane to separate the liquid components (hereinafter sometimes referred to as filtrate). The separated filtrate is passed through a concentrator to remove water from the filtrate, thereby obtaining a concentrated liquid from the filtrate, i.e., the treated fluid described above (see Patent Documents 1 and 2).

Patent No. 5062631 JP 2015-126763 A JP 2019-13487 A JP 2019-13488 A

As mentioned above, in CART, the raw liquid removed from the patient's body is treated and then returned to the patient's body. However, if the filter or concentrator becomes clogged, the raw liquid cannot be properly treated. Therefore, in order to unclog the filter or concentrator, it is necessary to properly clean the filter and concentrator.

In addition, the filter and concentrator are washed during the filtration and concentration process, but in order to prevent loss of the filtrate or concentrate in the circuit during washing, the filtrate or concentrate may be recovered before washing (see, for example, Patent Documents 3 and 4). In this case, the filtrate or concentrate is recovered by passing it through the concentrator, but if the concentrator is clogged, it may not be possible to properly recover the filtrate or concentrate.

In view of the above circumstances, an object of the present invention is to provide an equipment cleaning method capable of properly cleaning a filter or concentrator, an operating method for a stock solution treatment device, and a stock solution treatment device.
Another object of the present invention is to provide a method for operating a raw liquid treatment device and a raw liquid treatment device that can appropriately recover filtrate and concentrated liquid.

<Operation method of raw liquid treatment device>
The method of operating a raw liquid treatment device of the first invention is a method of operating an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus including a filter having a filtering member for filtering the raw liquid, a concentrator to which a filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated liquid, a raw liquid supply section for supplying the raw liquid to the filter, a liquid supply flow path communicating the raw liquid supply section with a raw liquid supply port of the filter, a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator, a concentrated liquid flow path connected to the concentrated liquid discharge port of the concentrator, and a flow path for supplying the concentrated liquid to the concentrator. The apparatus is equipped with a waste liquid flow path connected to a waste liquid outlet for discharging separated waste liquid, a liquid delivery unit for delivering liquid to each flow path, and a control unit for controlling the operation of the liquid delivery unit, and is characterized in that, before cleaning the filter, a gas or liquid is supplied to a space in the filter separated from the raw liquid supply port of the filter by the filtering member, and the filtrate and/or the concentrate in the apparatus is recovered while adjusting the flow rate of the concentrate flow path and/or the waste liquid flow path based on the pressure in the space separated from the waste liquid outlet by the moisture separating member in the concentrator or in the flow path connected to said space.
A method for operating a raw liquid treatment apparatus according to a second aspect of the present invention is a method for operating an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus comprising: a filter having a filtering member for filtering the raw liquid; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated liquid; a raw liquid supply section for supplying the raw liquid to the filter; a liquid supply flow path communicating the raw liquid supply section with a raw liquid supply port of the filter; a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator; a concentrated liquid flow path connected to the concentrated liquid discharge port of the concentrator; The apparatus is equipped with a waste liquid flow path connected to a waste liquid outlet for discharging liquid, a liquid delivery unit that delivers liquid to each flow path, and a control unit that controls the operation of the liquid delivery unit, and is characterized in that, before cleaning the filter, a gas or liquid is supplied to a space in the filter separated from the raw liquid supply port of the filter by the filtering member, and the filtrate and/or the concentrate in the apparatus are recovered while adjusting the flow rate of the concentrated liquid flow path or the waste liquid flow path and the flow rate of the filtrate supply flow path based on the pressure in the space separated from the waste liquid outlet by the moisture separating member in the concentrator or in the flow path connected to said space.
A method for operating a raw liquid treatment device according to a third aspect of the present invention is a method for operating an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus including a filter having a filtering member for filtering the raw liquid, a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated liquid, a raw liquid supply section for supplying the raw liquid to the filter, a liquid supply flow path communicating the raw liquid supply section with a raw liquid supply port of the filter, a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator, a concentrated liquid flow path connected to the concentrated liquid discharge port of the concentrator, and a liquid separated from the concentrated liquid in the concentrator. the waste liquid flow path connected to a waste liquid outlet through which the collected waste liquid is discharged, a liquid delivery unit for delivering liquid to each flow path, and a control unit for controlling the operation of the liquid delivery unit, and is characterized in that, when recovering filtrate and/or concentrated liquid within the device, a liquid is supplied to a space in the filter separated from the raw liquid supply port of the filter by the filtering member, and a flow rate of the liquid supplied to the flow path of the filtrate supply flow path and/or the space separated from the raw liquid supply port of the filter is adjusted based on the pressure within the space separated from the waste liquid outlet by the moisture separating member in the concentrator or within the flow path connected to said space.
A method for operating a raw liquid treatment device according to a fourth aspect of the present invention is a method for operating an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus comprising: a filter having a filtration member for filtering the raw liquid; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated liquid; a raw liquid supply unit for supplying the raw liquid to the filter; a liquid supply flow path communicating between the raw liquid supply unit and a raw liquid supply port of the filter; a filtrate supply flow path communicating between a filtrate discharge port of the filter and a filtrate supply port of the concentrator; a concentrated liquid flow path connected to a concentrated liquid discharge port of the concentrator; a waste liquid flow path connected to a waste liquid discharge port for discharging waste liquid separated from the concentrated liquid in the concentrator; flow paths branched from the filtrate supply flow path; a liquid delivery unit for delivering liquid to each flow path; and a control unit for controlling the operation of the liquid delivery unit, and characterized in that the filtrate in the apparatus is recovered from a flow path branched from the filtrate supply flow path before the filter is washed.
The method of operating a raw liquid treatment device of the fifth invention is characterized in that, in the fourth invention , when recovering filtrate and/or concentrated liquid in the device, gas or liquid is supplied to a space in the filter separated from the raw liquid supply port of the filter by the filtering member.
<Untreated Liquid Treatment Device>
A stock solution treatment device according to a sixth aspect of the present invention is a device for concentrating a stock solution to form a concentrate, the device comprising: a filter having a filtering member for filtering the stock solution; a concentrator to which filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate; a stock solution supply section for supplying the stock solution to the filter; a liquid supply flow path communicating the stock solution supply section with a stock solution supply port of the filter; a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator; a concentrate flow path connected to a concentrate discharge port of the concentrator; the control unit controls the operation of the liquid delivery unit before cleaning the filter, and adjusts the flow rate of the concentrated liquid flow path and/or the waste liquid flow path based on the pressure in the space separated from the waste liquid discharge port by a moisture separating member in the concentrator or in the flow path connected to the space, so that the gas or liquid is supplied from the flow path supplying the gas or liquid to the space separated from the raw liquid supply port by the filtering member in the filter, and the filtrate and/or concentrated liquid in the device is recovered .
A stock solution treatment device according to a seventh aspect of the present invention is a device for concentrating a stock solution to form a concentrate, the device comprising: a filter having a filtering member for filtering the stock solution; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate; a stock solution supply section for supplying the stock solution to the filter; a liquid supply flow path communicating the stock solution supply section with a stock solution supply port of the filter; a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator; a concentrate flow path connected to the concentrate discharge port of the concentrator; the control unit controls the operation of the liquid delivery unit before cleaning the filter, and adjusts the flow rate of the concentrated liquid flow path or the waste liquid flow path and the flow rate of the filtrate supply flow path based on the pressure in the space separated from the waste liquid discharge port by a moisture separating member in the concentrator or in a flow path connected to the space, so that the gas or liquid is supplied from the flow path supplying the gas or liquid to the space separated from the raw liquid supply port by the filtering member in the filter, and the filtrate and/or concentrated liquid in the device is recovered.
A raw liquid treatment apparatus according to an eighth aspect of the present invention is an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus comprising: a filter having a filtering member for filtering the raw liquid; a concentrator to which a filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated liquid; a raw liquid supply section for supplying the raw liquid to the filter; a liquid supply flow path communicating the raw liquid supply section with a raw liquid supply port of the filter; a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator; a concentrated liquid flow path connected to the concentrated liquid discharge port of the concentrator; a waste liquid flow path connected to a waste liquid discharge port for discharging waste liquid separated from the concentrated liquid in the concentrator; the control unit controls the operation of the liquid delivery unit before cleaning the filter, and adjusts the flow rate of the liquid supplied to the flow path of the filtrate supply flow path and/or the space separated from the raw liquid supply port of the filter based on the pressure in the space separated from the waste liquid discharge port by a moisture separating member in the concentrator or in the flow path connected to said space, so that the gas or liquid is supplied from the flow path supplying the gas or liquid to the space separated from the raw liquid supply port of the filter by the filtering member in the filter, and the filtrate and/or concentrated liquid in the device is recovered.
A stock solution treatment device according to a ninth aspect of the present invention is a device for concentrating a stock solution to form a concentrate, the device including a filter having a filtering member for filtering the stock solution, a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate, a stock solution supply section for supplying the stock solution to the filter, a liquid supply flow path communicating the stock solution supply section with a stock solution supply port of the filter, a filtrate supply flow path communicating a filtrate discharge port of the filter with a filtrate supply port of the concentrator, and a concentrate flow path connected to the concentrate discharge port of the concentrator. a waste liquid flow path connected to a waste liquid outlet port that discharges waste liquid separated from the concentrated liquid in the concentrator; a flow path that supplies gas or liquid to a space in the filter separated from the raw liquid supply port of the filter by the filtering member; a liquid delivery unit that delivers liquid to each flow path; and a control unit that controls the operation of the liquid delivery unit, wherein a collection container is connected to the filtrate supply flow path, and the control unit controls the operation of the liquid delivery unit so that the filtrate is supplied to the collection container before the filter is cleaned.
The raw liquid treatment device of the tenth invention is characterized in that, in the ninth invention , a flow path is provided for supplying gas or liquid to a space in the filter separated from the raw liquid supply port of the filter by the filtering member, and the control unit controls the operation of the liquid delivery unit so that gas or liquid is supplied from the flow path for supplying gas or liquid to the space in the filter separated from the raw liquid supply port by the filtering member during an operation of recovering the filtrate and/or concentrated liquid within the device .

<Operation method of raw liquid treatment device>
According to the first to third inventions, it is possible to prevent a decrease in the amount of the active ingredient recovered by filtration and concentration. Also, it is possible to effectively recover the filtrate in the filter and the filtrate supply flow path, and the concentrate in the concentrator and the concentrate flow path. Furthermore, even if the concentrator becomes clogged, it is possible to prevent the pressure inside the concentrator from increasing and to prevent the process from stopping, so that it is possible to effectively recover the filtrate in the filter and the concentrate in the concentrator and the concentrate flow path.
According to the fourth aspect of the present invention, it is possible to prevent a decrease in the amount of the active ingredient recovered by filtration and concentration. Since the filtrate can be recovered in a short time, the transition to the cleaning work can be quickly carried out.
According to the fifth aspect of the present invention , the filtrate in the filter and the filtrate supply flow path, and the concentrated liquid in the concentrator and the concentrated liquid flow path can be effectively recovered .
<Untreated Liquid Treatment Device>
According to the sixth to eighth aspects of the present invention, it is possible to prevent a decrease in the amount of the active ingredient recovered by filtration and concentration. Also, it is possible to effectively recover the filtrate in the filter and the filtrate supply flow path, and the concentrate in the concentrator and the concentrate flow path. Furthermore, even if the concentrator becomes clogged, it is possible to prevent the pressure inside the concentrator from increasing and to prevent the process from stopping, so that it is possible to effectively recover the filtrate in the filter and the concentrate in the concentrator and the concentrate flow path.
According to the ninth aspect of the present invention, it is possible to prevent a decrease in the amount of the active ingredient recovered by filtration and concentration. Since the filtrate can be recovered in a short time, the transition to the cleaning work can be quickly carried out.
According to the tenth aspect of the present invention , the filtrate in the filter and the filtrate supply flow path, and the concentrated liquid in the concentrator and the concentrated liquid flow path can be effectively recovered .

FIG. 1 is a circuit diagram of a raw liquid treatment apparatus 1 according to a first embodiment, and is a schematic explanatory diagram of a filtration and concentration operation. FIG. 2 is a circuit diagram of the raw liquid treatment apparatus 1 according to the first embodiment, and is a schematic explanatory diagram of a preparatory cleaning operation. FIG. 2 is a circuit diagram of the raw liquid treatment apparatus 1 according to the first embodiment, and is a schematic explanatory diagram of a reconcentration operation. FIG. 2 is a circuit diagram of the raw liquid treatment device 1 of the first embodiment, showing an example in which a waste liquid tube delivery section 5p is provided in the waste liquid tube 5. FIG. 1 is a schematic diagram of a filter 10. FIG. 11 is a circuit diagram of a raw liquid treatment device 1B according to a second embodiment, and is a schematic explanatory diagram of a preparatory cleaning operation. FIG. 11 is a circuit diagram of a raw liquid treatment device 1B according to a second embodiment, and is a schematic explanatory diagram of a filtration and concentration operation. FIG. 11 is a circuit diagram of a raw liquid treatment device 1B according to a second embodiment, and is a schematic explanatory diagram of a reconcentration operation. FIG. 13 is a circuit diagram of a raw liquid treatment device 1B according to a second embodiment, showing an example in which a waste liquid tube delivery section 5p is provided in a waste liquid tube 5. FIG. 13 is a circuit diagram of a raw liquid treatment device 1C according to a third embodiment, and is a schematic explanatory diagram of a preparatory cleaning operation. FIG. 11 is a circuit diagram of a raw liquid treatment device 1C according to a third embodiment, and is a schematic explanatory diagram of a filtration and concentration operation. FIG. 11 is a circuit diagram of a raw liquid treatment device 1C according to a third embodiment, and is a schematic explanatory diagram of a reconcentration operation. FIG. 1 is a schematic explanatory diagram of a raw liquid treatment device 1 according to a first embodiment, in which lids 112 of roller pumps 110 and 120 are in a closed state. FIG. 1 is a schematic explanatory diagram of a raw liquid treatment apparatus 1 according to a first embodiment, with lids 112 of roller pumps 110 and 120 in an open state. 1A and 1B are schematic explanatory diagrams of a roller pump 110, in which (A) is a schematic perspective view with a lid portion 112 open, and (B) is a schematic side view with the lid portion 112 open. 1A and 1B are schematic explanatory diagrams of a tube positioning member 160 with a tube T attached, in which (A) is a schematic oblique view of the bent state, (B) is a schematic plan view of the bent state, and (C) is a schematic rear view of the bent state. 1A is a schematic explanatory diagram of a tube positioning member 160 in an exploded state, and FIG. 1B is a schematic explanatory diagram of the tube positioning member 160 with a tube T attached thereto. 1A is a schematic perspective view of a tube holder 150, and FIG. 1B is a schematic explanatory diagram of the tube holder 150 attached to a bucket. 1 is a schematic explanatory diagram of a raw liquid treatment apparatus 1 according to a first embodiment. FIG. 2 is a schematic explanatory diagram of the filter 10 during a cleaning operation. FIG. 2 is a circuit diagram of the raw liquid treatment apparatus 1 according to the first embodiment, and is a schematic explanatory diagram of a cleaning operation. FIG. 11 is a circuit diagram of a raw liquid treatment device 1B according to a second embodiment, and is a schematic explanatory diagram of a cleaning operation. FIG. 13 is a circuit diagram of a raw liquid treatment device 1C according to a third embodiment, and is a schematic explanatory diagram of a cleaning operation. 1A is a diagram showing the filter membrane pressure difference when adjusting the flow rate of the raw liquid supplied to the filter 10, and FIG. 1B is a diagram showing the flow rate fluctuation in the liquid supply tube 2 when adjusting the flow rate of the raw liquid supplied to the filter 10.

The liquid treatment device of the present invention is a device for filtering and concentrating liquid such as pleural and ascites fluid to obtain a treated liquid that can be administered to a patient by intravenous drip or intraperitoneal administration.

The raw liquid to be treated by the raw liquid treatment device of the present invention is not particularly limited, but examples thereof include pleural and ascites fluids, plasma, and blood. Pleural and ascites fluids are pleural and ascites fluids that accumulate in the thoracic and abdominal cavities due to cancerous pleural peritonitis, liver cirrhosis, and the like. This pleural and ascites fluid contains plasma components (proteins, hormones, sugar, lipids, electrolytes, vitamins, bilirubin, amino acids, etc.) that have leaked from blood vessels and organs, hemoglobin, cancer cells, macrophages, histiocytes, white blood cells, red blood cells, platelets, bacteria, and the like. The raw liquid treatment device of the present invention can remove solids such as cancer cells, macrophages, histiocytes, white blood cells, red blood cells, platelets, and bacteria from this pleural and ascites fluid to produce a concentrated liquid containing the water and useful components contained in the pleural and ascites fluid.

Plasma includes waste plasma from plasma exchange therapy, and blood includes blood collected during surgery. In other words, waste plasma or blood collected during surgery can be purified using the raw liquid treatment device of the present invention to produce reusable regenerated plasma. In the raw liquid treatment device of the present invention, when treating waste plasma from plasma exchange therapy, a plasma component separator can be used instead of a filter, and when treating blood collected during surgery, a plasma separator can be used instead of a filter.

The filter material used in the filter of the raw liquid treatment device of the present invention is not particularly limited. The same filter material may also be used for concentrating the filtrate in the concentrator. The filter material used for such filtration and concentration is permeable to plasma, water, and the above-mentioned useful components contained in the pleural and ascites fluid, but is not permeable to cellular components (i.e., solids) such as cancer cells, macrophages, histiocytes, white blood cells, red blood cells, platelets, and bacteria, and is not permeable to gas, and its material, size, and shape are not particularly limited. For example, the shape of the filter material can be a hollow fiber membrane, a flat membrane, a laminated membrane, etc. In addition, the filter material can be made of a material that exhibits a function of not permeating gas when wetted with liquid. Of course, it is also possible to use a filter material that exhibits a function of not permeating gas even when not wetted with liquid. In this specification, the gas that does not permeate the filter material means an inert gas such as nitrogen, air, oxygen, etc., but means a gas used in general leak checks, etc.

As an example, hollow fiber membranes used in CART ascites filters, plasma separators for plasma exchange, and plasma component separators for plasma exchange can be used in the filters and concentrators of the raw liquid treatment device of the present invention.

<First embodiment of raw liquid treatment device 1>
The raw liquid treatment apparatus 1 of the first embodiment will be described with reference to FIGS.
It goes without saying that the appearance of the raw liquid treatment device 1 of the first embodiment, the arrangement of each device, the relative size, and the number of devices are not limited to those shown in Figures 13 to 19, and may be appropriately changed depending on the environment, purpose, etc. in which the raw liquid treatment device 1 of the first embodiment is used.

As shown in Figures 13, 14, and 19, the raw liquid treatment device 1 of the first embodiment includes a main body 100, a pair of roller pumps 110, 120 provided on the main body 100, a filter holder 101 that holds the filter 10, a concentrator holder 102 that holds the concentrator 20, and a pair of hanging parts 103, 103 from which the tube holder 150 and each bag B are hung.

When processing the raw liquid in the raw liquid processing device 1 of the first embodiment, each bag B is hung from a pair of hanging parts 103, 103, and the filter 10 and concentrator 20 are held by the filter holding part 101 and the concentrator holding part 102. Then, each bag B, filter 10, and concentrator 20 are appropriately connected by a plurality of tubes T, and the appropriate tubes T are set in the pair of roller pumps 110, 120. In this state, by operating the pair of roller pumps 110, 120, the raw liquid in the raw liquid bag UB can be filtered and concentrated to obtain a concentrated liquid.

In addition, by changing the operating state of the pair of roller pumps 110, 120, changing the bags B connected to each tube T, changing the tube T through which the liquid flows, etc., it is possible to not only obtain a concentrated liquid, but also to re-concentrate the concentrated liquid, clean the filter 10 and concentrator 20, recover the liquid present in the filter 10 and concentrator 20, etc.

<Description of each component of the raw liquid treatment device 1 according to the first embodiment>
Hereinafter, each part of the raw liquid treatment apparatus 1 of the first embodiment will be described.

<Main body 100>
As shown in Figures 13, 14 and 19, the main body 100 is provided with a control unit 106 at its center. This control unit 106 has a function of controlling the operation of the pair of roller pumps 110, 120 and the entire device. The control unit 106 is also provided with a panel unit 106p that serves as both an operation panel for operating the device and a display panel on which various displays are displayed. That is, by giving instructions to the control unit 106 from the panel unit 106p, an operator can instruct the processing to be performed on the raw liquid processing device 1 of the first embodiment. Also, by checking the numerical values and warnings displayed on the panel unit 106p according to instructions from the control unit 106, an operator can grasp the status of the raw liquid processing device 1 of the first embodiment.

In addition to the panel unit 106p, the control unit 106 may also have buttons for performing various operations.

<Roller pumps 110, 120>
13, 14 and 19, a pair of roller pumps 110, 120 are provided on both sides of the control unit 106 of the main body 100. Since the pair of roller pumps 110, 120 have substantially the same structure, only the roller pump 110 will be described below.

Note that in order to make the roller pump 110 easier to understand, FIG. 15 shows the portion that functions as the roller pump 110 removed from the main body 100. The roller pump 110 will be described below with reference to FIG. 15.

As shown in FIG. 15, the roller pump 110 includes a frame 111 and a lid portion 112 that is attached to the frame 111 so as to be able to open and close. Specifically, the lid portion 112 is provided so that when the lid portion 112 is opened, a roller portion 115 (described later) is exposed, and when the lid portion 112 is closed, the roller portion 115 can be covered by the lid portion 112. The lid portion 112 is provided so that when the lid portion 112 is closed, a space for accommodating the roller portion 115 is formed between the inner surface of the lid portion 112 and the upper surface of the frame 111.

A roller section 115 equipped with two rollers 116 is provided on the upper surface of the frame 111 (see FIG. 16). In this roller section 115, the two rollers 116 are attached to a single shaft 117, and this shaft 117 is rotated by a driving source 114 such as a motor. In other words, when the shaft 117 is rotated by the driving source 114, the two rollers 116 rotate. Note that the number of rollers 116 provided in the roller section 115 is not limited to two, and may be one or three or more. It is sufficient that the number of rollers 116 is appropriate for the processing work.

The upper surface of the frame 111 is provided with a holder 113 at a position facing the roller unit 115. The holder 113 has a recessed surface 113a on the surface facing the two rollers 116 of the roller unit 115, which sandwiches the tube T between the two rollers 116. The holder 113 can move toward and away from the roller unit 115 in conjunction with the opening and closing of the lid unit 112 by a slider mechanism or the like. Specifically, when the lid unit 112 is opened, the holder 113 moves away from the roller unit 115 so that the space between the recessed surface 113a of the holder 113 and the two rollers 116 becomes wider than the diameter of the tube T. When the lid unit 112 is closed, the holder 113 moves toward the roller unit 115 so that the gap between the recessed surface 113a of the holder 113 and the two rollers 116 becomes narrower than the diameter of the tube T. In other words, when the lid part 112 is opened, the tube T can be placed or removed between the roller part 115, and when the lid part 112 is closed, the tube T can be sandwiched between the recessed surface 113a of the holder 113 and the two rollers 116.

Therefore, by opening the lid portion 112 and placing the tube T between the roller portion 115 and the recessed surface 113a of the holder 113, and then closing the lid portion 112, the tube T can be clamped by the roller portion 115 and the holder 113. In addition, by operating the driving source 114 with the tube T clamped by the roller portion 115 and the holder 113, the liquid in the tube T can be pumped.

The rollers 116 may have the same structure as rollers used in general roller pumps. For example, as shown in FIG. 16(C), the rollers 116 may have multiple rollers 116b (e.g., three rollers 116b) between a pair of cover plates 116a. When such rollers 116 are used, the tube T can be sandwiched between the multiple rollers 116b and the recessed surface 113a of the holder 113, and when the rollers 116 rotate, the rollers 116b move to squeeze the tube T, thereby delivering the liquid in the tube T.

The size of the gap formed between the recessed surface 113a of the holder 113 and the two rollers 116 when the lid portion 112 is closed may be set to an appropriate gap according to the tube T placed on the rollers 116. An appropriate gap means a gap that can clamp the tube T so that liquid does not flow inside the tube T when the rollers 116 are not rotating, and that does not cause too much rotational resistance of the rollers 116 when they rotate.
Furthermore, in the case where multiple tubes T are placed on the rollers 116 and the diameters of the tubes T to be placed are different, the gap may be different depending on the position at which each tube T is placed. For example, by providing a step in the recessed surface 113a of the holder 113 so that the distance from the recessed surface 113a of the holder 113 to the rollers 116 is different, the gap can be changed depending on the position at which each tube T is placed (i.e., the roller 116 on which it is placed). On the other hand, if multiple rollers 116 are provided and the diameters of the tubes T to be placed on each roller 116 are different, the gap can be changed to match the tubes T by changing the diameter of the rollers 116.

<Control of roller pump 110>
Here, when the tube T is placed between the roller portion 115 and the recessed surface 113a of the holder 113, the tube T may not be placed in an appropriate position. When the driving source 114 is operated in this state, the tube T may interfere with parts of the roller 116 other than the roller portion 115. If the tube T interferes with parts of the roller 116 other than the roller portion 115, there is a risk that liquid cannot be delivered or that the tube T or the roller 116 may be damaged.

The control unit 106 may have a function of operating the drive source 114 to rotate the roller 116 in the forward and reverse directions when it detects that the lid unit 112 is closed. By rotating the roller 116 in the forward and reverse directions (for example, about ±180 to 360 degrees), the tube T can be moved to the correct position even if the position of the tube T is slightly deviated from the correct position. This eliminates the need to reposition the tube T, thereby shortening the operation time.

In addition, even if the rollers 116 are rotated forward and backward, the tube T may not be positioned in the correct position. Therefore, it is desirable for the control unit 106 to have a safety function that disables the drive source 114 when it detects that the tube T has not been positioned in the correct position, and an alarm function that notifies the operator that the tube T is not positioned properly. This can prevent damage to the device due to the tube T being positioned improperly, and allows the operator to quickly notice any abnormality in the positioning of the tube T.

For example, an example of the alarm function is a function in which, when the control unit 106 detects that the tube T is not placed in the proper position, the control unit 106 displays an abnormality alarm on the panel unit 106p or emits an abnormality alarm sound.

As a method for detecting that the tube T is not positioned in the correct position, for example, a method of detecting the driving force of the drive unit 114 can be adopted. In this case, if the driving force of the drive unit 114 exceeds a certain level, the control unit 106 can determine that an abnormality has occurred in the positioning of the tube T. If the drive unit 114 is a motor, the control unit 106 can be configured to determine that an abnormality has occurred in the positioning of the tube T if the rotational resistance applied to the main shaft exceeds a predetermined value. The rotational resistance applied to the main shaft can be determined, for example, by detecting the value of the current supplied to the motor.

<Tube positioning member 160>
As a method for positioning the tube T in the appropriate position, a tube positioning member 160 such as the one described below can be used. If the tube positioning member 160 described below is used, it becomes easier to bring the tube T and the roller 116 into close contact with each other when the tube T is wound around the roller 116, and it becomes easier to properly wind two tubes T around each of the two rollers 116.

The configuration of the tube positioning member 160 will now be described.
As shown in FIGS. 16 and 17 , the tube positioning member 160 includes a pair of holding members 161 , 161 and a connecting member 165 .

<Pair of Holding Members 161, 161>
16 and 17 , a pair of holding members 161, 161 hold two tubes T and are arranged at a distance from each other along the axial direction of the two tubes T. The pair of holding members 161, 161 have the same structure and are formed by combining a base member 162 and a guide member 163.

The base member 162 has a base portion 162b which is a rectangular plate-like member. The base member 162 has a structure for holding the tube T so that the long axis direction of the base portion 162b is perpendicular to the axial direction of the tube T. Specifically, a tube arrangement portion 162c extending from the base portion 162b is provided on the side of the short axis direction of the base member 162. The tube arrangement portion 162c has a pair of outer holding portions d, d standing from the surface of the tube arrangement portion 162c, and a pair of inner holding portions c, c located between the pair of outer holding portions d, d and the base portion 162b. The pair of inner holding portions c, c are arranged inward in the long axis direction of the base portion 162b than the pair of outer holding portions d, d. The pair of inner holding portions c, c have an erected portion erected from the surface of the tube arrangement portion 162c and a bent portion bent toward the long axis direction outward of the base portion 162b with respect to the erected portion. Moreover, the pair of inner holding parts c, c are formed so that the distance between the outer surface of the erected part and the inner surface of the pair of outer holding parts d, d in the longitudinal direction of the base part 162b is approximately the same as the diameter of the tube T. In addition, the pair of inner holding parts c, c are also formed so that the distance between the lower surface of the bent part and the surface of the base part 162b is approximately the same as the diameter of the tube T.

Then, when the base portion 162b is viewed from the short axis direction, two holes (hereinafter referred to as virtual holes) are formed by the inner surfaces of the pair of outer holding portions d, d, the outer surfaces of the erected portions and the undersides of the bent portions of the pair of inner holding portions c, c, and the surface of the base portion 162b.

On the other hand, the guide member 163 is disposed so as to be superimposed on the surface of the base portion 162b of the base member 162. In this guide member 163, a pair of grooves 163g, 163g for accommodating the tube T is provided on the surface located on the surface side of the base portion 162b when the guide member 163 is superimposed on the surface of the base portion 162b. The pair of grooves 163g, 163g are provided so that their axial directions are parallel to each other. Moreover, the pair of grooves 163g, 163g are formed so that when the guide member 163 is superimposed on the surface of the base portion 162b, the pair of grooves 163g, 163g and the two imaginary holes overlap (preferably coincide) when viewed from the short axis direction of the base portion 162b.

Therefore, by arranging two tubes T in the two virtual holes of the base member 162, the two tubes T can be arranged on the base member 162 so that they are parallel to each other. In this state, by overlapping the guide member 163 on the surface of the base portion 162b, the two tubes T can be arranged in the pair of grooves 163g, 163g, and the two tubes T can be held by the holding member 161 so that they do not come off.

The tube placement section 162c of the base member 162 and the pair of grooves 163g, 163g of the guide member 163 described above can also be called "multiple tube holding sections." The long axis direction of the base section 162b can also be called "the direction in which the multiple tube holding sections are lined up." Furthermore, the short axis direction of the base section 162b can also be called "the axial direction of the multiple tubes held in the multiple tube holding sections."

<Connecting member 165>
16 and 17, the connecting member 165 connects the pair of tube holding parts 161, 161 described above. More specifically, the connecting member 165 is provided between the pair of tube holding parts 161, 161 in order to maintain the pair of tube holding parts 161, 161 in a state in which the pair of tube holding parts 161, 161 are separated by a predetermined distance along the axial direction of the tube T.

The connecting member 165 has a connecting structure at both ends that connects to the pair of tube holding parts 161, 161, and can be detachably connected to the guide member 163 of the tube holding part 161 described above. Specifically, the end of the connecting member 165 is provided to be connected to the part between the pair of grooves 163g, 163g in the guide member 163. In other words, when the connecting member 165 is stretched, the connecting member 165 is connected to the guide member 163 so that it is located between the adjacent tubes T held by the tube holding part 161 when viewed from a direction intersecting the major axis direction and the minor axis direction of the base part 162b.

In addition, the connecting member 165 is connected to the guide member 163 so that, when the connecting member 165 is stretched, the connecting member 165 is positioned at a position offset toward the opposite side of the base portion 162b from the central axis of the tube T held by the tube holding portion 161.

The connecting member 165 has a structure that allows it to be bent between the pair of tube holding parts 161, 161 when both ends are connected to the pair of tube holding parts 161, 161. More specifically, the connecting member 165 has a structure that allows it to be bent between the pair of tube holding parts 161, 161 in directions that intersect with the long axis direction and the short axis direction of the base part 162b.

For example, the connecting member 165 is formed from a plastic plate-like member. Then, both ends of the connecting member 165 are connected to the guide members 163 of the pair of tube holding parts 161, 161 so that the width direction of the connecting member 165 is parallel to the long axis direction of the base part 162b. Then, the connecting member 165 can be bent in a direction intersecting the long axis direction and short axis direction of the base part 162b between the pair of tube holding parts 161, 161 (Figure 16).

When such a tube positioning member 160 is attached to two tubes T, the following advantages are obtained when the two tubes T are placed in the roller pump 110.

First, the stopper members T1, T2 are provided so as to be positioned at an appropriate length apart when the tube T is wound around the two roller parts 116, 116 of the roller pump 110 (see Figs. 16 and 17(B)). Meanwhile, a pair of tube holding parts 161, 161 are arranged between the stopper members T1, T2 so that the outer surfaces of the pair of tube holding parts 161, 161 are in contact with the stopper members T1, T2, respectively. Then, in a state where the tube T is stretched and the outer surfaces of the pair of tube holding parts 161, 161 are in contact with the stopper members T1, T2, respectively (hereinafter referred to as a proper arrangement state), a connecting member 165 is arranged between the pair of tube holding parts 161, 161 so as to be in a stretched state (see Fig. 17(B)).
Meanwhile, the roller pump 110 is provided with a pair of accommodation sections for accommodating the pair of tube holding parts 161, 161. Specifically, the pair of accommodation sections for accommodating the pair of tube holding parts 161, 161 are provided at positions sandwiching a surface including the rotation shaft 117 of the roller part 115. Moreover, the pair of accommodation sections are provided so that when the pair of tube holding parts 161, 161 are accommodated in the pair of accommodation sections, respectively, the tube T is wound around the two tubes 116, 116 of the roller part 115 in an appropriate state.
Then, simply by arranging the pair of tube holding portions 161, 161 in the pair of storage portions, the two tubes T can be properly wound around the two tubes 116, 116 of the roller portion 115 (see FIG. 15).

Moreover, the connecting member 165 is connected to the guide member 163 so that the connecting member 165 is located on the opposite side of the base portion 162b from the central axis of the tube T held by the tube holding portion 161. Then, when the tube T is wound around the roller 116 of the roller portion 115 so that the guide member 163 is located on the roller 116 side, the connecting member 165 is positioned between the two tubes T with the central portion between both ends slightly bent (see Figures 16 (A) and (B)). Then, even if two tubes T are arranged vertically side by side, the connecting member 165 can prevent the upper tube T from coming into contact with the lower tube T.

Note that the connecting member 165 does not necessarily have to be positioned on the opposite side of the base portion 162b from the central axis of the tube T. However, such a structure can provide the above-mentioned effects.

In addition, the tube holding portion 161 may not be symmetrical with respect to the middle of the longitudinal direction of the base portion 162b. In other words, the tube holding portion 161 may be formed to be asymmetrical with respect to the middle of the two tubes T held by the tube holding portion 161 in the longitudinal direction of the base portion 162b. For example, as shown in FIG. 17, the guide member 163 may have different lengths of the portions located outside the pair of grooves 163g, 163g. In this way, when placing the pair of tube holding portions 161, 161 in the pair of storage portions, it is possible to prevent the pair of tube holding portions 161, 161 from being inserted in the wrong way. In other words, even if the pair of tube holding portions 161, 161 is placed in the pair of storage portions from the wrong direction, it is possible to prevent the pair of tube holding portions 161, 161 from being stored in the pair of storage portions. This prevents operational errors when setting the tube T in the roller pump 110. For example, when setting the tube T in the roller pump, it is possible to prevent the tube T from being twisted or two tubes from being set on opposite rollers 116.

If multiple roller pumps are used, the size and shape of the tube holder 161 may be changed depending on the roller pump to be set. This can prevent the tube from being set to the wrong roller pump.

A function may also be provided that prevents the roller pump device from operating if the tube holding portion 161 is not properly set in the pair of storage portions. In this case, damage to the tube T or roller 116 can be prevented even if the roller 116 rotates erroneously when the tube T is not properly set. For example, the above function can be achieved by providing a button-type sensor or the like in the pair of storage portions that is pressed when the tube holding portion 161 is properly positioned.

In the above example, the tube positioning member 160 holds two tubes T. However, the number of tubes T held by the tube positioning member 160 may be three or more, and is not particularly limited. When the tube positioning member 160 holds three or more tubes T, it is desirable to provide a connecting member 165 between each of the adjacent tubes T.

The structure of the holding member 161 and the multiple tube holding parts is not limited to the above structure. The holding member 161 and the multiple tube holding parts may hold multiple tubes parallel to each other and in a row. For example, the multiple tube holding parts may be formed by simply forming through holes in a row in a plate-shaped holding member. The row here includes a case where the central axes of multiple tubes are arranged on approximately the same plane when multiple tubes are placed in the multiple tube holding parts, and a case where the position of the central axis of the tube T is shifted in the normal direction of the surface of the base member 162 when the tube T held in the multiple tube holding parts is viewed in its axial direction. For example, when the central axes of the tubes T held in the multiple tube holding parts are aligned in a staggered arrangement when viewed in its axial direction, the above-mentioned state of multiple tubes being held in a row is also included.

<Filter holder 101 and concentrator holder 102>
13, 14, and 19, a filter holder 101 and a concentrator holder 102 are provided on the outside of a pair of roller pumps 110, 120. In Fig. 13 and Fig. 14, the roller pump 110 provided on the left side of the control unit 106 includes the filter holder 101, and the roller pump 120 provided on the right side of the control unit 106 includes the concentrator holder 102.

The filter holder 101 and the concentrator holder 102 have clamps 101c and 102c on their surfaces, which allow the filter 10 and the concentrator 20 to be detachably held by the clamps 101c and 102c.

The base ends of the filter holder 101 and the concentrator holder 102 are swingably connected to the frames of the pair of roller pumps 110, 120. Specifically, the filter holder 101 and the concentrator holder 102 are connected to the frames of the pair of roller pumps 110, 120 so that the clamps 101c, 102c are exposed when the filter holder 101 and the concentrator holder 102 are swung outward. Conversely, the filter holder 101 and the concentrator holder 102 are connected to the frames of the pair of roller pumps 110, 120 so that the clamps 101c, 102c are opposed to the pair of rollers 116, 116 of the pair of roller pumps 110, 120 when the filter holder 101 and the concentrator holder 102 are swung inward. In other words, when the work of treating the raw liquid is not being performed, the filter holder 101 and the concentrator holder 102 can be stored in the roller pumps 110, 120. The filter holder 101 and the concentrator holder 102 do not necessarily have to be swingably connected to the frames of the pair of roller pumps 110, 120, and may be exposed to the outside of the roller pumps 110, 120 at all times. However, with the above configuration, the raw liquid treatment device 1 of the first embodiment can be advantageously stored compactly when it is not in use.

13, 14, and 19 show the case where the filter 10 and the concentrator 20 are held by the filter holder 101 and the concentrator holder 102 with their axial directions (for example, in the case where a hollow fiber membrane 16 is provided inside as shown in FIG. 5, the axial direction of the hollow fiber membrane 16 corresponds to the axial direction) facing up and down. However, the filter holder 101 and the concentrator holder 102 may be configured to hold the filter 10 and the concentrator 20 with their axial directions facing horizontally. The state where the axial directions of the filter 10 and the concentrator 20 face up and down is a concept that also includes the case where the axial directions of the filter 10 and the concentrator 20 are inclined at about 0 to 45 degrees with respect to the vertical direction. Also, the state where the axial directions of the filter 10 and the concentrator 20 face horizontally is a concept that also includes the case where the axial directions of the filter 10 and the concentrator 20 are inclined at about 0 to 45 degrees with respect to the horizontal direction.
Furthermore, the raw liquid treatment device 1 of the first embodiment does not necessarily have to have the filter holder 101 or the concentrator holder 102. However, if the main body 100 has the filter holder 101 or the concentrator holder 102, there is an advantage in that it is not necessary to separately prepare a holder for holding the filter 10 or the concentrator 20.

<Pair of hanging portions 103, 103>
As shown in Figures 13, 14 and 19, a pair of hanging parts 103, 103 are provided on the back surface of the main body part 100. The pair of hanging parts 103, 103 are formed of an axial member, and the base end of the shaft is detachably attached to a pair of mounting parts 100h, 100h provided on the back surface of the main body part 100. More specifically, the pair of mounting parts 100h, 100h are provided so that when the base ends of the pair of hanging parts 103, 103 are attached to the pair of mounting parts 100h, 100h, the axial direction of the pair of hanging parts 103, 103 becomes approximately vertical.

The pair of hanging parts 103, 103 are provided with hook parts 103b, similar to a typical IV holder. The pair of hanging parts 103, 103 are designed so that each bag B can be hung from the hook parts 103b.

The pair of hanging parts 103, 103 are provided with hook parts 103f, and the tube holder 150 can be hung from these hook parts 103f.

The pair of hanging parts 103, 103 do not necessarily have to be detachable from the main body 100. However, if the pair of hanging parts 103, 103 are detachable, the advantage is that the raw liquid treatment device 1 of the first embodiment can be stored compactly by removing the pair of hanging parts 103, 103 when the raw liquid treatment device 1 of the first embodiment is not in use.

The number of hanging parts 103 provided in the raw liquid treatment device 1 of the first embodiment is not limited to two, and may be one, or three or more. An appropriate number of hanging parts 103 may be provided according to the number of bags B and tubes T used in the treatment performed by the raw liquid treatment device 1 of the first embodiment.

The stock solution treatment device 1 of the first embodiment does not necessarily have to have a pair of hanging parts 103, 103. In this case, a general drip holder for hanging a drip can be used. However, if the main body 100 has a pair of hanging parts 103, 103, there is an advantage in that it is not necessary to prepare a separate drip holder, etc.

<Tube holder 150>
As shown in Fig. 18, the tube holder 150 is a member for holding a plurality of tubes T. By holding a plurality of tubes T in the tube holder 150, the plurality of tubes T can be hung from a pair of hanging parts 103, 103 as shown in Fig. 18 (see Fig. 19). Then, when setting the plurality of tubes T in the control part 106 of the main body part 100, the filter 10, the concentrator 20, and the pair of roller pumps 110, 120, only the necessary tubes T can be removed from the tube holder 150 for work. In other words, when setting the plurality of tubes T in the device, the operator does not need to hold the tubes T that will not be used immediately, which makes the operator's work easier.

<Main body portion 151>
18, tube holder 150 has a plate-shaped main body 151. A connecting portion 152 is provided at an upper edge 151a of main body 151. This connecting portion 152 has a through hole 152h that penetrates from the front to the back, and by passing hook portions 103f of a pair of hanging portions 103, 103 through this through hole 152h, tube holder 150 can be hung from hanging portion 103 with its upper edge 151a facing upward.

In order to stably hang the tube holder 150 from the pair of hanging parts 103, 103 with the upper edge 151a facing upward, it is desirable that the through hole 152h and the hook parts 103f of the pair of hanging parts 103, 103 have a horizontally elongated shape. In other words, it is desirable that the through hole 152h of the connecting part 152 is a horizontally elongated hole that is long in the direction along the upper edge 151a. It is also desirable that the hook parts 103f of the pair of hanging parts 103, 103 have a horizontally elongated shape that is long in the direction perpendicular to the axial direction of the pair of hanging parts 103, 103.

<Holding portion 155>
A surface 151c (first surface) of the main body 151 is provided with a plurality of holding portions 155 for detachably holding the tube T. The holding portions 155 have a cylindrical structure with a through hole 155h that penetrates in the vertical direction, and a slit-shaped opening 155s is formed on the front surface of the holding portion 155. The width of the opening 155s of the through hole 155h of the holding portion 155 is smaller than the diameter of the tube T. In other words, the tube T can be placed and held in the through hole 155h of the holding portion 155 by pushing the tube T into the through hole 155h from the opening 155s, and the tube T can be removed from the holding portion 155 by pulling the tube T.

The multiple holding parts 155 are arranged in a line along the upper edge 151a of the main body 151. Moreover, the multiple holding parts 155 are arranged so that the central axes of the through holes 155h are parallel to each other. Therefore, when the multiple tubes T are held by the multiple holding parts 155, the multiple tubes T can be arranged so that their axial directions are parallel to each other and lined up in a line along the surface 151c of the main body 155. Then, if the multiple tubes T are attached to the multiple holding parts 155 in a predetermined order, it is possible to prevent the worker from making mistakes such as mixing up the multiple tubes T. For example, the multiple tubes T are attached to the multiple holding parts 155 so that the multiple tubes T are lined up from left to right in the order in which they are connected to the device. Then, if the worker removes the tubes T in order from the left, there is no mistake in the tubes T to be connected, so that work mistakes can be prevented and the burden on the worker can be reduced.

Note that "the multiple holding parts 155 are aligned in a row along the upper edge 151a of the main body part 151" also includes cases where the multiple holding parts 155 are arranged in a staggered pattern or where there is a slight misalignment in the direction intersecting with the upper edge 151a of the main body part 151.

<Engagement Member 153>
The connecting portion 152 is provided with an engaging member 153 on the back surface 151d (i.e., the second surface opposite to the front surface 151c) side of the main body portion 151. The engaging member 153 is provided so as to protrude from the back surface 151d of the main body portion 151, has an opening 153s at one end (upper end), and is provided with a gap 153h that is continuous with the opening 153s.

By providing such an engagement member 153, the tubes T held by the multiple holding parts 155 of the main body 151 can be turned downward at once, or the tubes T can be maintained in a downward state. For example, by inserting the edge of a bucket or the like into the gap 153h through the opening 153s, the tube holder 150 can be attached to a bucket or the like so that the upper edge 115a of the main body 151 faces downward. Then, by attaching the multiple tubes T to the multiple holding parts 155 so that their tips face the upper edge 115a side of the main body 151 (upward when the main body 151 is suspended from the hanging part 103), the tips of the multiple tubes T can be arranged to face downward at once. In other words, when draining liquid from multiple tubes T into a bucket or the like, simply attaching the engagement member 153 to the edge of the bucket or the like makes it easy to drain liquid from the multiple tubes T.

The shape of the connecting portion 152 is not limited to the above-mentioned shape, but may be any shape that allows the main body portion 151 to be connected to the pair of hanging portions 103, 103, etc.
Furthermore, the shape of the engaging member 153 is not limited to the above-mentioned shape, and any shape that has the above-mentioned function may be used.
Furthermore, in the above example, the engaging member 153 is described as being provided on the back surface 151d of the main body portion 151, but the engaging member 153 may be provided on the front surface 151c of the main body portion 151, or on both the front surface 151c and the back surface 151d of the main body portion 151.

<Filter 10 and Concentrator 20>
Before describing the circuit of the raw liquid treatment device 1 of the first embodiment, an example of a filter and a concentrator used in the raw liquid treatment device 1 of the first embodiment will be described. Note that, although a filter and a concentrator using a hollow fiber membrane as a filtering member will be described below, the filter and the concentrator used in the raw liquid treatment device 1 of the first embodiment are not limited to those using a hollow fiber membrane as a filtering member, and a filter and a concentrator using a known filtering member other than a hollow fiber membrane can also be used.

<Filter 10>
The filter 10 is, for example, an ascites filter used in CART, a plasma separator used in plasma exchange, a plasma component separator, etc. This filter 10 has a filtering member housed therein, and can filter raw fluid such as pleural and ascites fluid with the filtering member to separate the raw fluid into a filtrate and a separated fluid containing cells, etc.

As shown in FIG. 5, the filter 10 has a main body 11 and a hollow fiber membrane bundle 15 arranged within the main body 11.

<Hollow fiber membrane bundle 15>
As shown in FIG. 5, the hollow fiber membrane bundle 15 is formed by bundling a plurality of hollow fiber membranes 16 together.

The hollow fiber membrane 16 is a tubular member having a wall 16w with a circular cross section and a through flow passage 16h formed inside the wall 16w that passes through the axial direction of the hollow fiber membrane 16. The wall 16w of the hollow fiber membrane 16 has a function of being permeable to liquids but not to solids such as cells and gases.
The thickness of the wall 16w of the hollow fiber membrane 16 is about 45 to 275 μm, and the diameter of the through passage 16h is about 50 to 500 μm, but the thickness of the wall 16w of the hollow fiber membrane 16 and the diameter of the through passage 16h are not particularly limited.

The hollow fiber membrane bundle 15 is formed by bundling one end of a plurality of hollow fiber membranes 16 together and the other end of the hollow fiber membranes 16 together. In other words, the hollow fiber membrane bundle 15 is formed by bundling a plurality of hollow fiber membranes 16 together so that the through flow passage 16h of each hollow fiber membrane 16 passes between one end and the other end of the hollow fiber membrane bundle 15.

The hollow fiber membranes 16 do not necessarily have to be bundled together at both ends. In that case, the hollow fiber membranes 16 are arranged such that both ends of the through-flow passages 16h are connected to the pair of headers 13, 14 of the main body 11.
Furthermore, the number of hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15 is not particularly limited. For example, the hollow fiber membrane bundle 15 may be formed by bundling about 1,000 to 20,000 hollow fiber membranes 16. Furthermore, the hollow fiber membrane bundle 15 may be formed by bundling a plurality of hollow fiber membranes 16 so that the cross-sectional area of the bundle is a desired cross-sectional area, without limiting the number of membranes. For example, if the cross section of the hollow fiber membrane bundle 15 is circular, the plurality of hollow fiber membranes 16 may be bundled so that the diameter of the bundle is about 20 to 75 mm.

<Main body portion 11>
As shown in Fig. 5, the main body 11 is provided with a body 12 having an internal space 12h that is a space airtight and liquidtightly isolated from the outside. The internal space 12 of the body 12 is formed so as to be communicated with the outside only through a port described later, and contains the hollow fiber membrane bundle 15 described above. When the hollow fiber membrane bundle 15 described above is contained inside, the internal space 12 is airtightly separated from the through-flow passages 16h of the multiple hollow fiber membranes 16, but liquid can pass between them through a wall 16w. In other words, the liquid in the internal space 12 can be supplied to the through-flow passages 16h, and the liquid in the through-flow passages 16h can be supplied to the internal space 12.

The size and shape of the internal space 12 are not particularly limited. When the hollow fiber membrane bundle 15 is housed, the size of the port needs to be large enough that the liquid flowing into the internal space 12 through the port can flow between the hollow fiber membrane bundle 15 and the inner surface of the body 12 (i.e., the inner surface of the internal space 12) and between the multiple hollow fiber membranes 16, and can flow into the through-flow passage 16h through the wall 16w of the hollow fiber membrane 16. In addition, the size of the port needs to be large enough that the liquid (filtrate) flowing from the through-flow passage 16h through the wall 16w of the hollow fiber membrane 16 to the internal space 12 can flow between the multiple hollow fiber membranes 16 and between the hollow fiber membrane bundle 15 and the inner surface of the internal space 12, and can flow out from the port.

As shown in FIG. 5, the main body 11 is provided with a pair of headers 13, 14 sandwiching the trunk 12, i.e., sandwiching the internal space 12h. The pair of headers 13, 14 are formed to have a space that is airtightly and liquidtightly isolated from the internal space 12h of the trunk 12 and the outside, and is connected to the outside only through a port described later. In addition, each end of the hollow fiber membrane bundle 15 described above is connected to the pair of headers 13, 14. Specifically, both ends of the hollow fiber membrane bundle 15 are connected to the pair of headers 13, 14 so that the openings at both ends of the through-flow passages 16h of the multiple hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15 are connected to the pair of headers 13, 14. Therefore, the internal spaces of the pair of headers 13, 14 are connected to each other through the through-flow passages 16h of the multiple hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15.

<Each port 11a to 11c>
As described above, the main body 11 is provided with the port 11c that communicates between the internal space 12h of the trunk 12 formed in the main body 11 and the outside. The pair of headers 13, 14 are provided with ports 11a, 11b, respectively, that communicate between the internal spaces and the outside.

As shown in FIG. 5, the header 13 provided at one end of the main body 11 is provided with a stock solution supply port 11a that communicates between the internal space and the outside. This stock solution supply port 11a is a port to which one end of a tube or the like is connected. For example, in FIG. 1, one end of a liquid supply tube 2, the other end of which is connected to the liquid outlet of the stock solution bag UB, is connected to the stock solution supply port 11a.

In the case of FIG. 1, the cleaning solution collection bag FB is connected to the raw solution supply port 11a via the supply tube 2 or directly to the raw solution supply port 11a. Specifically, one end of the cleaning solution collection tube 7, the other end of which is connected to the cleaning solution collection bag FB, is connected to the supply tube 2 or the raw solution supply port 11a.

On the side of the torso 12 of the main body 11, two ports 11c are provided that communicate between the internal space 12h and the outside. These two ports 11c are ports to which one end of a tube or the like is connected. For example, in FIG. 1, one end of a filtrate supply tube 3, the other end of which is connected to the filtrate supply port 20a of the concentrator 20, is connected to the lower port 11c. In other words, the lower port 11c functions as a filtrate discharge port 11c that discharges the filtrate to the outside. On the other hand, the upper port 11c may function as a filtrate discharge port 11c that discharges the filtrate to the outside like the lower port 11c, but it can also function as a port that supplies fluids such as liquids (cleaning fluid, etc.) and gases (air, etc.) from the outside to the torso 12 of the main body 11, or discharges fluids such as liquids (filtrate, cleaning fluid, etc.) and gases (air, etc.) from the torso 12 of the main body 11. In FIG. 5, two ports 11c are provided, but there may be only one port 11c, or three or more ports 11c.

The header section 14 provided at the other end of the main body section 11 is provided with a cleaning liquid supply port 11b that communicates between the internal space and the outside. This cleaning liquid supply port 11b is a port to which one end of a tube or the like is connected. For example, in FIG. 1, one end of a cleaning liquid supply tube 6, the other end of which is connected to a cleaning liquid bag SB, is connected to the cleaning liquid supply port 11b.

The pair of header sections 13, 14 described above correspond to the first liquid supply section and the second liquid supply section in the claims. The pair of header sections 13, 14 may be such that the header section 13 is the first liquid supply section and the header section 14 is the second liquid supply section, or the header section 13 is the second liquid supply section and the header section 14 is the first liquid supply section.

<Function of filter 10>
Since the filter 10 has the above-mentioned configuration, fluids such as liquids and gases can be supplied to and discharged from each of the ports 11a to 11c via tubes or the like.

For example, as shown in FIG. 1, if the raw solution bag UB and the cleaning solution bag SB are connected to each port 11a-11c via each tube, a filtrate obtained by filtering the raw solution can be obtained. That is, the raw solution can be supplied from the raw solution bag UB to the header section 13 of the main body section 11 via the raw solution supply tube 2 and the raw solution supply port 11a by operating the liquid supply tube liquid delivery section 2p. Then, the raw solution is supplied into the through flow passage 16h of the hollow fiber membrane 16 of the hollow fiber membrane bundle 15, and the raw solution is filtered by the hollow fiber membrane 16. That is, the solid content contained in the raw solution cannot pass through the hollow fiber membrane 16 and remains in the through flow passage 16h, and only the liquid content, i.e., the filtrate, passes through the wall 16w of the hollow fiber membrane 16, and a filtrate obtained by filtering the raw solution can be obtained.

When the ports 11a to 11c of the filter 10 are connected as shown in FIG. 1, the filtrate is discharged from the hollow fiber membrane 16 into the internal space 12h of the torso 12 of the main body 11, and then passes through the filtrate discharge port 11c, the filtrate supply tube 3, and the filtrate supply port 20a of the concentrator 20, and is supplied from the internal space 12h to the concentrator 20.

On the other hand, if the circuit shown in FIG. 1 is used, the filter 10 can be cleaned by operating the cleaning liquid recovery tube liquid delivery section 7p (or the liquid supply tube liquid delivery section 2p) to suck the liquid from the filter 10. In other words, the cleaning liquid can be supplied from the cleaning liquid bag SB to the header section 14 of the main body section 11 via the cleaning liquid supply tube 6 and the cleaning liquid supply port 11b, so that the cleaning liquid can be supplied from the header section 14 to the through flow passage 16h of the hollow fiber membrane 16 (see FIG. 5). Then, the cleaning liquid flows from the header section 14 to the header section 13 due to the force of sucking the fluid by the cleaning liquid recovery tube liquid delivery section 7p, so that the inside of the through flow passage 16h of the hollow fiber membrane 16, especially the inner surface of the through flow passage 16 (the inner surface of the wall 16w), can be cleaned by the cleaning liquid flowing along the inner surface of the through flow passage 16. Then, solid matter adhering to the inner wall of the through flow passage 16h of the hollow fiber membrane 16 can be effectively washed away.

<Cleaning of the filter 10>
In particular, the hollow fiber membrane 16 can be effectively washed by the following method.
In the following cleaning operation, the filtering operation is performed in a state where the raw liquid supply port 11a is positioned above the cleaning liquid supply port 11b, and the cleaning operation is performed in the same state.

As shown in FIG. 21, the filtrate supply tube 3 and the connecting tube 9 are blocked by the flow rate adjustment means 3c provided in the filtrate supply tube 3 and the connecting tube liquid delivery section 9p provided in the connecting tube 9. Meanwhile, the cleaning liquid supply tube 6 is opened by the flow rate adjustment means 6c. In this state, the cleaning liquid recovery tube liquid delivery section 7p of the cleaning liquid recovery tube 7 is operated.

As a result, negative pressure is generated in the cleaning liquid recovery tube 7 upstream of the cleaning liquid recovery tube delivery section 7p, i.e., on the filter 10 side. When this negative pressure is generated, the cleaning liquid flows from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 through the cleaning liquid supply tube 6, the cleaning liquid supply port 11b, the header section 14, the through-flow passage 16h of the hollow fiber membrane 16, the header section 13, and the raw liquid supply port 11a, and into the cleaning liquid recovery tube 7.

At this time, since the filtrate supply tube 3 and the connecting tube 9 are blocked, the cleaning liquid does not flow from the hollow fiber membrane 16 into the internal space 12h, but flows only through the through-flow passage 16h of the hollow fiber membrane 16. This allows the cleaning liquid to clean only the pair of headers 13, 14 and the through-flow passage 16h of the hollow fiber membrane 16, so that the amount of cleaning liquid used to clean the filter 10 can be reduced.

In addition, since the internal space 12h is not cleaned, even if the filter 10 is cleaned after filtration and concentration, the filtrate can remain in the internal space 12h. This prevents the filtrate in the internal space 12h from being discharged together with the cleaning liquid, thereby preventing a decrease in the recovery rate of the filtrate.

When cleaning the filter 10, both the liquid supply tube delivery section 2p of the liquid supply tube 2 and the cleaning liquid recovery tube delivery section 7p of the cleaning liquid recovery tube 7 may be operated.
Furthermore, when cleaning the filter 10, the liquid supply tube delivery part 2p may be operated instead of the cleaning liquid recovery tube delivery part 7p. In this case, the stock solution in the through flow passage 16h of the hollow fiber membrane 16 can be recovered in the stock solution bag UB together with the cleaning liquid, so that if the cleaning liquid containing the recovered stock solution is supplied again to the filter 10, it is possible to prevent the amount of stock solution used for filtration and concentration from becoming small.

As described above, when both or either of the liquid supply tube delivery section 2p and the cleaning liquid recovery tube delivery section 7p are operated, negative pressure is also generated in the through-flow passage 16h of the hollow fiber membrane 16. Then, even if solid matter is clogged inside the wall 16w of the hollow fiber membrane 16, this solid matter can be sucked out, and clogging of the wall 16w of the hollow fiber membrane 16 can also be eliminated.

In addition, if the main purpose is to also eliminate clogging of the wall 16w of the hollow fiber membrane 16, a cleaning solution bag SB may be connected to the connecting tube 9 (see FIG. 21), and the connecting tube liquid delivery section 9p may be operated so that the cleaning solution flows from the cleaning solution bag SB toward the filter 10. In this case, the amount of cleaning solution used will be greater because the internal space 12h will also be substantially cleaned, but the clogging of the wall 16w of the hollow fiber membrane 16 will be further eliminated. In other words, in addition to the suction effect due to the negative pressure described above, the cleaning solution is pushed in by the connecting tube liquid delivery section 9p, so that the clogging of the wall 16w of the hollow fiber membrane 16 will be further eliminated. In addition, if the suction effect of the supply tube liquid delivery section 2p and the cleaning solution recovery tube liquid delivery section 7p is sufficiently large, the connecting tube 9 may simply be maintained so that the cleaning solution supplied from the cleaning solution bag SB flows through its interior. For example, simply by providing a clamp or the like to the connecting tube 9 instead of the connecting tube liquid delivery section 9p and leaving the connecting tube 9 open, it is possible to effectively clean the internal space 12h and unclog the wall 16w of the hollow fiber membrane 16.

Furthermore, by carrying out the cleaning operation as described above, it becomes easier to unclog the header section 13 through which the raw liquid is supplied.

In the header section 13 where the raw liquid is supplied, the solids contained in the raw liquid are supplied as they are to the liquid supply tube 2. Therefore, if the solids are large, the opening of the through-flow passage 16h of the hollow fiber membrane 16 may be blocked by the solids. However, as described above, if negative pressure is generated on the filter 10 side of the cleaning liquid recovery tube liquid supply section 7p in the cleaning liquid recovery tube 7, the solids can be sucked out from the header section 13 to the cleaning liquid recovery tube 7 by this negative pressure, so that the clogging of the header section 13 can be eliminated. In this case, the cleaning liquid bag SB may be connected to the connecting tube 9, and the connecting tube liquid supply section 9p may be operated so that the cleaning liquid flows from the cleaning liquid bag SB toward the filter 10. Then, in addition to the sucking effect by the negative pressure described above, the cleaning liquid is pushed in by the connecting tube liquid supply section 9p, so that the clogging of the header section 13 is further easily eliminated.

In the above example, the cleaning liquid is flowed in the opposite direction to the direction in which the raw liquid flows, but the cleaning liquid may be flowed in the same direction as the direction in which the raw liquid flows (i.e., the direction in which the raw liquid flows during filtration and concentration). Even in this case, there is a possibility that clogging of the wall 16w of the hollow fiber membrane 16 can be eliminated. For example, in FIG. 21, a cleaning liquid recovery bag FB is connected to the connecting tube 9 instead of the cleaning liquid bag SB, and the connecting tube liquid sending part 9p is operated so that the liquid flows from the filter 10 to the cleaning liquid recovery bag FB. At that time, if the operation of the liquid supply tube liquid sending part 2p and the cleaning liquid recovery tube liquid sending part 7p is stopped, the cleaning liquid supplied from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 can be flowed so as to permeate the wall 16w of the hollow fiber membrane 16, so that the solid matter clogging the wall 16w of the hollow fiber membrane 16 can be pushed out. In this case, the liquid supply tube liquid sending part 2p or the cleaning liquid recovery tube liquid sending part 7p may also be operated. This makes it possible to simultaneously remove clogging from the walls 16w of the hollow fiber membranes 16 and clean the insides of the through-flow passages 16h of the hollow fiber membranes 16.
In the above-mentioned method (when the cleaning liquid is flowed in the direction in which the raw liquid flows during filtration and concentration), the cleaning liquid may be flowed so as to penetrate the wall 16w of the hollow fiber membrane 16 after cleaning the through-flow passage 16h of the hollow fiber membrane 16. That is, first, the liquid supply tube liquid supply section 2p or the cleaning liquid recovery tube liquid supply section 7p is operated with the operation of the connecting tube liquid supply section 9p stopped. Then, the cleaning liquid can be flowed into the through-flow passage 16h of the hollow fiber membrane 16, so that the inside of the through-flow passage 16h can be cleaned and the deposits in the through-flow passage 16h can be removed. Then, the operation of the liquid supply tube liquid supply section 2p and the cleaning liquid recovery tube liquid supply section 7p is stopped, and the connecting tube liquid supply section 9p is operated. Then, the cleaning liquid can be flowed so as to penetrate the wall 16w of the hollow fiber membrane 16, so that the clogging of the wall 16w of the hollow fiber membrane 16 can be eliminated. Moreover, in the case of this method, since the deposits in the through-flow passages 16h of the hollow fiber membranes 16 are removed in advance, clogging of the walls 16w of the hollow fiber membranes 16 with the deposits can be prevented.

<Another Example of Cleaning the Filter 10>
When cleaning the filter 10 during or after the filtration and concentration operation in the circuit shown in Figures 1, 7, and 11, the through-flow passage 16h of the hollow fiber membrane 16 of the filter 10 and the space of the pair of headers 13 and 14 are filled with the raw liquid, and the internal space 12h of the body 12 is filled with the filtrate. In this state, clogging in a predetermined area of the hollow fiber membrane 16 can be removed by supplying the cleaning liquid from the cleaning liquid supply port 11b and the filtrate discharge port 11c. In other words, clogging in the hollow fiber membrane 16 can be removed up to the position where the internal space 12h of the body is filled with the filtrate (for example, the position H1 in Figure 20).

However, when cleaning the filter 10 during the filtration and concentration work, the filter 10 may be cleaned after first performing either or both of the following: draining the raw liquid from the through-flow passage 16h of the hollow fiber membrane 16 and the space between the pair of headers 13 and 14, and draining the filtrate from the internal space 12h of the body (recovery work described below). In other words, the raw liquid from the through-flow passage 16h of the hollow fiber membrane 16 and the space between the pair of headers 13 and 14 may be left as is, and the filtrate from the internal space 12h of the body may be drained before cleaning the filter 10. Conversely, the filtrate from the through-flow passage 16h of the hollow fiber membrane 16 and the space between the pair of headers 13 and 14 may be left as is, and the raw liquid from the through-flow passage 16h of the hollow fiber membrane 16 and the space between the pair of headers 13 and 14 may be drained before cleaning the filter 10. In this case, even if a liquid such as a cleaning liquid (filling liquid) is supplied into the through-flow passage 16h of the hollow fiber membrane 16 or the internal space 12h of the body 12, clogging of the hollow fiber membrane 16 can only be removed up to the area where the filling liquid is present in the internal space 12h of the body 12 or the through-flow passage 16h of the hollow fiber membrane 16.

Therefore, when performing either or both of the operation of discharging the raw liquid in the through-flow passages 16h of the hollow fiber membrane 16 and in the spaces of the pair of headers 13, 14 and the operation of discharging the filtrate in the internal space 12h of the body portion (the recovery operation described later), it is desirable to supply the cleaning liquid to the filter 10 so that the cleaning liquid permeates the hollow fiber membrane 16 in a state where the hollow space 12h of the body portion 12 and/or the through-flow passages 16h of the hollow fiber membrane 16 are filled with the filling liquid up to the region of the hollow fiber membrane 16 where cleaning is to be performed. In other words, it is desirable to supply the cleaning liquid to the filter 10 so that the cleaning liquid permeates the hollow fiber membrane 16 in a state where the whole or part of the hollow fiber membrane 16 is filled with the filling liquid.
In addition, when the cleaning liquid is flowed from the outside of the hollow fiber membrane 16, that is, from the internal space 12h of the body, into the through passage 16h of the hollow fiber membrane 16, the through passage 16h of the hollow fiber membrane 16 does not necessarily have to be filled with the filling liquid up to the region to be cleaned. However, the internal space 12h of the body 12 needs to be filled with the filling liquid up to the region to be cleaned. In addition, when the cleaning liquid is flowed from the inside of the hollow fiber membrane 16, that is, from the through passage 16h of the hollow fiber membrane 16 into the internal space 12h of the body (when the cleaning liquid is flowed in the direction in which the raw liquid flows during the above-mentioned filtration concentration), the through passage 16h of the hollow fiber membrane 16 needs to be filled with the filling liquid up to the region to be cleaned.

The filling liquid filling the hollow space 12h of the body 12 and/or the through-flow passage 16h of the hollow fiber membrane 16 is not limited to the cleaning liquid used for cleaning (e.g., physiological saline, infusion (extracellular fluid), etc.). For example, waste liquid or a liquid containing a substance that enhances the cleaning effect (e.g., a surfactant, etc.) can also be used as the filling liquid.
The cleaning liquid used for cleaning is not particularly limited as long as it is a liquid that can be used for cleaning. For example, waste liquid or a liquid containing a substance that enhances the cleaning effect (e.g., a surfactant) can be used as the cleaning liquid.
In the following description, a case will be described in which a cleaning liquid that is generally used for cleaning is used as the filling liquid and the cleaning liquid.

For example, in FIG. 21, first, the filtrate supply tube 3 is blocked by the flow rate adjustment means 3c, and both the supply tube delivery section 2p and the cleaning liquid recovery tube delivery section 7p are stopped. The cleaning liquid supply tube 6 is also blocked by the flow rate adjustment means 6c. When the hollow space 12h of the body 12 is filled with cleaning liquid, the upper port 11c is opened to the atmosphere. When the through-flow passage 16h of the hollow fiber membrane 16 is filled with cleaning liquid, the part of the supply tube 2 and/or the cleaning liquid recovery tube 7 that is closer to the through-flow passage 16h of the hollow fiber membrane 16 than the supply tube delivery section 2p and/or the cleaning liquid recovery tube delivery section 7p (for example, the position of the pressure gauge P2 in FIG. 21) is opened to the atmosphere. In this state, the connecting tube delivery section 9p is operated to supply cleaning liquid from the cleaning liquid bag SB into the hollow space 12h of the body 12. Then, the cleaning solution is filled into the hollow space 12h of the body 12 and/or into the through passage 16h of the hollow fiber membrane 16 up to the area to be cleaned, for example, the area where the filtrate was present during the filtration and concentration process (for example, the height H1 in FIG. 20).

After the above-mentioned area is filled with the cleaning liquid, the flow rate adjustment means 6c opens the cleaning liquid supply tube 6 while the connecting tube delivery section 9p is still in operation, and the cleaning liquid recovery tube delivery section 7p is activated. Then, the hollow fiber membrane 16 and the hollow space 12h of the body 12 can be cleaned with the cleaning liquid supplied from the cleaning liquid supply tube 6 and the cleaning liquid bag SB connected to the connecting tube 9, and clogging of the hollow fiber membrane 16 in the area to be cleaned can be eliminated.

While cleaning is being performed, the control unit 106 controls the flow rate of the cleaning liquid recovery tube delivery unit 7p to be slightly higher than the flow rate of the cleaning liquid supplied from the connecting tube 9. In other words, cleaning is performed so that the cleaning liquid supplied from the cleaning liquid supply tube 6 flows through the through-flow path 16h of the hollow fiber membrane 16 while maintaining the state in which the cleaning liquid is present up to the area where the filtrate was present during the filtration and concentration work.

Furthermore, before cleaning, instead of carrying out a separate operation of filling the cleaning liquid up to the area to be cleaned, the cleaning liquid supply tube 6 may be opened by the flow rate adjustment means 6c, and the connecting tube supply part 9p may be operated while the cleaning liquid recovery tube supply part 7p is operated to supply the cleaning liquid from the cleaning liquid bag SB into the hollow space 12h of the body part 12. Even in this case, by controlling the operation of the connecting tube supply part 9p and the cleaning liquid recovery tube supply part 7p by the control part 106, the cleaning liquid can be filled up to the area to be cleaned in the hollow space 12h of the body part 12.
For example, the cleaning liquid supply tube 6 is closed by the flow rate adjustment means 6c, the upper port 11c is opened to the atmosphere, and the connecting tube liquid sending part 9p and the cleaning liquid recovery tube liquid sending part 7p are operated. At this time, the flow rate of the cleaning liquid supplied from the connecting tube 9 is set to be greater than the flow rate sucked out by the cleaning liquid recovery tube liquid sending part 7p. Then, over time, the cleaning liquid can be filled into the hollow space 12h of the body part 12 up to the area to be cleaned. After that, the cleaning liquid supply tube 6 is opened by the flow rate adjustment means 6c, the upper port 11c is closed, and the flow rate of the cleaning liquid supplied from the connecting tube 9 is made less than the flow rate sucked out by the cleaning liquid recovery tube liquid sending part 7p, so that cleaning can be performed in a stable state. In other words, cleaning of the hollow fiber membrane 16 can be performed while maintaining a state in which the cleaning liquid is filled into the hollow space 12h of the body part 12 up to the area to be cleaned.
In addition, the cleaning liquid in the hollow space 12h of the body 12 may be sucked out by a pump provided on a tube connected to the upper port 11c until the cleaning liquid is filled in the hollow space 12h of the body 12 up to the region where cleaning is performed. In this case, the cleaning liquid supply tube 6 may be opened by the flow rate adjustment means 6c while the flow rate of the cleaning liquid supplied from the connecting tube 9 is made larger than the flow rate sucked out by the cleaning liquid recovery tube liquid feeder 7p. Even in this case, if the cleaning liquid is filled in the hollow space 12h of the body 12 up to the region where cleaning is performed, the cleaning can be performed in a stable state by closing the upper port 11c and making the flow rate of the cleaning liquid supplied from the connecting tube 9 smaller than the flow rate sucked out by the cleaning liquid recovery tube liquid feeder 7p. In other words, the cleaning of the hollow fiber membrane 16 can be performed while maintaining the state in which the cleaning liquid is filled in the hollow space 12h of the body 12 up to the region where cleaning is performed.
Furthermore, even if the flow rate of the cleaning liquid supplied from the connecting tube 9 and the flow rate sucked out by the cleaning liquid recovery tube delivery section 7p are set to the same flow rate, it is possible to fill the through flow passage 16h of the hollow fiber membrane 16 with cleaning liquid up to the area to be cleaned, and to perform cleaning in a state in which the through flow passage 16h of the hollow fiber membrane 16 is filled with cleaning liquid up to the area to be cleaned.

The cleaning liquid is filled up to the area where cleaning is performed, but the area where cleaning is performed is not necessarily limited to the area where the filtrate was present during the filtration and concentration work, and may be a smaller area than this area (for example, up to the height of H3 in FIG. 20) or a larger area than this area (for example, up to the height of H2 in FIG. 20). The entire hollow space 12h of the body 12 may be filled with cleaning liquid. Furthermore, in the case where the filtrate supply tube 3 is connected only to the lower port 11c (filtrate discharge port 11c) of the pair of ports 11c, 11c as shown in FIG. 20, the entire hollow space 12h may be filled with cleaning liquid up to a position where the cleaning liquid does not leak from the upper port 11c (up to the height of H2 in FIG. 20).

In the above example, the axial direction of the hollow fiber membrane 16 of the filter 10 is vertical, but the filter 10 may be arranged so that the axial direction of the hollow fiber membrane 16 is approximately horizontal. In this case, it is desirable to perform the cleaning operation so that the entire hollow fiber membrane 16 is immersed in the cleaning liquid (or after filling the hollow space 12h of the body 12 with cleaning liquid so that the entire hollow fiber membrane 16 is immersed in the cleaning liquid). Of course, depending on the position of the port 11c, the cleaning operation may be performed so that only a part of the hollow fiber membrane 16 is immersed in the cleaning liquid (or after filling the hollow space 12h of the body 12 with cleaning liquid so that a part of the hollow fiber membrane 16 is immersed in the cleaning liquid). An example of a state in which only a portion of the hollow fiber membrane 16 is immersed in the cleaning liquid is when the entire hollow fiber membrane 16 cannot be immersed in the cleaning liquid, but the cleaning liquid does not leak from the port 11c to which the filtrate supply tube 3 is not connected.

In the above example, the case where the cleaning liquid is supplied from the connecting tube 9 connected to the filtrate supply tube 3 into the hollow space 12h of the body 12 has been described, but the cleaning liquid does not have to be supplied through the filtrate supply tube 3. For example, as shown in FIG. 20, when the filtrate supply tube 3 is connected only to the lower port 11c (filtrate discharge port 11c) of the pair of ports 11c, 11c, the cleaning liquid may be supplied only from the upper discharge port 11c. In addition, when the cleaning liquid is supplied into the hollow space 12h of the body 12 through the filtrate supply tube 3, the cleaning liquid may be supplied to the concentrator 20 connected to the filtrate supply tube 3, and the cleaning liquid that has passed through the concentrator 20 may be supplied into the hollow space 12h of the body 12. In this case, when the filter 10 is washed, the concentrator 20 can also be washed (for example, the inside of the hollow fiber membrane of the filter 20).

For example, as shown in FIG. 22, cleaning liquid is supplied from a cleaning liquid bag SB to the concentrator 20 directly to the concentrated liquid outlet 20b of the concentrator 20, or via a concentrated liquid tube 4 connected to the concentrated liquid outlet 20b. The supplied cleaning liquid then passes through the concentrator 20, flows from the filtrate supply port 20a into the filtrate supply tube 3, and is supplied from the filtrate supply tube 3 through the filtrate discharge port 11c into the hollow space 12h of the body 12 of the filter 10. In other words, the cleaning liquid supplied to the concentrator 20 can be used not only for cleaning the concentrator 20, but also for cleaning the filter 10.

In this case, the substance in the concentrator 20 will flow into the hollow space 12h of the body 12. However, this substance is the filtrate discharged from the filter 10 or a substance that was contained in the filtrate, and there is no problem if it flows into the hollow space 12h of the body 12. The filtrate diluted with the cleaning liquid can be concentrated again.
Furthermore, the cleaning liquid may be supplied to the concentrator 20 through the waste liquid outlet 20c instead of the concentrated liquid outlet 20b. If the cleaning liquid is supplied to the concentrator 20 through the waste liquid outlet 20c, the cleaning liquid can be made to flow in a direction perpendicular to the wall 16w of the hollow fiber membrane 16. In other words, the cleaning liquid can be supplied in a direction in which the cleaning liquid permeates the wall 16w of the hollow fiber membrane 16, which provides the advantage that the clogging components accumulated in the concentrator 20 can be efficiently washed away and cleaned.

<Detailed Description of Concentrator 20>
In the raw liquid treatment device 1 of the first embodiment, it is preferable that each tube to the concentrator 20 is connected as follows. The configuration of the concentrator 20 and the connection of each tube to the concentrator 20 will be described below.

The concentrator 20 receives the filtrate from the filter 10 and concentrates the filtrate. The concentrator 20 has a structure substantially similar to that of the filter 10 described above, and has a function of separating water from the filtrate to produce a concentrated liquid. In other words, the concentrator 20 has a structure in which a water separation member that has a function of separating water from the filtrate is housed inside instead of the separation member of the filter 10. For example, the concentrator 20 can be an ascites concentrator used in CART, a dialysis filter used in dialysis, or a membrane-type plasma component fractionator used in double filtration plasma exchange therapy.

To explain this concentrator 20 in detail, the concentrator 20 has a filtrate supply port 20a that is connected to the filtrate discharge port 11c of the filter 10 by a filtrate supply tube 3. In other words, the filtrate, which is the liquid to be concentrated, is supplied to the concentrator 20 from this filtrate supply port 20a.

The concentrator 20 also has a waste liquid outlet 20c for discharging the liquid separated from the filtrate (separated liquid, waste liquid), i.e., moisture, etc. This waste liquid outlet 20c is connected to the waste liquid bag DB via the waste liquid tube 5. The concentrator 20 also has a concentrated liquid outlet 20b from which the concentrated liquid is discharged. This concentrated liquid outlet 20b is connected to the concentrated liquid bag CB via the concentrated liquid tube 4.

The concentrator 20 is equipped with a water separation member. This water separation member has the function of allowing water to pass through but not allowing useful components such as useful proteins contained in the plasma to pass through. If the concentrator 20 has a structure as shown in Figure 5, the hollow fiber membrane bundle 15 in Figure 5 serves as the water separation member.

Therefore, when filtrate is supplied into the concentrator 20 from the filtrate supply port 20a, the moisture is separated from the filtrate by the moisture separating member, and the separated moisture is discharged from the waste liquid discharge port 20c and supplied to the waste liquid bag DB through the waste liquid tube 5. On the other hand, the concentrated liquid from which some of the moisture has been removed is discharged from the concentrate discharge port 20b, and the discharged concentrate is supplied to the concentrate bag CB through the concentrate tube 4 (see Figure 1).

In addition, when the concentrator 20 has a hollow fiber membrane as a moisture separating member, it has a structure substantially similar to that of the filter 10 (see FIG. 5). That is, it has a structure having a body part having a hollow space for accommodating a plurality of hollow fiber membranes (or a hollow fiber membrane bundle in which a plurality of hollow fiber membranes are bundled) which are moisture separating members, and a pair of header parts in which both ends of the plurality of hollow fiber membranes are connected. The pair of header parts have ports serving as the filtrate supply port 20a and the concentrated liquid discharge port 20b, and the body part has a port serving as the waste liquid discharge port 20c. For example, the port 11a provided in the header part 13 in FIG. 5 becomes the filtrate supply port 20a, and the port 11b provided in the header part 14 in FIG. 5 becomes the concentrated liquid discharge port 20b. Also, the port 11c provided in the body part 12 in FIG. 5 becomes the waste liquid discharge port 20c. (See FIG. 5).
In the case of concentrator 20 having such a structure, the pair of header sections described above (the pair of header sections 13, 14 in Figure 5) correspond to the first liquid supply section and the second liquid supply section as defined in the claims.

In addition, if the concentrator 20 has a structure substantially similar to that of the filter 10, cleaning it using the same cleaning method as the filter 10 described above can effectively remove blockages in the hollow fiber membrane and clean the flow path within the hollow fiber membrane.

For example, in the case of FIG. 21, first, the filtrate supply tube 3 is blocked by the flow rate adjustment means 3c. Also, the concentrated liquid tube 4 is also blocked by stopping the operation of the concentrated liquid tube delivery section 4p. Then, when filling the hollow space in the body of the concentrator 20 with cleaning liquid, the upper port 20c of the two ports 20c is opened to the atmosphere. Also, when filling the through-flow passage of the hollow fiber membrane with cleaning liquid, the part of the filtrate supply tube 3 that is closer to the hollow space in the body than the flow rate adjustment means 3c is opened to the atmosphere. In this state, a cleaning liquid bag SB is connected to the other end of the waste liquid tube 5 connected to the lower port 20c instead of the waste liquid bag DB, and cleaning liquid is supplied from the cleaning liquid bag SB into the hollow space in the body of the concentrator 20. Then, the cleaning liquid is filled into the hollow space in the body, up to the area where cleaning is to be performed, for example, the area where waste liquid was present during the filtration and concentration work.

After the above-mentioned area is filled with the cleaning solution, the flow rate adjustment means 3c opens the filtrate supply tube 3, the connecting tube liquid delivery section 9p is operated to supply the cleaning solution from the cleaning solution bag SB connected to the connecting tube 9 to the concentrator, and the concentrated solution tube liquid delivery section 4p is also operated. This allows the hollow fiber membrane in the concentrator 20 and the hollow space in the body to be cleaned, and clogging of the hollow fiber membrane 16 in the area to be cleaned can be eliminated.

During the cleaning process, the control unit 106 controls the flow rate of the concentrated liquid tube delivery unit 4p to be slightly higher than the flow rate of the cleaning liquid supplied from the connecting tube delivery unit 9p. In other words, cleaning is performed so that the cleaning liquid supplied from the waste liquid tube 5 permeates the hollow fiber membrane 16 while maintaining the state in which the cleaning liquid is present up to the area where the concentrated liquid was present during the filtration and concentration process.

In addition, while the cleaning liquid is being supplied from the port serving as the waste liquid outlet 20c into the hollow space 12h of the body 12 of the concentrator 20, the concentrated liquid tube supply unit 4p may be operated while the connecting tube supply unit 9p is operated to supply the cleaning liquid from the cleaning liquid bag SB into the hollow space 12h of the body 12. Even in this case, if the control unit 106 controls the operation of the connecting tube supply unit 9p and the concentrated liquid tube supply unit 4p, the cleaning liquid can be filled up to the area to be cleaned in the hollow space 12h of the body 12. In this case, the flow rate of the cleaning liquid supplied from the connecting tube supply unit 9p is set to be higher than the flow rate of the concentrated liquid tube supply unit 4p sucking out until the cleaning liquid is filled up to the area to be cleaned. Then, when the cleaning liquid is filled up to the area to be cleaned, the control unit 106 may control the flow rate of the concentrated liquid tube supply unit 4p sucking out to be slightly higher than the flow rate of the cleaning liquid supplied from the connecting tube supply unit 9p.

The cleaning liquid is filled up to the area where cleaning is to be performed, but the area where cleaning is to be performed is not necessarily limited to the area where the concentrated liquid was present during the filtration and concentration process, and may be a smaller area than this area (for example, up to the height of H3 in FIG. 20) or a larger area than this area. The entire hollow space 12h of the body may be filled with cleaning liquid. Furthermore, in cases where the waste liquid tube 5 is connected only to the lower port 20c of the pair of ports 20c, 20c, the entire hollow space may be filled with cleaning liquid up to a position where cleaning liquid does not leak from the upper port 20c (up to the height of H2 in FIG. 20).

In the above example, the axial direction of the hollow fiber membrane of the concentrator 20 faces the vertical direction, and the filtrate supply port 20a is located above the concentrated liquid discharge port 20b, and the concentration operation is performed in the same state, and the cleaning operation is performed in the same state. The concentrator 20 may be arranged so that the axial direction of the hollow fiber membrane faces approximately horizontally. In this case, it is desirable to perform the cleaning operation so that the entire hollow fiber membrane is immersed in the cleaning liquid (or after filling the hollow space of the body with cleaning liquid so that the entire hollow fiber membrane is immersed in the cleaning liquid). Of course, depending on the position of the port 20c, the cleaning operation may be performed so that only a part of the hollow fiber membrane is immersed in the cleaning liquid (or after filling the hollow space of the body with cleaning liquid so that a part of the hollow fiber membrane is immersed in the cleaning liquid). An example of a state in which only a portion of the hollow fiber membrane is immersed in the cleaning liquid is when the entire hollow fiber membrane cannot be immersed in the cleaning liquid, but the cleaning liquid does not leak from port 20c to which the waste liquid tube 5 is not connected.

<Circuit configuration of the raw liquid treatment device 1 according to the first embodiment>
Next, the circuit configuration of the raw liquid treatment apparatus 1 of the first embodiment will be described with reference to FIG.

In the following, we will explain the case where the raw fluid to be treated is pleural and ascites fluid.

In the following description, each flow path (supply flow path, filtrate supply flow path, concentrate flow path, waste liquid flow path, cleaning liquid supply flow path, cleaning liquid recovery flow path, connecting flow path) in the claims is formed of a flexible tube (supply tube 2, filtrate supply tube 3, concentrate tube 4, waste liquid tube 5, cleaning liquid supply tube 6, cleaning liquid recovery tube 7, connecting tube 9). However, each flow path may be formed of a tube that is not flexible or flexible (e.g., a hard plastic pipe, a steel pipe, a PVC pipe, etc.), or an integrated circuit in which all or some of the flow paths are integrally formed by resin molding, etc.

Furthermore, since the raw liquid treatment device 1 of the first embodiment has a pair of roller pumps 110, 120, the following description will be given on the assumption that each flow path is formed of a tube having flexibility and pliability, and a roller pump is used as the liquid delivery section of each flow path. However, in the raw liquid treatment device 1 of the first embodiment, the liquid delivery section is not limited to a roller pump, and various devices capable of delivering the liquid in each flow path can be adopted. The liquid delivery section may be appropriately selected according to the material of the tube constituting each flow path and the liquid flowing in the flow path. For example, an infusion pump, a diaphragm pump, or the like may be used as the liquid delivery section. In addition, since the roller pump exerts a clamping function (a function of blocking the flow path to prevent the liquid from flowing) when it stops operating, in the following description, no device having a clamping function is provided in the flow path provided with the liquid delivery section. However, when a device that does not exert a clamping function even when the operation is stopped or a device that does not have a clamping function is used as the liquid delivery unit, a separate tool having a clamping function (e.g., a clamp, a clip, a solenoid valve, etc.) may be provided in the flow path in which the liquid delivery unit is provided, and the tool having the clamping function may exert the clamping function when the operation of the liquid delivery unit is stopped. When a solenoid valve is used, it becomes possible to exert the clamping function at the same time as the operation of the liquid delivery unit is stopped by the control unit 106 or at a desired timing.
In addition, since the operation of each liquid delivery unit is controlled by the above-mentioned control unit 106, the following description will be given on the assumption that each liquid delivery unit is controlled by the control unit 106.

<Overall configuration of the raw liquid treatment device 1 according to the first embodiment>
First, a schematic configuration of a raw liquid treatment apparatus 1 according to a first embodiment will be described.

In FIG. 1, the symbol UB indicates a raw liquid bag that contains raw liquid, such as pleural or ascites fluid drawn from the chest or abdomen. The symbol CB indicates a concentrated liquid bag that contains concentrated liquid obtained by filtering and concentrating the raw liquid. The symbol DB indicates a waste liquid bag that contains waste liquid (i.e., water) separated from the concentrated liquid. The symbol SB indicates a washing liquid bag that contains washing liquid such as saline or infusion (extracellular fluid), and the symbol FB indicates a washing liquid recovery bag for recovering the washing liquid.

As shown in FIG. 1, in the first embodiment of the raw liquid treatment device 1, the raw liquid bag UB is connected to the filter 10 via a liquid supply tube 2. The liquid supply tube 2 is a tube that supplies the raw liquid in the raw liquid bag UB to the filter 10. The liquid supply tube 2 is provided with a liquid supply tube liquid supply section 2p that delivers the liquid in the liquid supply tube 2.

The filter 10 filters the raw liquid to produce a filtrate. This filter 10 is connected to the concentrator 20 via a filtrate supply tube 3. The filtrate supply tube 3 is a tube that supplies the filtrate produced by the filter 10 to the concentrator 20. This filtrate supply tube 3 is provided with a flow rate adjustment means 3c, such as a clamp, clip, or solenoid valve, that stops and opens the flow of liquid in the filtrate supply tube 3.

One end of a connecting tube 9 is connected to the filtrate supply tube 3 between the filter 10 and the flow rate adjustment means 3c. The connecting tube 9 is provided with a connecting tube liquid delivery section 9p that delivers the liquid in the connecting tube 9.

The filter 10 is also connected to a cleaning solution bag SB via a cleaning solution supply tube 6. The cleaning solution supply tube 6 is a tube that supplies cleaning solution from the cleaning solution bag SB to the filter 10. The cleaning solution supply tube 6 is provided with a flow rate adjustment means 6c, such as a clamp, clip, or solenoid valve, that stops and opens the flow of liquid in the cleaning solution supply tube 6.

Furthermore, the filter 10 is connected to a cleaning liquid recovery bag FB that recovers the cleaning liquid used to clean the filter 10 via a cleaning liquid recovery tube 7. This cleaning liquid recovery tube 7 is provided with a cleaning liquid recovery tube liquid delivery section 7p that delivers the liquid in the cleaning liquid recovery tube 7.

The cleaning liquid collection tube 7 may be connected to the filter 10 via the liquid supply tube 2, or may be connected directly to the filter 10.

The concentrator 20 produces a concentrated liquid by concentrating the filtrate. The concentrator 20 is connected to the concentrated liquid bag CB via the concentrated liquid tube 4. The concentrated liquid tube 4 is a tube that supplies the concentrated liquid concentrated by the concentrator 20 to the concentrated liquid bag CB. The concentrated liquid tube 4 is provided with a concentrated liquid tube delivery section 4p that delivers the liquid in the concentrated liquid tube 4. Instead of the concentrated liquid tube delivery section 4p, a waste liquid tube delivery section 5p may be provided in the waste liquid tube 5 (see FIG. 4). Even in this case, if the waste liquid tube delivery section 5p reduces the amount of waste liquid delivered under conditions in which the concentrated liquid tube delivery section 4p increases the amount of concentrated liquid delivered, and if the waste liquid tube delivery section 5p increases the amount of waste liquid delivered under conditions in which the concentrated liquid tube delivery section 4p decreases the amount of concentrated liquid delivered, the function can be the same as when the concentrated liquid tube 4 is provided with the concentrated liquid tube delivery section 4p. The case in which the concentrated liquid tube 4 is provided with the concentrated liquid tube delivery section 4p will be described below.

The concentrator 20 is also connected to a waste liquid bag DB via a waste liquid tube 5. The waste liquid tube 5 is a tube that supplies the waste liquid (water) separated from the concentrated liquid in the concentrator 20 to the waste liquid bag DB.

As a result of the above configuration, in the raw liquid treatment device 1 of the first embodiment, if the raw liquid is supplied from the raw liquid bag UB to the filter 10 via the liquid supply tube 2, the raw liquid can be filtered by the filter 10 to produce a filtrate. If the filtrate produced via the filtrate supply tube 3 is supplied to the concentrator 20, a concentrated liquid can be produced by the concentrator 20, and this concentrated liquid can be collected in the concentrated liquid bag CB via the concentrated liquid tube 4.

On the other hand, if cleaning liquid is supplied to the filter 10 from a cleaning liquid bag SB connected to the cleaning liquid supply tube 6, the filter 10 can be cleaned with the cleaning liquid. Also, if a cleaning liquid bag SB is connected to the concentrated liquid tube 4 instead of the concentrated liquid bag CB, the concentrator 20 can be cleaned with the cleaning liquid (see Figure 2).

When a cleaning solution bag SB is connected to the concentrated solution tube 4 instead of the concentrated solution bag CB, the cleaning solution used to clean the concentrator 20 can be supplied to the filter 10 through the filtrate supply tube 3. In other words, it is possible to clean the concentrator 20 and the filter 10 at the same time.

The operation of the first embodiment of the raw liquid treatment device 1 is described below.

<Preparatory cleaning work>
2, in the preparatory cleaning operation of the raw liquid treatment device 1 of the first embodiment, a cleaning liquid bag SB is connected to the other end of the concentrated liquid tube 4 instead of the concentrated liquid bag CB, and a cleaning liquid recovery bag FB is connected to the other end of the waste liquid tube 5 instead of the waste liquid bag DB. The other end of the waste liquid tube 5 may be left connected to the waste liquid bag DB, or the other end of the waste liquid tube 5 may be simply placed in a bucket or the like.
A cleaning liquid recovery bag FB is connected to the other end of the liquid supply tube 2 instead of the stock solution bag UB. A waste liquid bag DB may be connected to the other end of the liquid supply tube 2, or the other end of the liquid supply tube 2 may be simply placed in a bucket or the like.
A cleaning liquid recovery bag FB is also connected to the other end of the connecting tube 9. A waste liquid bag DB may be connected to the other end of the connecting tube 9, or the other end of the connecting tube 9 may be simply placed in a bucket or the like.

Next, the flow rate adjustment means 3c and the flow rate adjustment means 6c are opened to allow the cleaning liquid to flow through the filtrate supply tube 3 and the cleaning liquid supply tube 6.

In the above state, the concentrated liquid tube delivery unit 4p is operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the concentrated liquid tube 4 to the concentrator 20, and the connecting tube delivery unit 9p is operated to flow the cleaning liquid from the concentrator 20 (i.e., the filtrate supply tube 3) to the cleaning liquid recovery bag FB connected to the connecting tube 9. Then, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the concentrated liquid tube 4 to the concentrator 20 through the concentrated liquid tube 4. The supplied cleaning liquid passes through the concentrator 20, then passes through the filtrate supply tube 3 and the connecting tube 9, and is collected in the cleaning liquid recovery bag FB connected to the connecting tube 9. Note that a part of the cleaning liquid passes through the waste liquid tube 5 and is collected in the cleaning liquid recovery bag FB connected to the other end of the waste liquid tube 5.

The connecting tube liquid sending section 9p is operated to flow the cleaning liquid from the concentrator 20 to the cleaning liquid recovery bag FB connected to the connecting tube 9, and the liquid supply tube liquid sending section 2p is operated to flow the cleaning liquid from the filter 10 to the cleaning liquid recovery bag FB connected to the liquid supply tube 2. Then, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 to the filter 10 through the cleaning liquid supply tube 6. After passing through the filter 10, a part of the supplied cleaning liquid passes through the filtrate supply tube 3 and the connecting tube 9 to be collected in the cleaning liquid recovery bag FB connected to the connecting tube 9, and a part passes through the liquid supply tube 2 to be collected in the cleaning liquid recovery bag FB connected to the liquid supply tube 2. In addition, by operating the cleaning liquid recovery tube liquid sending section 7p, a part of the cleaning liquid supplied to the filter 10 can also be flowed to the cleaning liquid recovery tube 7.

This allows the cleaning liquid to flow through the filter 10, the concentrator 20, and all the tubes, so that the entire raw liquid treatment device 1 of the first embodiment can be cleaned.

In FIG. 2, the inside of the filter 10 is cleaned by operating the liquid supply tube delivery section 2p and the cleaning liquid recovery tube delivery section 7p to suck the cleaning liquid out of the filter 10 and generate a flow of the cleaning liquid within the filter 10. However, the inside of the filter 10 may also be cleaned by forcing the cleaning liquid into the filter 10 to generate a flow of the cleaning liquid within the filter 10.

2, for example, a cleaning liquid supply tube delivery section 6p is provided in the cleaning liquid supply tube 6 instead of the flow rate adjustment means 6c, and a cleaning liquid recovery tube delivery section 7p is provided in the cleaning liquid recovery tube 7 instead of the cleaning liquid recovery tube delivery section 7p. The cleaning liquid recovery tube 7 is opened by the flow rate adjustment means 7c, and the cleaning liquid supply tube delivery section 6p is operated so that the cleaning liquid flows in the cleaning liquid supply tube 6 from the cleaning liquid bag SB toward the filter 10. Then, the cleaning liquid is pushed into the filter 10, and a flow of the cleaning liquid can be generated in the filter 10, so that the inside of the filter 10 can be cleaned with the cleaning liquid. In this case, the supply tube delivery section 2p of the supply tube 2 may be operated to suck out the cleaning liquid from the filter 10, and the cleaning liquid may be flowed into the supply tube 2. Alternatively, the supply tube delivery section 2p may not be operated, and the cleaning liquid may be flowed only into the cleaning liquid recovery tube 7.

<Filtration and concentration work>
Once the preparatory cleaning process is completed, the filtration and concentration process is carried out.

As shown in Figure 1, in the filtration and concentration operation of the raw liquid treatment device 1 of the first embodiment, from the state of the preparatory cleaning operation (see Figure 2), a concentrate bag CB is connected to the concentrate tube 4 instead of the cleaning liquid bag SB, and a waste liquid bag DB is connected to the waste liquid tube 5 instead of the cleaning liquid recovery bag FB.
On the other hand, a stock solution bag UB is connected to the liquid supply tube 2 in place of the cleaning solution recovery bag FB.
Further, the flow rate adjusting means 3c maintains a state in which liquid can flow through the filtrate supply tube 3, while the flow rate adjusting means 6c blocks liquid from flowing through the cleaning liquid supply tube 6. In addition, the cleaning liquid recovery tube sending part 7p and the connecting tube sending part 9p are not operated, and function as clamps.

In the above state, the liquid supply tube delivery unit 2p is operated to flow the raw liquid from the raw liquid bag UB connected to the liquid supply tube 2 to the filter 10, and the concentrated liquid tube delivery unit 4p is operated to flow the concentrated liquid from the concentrator 20 to the concentrated liquid bag CB connected to the concentrated liquid tube 4.

The raw liquid is then supplied from the raw liquid bag UB to the filter 10 through the liquid supply tube 2. The supplied raw liquid is filtered by the filter 10, and the resulting filtrate is supplied to the concentrator 20 through the filtrate supply tube 3. The filtrate supplied to the concentrator 20 is then concentrated by the concentrator 20, and the resulting concentrated liquid is collected in the concentrated liquid bag CB through the concentrated liquid tube 4. Meanwhile, the water separated from the concentrated liquid is collected in the waste liquid bag DB through the waste liquid tube 5.

<About filtration and concentration operations>
Here, in the filtration and concentration operation, the operation of the liquid supply tube delivery section 2p and the concentrated liquid tube delivery section 4p is controlled so that the concentration ratio is within a predetermined range. However, as described below, the operation of the liquid supply tube delivery section 2p and the concentrated liquid tube delivery section 4p, that is, the flow rate through the liquid supply tube delivery section 2p and the concentrated liquid tube delivery section 4p, may be controlled by utilizing the filter transmembrane pressure difference and the concentrator transmembrane pressure difference. In this way, the capacity of the filter 10 and the concentrator 20 can be effectively utilized to perform filtration and concentration, so that the time required to produce the concentrated liquid can be shortened and the efficiency of the concentration operation can be increased.
In the following, the operation of filtering and concentrating by controlling the operation of the liquid supply tube sending section 2p and the concentrated liquid tube sending section 4p using the filter transmembrane pressure difference and the concentrator transmembrane pressure difference will be described.

The filter transmembrane pressure difference means the pressure difference between the liquid supply side and the liquid discharge side of a filtering member (e.g., hollow fiber membrane) of the filter 10. For example, if the filtering member of the filter 10 is a hollow fiber membrane 16, the difference between the pressure in the through flow passage 16h of the hollow fiber membrane 16 and the pressure in the hollow space 12h of the body 12 corresponds to the filter transmembrane pressure difference.
The concentrator transmembrane pressure difference means the pressure difference between the liquid supply side and the liquid discharge side of a water separation member (e.g., hollow fiber membrane) of the concentrator 20. For example, if the filtration member of the concentrator 20 is a hollow fiber membrane, the difference between the pressure in the through passage of the hollow fiber membrane and the pressure in the hollow space of the body corresponds to the concentrator transmembrane pressure difference.

The filter transmembrane pressure and the concentrator transmembrane pressure can be calculated by measuring the pressure inside the tubes connected to the filter 10 and the concentrator 20. For example, if a pressure gauge is provided in the liquid supply tube 2 and the filtrate supply tube 3 and the signal is supplied to the control unit 106, the control unit 106 can calculate the filter transmembrane pressure. As shown in FIG. 1, even if a pressure gauge is provided in the port 11c (or the tube connected to this port 11c) to which the filtrate supply tube 3 is not connected, the control unit 106 can calculate the filter transmembrane pressure. Also, if a pressure gauge is provided in the filtrate supply tube 3 and the waste liquid tube 5 and the signal is supplied to the control unit 106, the control unit 106 can calculate the concentrator transmembrane pressure. If there is a port 20c to which the waste liquid tube 5 is not connected, the control unit 106 can calculate the concentrator transmembrane pressure even if a pressure gauge is provided in this port 20c (or the tube connected to this port 20c).

In addition, in the filter 10 or the concentrator 20, if either the liquid supply side or the liquid discharge side is close to being open to the atmosphere, the control unit 106 can calculate the filter transmembrane pressure or the concentrator transmembrane pressure by simply measuring the pressure inside the tube connected to the side of the liquid supply side or the liquid discharge side that is not open to the atmosphere. In other words, instead of the filter transmembrane pressure or the concentrator transmembrane pressure, the control unit 106 can control the operation of the liquid delivery unit by using only the pressure inside the tube connected to the side that is not open to the atmosphere. For example, if the tube connected to the filter 10 or the concentrator 20 is connected to a bag and is not blocked by the liquid delivery unit or the flow rate adjustment means, the tube can be considered to be close to being open to the atmosphere. In the state of FIG. 1, the liquid supply tube 2 connected to the raw liquid bag UB of the tubes 2 and 3 connected to the filter 10 can also be considered to be open to the atmosphere. In addition, the liquid discharge tube 5 connected to the waste liquid bag DB of the tubes 3 and 5 connected to the concentrator 20 can also be considered to be open to the atmosphere. In this state, as shown in FIG. 1, the control unit 106 can control the operation of the liquid delivery unit using only the internal pressure of the filter supply tube 3.

The flow rate of the liquid flowing through the liquid supply tube 2 and the filtrate supply tube 3 may be estimated from the operation of the liquid supply tube delivery section 2p and the concentrated liquid tube delivery section 4p, or the flow rate may be measured directly by providing a flow meter in the liquid supply tube 2, the liquid supply tube delivery section 2p, the concentrated liquid tube 4, or the concentrated liquid tube delivery section 4p.

<Explanation of filtration and concentration using the filter transmembrane pressure difference and the concentrator transmembrane pressure difference>
When performing a filtration and concentration operation using a filter transmembrane pressure difference or a concentrator transmembrane pressure difference, an allowable pressure difference is set in advance. That is, a pressure difference (allowable pressure difference) that the filter 10 and the concentrator 20 can tolerate is set according to the filter 10 and the concentrator 20, respectively. This allowable pressure difference may have a predetermined range, or may be set to a specific value. In the following, a case where the allowable pressure difference has a predetermined range will be described as a representative example.

When performing filtration and concentration using the filter transmembrane pressure difference or the concentrator transmembrane pressure difference, it is desirable to set an allowable flow rate in advance. That is, it is desirable to set an allowable flow rate (allowable flow rate) of the raw liquid in the liquid supply tube 2. This allowable flow rate may have a predetermined range or may be set to a specific value. Such an allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the liquid supply tube 2 becomes too low, the time required for filtration and concentration becomes too long. Therefore, in order to prevent the processing time of the raw liquid from becoming too long, it is desirable to set an allowable flow rate.
Furthermore, when performing filtration and concentration work using the filter transmembrane pressure difference or the concentrator transmembrane pressure difference, it is desirable to set an allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the raw liquid in the liquid supply tube 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 (allowable concentration ratio). This allowable concentration ratio may have a predetermined range or may be set to a specific value. Such an allowable concentration ratio does not necessarily have to be set. However, if the concentration ratio, which is the ratio of the flow rate of the raw liquid in the liquid supply tube 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4, is too low (i.e., if the flow rate of the concentrated liquid becomes too large), the concentration efficiency will deteriorate. Moreover, there is a risk that the amount of concentrated liquid increases and a large amount of the filtered concentrated liquid is reinfused intravenously, which may cause an increase in blood pressure and an exacerbation of cardiac failure or respiratory failure. For this reason, if the amount of concentrated liquid becomes too large, a reconcentration process must be added, which takes time. When the concentrated liquid is reconcentrated, the reconcentration process takes time, so the total time for processing the raw liquid will be long. Therefore, in order to prevent the concentration ratio from decreasing too much, it is desirable to set an allowable concentration ratio.

At the start of filtration and concentration, the liquid supply tube delivery section 2p is operated to increase the amount of raw liquid sent to the filter 10. At this time, the concentrated liquid tube delivery section 4p is operated so that the concentrated liquid is concentrated to a predetermined concentration ratio in accordance with the flow rate of the raw liquid in the liquid supply tube 2. For example, when producing a concentrated liquid with a concentration ratio of 10 times, the operation of the concentrated liquid tube delivery section 4p is adjusted so that the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 is 1/10 of the flow rate of the raw liquid flowing through the liquid supply tube 2. In addition, the operation of the concentrated liquid tube delivery section 4p may be adjusted so that the concentrator transmembrane pressure becomes a set value within the allowable pressure difference (or is maintained within the allowable pressure difference) instead of the concentration ratio of the concentrated liquid or while maintaining the concentrated liquid at a predetermined concentration ratio. Note that while the amount of raw liquid sent to the filter 10 is being increased, the operation of the concentrated liquid tube delivery section 4p is controlled so that one of the above states is achieved.

As the filtration and concentration progresses, clogging gradually occurs in the filter 10 and concentrator 20. This causes the filter transmembrane pressure difference and the concentrator transmembrane pressure difference to rise. However, the liquid supply tube liquid supply section 2p operates to increase the amount of raw liquid sent to the filter 10 until the filter transmembrane pressure difference and the concentrator transmembrane pressure difference fall within the allowable pressure difference range.

<First Method>
The increase in the amount of the stock solution sent to the filter 10 continues until the filter transmembrane pressure falls within the allowable pressure difference of the filter 10. Then, when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10, the supply tube sending unit 2p is controlled so as to maintain the flow rate of the stock solution in the supply tube 2 at the flow rate in the state in which the filter transmembrane pressure falls within the allowable pressure difference of the filter 10. Meanwhile, the concentrate tube sending unit 4p is operated to adjust the flow rate of the concentrate flowing through the concentrate tube 4.

Here, when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the operation of the liquid supply tube liquid supply section 2p is controlled so that the amount of filtrate sent to the concentrator 20, in other words, the amount of raw liquid sent to the filter 10, is maintained. Then, the filtration by the filter 10 and the concentration state by the concentrator 20 can be maintained in a predetermined state. If the amount of raw liquid sent to the filter 10 is increased or decreased according to the value of the filter transmembrane pressure difference, the amount of raw liquid sent to the filter 10 can be increased while maintaining the filter transmembrane pressure within the allowable pressure difference of the filter 10. In other words, there is a possibility that the efficiency of the filtration and concentration work can be improved. In particular, if the filter transmembrane pressure difference is maintained to be the maximum allowable pressure difference PM of the filter 10, the amount of raw liquid sent to the filter 10 can be increased to the maximum, so that the effect of shortening the time of the filtration work can be further improved.

On the other hand, when the filter transmembrane pressure difference becomes greater than the allowable differential pressure (maximum allowable differential pressure PM) of the filter 10, the operation of the liquid supply tube liquid supply section 2p is controlled so that the amount of raw liquid sent to the filter 10 is reduced. Even if the amount of raw liquid sent to the filter 10 is constant, if clogging of the hollow fiber membrane 16 or the like occurs, the filter transmembrane pressure difference may increase and filtration may not be able to continue. However, if the amount of raw liquid sent to the filter 10 is reduced, the filter transmembrane pressure difference can be reduced, so that filtration work can be continued even if clogging of the filter 10 occurs. Moreover, by reducing the amount of raw liquid sent to the filter 10, clogging of the hollow fiber membrane 16 or the like may be slightly reduced, making it easier to continue filtration work and shortening the time for filtration work. In particular, if the filter transmembrane pressure difference becomes greater than the maximum allowable pressure difference PM of the filter 10, the effect of reducing clogging of the hollow fiber membrane, etc. may be enhanced by temporarily stopping the supply of the raw liquid to the filter 10 and then resuming the supply after a certain period of time.

In addition, when the filter transmembrane pressure difference becomes smaller than the minimum allowable pressure difference PL of the filter 10 by, for example, reducing the amount of stock solution sent to the filter 10, the operation of the liquid supply tube liquid sending section 2p is controlled so that the amount of stock solution sent to the filter 10 is increased. This increases the amount of filtration by the filter 10, which may shorten the filtration operation time. Furthermore, if the amount of stock solution sent to the filter 10 is increased until the filter transmembrane pressure difference becomes within the allowable pressure difference of the filter 10, in particular the maximum allowable pressure difference PM, the filtering capacity of the filter 10 can be used effectively, thereby further enhancing the effect of shortening the filtration operation time.

In addition, when the amount of the raw liquid fed to the filter 10 is reduced when the filter transmembrane pressure becomes larger than the maximum allowable differential pressure PM of the filter 10, the amount of the raw liquid fed may be gradually reduced, or the amount of the raw liquid fed may be reduced in a stepwise manner. In addition, when the filter transmembrane pressure becomes larger than the maximum allowable differential pressure PM of the filter 10 (PM in FIG. 24), the feed of the raw liquid to the filter 10 may be stopped for a certain period of time and then started (see FIG. 24). In this case, the amount of the raw liquid fed to the filter 10 may be adjusted while checking the filter transmembrane pressure. For example, as in pattern 1 in FIG. 24, when the feed of the raw liquid to the filter 10 is stopped for a certain period of time and then started, the feed is started at a flow rate of about 1/2 the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is checked. In this state, if the filter transmembrane pressure is smaller than the minimum allowable pressure PL (PL in FIG. 24), the flow rate is increased by about 1/2 the difference between the current flow rate and the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is confirmed. In this state, if the filter transmembrane pressure is still smaller than the minimum allowable pressure PL, the flow rate is further increased by about 1/2 the difference between the current flow rate and the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is confirmed. This operation is repeated, and when the filter transmembrane pressure becomes equal to or greater than the minimum allowable pressure PL and equal to or less than the maximum allowable pressure PM of the filter 10 (or becomes equal to the maximum allowable pressure PM), the increase in the flow rate is stopped. In addition, if the filter transmembrane pressure is within the allowable pressure of the filter 10 but does not reach the maximum allowable flow rate LM, the amount of raw liquid sent to the filter 10 may be increased in the same manner while checking the filter transmembrane pressure until it reaches the maximum allowable flow rate LM.
When the amount of the stock solution fed to the filter 10 is increased when the filter transmembrane pressure becomes smaller than the minimum allowable pressure difference PL of the filter 10, the amount of the stock solution fed may be increased gradually. For example, the amount of the stock solution fed to the filter 10 may be increased by a method similar to the above-mentioned method of increasing the flow rate, that is, the method of increasing the flow rate after stopping the feed of the stock solution to the filter 10 for a certain period of time.

In addition, when the filter transmembrane pressure difference is maintained within the allowable pressure difference of the filter 10, the amount of raw liquid sent to the filter 10 may be maintained, but if the flow rate is smaller than the maximum allowable flow rate LM, the amount of raw liquid sent to the filter 10 may be increased until it reaches the maximum allowable flow rate LM.

In addition, if the filter transmembrane pressure difference becomes equal to or exceeds the minimum allowable pressure difference PL of the filter 10, but the amount of raw liquid sent to the filter 10 does not reach the minimum allowable flow rate LL (pattern 3 in Figure 24), it is determined that the hollow fiber membrane 16 or the like is clogged, and the filtration and concentration operation may be stopped and a cleaning operation may be started.

Now, in a state where the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10 and the flow rate of the raw liquid in the liquid supply tube 2 is maintained at the flow rate when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the concentrated liquid tube liquid delivery section 4p can be controlled as follows based on the concentrator transmembrane pressure difference.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the concentrate tube delivery unit 4p is operated to reduce the amount of concentrate delivered to the concentrate bag CB. In other words, the operation of the concentrate tube delivery unit 4p is controlled to increase the concentration of the concentrate.

<Step 2>
Then, the amount of concentrate sent to the concentrate bag CB is reduced until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the concentrate tube sending unit 4p is controlled so as to maintain the flow rate of the concentrate in the concentrate tube 4 at the flow rate when the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20.

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrated liquid tube sending unit 4p is controlled to increase the amount of concentrated liquid sent to the concentrated liquid bag CB. Note that as the amount of concentrated liquid sent increases, the concentration ratio decreases, but the operation of the concentrated liquid tube sending unit 4p is controlled to decrease the concentration ratio (to decrease the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.
In addition, if the concentration ratio becomes smaller than the allowable concentration ratio when the amount of concentrated liquid sent is increased in order to maintain the concentrator transmembrane pressure within the allowable pressure range, the following method (method 2) can be used to deal with this.

When the amount of concentrated liquid sent to the concentrated liquid bag CB increases, the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid tube sending section 4p is again operated to reduce the amount of concentrated liquid sent to the concentrated liquid bag CB.

That is, while the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the above steps 1 to 3 are repeated. By adopting this method, it is possible to ensure the maximum filtration flow rate (i.e., the above-mentioned maximum allowable flow rate LM) and the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the filter 10 and the concentrator 20, which is impossible when the amount of liquid sent to the filter 10 and the concentrated liquid bag CB is constant, and according to the state of the raw liquid (concentration of the substance causing the clogging of the filter or concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated liquid from the raw liquid can be shortened, and re-concentration work can be prevented or the time required for re-concentration work can be shortened.
Moreover, by operating as described above, it becomes possible to quickly remove the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit when filtration and concentration starts, and the cleaning liquid in the filter 10 and the circuit immediately after cleaning the filter 10, as waste liquid from the concentrator 20. In other words, it is possible to efficiently prevent dilution of the concentrated liquid by the cleaning liquid at the start of filtration and concentration and immediately after cleaning the filter, as described above.

The above method (first method) is preferably adopted when the maximum allowable pressure difference PM of the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM of the concentrator transmembrane pressure difference, but is not limited to this condition. It can also be adopted when the maximum allowable pressure difference PM of the filter transmembrane pressure difference is smaller than the maximum allowable pressure difference PM of the concentrator transmembrane pressure difference.
In addition, when the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM, or when the filter transmembrane pressure difference is smaller than the minimum allowable pressure difference PL, and further when the amount of raw liquid sent to the filter 10 is constant regardless of the filter transmembrane pressure difference, the above steps 1 to 3 may be repeated to adjust the amount of concentrated liquid sent to the concentrator 20.

<Second Method>
In the first method, the flow rate of the concentrated liquid in the concentrated liquid tube 4 was adjusted based on the concentrator transmembrane pressure difference, but the flow rate of the raw liquid in the liquid supply tube 2 can also be adjusted based on the concentrator transmembrane pressure difference as described below.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the liquid supply tube delivery section 2p is operated to increase the amount of raw liquid delivered to the filter 10. In other words, the operation of the liquid supply tube delivery section 2p is controlled so as to increase the amount of filtrate produced and delivered to the concentrator 20.

<Step 2>
Then, the amount of filtrate produced and sent to the concentrator 20 (in other words, the amount of raw liquid sent to the filter 10) is increased until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20 (above the minimum allowable pressure and below the maximum allowable pressure). When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the operation of the feed tube feed section 2p is controlled so as to maintain the flow rate of the raw liquid in the feed tube 2 at the flow rate when the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. In this case, the flow rate of the raw liquid in the feed tube 2 will deviate from the flow rate when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10, but it is desirable to maintain the flow rate of the raw liquid within the allowable flow rate (above the minimum allowable flow rate and below the maximum allowable flow rate).

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the operation of the liquid supply tube delivery section 2p is controlled so as to reduce the flow rate of the raw liquid in the liquid supply tube 2. In other words, the operation of the liquid supply tube delivery section 2p is controlled so as to reduce the amount of filtrate produced and sent to the concentrator 20. Note that even in this case, the flow rate of the raw liquid in the liquid supply tube 2 will deviate from the flow rate in the state in which the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, but it is desirable that the flow rate of the raw liquid be maintained within the allowable flow rate range.

When the flow rate of the raw liquid in the liquid supply tube 2 decreases, the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference becomes lower than the minimum allowable differential pressure of the concentrator 20, the liquid supply tube delivery section 2p is again operated to increase the flow rate of the raw liquid in the liquid supply tube 2.

That is, while the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the above steps 1 to 3 are repeated. By adopting this method, it is possible to ensure the maximum filtration flow rate (i.e., the above-mentioned maximum allowable flow rate LM) and the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the filter 10 and the concentrator 20, which is impossible when the amount of liquid sent to the filter 10 and the concentrated liquid bag CB is constant, and according to the state of the raw liquid (concentration of the substance causing the clogging of the filter or concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated liquid from the raw liquid can be shortened, and re-concentration work can be prevented or the time required for re-concentration work can be shortened.
Moreover, by operating as described above, it becomes possible to quickly remove the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit when filtration and concentration starts, and the cleaning liquid in the filter 10 and the circuit immediately after cleaning the filter 10, as waste liquid from the concentrator 20. In other words, it is possible to efficiently prevent dilution of the concentrated liquid by the cleaning liquid at the start of filtration and concentration and immediately after cleaning the filter, as described above.

The above method (second method) is preferably adopted when the maximum allowable differential pressure PM of the filter transmembrane pressure is greater than the maximum allowable differential pressure PM of the concentrator transmembrane pressure, but is not limited to this condition. It can also be adopted when the maximum allowable differential pressure PM of the filter transmembrane pressure is smaller than the maximum allowable differential pressure PM of the concentrator transmembrane pressure.
In addition, when the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM, or when the filter transmembrane pressure difference is smaller than the minimum allowable pressure difference PL, and further when the amount of raw liquid sent to the filter 10 is constant regardless of the filter transmembrane pressure difference, the above steps 1 to 3 may be repeated to adjust the amount of concentrated liquid sent to the concentrator 20.

<About cleaning the filter>
When the above-mentioned filtration and concentration work is performed, the filter transmembrane pressure becomes larger than the maximum allowable pressure PM of the filter 10 due to clogging of the filter 10, etc. In this case, if the operation of the liquid supply tube delivery section 2p is controlled to reduce the flow rate of the raw liquid in the liquid supply tube 2, the filter transmembrane pressure can be made smaller than the maximum allowable pressure PM of the filter 10, and the filter transmembrane pressure can be maintained within the allowable pressure difference (a range from the minimum allowable pressure PL to the maximum allowable pressure PM). However, if the clogging of the filter 10 becomes severe, the flow rate of the raw liquid in the liquid supply tube 2 is reduced in order to maintain the filter transmembrane pressure within the allowable pressure difference of the filter 10, and the flow rate of the raw liquid in the liquid supply tube 2 may become smaller than the minimum allowable flow rate LL. When this state occurs, the filter 10 is cleaned during the filtration and concentration work of the raw liquid treatment device 1 of the first embodiment.

As shown in FIG. 21, during the cleaning operation of the filter 10, the flow rate adjustment means 3c closes the filtrate supply tube 3 so that no liquid flows through it. In addition, the operation of the liquid supply tube delivery section 2p is stopped and it functions as a clamp. Meanwhile, the flow rate adjustment means 6c is opened to allow liquid to flow through the cleaning liquid supply tube 6.

In the above state, the cleaning liquid recovery tube liquid delivery section 7p is operated to flow liquid from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 through the filter 10 to the cleaning liquid recovery bag FB connected to the cleaning liquid recovery tube 7. This allows the cleaning liquid to flow in the flow path of the filter 10 in the opposite direction to the direction in which the raw liquid flows during filtration and concentration, so that the inside of the flow path of the filter 10 through which the raw liquid flows can be cleaned.

In addition to the above state, if the connecting tube liquid sending unit 9p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the connecting tube 9 to the filter 10, the cleaning liquid is also supplied to the filter 10 from the cleaning liquid bag SB connected to the connecting tube 9. This cleaning liquid then passes through the filter member in the opposite direction to the direction in which the filtrate passes through the filter member, so clogging of the filter member can be eliminated. In this case, the cleaning liquid is supplied to the filter 10 from both the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 and the cleaning liquid bag SB connected to the connecting tube 9, so that the operation of the cleaning liquid recovery tube liquid sending unit 7p and the connecting tube liquid sending unit 9p is adjusted so that the flow rate of the cleaning liquid flowing through the cleaning liquid recovery tube 7 by the cleaning liquid recovery tube liquid sending unit 7p is greater than the flow rate of the cleaning liquid flowing through the connecting tube 9 by the connecting tube liquid sending unit 9p.

The cleaning liquid recovery tube delivery section 7p and the connecting tube delivery section 9p may be operated with the flow rate adjustment means 6c closed. In this case, cleaning liquid is supplied to the filtrate 10 only from the cleaning liquid bag SB connected to the connecting tube delivery section 9p. In this case, the cleaning liquid also passes through the filtration member in the opposite direction to the direction in which the filtrate passes through the filtration member, so clogging of the filtration member can be eliminated.

When a filter having a hollow fiber membrane 16 as shown in FIG. 5 is used as the filter 10, it is desirable for the control unit 106 to adjust the amount and timing of the cleaning liquid supplied to the filter 10 so that the above-mentioned cleaning of the filter 10 and the concentrator 20 can be properly performed. In other words, it is desirable to adjust the amount and timing of the cleaning liquid supplied to the filter 10 so that the cleaning liquid permeates the hollow fiber membrane 16 while filling the hollow space 12h of the body 12 up to the region of the hollow fiber membrane 16 where cleaning is to be performed.

<Filtrate recovery>
On the other hand, when the filter is washed by the above-mentioned method, the filtrate remaining in the internal space 12h of the main body 11 of the filter 10 is mixed with the washing liquid and discharged, which reduces the amount of the active ingredient recovered by filtration and concentration.

Therefore, when cleaning the filter, it is preferable to first send the filtrate present in the internal space 12h of the main body 11 of the filter 10 to the concentrator 20 and then perform the filter cleaning.

<Recovery using cleaning fluid (outside)>
As shown in FIG. 1, a cleaning solution bag SB is connected to a port 11c (a port 11c to which a filtrate supply tube 3 is not connected, hereinafter referred to as a cleaning port 11c) of a main body 11 of a filter 10 via a tube. Then, the flow rate adjustment means 3c maintains a state in which liquid flows in the filtrate supply tube 3, and while the concentrated liquid tube sending part 4p continues to operate, the operation of the liquid supply tube sending part 2p is stopped and made to function as a clamp. In this state, if a cleaning solution is supplied from the cleaning solution bag SB to the filter 10 by a pump provided on a tube connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20, and instead, the cleaning solution is supplied from the cleaning solution bag SB to the internal space 12h. Eventually, when all the filtrate in the internal space 12h is replaced with the cleaning solution, the flow rate adjustment means 3c closes the filtrate supply tube 3 and stops the operation of the concentrated liquid tube sending part 4p. After this state has been reached, by cleaning the filter 10 using the cleaning method for the filter 10 as described above, it is possible to prevent the filtrate discharged together with the cleaning liquid from being re-concentrated.

In the above example, the recovery was performed by stopping the operation of the liquid supply tube delivery unit 2p, but the recovery may be performed while continuing the operation of the liquid supply tube delivery unit 2p. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the liquid supply tube delivery unit 2p to reduce the amount of raw liquid supplied to the filter 10.

Whether or not all of the filtrate in the internal space 12h has been replaced with the cleaning liquid can be determined theoretically by counting the amount of pumping provided in the tube connected to the cleaning port 11c, or by measuring the concentration of the concentrated liquid. It can also be determined by looking at the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a hydrometer.

In addition, the tube connected to the cleaning port 11c of the main body 11 of the filter 10 does not necessarily need to be provided with a pump. Even in this case, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be replaced with cleaning liquid by operating the concentrated liquid tube delivery unit 4p.

<Recovery using air or other gas>
In addition, in the above explanation, a case was described in which the cleaning solution bag SB was connected to the cleaning port 11c of the main body 11 of the filter 10 via a tube, but a gas such as air may also be supplied to the cleaning port 11c of the main body 11 of the filter 10 via a tube.

In this case, the flow rate adjusting means 3c maintains the state in which liquid flows in the filtrate supply tube 3, and while the concentrated liquid tube sending section 4p continues to operate, the operation of the liquid supply tube sending section 2p is stopped and made to function as a clamp. In this state, if a gas such as air is supplied to the filter 10 from a tube connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be supplied to the concentrator 20. When all of the filtrate in the internal space 12h is eventually discharged, the flow rate adjusting means 3c closes the filtrate supply tube 3 and stops the operation of the concentrated liquid tube sending section 4p. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the recovery was performed by stopping the operation of the liquid supply tube delivery unit 2p, but the recovery may be performed while continuing the operation of the liquid supply tube delivery unit 2p. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the liquid supply tube delivery unit 2p to reduce the amount of raw liquid supplied to the filter 10.

Whether or not all of the filtrate in the internal space 12h has been discharged can be determined by installing a liquid detector or air bubble detector in the filtrate supply tube 3, measuring the pressure in the filtrate supply tube 3, or theoretically calculating the amount of water pumped out by counting the amount of water pumped out.

In addition, when the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the internal space 12h of the main body 11 of the filter 10 is filled with a gas such as air. Therefore, when performing a cleaning operation after collecting the filtrate, it is desirable to first fill the hollow space 12h of the body 12 up to the area to be cleaned in the hollow fiber membrane 16 (or the entire hollow space 12h of the body 12) with cleaning liquid before performing the cleaning operation.

<Collecting in a bag>
In the above example, the filtrate is sent to the concentrator 20 and collected in a concentrated state, but the filtrate may be collected as it is. For example, a bag for collecting the filtrate is connected to the filtrate supply tube 3 upstream of the flow rate adjustment means 3c (i.e., the filter 10 side). In this state, if the flow rate adjustment means 3c makes the filtrate supply tube 3 in a state where liquid does not flow, and a cleaning liquid or a gas such as air is supplied to the filter 10 from the cleaning port 11c as described above, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be collected in the bag. In this case, the filtrate can be collected in a short time compared to the case where the filtrate is sent to the concentrator 20 and collected in a concentrated state, so that the transition to the cleaning operation can be performed quickly.

<Recovery using cleaning fluid (inside)>
In the above description, the raw liquid is supplied into the through-flow passages 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15 of the filter 10, and the filtrate is discharged into the internal space 12h of the trunk 12 of the main body 11 of the filter 10. However, the raw liquid may be supplied from the filtrate discharge port 11c into the internal space 12h of the trunk 12 of the main body 11, and the filtered filtrate may be discharged into the through-flow passages 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15, and then discharged to the outside from the raw liquid supply port 11a.

In this case, the tubes are connected as follows.
First, the filtrate supply tube 3 is connected to the raw liquid supply port 11a, the supply tube 2 is connected to the port 11c (i.e., the above-mentioned cleaning port 11c), the cleaning liquid supply tube 6 is connected to the port 11c (i.e., the above-mentioned filtrate discharge port 11c) to which the supply tube 2 is not connected, and the cleaning liquid bag SB that was connected to the cleaning port 11c is connected to the cleaning liquid supply port 11b.

Then, the flow rate adjusting means 3c maintains the state in which the liquid flows in the filtrate supply tube 3, and while the concentrated liquid tube sending part 4p continues to operate, the operation of the liquid supply tube sending part 2p is stopped and made to function as a clamp. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by the pump provided on the tube connected to the cleaning liquid supply port 11b, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20, and instead, the cleaning liquid is supplied from the cleaning liquid bag SB to the through flow path 16h. When all the filtrate in the through flow path 16h is replaced with the cleaning liquid, the flow rate adjusting means 3c closes the filtrate supply tube 3 and stops the operation of the concentrated liquid tube sending part 4p. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the recovery was performed by stopping the operation of the liquid supply tube delivery unit 2p, but the recovery may be performed while continuing the operation of the liquid supply tube delivery unit 2p. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the liquid supply tube delivery unit 2p to reduce the amount of raw liquid supplied to the filter 10.

Whether or not all of the filtrate in the internal space 12h has been replaced with the cleaning liquid can be determined theoretically by counting the amount of pumping provided in the tube connected to the cleaning port 11c, or by measuring the concentration of the concentrated liquid. It can also be determined by looking at the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a hydrometer.

<Recovery using air or other gas>
In addition, in the above explanation, a case was described in which the cleaning solution bag SB was connected to the cleaning solution supply port 11b of the main body 11 of the filter 10 via a tube, but a gas such as air may also be supplied to the cleaning solution supply port 11b of the main body 11 of the filter 10 via a tube.

In this case, the flow rate adjustment means 3c maintains the state in which liquid flows in the filtrate supply tube 3, and while the concentrated liquid tube delivery section 4p continues to operate, the operation of the liquid supply tube delivery section 2p is stopped and made to function as a clamp. In this state, if a gas such as air is supplied to the filter 10 from the tube, the filtrate in the through flow passage 16h of the hollow fiber membrane 16 of the filter 10 can be supplied to the concentrator 20. When all of the filtrate in the through flow passage 16h of the hollow fiber membrane 16 is eventually discharged, the flow rate adjustment means 3c closes the filtrate supply tube 3 and stops the operation of the concentrated liquid tube delivery section 4p. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, recovery was performed by stopping the operation of the liquid supply tube delivery unit 2p, but recovery may be performed while continuing the operation of the liquid supply tube delivery unit 2p. In other words, it is possible to recover the filtrate in the filter 10 while continuing filtration and concentration. In this case, it is desirable to adjust the operation of the liquid supply tube delivery unit 2p to reduce the amount of raw liquid supplied to the filter 10.

Whether or not all of the filtrate in the through-flow passage 16h of the hollow fiber membrane 16 has been discharged can be determined by providing a liquid detector or air bubble detector in the filtrate supply tube 3, measuring the pressure in the filtrate supply tube 3, or theoretically calculating the amount of pump feed by counting the amount of pump feed.

In addition, when the filtrate in the through passage 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the through passage 16h of the hollow fiber membrane 16 of the filter 10 is filled with a gas such as air. Therefore, when performing a cleaning operation after collecting the filtrate, it is desirable to first fill the through passage 16h with cleaning liquid up to the area of the hollow fiber membrane 16 to be cleaned (or the entire hollow fiber membrane 16) before performing the cleaning operation.

<Collecting in a bag>
In the above example, the filtrate is sent to the concentrator 20 and collected in a concentrated state, but the filtrate may be collected as it is. For example, a bag for collecting the filtrate is connected to the filtrate supply tube 3 upstream of the flow rate adjustment means 3c (i.e., the filter 10 side). In this state, if the flow rate adjustment means 3c makes the filtrate supply tube 3 in a state where no liquid flows, and the cleaning liquid or gas such as air is supplied to the filter 10 from the cleaning liquid supply port 11b as described above, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be collected in the bag. In this case, the filtrate can be collected in a short time compared to the case where the filtrate is sent to the concentrator 20 and collected in a concentrated state, so that the transition to the cleaning operation can be performed quickly.

<Another Example of Method for Recovering Liquid from Filter 10>
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, it is desirable to adjust the flow rate when sending the filtrate to the concentrator 20 based on the transmembrane pressure of the concentrator 20. By adopting such a method, even in the unlikely event that the concentrator 20 becomes clogged, an increase in the transmembrane pressure of the concentrator can be suppressed and processing can be prevented from being stopped, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate when sending liquid to the concentrator 20 based on the concentrator transmembrane pressure of the concentrator 20, the flow rate can be adjusted as follows. First, when the concentrator transmembrane pressure of the concentrator 20 is within a set differential pressure range, the operation of the concentrated liquid tube sending unit 4p and the operation of the pump provided on the tube connected to the cleaning port 11c are controlled so as to maintain the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the transmembrane pressure of the concentrator 20 is greater than the maximum set pressure difference, the operation of the concentrated liquid tube delivery section 4p and the operation of the pump provided on the tube connected to the cleaning port 11c are controlled so as to reduce the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the transmembrane pressure of the concentrator continuing to rise above the maximum set pressure difference and being unable to continue processing.
Conversely, when the transmembrane pressure difference of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrated liquid tube delivery section 4p and the operation of the pump provided on the tube connected to the cleaning port 11c are controlled so as to increase the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference and the concentrated liquid becoming diluted.

<Yet another example of the method for recovering liquid from the filter 10>
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, the flow rate from the concentrator 20 to the concentrated liquid bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the concentration ratio, may be adjusted based on the transmembrane pressure of the concentrator 20. In this method, the increase in the transmembrane pressure of the concentrator can be suppressed, and at the same time, the rate at which the concentrated liquid is recovered can be kept constant without changing the flow rate of the liquid sent from the filter 10 to the concentrator 20, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB based on the transmembrane pressure difference of the concentrator 20, the flow rates can be adjusted as follows:

First, when the transmembrane pressure of the concentrator 20 is within the set differential pressure range, the operation of the concentrated liquid tube sending unit 4p (or the operation of the waste liquid tube sending unit 5p if provided) or the operation of the pump provided on the tube connected to the cleaning port 11c is controlled so as to maintain the flow rate from the concentrator 20 to the concentrated liquid bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the transmembrane pressure of the concentrator 20 is greater than the maximum set pressure, the operation of the concentrated liquid tube sending part 4p (or the operation of the waste liquid tube sending part 5p if provided) or the operation of the pump provided on the tube connected to the cleaning port 11c is controlled so that the flow rate from the concentrator 20 to the concentrated liquid bag CB increases and/or the flow rate from the concentrator 20 to the waste liquid bag DB decreases. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set pressure, making it impossible to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrated liquid tube sending part 4p (or the operation of the waste liquid tube sending part 5p if provided) or the operation of the pump provided on the tube connected to the washing port 11c is controlled so that the flow rate from the concentrator 20 to the concentrated liquid bag CB decreases and/or the flow rate from the concentrator 20 to the waste liquid bag DB increases. This makes it possible to prevent problems such as the concentrated liquid becoming diluted due to the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference.

The set differential pressure of the concentrator transmembrane pressure when recovering the filtrate from the filter 10 may be the same as the allowable differential pressure in the filtration and concentration work, or the set differential pressure may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the set differential pressure range may be wider than the allowable differential pressure range. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the set differential pressure range is narrower than the allowable differential pressure range, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, there may be a discrepancy between the allowable differential pressure range and the set differential pressure range.

<Reconcentration process>
When the concentrate obtained by the filtration and concentration process is to be further concentrated, a re-concentration process is carried out.

As shown in FIG. 3, in the re-concentration operation of the raw liquid treatment apparatus 1 of the first embodiment, the other end of the connecting tube 9 is detached from the cleaning liquid bag SB and connected to the concentrated liquid bag CB.
The flow rate adjusting means 3c maintains a state in which liquid can flow through the filtrate supply tube 3, while the liquid supply tube sending section 2p and the cleaning liquid recovery tube sending section 7p are not operated and function as clamps. In addition, the flow rate adjusting means 6c closes the cleaning liquid supply tube 6 so that no liquid flows through it. This brings about a state in which no liquid flows through the filter 10.

In the above state, the connecting tube delivery unit 9p is operated so that the concentrated liquid flows from the concentrated liquid bag CB through the connecting tube 9 to the concentrator 20, and the concentrated liquid tube delivery unit 4p is operated so that the concentrated liquid flows from the concentrator 20 through the concentrated liquid tube 4 to the concentrated liquid bag CB.

Then, the concentrated liquid is supplied from the concentrated liquid bag CB connected to the connecting tube 9 to the concentrator 20 through the connecting tube 9, and the re-concentrated liquid further concentrated by the concentrator 20 is collected in the concentrated liquid bag CB through the concentrated liquid tube 4. Meanwhile, the water separated from the concentrated liquid is collected in the waste liquid bag DB through the waste liquid tube 5. In other words, a concentrated liquid (re-concentrated liquid) with a higher concentration rate can be obtained.

<Explanation of reconcentration using transmembrane pressure difference in concentrator>
In the reconcentration operation, the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the reconcentration rate, may be adjusted based on the transmembrane pressure of the concentrator 20. This method has the effect of suppressing an increase in the transmembrane pressure of the concentrator, while at the same time shortening the time required to produce a highly concentrated liquid.

In this case, when performing reconcentration work using the concentrator transmembrane pressure difference in advance, it is desirable to set an allowable pressure difference. In other words, a pressure difference (allowable pressure difference) that the concentrator 20 can tolerate is set according to the concentrator 20. This allowable pressure difference may have a predetermined range, or may be set to a specific value. In the following, a case where the allowable pressure difference has a predetermined range will be described as a representative example.

When performing reconcentration using the transmembrane pressure difference of the concentrator, it is desirable to set an allowable flow rate in advance. In other words, it is desirable to set the allowable flow rate (allowable flow rate) of the concentrated liquid in the connecting tube 9. This allowable flow rate may have a predetermined range, or may be set to a specific value. Such an allowable flow rate does not necessarily have to be set. However, if the flow rate of the concentrated liquid in the connecting tube 9 becomes too low, the time required for reconcentration becomes too long. Therefore, in order to prevent the processing time of the concentrated liquid from becoming too long, it is desirable to set an allowable flow rate. Also, the allowable flow rate in the reconcentration operation may be the same as the allowable flow rate in filtration concentration, or may be different from the allowable flow rate in filtration concentration.

Furthermore, when performing reconcentration using the transmembrane pressure difference of the concentrator, it is desirable to set an allowable concentration ratio in advance. In other words, it is desirable to set the ratio of the flow rate of the concentrate flowing through the concentrate tube 4 to the flow rate of the concentrate in the connecting tube 9 (allowable concentration ratio). This allowable concentration ratio may have a predetermined range or may be set to a specific value. Such an allowable concentration ratio does not necessarily have to be set. However, if the concentration ratio, which is the ratio of the flow rate of the concentrate flowing through the concentrate tube 4 to the flow rate of the concentrate in the connecting tube 9, drops too much (i.e., if the flow rate of the concentrate becomes too large), the concentration efficiency will deteriorate, and the reconcentration process will take time. Therefore, in order to prevent the concentration ratio from dropping too much, it is desirable to set an allowable concentration ratio. In addition, the allowable concentration ratio in the reconcentration work may be the same as the allowable flow rate in filtration concentration, or may be different from the allowable concentration ratio in filtration concentration.

At the start of reconcentration, the connecting tube liquid sending unit 9p is operated to increase the amount of concentrated liquid sent to the concentrator 20. At this time, the concentrated liquid tube liquid sending unit 4p is operated so that the concentrated liquid is concentrated to a predetermined concentration ratio in accordance with the flow rate of the concentrated liquid in the connecting tube 9. For example, when a concentrated liquid with a concentration ratio of 10 is produced, the operation of the concentrated liquid tube liquid sending unit 4p is adjusted so that the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 is 1/10 of the flow rate of the concentrated liquid flowing through the connecting tube 9. In addition, the operation of the concentrated liquid tube liquid sending unit 4p may be adjusted so that the concentrator transmembrane pressure becomes a set value within the allowable pressure difference (or is maintained within the allowable pressure difference) instead of the concentration ratio of the concentrated liquid or while maintaining the concentrated liquid at a predetermined concentration ratio. Note that while the amount of concentrated liquid sent to the concentrator 20 is being increased, the operation of the concentrated liquid tube liquid sending unit 4p is controlled so that one of the above states is achieved.

As the reconcentration progresses, clogging of the concentrator 20 gradually occurs. This causes the concentrator transmembrane pressure difference to rise. However, the connecting tube liquid delivery section 9p operates to increase the amount of concentrated liquid delivered to the concentrator 20 until the transmembrane pressure difference of the concentrator reaches the allowable pressure difference.

<First Method>
The increase in the amount of concentrated liquid sent to the concentrator 20 continues until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. Then, when the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the connecting tube liquid sending unit 9p is controlled so as to maintain the flow rate of the concentrated liquid in the connecting tube 9 at the flow rate in the state in which the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. Meanwhile, based on the concentrator transmembrane pressure, the concentrated liquid tube liquid sending unit 4p is operated as follows to adjust the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the concentrate tube delivery unit 4p is operated to reduce the amount of concentrate delivered to the concentrate bag CB. In other words, the operation of the concentrate tube delivery unit 4p is controlled to increase the concentration of the concentrate.

<Step 2>
Then, the amount of concentrate sent to the concentrate bag CB is reduced until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the concentrate tube sending unit 4p is controlled so as to maintain the flow rate of the concentrate in the concentrate tube 4 at the flow rate when the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20.

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrated liquid tube sending unit 4p is controlled to increase the amount of concentrated liquid sent to the concentrated liquid bag CB. Note that as the amount of concentrated liquid sent increases, the concentration ratio decreases, but the operation of the concentrated liquid tube sending unit 4p is controlled to decrease the concentration ratio (to decrease the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.
In addition, if the concentration ratio becomes smaller than the allowable concentration ratio when the amount of concentrated liquid sent is increased in order to maintain the concentrator transmembrane pressure within the allowable pressure range, the following method (method 2) can be used to deal with this.

When the amount of concentrated liquid sent to the concentrated liquid bag CB increases, the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid tube sending section 4p is again operated to reduce the amount of concentrated liquid sent to the concentrated liquid bag CB.

In other words, steps 1 to 3 are repeated as long as the concentrator transmembrane pressure difference is within the allowable pressure difference of the concentrator 20. By adopting this method, it is possible to ensure the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the concentrator 20, which is not possible when the amount of liquid sent to the concentrate bag CB is constant, and according to the state of the concentrate (concentration of the substance causing the clogging of the concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the concentration efficiency, the time required to produce a highly concentrated concentrate can be shortened, and the time required for re-concentration work can be shortened.

<Second Method>
In the first method, the flow rate of the concentrate in the concentrate tube 4 is adjusted based on the transmembrane pressure difference of the concentrator. However, the flow rate of the concentrate in the connecting tube 9 can also be adjusted based on the transmembrane pressure difference of the concentrator as described below.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the connecting tube liquid sending section 9p is operated so as to increase the amount of concentrated liquid sent to the concentrator 20.

<Step 2>
Then, the amount of concentrated liquid sent to the concentrator 20 is increased until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the operation of the connecting tube liquid sending unit 9p is controlled so as to maintain the flow rate of the concentrated liquid in the connecting tube 9 at the flow rate in the state in which the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. In this case, it is desirable to maintain the flow rate of the concentrated liquid in the connecting tube 9 within the allowable flow rate (above the minimum allowable flow rate and below the maximum allowable flow rate).

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the operation of the connecting tube liquid sending part 9p is controlled so as to reduce the flow rate of the concentrated liquid in the connecting tube 9. In other words, the operation of the connecting tube liquid sending part 9p is controlled so as to reduce the flow rate sent to the concentrator 20. Note that even in this case, it is desirable to maintain the flow rate of the concentrated liquid in the connecting tube 9 within the allowable flow rate.

When the flow rate of the concentrated liquid in the connecting tube 9 decreases, the concentrator transmembrane pressure difference becomes smaller, so when the transmembrane pressure difference becomes lower than the minimum allowable differential pressure of the concentrator 20, the connecting tube liquid delivery section 9p is again operated to increase the flow rate of the concentrated liquid in the connecting tube 9.

In other words, steps 1 to 3 are repeated as long as the concentrator transmembrane pressure difference is within the allowable pressure difference of the concentrator 20. By adopting this method, it is possible to ensure the maximum recirculation flow rate and maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the concentrator 20, which is not possible when the amount of liquid sent to the concentrator 20 is constant, and according to the state of the concentrated liquid (concentration of the substance causing the clogging of the concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the recirculation efficiency and concentration efficiency, the time required to produce a highly concentrated liquid can be shortened, and the time required for reconcentration work can be shortened.

The allowable pressure difference of the concentrator transmembrane pressure during reconcentration may be the same as the allowable pressure difference during the filtration and concentration work, or may be a value (range) different from the allowable pressure difference during the filtration and concentration work. For example, when the allowable pressure difference during the filtration and concentration work has a certain range, the allowable pressure difference during the reconcentration may be wider than that range. In this case, when treating a stock solution that is prone to clogging the filter 10, the filtration and concentration work is performed slowly so as not to apply pressure to the filter 10, but instead a highly concentrated solution can be produced, which is desirable in that the time required for the reconcentration work can be shortened. In addition, when the allowable pressure difference during reconcentration is narrower than the allowable pressure difference during the filtration and concentration work, when treating a stock solution that is prone to clogging the concentrator 20, the filtration and concentration work is performed in a short time without applying pressure to the concentrator 20, which is desirable in that a highly concentrated solution can be produced in the reconcentration work. Furthermore, there may be a difference between the allowable pressure difference during the filtration and concentration work and the allowable pressure difference during the reconcentration work.
The allowable concentration ratio in reconcentration may be the same as the allowable concentration ratio in the filtration and concentration work, or may be a value (range) different from the allowable concentration ratio in the filtration and concentration work. For example, when the allowable concentration ratio in the filtration and concentration work has a certain range, the range of the allowable concentration ratio in the reconcentration may be wider than that range. In this case, it is desirable in that the time of the reconcentration work can be shortened instead of concentrating the filtration and concentration work for a long time. In addition, when the range of the allowable concentration ratio in the reconcentration is narrower than the range of the allowable concentration ratio in the filtration and concentration work, it is desirable in that the filtration and concentration work can be completed quickly instead of concentrating the reconcentration work for a long time. Furthermore, there may be a difference between the range of the allowable concentration ratio in the filtration and concentration work and the range of the allowable concentration ratio in the reconcentration.

<Example of method for recovering liquid from filter 10>
Before carrying out the above-mentioned reconcentration operation, the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as a concentrated liquid. In this case, it is desirable to adjust the flow rate when sending the filtrate to the concentrator 20 based on the transmembrane pressure of the concentrator 20. By adopting such a method, even if the concentrator 20 is clogged, the increase in the transmembrane pressure of the concentrator can be suppressed and the process can be prevented from being stopped, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate when sending liquid to the concentrator 20 based on the concentrator transmembrane pressure of the concentrator 20, the flow rate can be adjusted as follows. First, when the concentrator transmembrane pressure of the concentrator 20 is within a set differential pressure range, the operation of the concentrated liquid tube sending unit 4p and the operation of the pump provided on the tube connected to the cleaning port 11c are controlled so as to maintain the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the transmembrane pressure of the concentrator 20 is greater than the maximum set pressure difference, the operation of the concentrated liquid tube delivery section 4p and the operation of the pump provided on the tube connected to the cleaning port 11c are controlled so as to reduce the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the transmembrane pressure of the concentrator continuing to rise above the maximum set pressure difference and being unable to continue processing.
Conversely, when the transmembrane pressure difference of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrated liquid tube delivery section 4p and the operation of the pump provided on the tube connected to the cleaning port 11c are controlled so as to increase the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference and the concentrated liquid becoming diluted.

<Another Example of Method for Recovering Liquid from Filter 10>
Furthermore, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, the flow rate from the concentrator 20 to the concentrated liquid bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the concentration ratio, may be adjusted based on the transmembrane pressure of the concentrator 20. In this method, the increase in the transmembrane pressure of the concentrator can be suppressed, and at the same time, the recovery speed can be kept constant without changing the flow rate of the liquid sent from the filter 10 to the concentrator 20, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB based on the transmembrane pressure difference of the concentrator 20, the flow rates can be adjusted as follows:

First, when the transmembrane pressure of the concentrator 20 is within the set differential pressure range, the operation of the concentrated liquid tube sending unit 4p (or the operation of the waste liquid tube sending unit 5p if provided) or the operation of the pump provided on the tube connected to the cleaning port 11c is controlled so as to maintain the flow rate from the concentrator 20 to the concentrated liquid bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the transmembrane pressure of the concentrator 20 is greater than the maximum set pressure, the operation of the concentrated liquid tube sending part 4p (or the operation of the waste liquid tube sending part 5p if provided) or the operation of the pump provided on the tube connected to the cleaning port 11c is controlled so that the flow rate from the concentrator 20 to the concentrated liquid bag CB increases and/or the flow rate from the concentrator 20 to the waste liquid bag DB decreases. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set pressure, making it impossible to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrated liquid tube sending part 4p (or the operation of the waste liquid tube sending part 5p if provided) or the operation of the pump provided on the tube connected to the washing port 11c is controlled so that the flow rate from the concentrator 20 to the concentrated liquid bag CB decreases and/or the flow rate from the concentrator 20 to the waste liquid bag DB increases. This makes it possible to prevent problems such as the concentrated liquid becoming diluted due to the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference.

The set differential pressure of the concentrator transmembrane pressure when recovering the filtrate from the filter 10 may be the same as the allowable differential pressure in the filtration and concentration work, or the set differential pressure may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the set differential pressure range may be wider than the allowable differential pressure range. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the set differential pressure range is narrower than the allowable differential pressure range, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, there may be a discrepancy between the allowable differential pressure range and the set differential pressure range.

<Recovery of concentrator 20>
When recovering the concentrate in the concentrator 20 after recovering the raw liquid or filtrate in the filter 10, the recovery of the concentrate may be performed by simply passing a fluid such as a cleaning liquid or a gas (hereinafter simply referred to as a fluid) through the concentrator 20. However, as in the above-mentioned case, the flow rate of the fluid supplied to the concentrate 20 may be adjusted while measuring the concentrator transmembrane pressure difference. This can prevent problems such as the concentrator transmembrane pressure increasing and the inability to continue the treatment from occurring. If the concentrator transmembrane pressure of the concentrator 20 becomes greater than the maximum set pressure difference, the flow of liquid (including the flow of gas) from the filter 10 to the concentrator 20 can be stopped to prevent problems such as the concentrator transmembrane pressure continuing to increase.

The set differential pressure (second set differential pressure) of the concentrator transmembrane pressure when recovering the concentrated liquid from the concentrator 20 may be the same as the allowable differential pressure in the filtration concentration operation or the set differential pressure (first set differential pressure) when recovering the filtrate from the filter 10, or may be a different value (range). For example, when the allowable differential pressure or the first set differential pressure has a certain range, the range of the second set differential pressure may be wider than the range of the allowable differential pressure or the first set differential pressure. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the range of the second set differential pressure is narrower than the range of the allowable differential pressure or the first set differential pressure, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, the range of the second set differential pressure may deviate from the range of the allowable differential pressure or the first set differential pressure.

<Recovery of liquid in filtrate supply tube 3>
After the above-mentioned recovery of the concentrated liquid in the concentrator 20 is performed, if the concentrator transmembrane pressure difference reaches a set pressure difference or a specified amount of liquid has been recovered, the liquid transfer (including the flow of gas) from the filter 10 to the concentrator 20 may be stopped and then a gas such as air may be supplied to the filtrate supply tube 3. This makes it possible to prevent recovery leakage of the concentrated liquid in the concentrator 20 or the concentrated liquid flow path 4, and the liquid in the flow path downstream of the filtrate supply tube 3. If the concentrator transmembrane pressure difference has not reached the set pressure difference, the liquid transfer from the filter 10 to the concentrator 20 does not necessarily have to be stopped.

<Raw solution treatment device 1B of second embodiment>
In the above-described first embodiment of the raw liquid treatment device 1, the raw liquid is supplied to the filter 10 in a manner that forces it in during filtration and concentration, but the raw liquid may also be supplied to the filter 10 by sucking it out of the filter 10.

In other words, as shown in FIG. 7, the raw liquid treatment device 1B of the second embodiment is configured to supply raw liquid to the filter 10 by sucking the raw liquid from the filter 10. In other words, the raw liquid treatment device 1B of the second embodiment is configured such that the filtrate supply tube 3 is provided with a filtrate supply tube liquid delivery section 3p instead of the flow rate adjustment means 3c in the raw liquid treatment device 1 of the first embodiment, and the liquid supply tube 2 is provided with a flow rate adjustment means 2c instead of the liquid supply tube liquid delivery section 2p.

In this stock solution processing device 1B, during filtration and concentration, the filtrate supply tube liquid sending section 3p is operated so that liquid (filtrate) flows from the filter 10 to the concentrator 20. When the filtrate supply tube liquid sending section 3p is operated, the upstream side of the filtrate supply tube liquid sending section 3p in the filtrate supply tube 3, i.e., the filter 10 side, becomes negative pressure, and the inside of the filter 10 (for example, the internal space 12h of the trunk part 12 of the main body part 11) also becomes negative pressure. Then, if the liquid supply tube 2 is set in a state where it can send liquid by the flow rate adjustment means 2c, the stock solution in the stock solution bag UB can be sucked into the filter 10 through the liquid supply tube 2, and the sucked stock solution can be sucked into the filtrate supply tube 3.

In this raw liquid processing device 1B, the preparatory washing operation, the filtration concentration operation, and the reconcentration operation can be performed by appropriately changing the bags connected to each tube and adjusting the operation of the flow rate adjustment means and the liquid delivery unit provided in each tube. In addition, in the raw liquid processing device 1B, instead of the concentrated liquid tube delivery unit 4p, the waste liquid tube delivery unit 5p may be provided in the waste liquid tube 5 (see FIG. 9). Even in this case, if the waste liquid tube delivery unit 5p decreases the amount of waste liquid delivered under the condition that the concentrated liquid tube delivery unit 4p increases the amount of concentrated liquid delivered, and if the waste liquid tube delivery unit 5p increases the amount of waste liquid delivered under the condition that the concentrated liquid tube delivery unit 4p decreases the amount of concentrated liquid delivered, the function can be made to be the same as when the concentrated liquid tube delivery unit 4p is provided in the concentrated liquid tube 4. The case where the concentrated liquid tube delivery unit 4p is provided in the concentrated liquid tube 4 will be described below.

<Preparatory cleaning work>
6, a cleaning solution bag SB is connected to the other end of the concentrated solution tube 4 instead of the concentrated solution bag CB, and a cleaning solution recovery bag FB is connected to the other end of the waste solution tube 5 instead of the waste solution bag DB. The other end of the waste solution tube 5 may remain connected to the waste solution bag DB, or may be simply placed in a bucket or the like.
A cleaning solution recovery bag FB is connected to the other end of the liquid supply tube 2 instead of the stock solution bag UB. A waste solution bag DB may be connected to the other end of the liquid supply tube 2, or the other end of the liquid supply tube 2 may be simply placed in a bucket or the like.
A cleaning liquid recovery bag FB is also connected to the other end of the connecting tube 9. A waste liquid bag DB may be connected to the other end of the connecting tube 9, or the other end of the connecting tube 9 may be simply placed in a bucket or the like.
Furthermore, a cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid supply tube 6 in place of the cleaning liquid bag SB, and a cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid recovery tube 7 in place of the cleaning liquid recovery bag FB. A waste liquid bag DB may also be connected to the other end of the cleaning liquid supply tube 6 and the other end of the cleaning liquid recovery tube 7, or the other end of the cleaning liquid supply tube 6 and the other end of the cleaning liquid recovery tube 7 may be placed in a simple bucket or the like.

Next, the flow rate adjustment means 2c and the flow rate adjustment means 9c are opened to allow the cleaning liquid to flow through the liquid supply tube 2 and the connecting tube 9.

In the above state, the concentrated liquid tube delivery unit 4p is operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the concentrated liquid tube 4 to the concentrated liquid 20, and the filtrate supply tube delivery unit 3p is operated to flow the cleaning liquid from the concentrator 20 (i.e., the filtrate supply tube 3) to the cleaning liquid recovery bag FB connected to the connecting tube 9. Then, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the concentrated liquid tube 4 to the concentrator 20 through the concentrated liquid tube 4. The supplied cleaning liquid passes through the concentrator 20, then passes through the filtrate supply tube 3 and the connecting tube 9, and is collected in the cleaning liquid recovery bag FB connected to the connecting tube 9. Note that a part of the cleaning liquid passes through the waste liquid tube 5 and is collected in the cleaning liquid recovery bag FB connected to the other end of the waste liquid tube 5.

The cleaning liquid recovery tube delivery unit 7p is also operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the cleaning liquid recovery tube 7 to the filter 10. Then, a portion of the cleaning liquid is supplied from the cleaning liquid bag SB connected to the cleaning liquid recovery tube 7 to the filter 10 through the cleaning liquid recovery tube 7. The cleaning liquid supplied to the filter 10 passes through the filter 10, then passes through the filtrate supply tube 3 and the connecting tube 9, and is collected in the cleaning liquid recovery bag FB connected to the connecting tube 9. In addition, by operating the cleaning liquid supply tube delivery unit 6p, a portion of the cleaning liquid supplied to the filter 10 can also be flowed into the cleaning liquid supply tube 6. Furthermore, a portion of the cleaning liquid is collected from the cleaning liquid recovery tube 7 through the supply tube 2 to the cleaning liquid recovery bag FB connected to the supply tube 2.

This allows the cleaning liquid to flow through the filter 10, the concentrator 20, and all the tubes, so that the entire raw liquid processing device 1B of the second embodiment can be cleaned.

<Filtration and concentration work>
Once the preparatory cleaning process is completed, the filtration and concentration process is carried out.

As shown in Figure 7, in the filtration and concentration operation of the raw liquid treatment device 1B of the second embodiment, from the state of the preparatory cleaning operation (see Figure 6), a concentrate bag CB is connected to the other end of the concentrate tube 4 instead of the cleaning liquid bag SB, and a waste liquid bag DB is connected to the other end of the waste liquid tube 5 instead of the cleaning liquid recovery bag FB.
On the other hand, a stock solution bag UB is connected to the other end of the liquid supply tube 2 in place of the cleaning liquid recovery bag FB.
Also, the flow rate adjusting means 2c is opened to maintain a state in which liquid can flow through the liquid supply tube 2, while the flow rate adjusting means 9c is used to close the connecting tube 9 so that liquid does not flow through the connecting tube 9. In addition, the cleaning liquid recovery tube sending part 7p and the cleaning liquid supply tube sending part 6p are not operated and function as clamps.

In the above state, the filtrate supply tube delivery unit 3p is operated to flow the filtrate from the filter 10 to the concentrator 20, and the concentrate tube delivery unit 4p is operated to flow the concentrate from the concentrator 20 to the concentrate bag CB.

The raw liquid is then supplied from the raw liquid bag UB to the filter 10 through the liquid supply tube 2. The supplied raw liquid is filtered by the filter 10, and the filtrate produced is supplied to the concentrator 20 through the filtrate supply tube 3. The filtrate supplied to the concentrator 20 is then concentrated by the concentrator 20, and the concentrate produced is collected in the concentrate bag CB through the concentrate tube 4. Meanwhile, the water separated from the concentrate is collected in the waste liquid bag DB through the waste liquid tube 5.

<About filtration and concentration operations>
Here, in the filtration and concentration operation, the operation of the filtrate supply tube sending section 3p and the concentrate tube sending section 4p is controlled so that the concentration ratio falls within a predetermined range. However, as described below, the operation of the filtrate supply tube sending section 3p and the concentrate tube sending section 4p, that is, the flow rate of the liquid flowing through the filtrate supply tube 3 and the concentrate tube 4, may be controlled by utilizing the filter transmembrane pressure difference and the concentrator transmembrane pressure difference. In this way, the capacity of the filter 10 and the concentrator 20 can be effectively utilized to perform filtration and concentration, so that the time required to produce the concentrate can be shortened and the efficiency of the concentration operation can be increased.
In the following, the operation of filtering and concentrating by controlling the operation of the filtrate supply tube sending section 3p and the concentrate tube sending section 4p using the filter transmembrane pressure difference and the concentrator transmembrane pressure difference will be described.

The filter transmembrane pressure and the concentrator transmembrane pressure can be calculated by measuring the pressure inside the tubes connected to the filter 10 and the concentrator 20. For example, if a pressure gauge is provided in the liquid supply tube 2 and the filtrate supply tube 3 and the signal is supplied to the control unit 106, the control unit 106 can calculate the filter transmembrane pressure. If a pressure gauge is provided in the port 11c (or the tube connected to this port 11c) to which the filtrate supply tube 3 is not connected, the control unit 106 can calculate the filter transmembrane pressure. If a pressure gauge is provided in the filtrate supply tube 3 and the waste liquid tube 5 and the signal is supplied to the control unit 106, the control unit 106 can calculate the concentrator transmembrane pressure. If a port 20c to which the waste liquid tube 5 is not connected is present, the control unit 106 can calculate the concentrator transmembrane pressure even if a pressure gauge is provided in this port 20c (or the tube connected to this port 20c).

In addition, in the filter 10 or the concentrator 20, if either the liquid supply side or the liquid discharge side is close to being open to the atmosphere, the control unit 106 can calculate the filter transmembrane pressure or the concentrator transmembrane pressure by simply measuring the pressure inside the tube connected to the side of the liquid supply side or the liquid discharge side that is not open to the atmosphere. In other words, instead of the filter transmembrane pressure or the concentrator transmembrane pressure, the control unit 106 can control the operation of the liquid delivery unit by using only the pressure inside the tube connected to the side that is not open to the atmosphere. For example, if the tube connected to the filter 10 or the concentrator 20 is connected to a bag and is not blocked by the liquid delivery unit or the flow rate adjustment means, the tube can be considered to be close to being open to the atmosphere. In the state of FIG. 7, the liquid supply tube 2 connected to the raw liquid bag UB of the tubes 2 and 3 connected to the filter 10 can also be considered to be open to the atmosphere. In addition, the liquid discharge tube 5 connected to the waste liquid bag DB of the tubes 3 and 5 connected to the concentrator 20 can also be considered to be open to the atmosphere. In this state, as shown in FIG. 7, the control unit 106 can control the operation of the liquid delivery unit using only the internal pressure of the filter supply tube 3.

The flow rate of the liquid flowing through the filtrate supply tube 3 and the concentrate tube 4 may be estimated from the operation of the filtrate supply tube delivery section 3p and the concentrate tube delivery section 4p, or the flow rate may be measured directly by providing a flow meter in the filtrate supply tube 3, the filtrate supply tube delivery section 3p, the concentrate tube 4, or the concentrate tube 4p.

<Explanation of filtration and concentration using the filter transmembrane pressure difference and the concentrator transmembrane pressure difference>
When performing a filtration and concentration operation using a filter transmembrane pressure difference or a concentrator transmembrane pressure difference, an allowable pressure difference is set in advance. That is, a pressure difference (allowable pressure difference) that the filter 10 and the concentrator 20 can tolerate is set according to the filter 10 and the concentrator 20, respectively. This allowable pressure difference may have a predetermined range, or may be set to a specific value. In the following, a case where the allowable pressure difference has a predetermined range will be described as a representative example.

When performing filtration and concentration using the filter transmembrane pressure difference or the concentrator transmembrane pressure difference, it is desirable to set an allowable flow rate in advance. That is, it is desirable to set an allowable flow rate (allowable flow rate) of the raw liquid in the liquid supply tube 2. This allowable flow rate may have a predetermined range or may be set to a specific value. Such an allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the liquid supply tube 2 becomes too low, the time required for filtration and concentration becomes too long. Therefore, in order to prevent the processing time of the raw liquid from becoming too long, it is desirable to set an allowable flow rate.
Furthermore, when performing filtration and concentration work using the filter transmembrane pressure difference or the concentrator transmembrane pressure difference, it is desirable to set an allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the raw liquid in the liquid supply tube 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 (allowable concentration ratio). This allowable concentration ratio may have a predetermined range or may be set to a specific value. Such an allowable concentration ratio does not necessarily have to be set. However, if the concentration ratio, which is the ratio of the flow rate of the raw liquid in the liquid supply tube 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4, is too low (i.e., if the flow rate of the concentrated liquid becomes too large), the concentration efficiency will deteriorate. Moreover, there is a risk that the amount of concentrated liquid increases and a large amount of the filtered concentrated liquid is reinfused intravenously, which may cause an increase in blood pressure and an exacerbation of cardiac failure or respiratory failure. For this reason, if the amount of concentrated liquid becomes too large, a reconcentration process must be added, which takes time. When the concentrated liquid is reconcentrated, the reconcentration process takes time, so the total time for processing the raw liquid will be long. Therefore, in order to prevent the concentration ratio from decreasing too much, it is desirable to set an allowable concentration ratio.

At the start of filtration and concentration, the filtrate supply tube sending section 3p is operated to increase the amount of raw liquid sent to the filter 10. At this time, the concentrated liquid tube sending section 4p is operated so that the concentrated liquid becomes a predetermined concentration ratio according to the flow rate of the filtrate in the filtrate supply tube 3. For example, when a concentrated liquid with a concentration ratio of 10 is produced, the operation of the concentrated liquid tube sending section 4p is adjusted so that the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 becomes 1/10 of the flow rate of the filtrate flowing through the filtrate supply tube 3. In addition, the operation of the concentrated liquid tube sending section 4p may be adjusted so that the concentrator transmembrane pressure becomes a set value within the allowable pressure difference (or is maintained within the allowable pressure difference) instead of the concentration ratio of the concentrated liquid or while maintaining the concentrated liquid at a predetermined concentration ratio. Note that while the amount of filtrate sent to the concentrator 20 is being increased, the operation of the concentrated liquid tube sending section 4p is controlled so that one of the above states is achieved.

As filtration and concentration progresses, clogging gradually occurs in the filter 10 and concentrator 20. This causes the filter transmembrane pressure difference and the concentrator transmembrane pressure difference to rise. However, the filtrate supply tube delivery section 3p operates to increase the amount of filtrate delivered to the concentrator 20 (in other words, the amount of raw liquid delivered to the filter 10) until the filter transmembrane pressure difference and the concentrator transmembrane pressure difference fall within the allowable pressure difference range.

<First Method>
The increase in the amount of filtrate sent to the concentrator 20 continues until the filter transmembrane pressure falls within the allowable pressure difference of the filter 10. Then, when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10, the filtrate supply tube sending unit 3p is controlled so as to maintain the amount of filtrate sent to the concentrator 20 at the flow rate when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10. Meanwhile, the concentrate tube sending unit 4p is operated to adjust the flow rate of the concentrate flowing through the concentrate tube 4.

Here, when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the operation of the filtrate supply tube liquid sending section 3p is controlled so that the amount of filtrate sent to the concentrator 20, in other words, the amount of raw liquid sent to the filter 10, is maintained. Then, the filtration by the filter 10 and the concentration state by the concentrator 20 can be maintained in a predetermined state. If the amount of raw liquid sent to the filter 10 is increased or decreased according to the value of the filter transmembrane pressure difference, the amount of raw liquid sent to the filter 10 can be increased while maintaining the filter transmembrane pressure within the allowable pressure difference of the filter 10. In other words, there is a possibility that the efficiency of the filtration and concentration work can be improved. In particular, if the filter transmembrane pressure difference is maintained to be the maximum allowable pressure difference PM of the filter 10, the amount of raw liquid sent to the filter 10 can be increased to the maximum, so that the effect of shortening the time of the filtration work can be further improved.

On the other hand, when the filter transmembrane pressure difference becomes greater than the maximum allowable differential pressure PM of the filter 10, the operation of the filtrate supply tube liquid sending section 3p is controlled so that the amount of raw liquid sent to the filter 10 is reduced. Even if the amount of raw liquid sent to the filter 10 is constant, if clogging of the hollow fiber membrane or the like occurs, the filter transmembrane pressure difference may increase and filtration may not be able to continue. However, if the amount of raw liquid sent to the filter 10 is reduced, the filter transmembrane pressure difference can be reduced, so that filtration work can be continued even if clogging of the filter 10 occurs. Moreover, by reducing the amount of raw liquid sent to the filter 10, clogging of the hollow fiber membrane 16 or the like may be slightly reduced, making it easier to continue filtration work and shortening the time for filtration work. In particular, if the filter transmembrane pressure difference becomes greater than the maximum allowable pressure difference PM of the filter 10, the effect of reducing clogging of the hollow fiber membrane, etc. may be enhanced by temporarily stopping the supply of the raw liquid to the filter 10 and then resuming the supply after a certain period of time.

In addition, when the filter transmembrane pressure difference becomes smaller than the minimum allowable pressure difference PL of the filter 10 by, for example, reducing the amount of stock solution sent to the filter 10, the operation of the filtrate supply tube liquid sending section 3p is controlled so that the amount of stock solution sent to the filter 10 is increased. This increases the amount of filtration by the filter 10, which may shorten the filtration operation time. Furthermore, if the amount of stock solution sent to the filter 10 is increased until the filter transmembrane pressure difference falls within the allowable pressure difference of the filter 10, the filtering capacity of the filter 10 can be used effectively, which further enhances the effect of shortening the filtration operation time.

In addition, when the amount of the raw liquid fed to the filter 10 is reduced when the filter transmembrane pressure becomes larger than the maximum allowable differential pressure PM of the filter 10, the amount of the raw liquid fed may be gradually reduced, or the amount of the raw liquid fed may be reduced in a stepwise manner. In addition, when the filter transmembrane pressure becomes larger than the maximum allowable differential pressure PM of the filter 10 (PM in FIG. 24), the feed of the raw liquid to the filter 10 may be stopped for a certain period of time and then started (see FIG. 24). In this case, the amount of the raw liquid fed to the filter 10 may be adjusted while checking the filter transmembrane pressure. For example, as in pattern 1 in FIG. 24, when the feed of the raw liquid to the filter 10 is stopped for a certain period of time and then started, the feed is started at a flow rate of about 1/2 the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is checked. In this state, if the filter transmembrane pressure is smaller than the minimum allowable pressure PL (PL in FIG. 24), the flow rate is increased by about 1/2 the difference between the current flow rate and the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is confirmed. In this state, if the filter transmembrane pressure is still smaller than the minimum allowable pressure PL, the flow rate is further increased by about 1/2 the difference between the current flow rate and the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is confirmed. This operation is repeated, and when the filter transmembrane pressure becomes equal to or greater than the minimum allowable pressure PL and equal to or less than the maximum allowable pressure PM of the filter 10 (or equal to the maximum allowable pressure PM), the increase in the flow rate is stopped. In addition, even if the filter transmembrane pressure is equal to or greater than the minimum allowable pressure PL and equal to or less than the maximum allowable pressure PM of the filter 10, if the maximum allowable flow rate LM has not been reached, the amount of raw liquid sent to the filter 10 may be increased in the same manner while checking the filter transmembrane pressure until it becomes equal to the maximum allowable flow rate LM.
When the amount of the stock solution fed to the filter 10 is increased when the filter transmembrane pressure becomes smaller than the minimum allowable pressure difference PL of the filter 10, the amount of the stock solution fed may be increased gradually. For example, the amount of the stock solution fed to the filter 10 may be increased by a method similar to the above-mentioned method of increasing the flow rate, that is, the method of increasing the flow rate after stopping the feed of the stock solution to the filter 10 for a certain period of time.

In addition, when the filter transmembrane pressure difference is maintained within the allowable pressure difference of the filter 10, the amount of raw liquid sent to the filter 10 may be maintained, but if the flow rate is smaller than the maximum allowable flow rate LM, the amount of raw liquid sent to the filter 10 may be increased until it reaches the maximum allowable flow rate LM.

In addition, if the filter transmembrane pressure difference becomes equal to or exceeds the minimum allowable pressure difference PL of the filter 10, but the amount of raw liquid sent to the filter 10 does not reach the minimum allowable flow rate LL (pattern 3 in Figure 24), it is determined that the hollow fiber membrane 16 or the like is clogged, and the filtration and concentration operation may be stopped and a cleaning operation may be started.

Now, when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10 and the flow rate of the raw liquid in the liquid supply tube 2 is maintained at a flow rate when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the concentrated liquid tube delivery section 4p can be controlled as follows based on the concentrator transmembrane pressure difference.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the concentrate tube delivery unit 4p is operated to reduce the amount of concentrate delivered to the concentrate bag CB. In other words, the operation of the concentrate tube delivery unit 4p is controlled to increase the concentration of the concentrate.

<Step 2>
Then, the amount of concentrate sent to the concentrate bag CB is reduced until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the concentrate tube sending unit 4p is controlled so as to maintain the flow rate of the concentrate in the concentrate tube 4 at the flow rate when the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20.

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrated liquid tube sending unit 4p is controlled to increase the amount of concentrated liquid sent to the concentrated liquid bag CB. Note that as the amount of concentrated liquid sent increases, the concentration ratio decreases, but the operation of the concentrated liquid tube sending unit 4p is controlled to decrease the concentration ratio (to decrease the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.
In addition, if the concentration ratio becomes smaller than the allowable concentration ratio when the amount of concentrated liquid sent is increased in order to maintain the concentrator transmembrane pressure within the allowable pressure range, the following method (method 2) can be used to deal with this.

When the amount of concentrated liquid sent to the concentrated liquid bag CB increases, the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid tube sending section 4p is again operated to reduce the amount of concentrated liquid sent to the concentrated liquid bag CB.

That is, while the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the above steps 1 to 3 are repeated. By adopting this method, it is possible to ensure the maximum filtration flow rate (i.e., the above-mentioned maximum allowable flow rate LM) and the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the filter 10 and the concentrator 20, which is impossible when the amount of liquid sent to the filter 10 and the concentrated liquid bag CB is constant, and according to the state of the raw liquid (concentration of the substance causing the clogging of the filter or concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated liquid from the raw liquid can be shortened, and re-concentration work can be prevented or the time required for re-concentration work can be shortened.
Moreover, by operating as described above, it becomes possible to quickly remove the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit when filtration and concentration starts, and the cleaning liquid in the filter 10 and the circuit immediately after cleaning the filter 10, as waste liquid from the concentrator 20. In other words, it is possible to efficiently prevent dilution of the concentrated liquid by the cleaning liquid at the start of filtration and concentration and immediately after cleaning the filter, as described above.

The above method (first method) is preferably adopted when the maximum allowable pressure difference PM of the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM of the concentrator transmembrane pressure difference, but is not limited to this condition. It can also be adopted when the maximum allowable pressure difference PM of the filter transmembrane pressure difference is smaller than the maximum allowable pressure difference PM of the concentrator transmembrane pressure difference.
In addition, when the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM, or when the filter transmembrane pressure difference is smaller than the minimum allowable pressure difference PL, and further when the amount of raw liquid sent to the filter 10 is constant regardless of the filter transmembrane pressure difference, the above steps 1 to 3 may be repeated to adjust the amount of concentrated liquid sent to the concentrator 20.

<Second Method>
In the first method, the flow rate of the concentrated liquid in the concentrated liquid tube 4 was adjusted based on the concentrator transmembrane pressure difference. However, the amount of the filtrate sent to the concentrator 20 can also be adjusted based on the concentrator transmembrane pressure difference as described below.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the filtrate supply tube delivery section 3p is operated to increase the amount of filtrate delivered to the concentrator 20 (in other words, the amount of raw liquid delivered to the filter 10). In other words, the operation of the filtrate supply tube delivery section 3p is controlled so as to increase the amount of filtrate produced and delivered to the concentrator 20.

<Step 2>
Then, the amount of filtrate produced and sent to the concentrator 20 (in other words, the amount of raw liquid sent to the filter 10) is increased until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20 (above the minimum allowable pressure and below the maximum allowable pressure). When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the operation of the filtrate supply tube sending section 3p is controlled so that the amount of filtrate sent to the concentrator 20 is maintained at the flow rate when the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. In this case, the amount of raw liquid sent to the filter 10 deviates from the flow rate when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10, but it is desirable to maintain the flow rate of the raw liquid within the allowable flow rate (above the minimum allowable flow rate and below the maximum allowable flow rate).

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the operation of the filtrate supply tube delivery section 3p is controlled so as to reduce the amount of filtrate sent to the concentrator 20. In other words, the operation of the filtrate supply tube delivery section 3p is controlled so as to reduce the amount of filtrate produced and sent to the concentrator 20. Note that even in this case, the amount of stock solution sent to the filter 10 will deviate from the flow rate when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, but it is desirable to maintain the flow rate of the stock solution within the allowable flow rate.

When the amount of filtrate sent to the concentrator 20 decreases, the concentrator transmembrane pressure difference decreases, so when the transmembrane pressure difference falls below the minimum allowable pressure difference of the concentrator 20, the filtrate supply tube delivery section 3p is again operated to increase the flow rate of the raw liquid in the supply tube 2.

That is, while the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the above steps 1 to 3 are repeated. By adopting this method, it is possible to ensure the maximum filtration flow rate (i.e., the above-mentioned maximum allowable flow rate LM) and the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the filter 10 and the concentrator 20, which is impossible when the amount of liquid sent to the filter 10 and the concentrated liquid bag CB is constant, and according to the state of the raw liquid (concentration of the substance causing the clogging of the filter or concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated liquid from the raw liquid can be shortened, and re-concentration work can be prevented or the time required for re-concentration work can be shortened.
Moreover, by operating as described above, it becomes possible to quickly remove the cleaning liquid filled in the filter 10, concentrator 20, and the circuit at the start of filtration and concentration, and the cleaning liquid in the filter 10 and the circuit immediately after cleaning the filter 10, as waste liquid from the concentrator 20. In other words, it is possible to efficiently prevent dilution of the concentrated liquid by the cleaning liquid at the start and immediately after cleaning the filter, as described above.

The above method (second method) is preferably adopted when the maximum allowable differential pressure PM of the filter transmembrane pressure is greater than the maximum allowable differential pressure PM of the concentrator transmembrane pressure, but is not limited to this condition. It can also be adopted when the maximum allowable differential pressure PM of the filter transmembrane pressure is smaller than the maximum allowable differential pressure PM of the concentrator transmembrane pressure.
In addition, when the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM, or when the filter transmembrane pressure difference is smaller than the minimum allowable pressure difference PL, and further when the amount of raw liquid sent to the filter 10 is constant regardless of the filter transmembrane pressure difference, the above steps 1 to 3 may be repeated to adjust the amount of concentrated liquid sent to the concentrator 20.

<About cleaning the filter>
In the raw liquid treatment device 1B of the second embodiment, when the above-mentioned filtration and concentration work is performed, the filter transmembrane pressure becomes larger than the maximum allowable differential pressure PM of the filter 10 due to clogging of the filter 10, etc. In this case, by reducing the flow rate of the raw liquid in the liquid supply tube 2, the filter transmembrane pressure can be made smaller than the maximum allowable differential pressure PM of the filter 10, and the filter transmembrane pressure can be maintained within the allowable differential pressure (a range from the minimum allowable differential pressure PL to the maximum allowable differential pressure PM). However, when the clogging of the filter 10 becomes severe, the flow rate of the raw liquid in the liquid supply tube 2 is reduced in order to maintain the filter transmembrane pressure within the allowable differential pressure of the filter 10, and the flow rate of the raw liquid in the liquid supply tube 2 may become smaller than the minimum allowable flow rate LL. When this state occurs, the filter 10 is cleaned during the filtration and concentration work of the raw liquid treatment device 1B of the second embodiment.

As shown in FIG. 22, the flow rate adjustment means 2c blocks the liquid supply tube 2 so that no liquid flows inside. In addition, the operation of the filtrate supply tube delivery section 3p and the concentrate tube delivery section 4p is stopped and they function as clamps. When cleaning the filter during the filtration and concentration work, after the completion of the preparatory cleaning work, a cleaning liquid bag SB is connected to the other end of the cleaning liquid supply tube 6 instead of the cleaning liquid recovery bag FB, and a cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid recovery tube 7 instead of the cleaning liquid bag SB.

In the above state, the cleaning liquid supply tube delivery unit 6p is operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 to the filter 10, and the cleaning liquid recovery tube delivery unit 7p is operated to flow the cleaning liquid from the filter 10 to the cleaning liquid recovery bag FB connected to the cleaning liquid recovery tube 7. This allows the cleaning liquid to flow inside the hollow fiber membrane 16 in the opposite direction to the direction in which the raw liquid flows during filtration and concentration, so that the inside of the hollow fiber membrane 16 can be cleaned with the cleaning liquid.

After the preparatory cleaning operation is completed, a cleaning liquid bag SB is connected to the other end of the connecting tube 9 instead of the cleaning liquid recovery bag FB. Then, if the flow rate adjustment means 9c is used to allow liquid to flow through the connecting tube 9, in addition to the above state, cleaning liquid can also be supplied to the filter 10 from the cleaning liquid bag SB connected to the connecting tube 9. Then, the cleaning liquid supplied through the connecting tube 9 permeates the hollow fiber membrane 16 in the opposite direction to the direction in which the filtrate permeates the hollow fiber membrane 16, so clogging of the hollow fiber membrane 16 can be eliminated. In this case, cleaning liquid is supplied to the filter 10 from both the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 and the cleaning liquid bag SB connected to the connecting tube 9, so that the flow rate of the cleaning liquid flowing through the cleaning liquid recovery tube 7 by the cleaning liquid recovery tube liquid delivery part 7p is adjusted to be greater than the flow rate of the cleaning liquid flowing through the cleaning liquid supply tube 6 by the cleaning liquid supply tube liquid delivery part 6p.

When the flow rate adjustment means 9c is used to allow liquid to flow through the connecting tube 9, the cleaning liquid recovery tube sending section 7p may be operated while the cleaning liquid supply tube sending section 6p is stopped. In this case, cleaning liquid is supplied to the filtrate 10 only from the cleaning liquid bag SB connected to the connecting tube 9. In this case, too, the cleaning liquid permeates the hollow fiber membrane 16 in the opposite direction to the direction in which the filtrate permeates the hollow fiber membrane 16, so clogging of the hollow fiber membrane 16 can be eliminated.

When a filter having a hollow fiber membrane 16 as shown in FIG. 5 is used as the filter 10, it is desirable for the control unit 106 to adjust the amount and timing of the cleaning liquid supplied to the filter 10 so that the above-mentioned cleaning of the filter 10 and the concentrator 20 can be properly performed. In other words, it is desirable to adjust the amount and timing of the cleaning liquid supplied to the filter 10 so that the cleaning liquid permeates the hollow fiber membrane 16 while filling the hollow space 12h of the body 12 up to the region of the hollow fiber membrane 16 where cleaning is to be performed.

<Filtrate recovery>
On the other hand, when the filter is washed by the above-mentioned method, the filtrate remaining in the internal space 12h of the main body 11 of the filter 10 is mixed with the washing liquid and discharged, which reduces the amount of the active ingredient recovered by filtration and concentration.

Therefore, when cleaning the filter, it is preferable to first send the filtrate present in the internal space 12h of the main body 11 of the filter 10 to the concentrator 20 and then perform the filter cleaning.

<Recovery using cleaning fluid (outside)>

7, the cleaning solution bag SB is connected to the port 11c (the port 11c to which the filtrate supply tube 3 is not connected, hereinafter referred to as the cleaning port 11c) of the main body 11 of the filter 10 via a tube. Then, the filtrate supply tube sending part 3p maintains the state in which the liquid flows from the filter 10 to the concentrator 20, and the concentrated liquid tube sending part 4p continues to operate, while the liquid supply tube 2 is blocked by the flow rate adjustment means 2c. In this state, if the cleaning solution is supplied from the cleaning solution bag SB to the filter 10 by the pump provided on the tube, the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20, and instead the cleaning solution is supplied from the cleaning solution bag SB to the internal space 12h. Eventually, when all the filtrate in the internal space 12h is replaced with the cleaning solution, the operation of the filtrate supply tube sending part 3p is stopped to block the filtrate supply tube 3, and the operation of the concentrated liquid tube sending part 4p is stopped. After this state is reached, cleaning the filter 10 using the cleaning method for the filter 10 described above can prevent the filtrate discharged together with the cleaning liquid from being reconcentrated.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the internal space 12h has been replaced with the cleaning liquid can be determined theoretically by counting the amount of pumping provided in the tube connected to the cleaning port 11c, or by measuring the concentration of the concentrated liquid. It can also be determined by looking at the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a hydrometer.

The tube connected to the cleaning port 11c of the main body 11 of the filter 10 does not necessarily need to be provided with a pump. Even in this case, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be replaced with cleaning liquid by operating the filtrate supply tube delivery unit 3p. When both the pump provided on the tube connected to the cleaning port 11c and the filtrate supply tube delivery unit 3p are operated, they are operated so that the flow rates of both are the same.

<Recovery using air or other gas>
In addition, in the above explanation, a case was described in which the cleaning solution bag SB was connected to the cleaning port 11c of the main body 11 of the filter 10 via a tube, but a gas such as air may also be supplied to the cleaning port 11c of the main body 11 of the filter 10 via a tube.

In this case, the filtrate supply tube sending part 3p maintains the state in which the liquid flows from the filter 10 to the concentrator 20, and the flow rate adjustment means 2c closes the liquid supply tube 2 while the concentrated liquid tube sending part 4p continues to operate. In this state, if a gas such as air is supplied to the filter 10 from a tube connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body part 11 of the filter 10 can be supplied to the concentrator 20. When all the filtrate in the internal space 12h is eventually discharged, the operation of the filtrate supply tube sending part 3p is stopped and it functions as a clamp to block the filtrate supply tube 3, and the operation of the concentrated liquid tube sending part 4p is stopped. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the internal space 12h has been discharged can be determined by installing a liquid detector or air bubble detector in the filtrate supply tube 3, measuring the pressure in the filtrate supply tube 3, or theoretically calculating the amount of water pumped out by counting the amount of water pumped out.

In addition, when the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the internal space 12h of the main body 11 of the filter 10 is filled with a gas such as air. Therefore, when performing a cleaning operation after collecting the filtrate, it is desirable to first fill the hollow space 12h of the body 12 up to the area to be cleaned in the hollow fiber membrane 16 (or the entire hollow space 12h of the body 12) with cleaning liquid before performing the cleaning operation.

<Collecting in a bag>
In the above example, the filtrate is sent to the concentrator 20 and collected in a concentrated state, but the filtrate may be collected as it is. For example, a bag for collecting the filtrate is connected to the filtrate supply tube 3 upstream of the filtrate supply tube sending section 3p (i.e., the filter 10 side). In this state, if the filtrate supply tube sending section 3p makes the filtrate supply tube 3 in a state where liquid does not flow, and a cleaning liquid or a gas such as air is supplied to the filter 10 from the cleaning port 11c as described above, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be collected in the bag. In this case, the filtrate can be collected in a short time compared to the case where the filtrate is sent to the concentrator 20 and collected in a concentrated state, so that the transition to the cleaning operation can be performed quickly.

Although the bag for collecting the filtrate is placed upstream of the filtrate supply tube sending section 3p, it may be placed downstream of the filtrate supply tube sending section 3p as long as it is placed before the concentrator 20. In this case, the filtrate can be made to flow toward the bag by operating the filtrate supply tube sending section 3p, so there is no need to provide a pump on the tube connected to the cleaning port 11c. Instead, it is necessary to provide a device capable of closing and opening the tube, such as a clamp, on the upstream side of the bag and on the tube connected to the cleaning port 11c.

<Recovery using cleaning fluid (inside)>
In the above description, the raw liquid is supplied into the through-flow passages 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15 of the filter 10, and the filtrate is discharged into the internal space 12h of the trunk 12 of the main body 11 of the filter 10. However, the raw liquid may be supplied from the filtrate discharge port 11c into the internal space 12h of the trunk 12 of the main body 11, and the filtered filtrate may be discharged into the through-flow passages 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15, and then discharged to the outside from the raw liquid supply port 11a.

In this case, the tubes are connected as follows.
First, the filtrate supply tube 3 is connected to the raw liquid supply port 11a, the supply tube 2 is connected to the port 11c (i.e., the above-mentioned cleaning port 11c), the cleaning liquid supply tube 6 is connected to the port 11c (i.e., the above-mentioned filtrate discharge port 11c) to which the supply tube 2 is not connected, and the cleaning liquid bag SB that was connected to the cleaning port 11c is connected to the cleaning liquid supply port 11b.

Then, while maintaining the state in which the liquid flows from the filter 10 to the concentrator 20 by the filtrate supply tube liquid sending part 3p and continuing the operation of the concentrated liquid tube liquid sending part 4p, the liquid supply tube 2 is blocked by the flow rate adjustment means 2c. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by the pump provided on the tube connected to the cleaning liquid supply port 11b, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20, and instead, the cleaning liquid is supplied from the cleaning liquid bag SB to the through flow path 16h. When the filtrate in the through flow path 16h is completely replaced with the cleaning liquid, the operation of the filtrate supply tube liquid sending part 3p is stopped to block the filtrate supply tube 3, and the operation of the concentrated liquid tube liquid sending part 4p is stopped. After this state is reached, if the filter 10 is washed by the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the internal space 12h has been replaced with the cleaning liquid can be determined theoretically by counting the amount of pumping provided in the tube connected to the cleaning port 11c, or by measuring the concentration of the concentrated liquid. It can also be determined by looking at the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a hydrometer.

<Recovery using air or other gas>
In addition, in the above explanation, a case was described in which the cleaning solution bag SB was connected to the cleaning solution supply port 11b of the main body 11 of the filter 10 via a tube, but a gas such as air may also be supplied to the cleaning solution supply port 11b of the main body 11 of the filter 10 via a tube.

In this case, the filtrate supply tube delivery section 3p maintains the state in which the liquid flows from the filter 10 to the concentrator 20, and the flow rate adjustment means 2c closes the liquid supply tube 2. In this state, if a gas such as air is supplied to the filter 10 from the tube, the filtrate in the through passage 16h of the hollow fiber membrane 16 of the filter 10 can be supplied to the concentrator 20. When all the filtrate in the through passage 16h of the hollow fiber membrane 16 is eventually discharged, the operation of the filtrate supply tube delivery section 3p is stopped and made to function as a clamp to block the filtrate supply tube 3, and the operation of the concentrated liquid tube delivery section 4p is stopped. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the through-flow passage 16h of the hollow fiber membrane 16 has been discharged can be determined by providing a liquid detector or air bubble detector in the filtrate supply tube 3, measuring the pressure in the filtrate supply tube 3, or theoretically calculating the amount of pump feed by counting the amount of pump feed.

In addition, when the filtrate in the through passage 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the through passage 16h of the hollow fiber membrane 16 of the filter 10 is filled with a gas such as air. Therefore, when performing a cleaning operation after collecting the filtrate, it is desirable to first fill the through passage 16h with cleaning liquid up to the area of the hollow fiber membrane 16 to be cleaned (or the entire hollow fiber membrane 16) before performing the cleaning operation.

<Collecting in a bag>
In the above example, the filtrate is sent to the concentrator 20 and collected in a concentrated state, but the filtrate may be collected as it is. For example, a bag for collecting the filtrate is connected to the filtrate supply tube 3 upstream of the filtrate supply tube sending section 3p (i.e., the filter 10 side). In this state, if the filtrate supply tube sending section 3p makes the filtrate supply tube 3 in a state where no liquid flows, and the cleaning liquid or gas such as air is supplied to the filter 10 from the cleaning liquid supply port 11b as described above, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be collected in the bag. In this case, the filtrate can be collected in a short time compared to the case where the filtrate is sent to the concentrator 20 and collected in a concentrated state, so that the transition to the cleaning operation can be performed quickly.

Although the bag for collecting the filtrate is placed upstream of the filtrate supply tube sending section 3p, it may be placed downstream of the filtrate supply tube sending section 3p as long as it is placed before the concentrator 20. In this case, the filtrate can be made to flow toward the bag by operating the filtrate supply tube sending section 3p, so there is no need to provide a pump on the tube connected to the cleaning port 11c. Instead, it is necessary to provide a device capable of closing and opening the tube, such as a clamp, on the upstream side of the bag and on the tube connected to the cleaning port 11c.

<Another Example of Method for Recovering Liquid from Filter 10>
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, it is desirable to adjust the flow rate when sending the filtrate to the concentrator 20 based on the transmembrane pressure of the concentrator 20. By adopting such a method, even if the concentrator 20 should become clogged, an increase in the transmembrane pressure of the concentrator can be suppressed and processing can be prevented from being stopped, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate when sending liquid to the concentrator 20 based on the concentrator transmembrane pressure of the concentrator 20, the flow rate can be adjusted as follows. First, when the concentrator transmembrane pressure of the concentrator 20 is within a set differential pressure range, the operation of the filtrate supply tube sending unit 3p and the operation of the concentrate tube sending unit 4p are controlled so as to maintain the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the concentrator transmembrane pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the filtrate supply tube delivery unit 3p and the operation of the concentrate tube delivery unit 4p are controlled so as to reduce the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the set differential pressure and being unable to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the filtrate supply tube delivery unit 3p and the operation of the concentrate tube delivery unit 4p are controlled so as to increase the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference and the concentrated liquid becoming diluted.

<Yet another example of the method for recovering liquid from the filter 10>
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, the flow rate from the concentrator 20 to the concentrated liquid bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the concentration ratio, may be adjusted based on the transmembrane pressure of the concentrator 20. In this method, the increase in the transmembrane pressure of the concentrator can be suppressed, and at the same time, the speed at which the concentrated liquid is recovered can be kept constant without changing the flow rate of the liquid sent from the filter 10 to the concentrator 20, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB based on the transmembrane pressure difference of the concentrator 20, the flow rates can be adjusted as follows:

First, when the transmembrane pressure of the concentrator 20 is within the set differential pressure range, the operation of the concentrate tube sending part 4p (or the operation of the waste tube sending part 5p if provided) or the operation of the filtrate supply tube sending part 3p is controlled so as to maintain the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range.
On the other hand, when the concentrator transmembrane pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the concentrate tube sending part 4p (if the waste liquid tube sending part 5p is provided, the operation of the waste liquid tube sending part 5p) or the filtrate supply tube sending part 3p is controlled so as to increase the flow rate from the concentrator 20 to the concentrate bag CB and/or decrease the flow rate from the concentrator 20 to the waste liquid bag DB. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set differential pressure and being unable to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrate tube sending part 4p (or the operation of the waste liquid tube sending part 5p if provided) or the operation of the filtrate supply tube sending part 3p is controlled so as to decrease the flow rate from the concentrator 20 to the concentrate bag CB and/or increase the flow rate from the concentrator 20 to the waste liquid bag DB. This prevents the concentrator transmembrane pressure from continuing to decrease below the minimum set pressure difference, thereby preventing problems such as dilution of the concentrate.

The set differential pressure of the concentrator transmembrane pressure when recovering the filtrate from the filter 10 may be the same as the allowable differential pressure in the filtration and concentration work, or the set differential pressure may be a value different from the allowable differential pressure. For example, if the allowable differential pressure has a certain range, the set differential pressure range may be wider than the allowable differential pressure range. In this case, it is desirable in that even if the concentrated liquid is in a diluted state, it can be recovered to the end as much as possible. Furthermore, there may be a discrepancy between the allowable differential pressure range and the set differential pressure range.

<Reconcentration process>
When the concentrate obtained by the filtration and concentration process is to be further concentrated, a re-concentration process is carried out.

As shown in FIG. 8, in the re-concentration operation of the raw liquid treatment device 1B of the second embodiment, the other end of the connecting tube 9 is detached from the cleaning liquid bag SB, and a concentrated liquid bag CB is connected to the other end of the connecting tube 9.
The flow rate adjusting means 9c maintains a state in which liquid can flow through the connecting tube 9, while the cleaning liquid supply tube sending section 6p and the cleaning liquid recovery tube sending section 7p are not operated and function as clamps. In addition, the flow rate adjusting means 2c closes the liquid supply tube 2 so that no liquid flows through it. This puts the filter 10 in a state in which no liquid flows through it.

In the above state, the filtrate supply tube delivery unit 3p is operated so that the concentrate flows from the concentrate bag CB through the connecting tube 9 to the concentrator 20, and the concentrate tube delivery unit 4p is operated so that the concentrate flows from the concentrator 20 through the concentrate tube 4 to the concentrate bag CB.

Then, the concentrated liquid is supplied from the concentrated liquid bag CB connected to the connecting tube 9 to the concentrator 20 through the connecting tube 9, and the re-concentrated liquid further concentrated by the concentrator 20 is collected in the concentrated liquid bag CB through the concentrated liquid tube 4. Meanwhile, the water separated from the concentrated liquid is collected in the waste liquid bag DB through the waste liquid tube 5. In other words, a concentrated liquid (re-concentrated liquid) with a higher concentration rate can be obtained.

<Explanation of reconcentration using transmembrane pressure difference in concentrator>
In the reconcentration operation, the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the reconcentration rate, may be adjusted based on the transmembrane pressure of the concentrator 20. This method has the effect of suppressing an increase in the transmembrane pressure of the concentrator, while at the same time shortening the time required to produce a highly concentrated liquid.

In this case, when performing reconcentration work using the concentrator transmembrane pressure difference in advance, it is desirable to set an allowable pressure difference. In other words, a pressure difference (allowable pressure difference) that the concentrator 20 can tolerate is set according to the concentrator 20. This allowable pressure difference may have a predetermined range, or may be set to a specific value. In the following, a case where the allowable pressure difference has a predetermined range will be described as a representative example.

When performing reconcentration using the concentrator transmembrane pressure difference, it is desirable to set an allowable flow rate in advance. In other words, it is desirable to set the allowable flow rate (allowable flow rate) of the concentrated liquid in the filtrate supply tube 3. This allowable flow rate may have a predetermined range, or may be set to a specific value. Such an allowable flow rate does not necessarily have to be set. However, if the flow rate of the concentrated liquid in the filtrate supply tube 3 becomes too low, the time required for reconcentration will be too long. Therefore, in order to prevent the processing time of the concentrated liquid from becoming too long, it is desirable to set an allowable flow rate.

Furthermore, when performing reconcentration using the transmembrane pressure difference of the concentrator, it is desirable to set an allowable concentration ratio in advance. In other words, it is desirable to set the ratio (allowable concentration ratio) of the flow rate of the concentrate flowing through the concentrate tube 4 to the flow rate of the concentrate in the filtrate supply tube 3 (in other words, in the connecting tube 9). This allowable concentration ratio may have a predetermined range or may be set to a specific value. Such an allowable concentration ratio does not necessarily have to be set. However, if the concentration ratio, which is the ratio of the flow rate of the concentrate flowing through the concentrate tube 4 to the flow rate of the concentrate in the filtrate supply tube 3, drops too much (i.e., if the flow rate of the concentrate becomes too large), the concentration efficiency will deteriorate, and the reconcentration process will take time. Therefore, in order to prevent the concentration ratio from dropping too much, it is desirable to set an allowable concentration ratio. In addition, the allowable concentration ratio in the reconcentration work may be the same as the allowable flow rate in filtration concentration, or may be different from the allowable concentration ratio in filtration concentration.

At the start of reconcentration, the filtrate supply tube sending section 3p is operated to increase the amount of concentrated liquid sent to the concentrator 20. At this time, the concentrated liquid tube sending section 4p is operated so that the concentrated liquid is concentrated to a predetermined concentration ratio in accordance with the flow rate of the filtrate in the filtrate supply tube 3. For example, when a concentrated liquid with a concentration ratio of 10 is produced, the operation of the concentrated liquid tube sending section 4p is adjusted so that the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 is 1/10 of the flow rate of the filtrate flowing through the filtrate supply tube 3. In addition, the operation of the concentrated liquid tube sending section 4p may be adjusted so that the concentrator transmembrane pressure becomes a set value within the allowable pressure difference (or is maintained within the allowable pressure difference) instead of the concentration ratio of the concentrated liquid or while maintaining the concentrated liquid at a predetermined concentration ratio. Note that while the amount of concentrated liquid sent to the concentrator 20 is being increased, the operation of the concentrated liquid tube sending section 4p is controlled so that any of the above states is achieved.

As the reconcentration progresses, clogging of the concentrator 20 gradually occurs. This causes the concentrator transmembrane pressure difference to rise. However, the filtrate supply tube delivery section 3p operates to increase the amount of concentrated liquid delivered to the concentrator 20 until the concentrator transmembrane pressure difference reaches the allowable pressure difference.

<First Method>
The amount of filtrate sent to the concentrator 20 continues to increase until the concentrator transmembrane pressure becomes the allowable differential pressure of the concentrator 20. Then, the filtrate supply tube sending unit 3p is controlled so as to maintain the amount of concentrated liquid sent to the concentrator 20 at a flow rate when the concentrator transmembrane pressure becomes the allowable differential pressure of the concentrator 20. Meanwhile, based on the concentrator transmembrane pressure, the concentrated liquid tube sending unit 4p is operated as follows to adjust the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the allowable pressure difference of the concentrator 20, the concentrated liquid tube sending unit 4p is operated to reduce the amount of concentrated liquid sent to the concentrated liquid bag CB. In other words, the operation of the concentrated liquid tube sending unit 4p is controlled to increase the concentration of the concentrated liquid.

<Step 2>
Then, the amount of concentrate sent to the concentrate bag CB is reduced until the concentrator transmembrane pressure becomes equal to the allowable differential pressure of the concentrator 20. When the concentrator transmembrane pressure becomes equal to the allowable differential pressure of the concentrator 20, the concentrate tube sending unit 4p is controlled so as to maintain the flow rate of the concentrate in the concentrate tube 4 at the flow rate when the concentrator transmembrane pressure becomes the allowable differential pressure of the concentrator 20.

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrated liquid tube sending unit 4p is controlled to increase the amount of concentrated liquid sent to the concentrated liquid bag CB. Note that as the amount of concentrated liquid sent increases, the concentration ratio decreases, but the operation of the concentrated liquid tube sending unit 4p is controlled to decrease the concentration ratio (to decrease the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.
In addition, if the concentration ratio becomes smaller than the allowable concentration ratio when the amount of concentrated liquid sent is increased in order to maintain the concentrator transmembrane pressure within the allowable pressure range, the following method (method 2) can be used to deal with this.

When the amount of concentrated liquid sent to the concentrated liquid bag CB increases, the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid tube sending section 4p is again operated to reduce the amount of concentrated liquid sent to the concentrated liquid bag CB.

In other words, steps 1 to 3 are repeated as long as the concentrator transmembrane pressure difference is within the allowable pressure difference of the concentrator 20. By adopting this method, it is possible to ensure the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the concentrator 20, which is not possible when the amount of liquid sent to the concentrate bag CB is constant, and according to the state of the concentrate (concentration of the substance causing the clogging of the concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the concentration efficiency, the time required to produce a highly concentrated concentrate can be shortened, and the time required for re-concentration work can be shortened.

<Second Method>
In the first method, the flow rate of the concentrated liquid in the concentrated liquid tube 4 was adjusted based on the transmembrane pressure difference of the concentrator. However, it is also possible to adjust the flow rate of the concentrated liquid in the connecting tube 9 based on the transmembrane pressure difference of the concentrator as described below.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the allowable pressure difference (minimum allowable pressure difference) of the concentrator 20, the filtrate supply tube delivery section 3p is operated to increase the amount of concentrated liquid delivered to the concentrator 20.

<Step 2>
Then, the amount of concentrated liquid sent to the concentrator 20 is increased until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the operation of the filtrate supply tube liquid sending section 3p is controlled so as to maintain the amount of concentrated liquid sent to the concentrator 20 at a flow rate in a state in which the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. In this case, it is desirable to maintain the amount of concentrated liquid sent to the concentrator 20 within the allowable flow rate (not less than the minimum allowable flow rate and not more than the maximum allowable flow rate).

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the operation of the filtrate supply tube sending unit 3p is controlled so as to reduce the amount of concentrated liquid sent to the concentrator 20. In other words, the operation of the filtrate supply tube sending unit 3p is controlled so as to reduce the flow rate sent to the concentrator 20. Note that even in this case, it is desirable to maintain the amount of concentrated liquid sent to the concentrator 20 within the allowable flow rate range.

When the amount of concentrated liquid sent to the concentrator 20 decreases, the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference falls below the minimum allowable pressure difference of the concentrator 20, the filtrate supply tube liquid sending section 3p is again operated to increase the flow rate of concentrated liquid in the filtrate supply tube 3.

That is, while the concentrator transmembrane pressure difference is within the allowable pressure difference of the concentrator 20, the above steps 1 to 3 are repeated. By adopting this method, it becomes possible to ensure the maximum recirculation flow rate and maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the concentrator 20, which is impossible when the amount of liquid sent to the concentrator 20 is constant, and according to the state of the concentrated liquid (concentration of the substance causing the clogging of the concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the recirculation efficiency and concentration efficiency, the time required to produce a highly concentrated liquid can be shortened, and the time required for the reconcentration work can be shortened.
Moreover, by operating as described above, it becomes possible to quickly remove the cleaning liquid in the concentrator 20 and in the circuit immediately after cleaning the filter 10 as waste liquid from the concentrator 20. In other words, it is possible to effectively prevent dilution of the concentrated liquid by the cleaning liquid immediately after cleaning the filter, as described above.

The allowable pressure difference of the concentrator transmembrane pressure during reconcentration may be the same as the allowable pressure difference during the filtration and concentration work, or may be a value (range) different from the allowable pressure difference during the filtration and concentration work. For example, when the allowable pressure difference during the filtration and concentration work has a certain range, the allowable pressure difference during the reconcentration may be wider than that range. In this case, when treating a stock solution that is prone to clogging the filter 10, the filtration and concentration work is performed slowly so as not to apply pressure to the filter 10, but instead a highly concentrated solution can be produced, which is desirable in that the time required for the reconcentration work can be shortened. In addition, when the allowable pressure difference during reconcentration is narrower than the allowable pressure difference during the filtration and concentration work, when treating a stock solution that is prone to clogging the concentrator 20, the filtration and concentration work is performed in a short time without applying pressure to the concentrator 20, which is desirable in that a highly concentrated solution can be produced in the reconcentration work. Furthermore, there may be a difference between the allowable pressure difference during the filtration and concentration work and the allowable pressure difference during the reconcentration work.
The allowable concentration ratio in reconcentration may be the same as the allowable concentration ratio in the filtration and concentration work, or may be a value (range) different from the allowable concentration ratio in the filtration and concentration work. For example, when the allowable concentration ratio in the filtration and concentration work has a certain range, the range of the allowable concentration ratio in the reconcentration may be wider than that range. In this case, it is desirable in that the time of the reconcentration work can be shortened instead of concentrating the filtration and concentration work for a long time. In addition, when the range of the allowable concentration ratio in the reconcentration is narrower than the range of the allowable concentration ratio in the filtration and concentration work, it is desirable in that the filtration and concentration work can be completed quickly instead of concentrating the reconcentration work for a long time. Furthermore, there may be a difference between the range of the allowable concentration ratio in the filtration and concentration work and the range of the allowable concentration ratio in the reconcentration.

<Example of method for recovering liquid from filter 10>
Before carrying out the above-mentioned reconcentration operation, the filtrate in the filter 10 is sent to the concentrator 20 and collected as a concentrated liquid. In this case, it is desirable to adjust the flow rate when sending the filtrate to the concentrator 20 based on the transmembrane pressure of the concentrator 20. By adopting such a method, even if the concentrator 20 becomes clogged, the increase in the transmembrane pressure of the concentrator can be suppressed and the process can be prevented from being stopped, so that the filtrate in the filter 10 can be effectively collected.

For example, when adjusting the flow rate when sending liquid to the concentrator 20 based on the concentrator transmembrane pressure of the concentrator 20, the flow rate can be adjusted as follows. First, when the concentrator transmembrane pressure of the concentrator 20 is within a set differential pressure range, the operation of the filtrate supply tube sending unit 3p and the operation of the concentrate tube sending unit 4p are controlled so as to maintain the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the concentrator transmembrane pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the filtrate supply tube delivery unit 3p and the operation of the concentrate tube delivery unit 4p are controlled so as to reduce the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set differential pressure and being unable to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the filtrate supply tube delivery unit 3p and the operation of the concentrate tube delivery unit 4p are controlled so as to increase the amount of liquid delivered from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference and the concentrated liquid becoming diluted.

<Another Example of Method for Recovering Liquid from Filter 10>
Furthermore, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, the flow rate from the concentrator 20 to the concentrated liquid bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the concentration ratio, may be adjusted based on the transmembrane pressure of the concentrator 20. In this method, the increase in the transmembrane pressure of the concentrator can be suppressed, and at the same time, the recovery speed can be kept constant without changing the flow rate of the liquid sent from the filter 10 to the concentrator 20, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB based on the transmembrane pressure difference of the concentrator 20, the flow rates can be adjusted as follows:

First, when the transmembrane pressure of the concentrator 20 is within the set differential pressure range, the operation of the concentrate tube sending part 4p (or the operation of the waste tube sending part 5p if provided) or the operation of the filtrate supply tube sending part 3p is controlled so as to maintain the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range.
On the other hand, when the concentrator transmembrane pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the concentrate tube sending part 4p (if the waste liquid tube sending part 5p is provided, the operation of the waste liquid tube sending part 5p) or the filtrate supply tube sending part 3p is controlled so as to increase the flow rate from the concentrator 20 to the concentrate bag CB and/or decrease the flow rate from the concentrator 20 to the waste liquid bag DB. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set differential pressure and being unable to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrate tube sending part 4p (or the operation of the waste liquid tube sending part 5p if provided) or the operation of the filtrate supply tube sending part 3p is controlled so as to decrease the flow rate from the concentrator 20 to the concentrate bag CB and/or increase the flow rate from the concentrator 20 to the waste liquid bag DB. This prevents the concentrator transmembrane pressure from continuing to decrease below the minimum set pressure difference, thereby preventing problems such as dilution of the concentrate.

The set differential pressure of the concentrator transmembrane pressure when recovering the filtrate from the filter 10 may be the same as the allowable differential pressure in the filtration and concentration work, or the set differential pressure may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the set differential pressure range may be wider than the allowable differential pressure range. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the set differential pressure range is narrower than the allowable differential pressure range, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, there may be a discrepancy between the allowable differential pressure range and the set differential pressure range.

<Recovery of concentrator 20>
In the case where the concentrate in the concentrator 20 is also recovered after recovering the raw liquid or filtrate in the filter 10, the concentrate may be recovered by simply passing a fluid such as a cleaning liquid or a gas (hereinafter simply referred to as a fluid) through the concentrator 20. However, as in the above-mentioned case, the flow rate of the fluid supplied to the concentrate 20 may be adjusted while measuring the concentrator transmembrane pressure difference. This can prevent problems such as the concentrator transmembrane pressure increasing and making it impossible to continue the treatment. If the concentrator transmembrane pressure of the concentrator 20 becomes larger than the set pressure difference, the liquid transfer (including the flow of gas) from the filter 10 to the concentrator 20 is stopped, and problems such as the concentrator transmembrane pressure continuing to rise can be prevented.

The set differential pressure (second set differential pressure) of the concentrator transmembrane pressure when recovering the concentrated liquid from the concentrator 20 may be the same as the allowable differential pressure in the filtration concentration operation or the set differential pressure (first set differential pressure) when recovering the filtrate from the filter 10, or may be a different value (range). For example, when the allowable differential pressure or the first set differential pressure has a certain range, the range of the second set differential pressure may be wider than the range of the allowable differential pressure or the first set differential pressure. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the range of the second set differential pressure is narrower than the range of the allowable differential pressure or the first set differential pressure, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, the range of the second set differential pressure may deviate from the range of the allowable differential pressure or the first set differential pressure.

<Recovery of liquid in filtrate supply tube 3>
After the above-mentioned recovery of the concentrated liquid in the concentrator 20 is performed, if the concentrator transmembrane pressure difference reaches a set pressure difference or a specified amount of liquid has been recovered, the liquid transfer (including the flow of gas) from the filter 10 to the concentrator 20 may be stopped and then a gas such as air may be supplied to the filtrate supply tube 3. This makes it possible to prevent recovery leakage of the concentrated liquid in the concentrator 20 or the concentrated liquid flow path 4, and the liquid in the flow path downstream of the filtrate supply tube 3. If the concentrator transmembrane pressure difference has not reached the set pressure difference, the liquid transfer from the filter 10 to the concentrator 20 does not necessarily have to be stopped.

<Stock solution treatment device 1C of third embodiment>
In the raw liquid treatment device 1B of the second embodiment described above, the filtrate supply tube 3 is provided with a filtrate supply tube delivery section 3p so that the raw liquid is sucked out from the filter 10 during filtration and concentration. In such a configuration, instead of providing the filtrate supply tube 3 with the filtrate supply tube delivery section 3p, the waste liquid tube 5 can also be provided with a waste liquid tube delivery section 5p (see FIGS. 10 to 12).

In the third embodiment of the raw liquid processing device 1C, the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p are operated during filtration and concentration so that the liquid (filtrate) flows from the filter 10 to the concentrator 20. When the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p are operated, the filtrate supply tube 3 becomes negative pressure, and the inside of the filter 10 (for example, the internal space 12h of the trunk section 12 of the main body section 11) also becomes negative pressure. Then, if the flow rate adjustment means 2c is set in a state where the supply tube 2 can deliver liquid, the raw liquid in the raw liquid bag UB can be sucked into the filter 10 through the supply tube 2, and the sucked raw liquid can be sucked into the filtrate supply tube 3.

With this raw liquid processing device 1C, by appropriately changing the bags connected to each tube and adjusting the operation of the flow rate adjustment means and liquid delivery section provided in each tube, it is possible to perform preparatory washing, filtration concentration, and reconcentration.

<Preparatory cleaning work>
10, in the preparatory cleaning operation of the stock solution treatment device 1C of the third embodiment, a cleaning solution bag SB is connected to the other end of the concentrated solution tube 4 instead of the concentrated solution bag CB, and a cleaning solution recovery bag FB is connected to the other end of the waste solution tube 5 instead of the waste solution bag DB. The other end of the waste solution tube 5 may remain connected to the waste solution bag DB, or may be simply placed in a bucket or the like.
A cleaning liquid recovery bag FB is connected to the other end of the liquid supply tube 2 instead of the stock solution bag UB. A waste liquid bag DB may be connected to the other end of the liquid supply tube 2, or the other end of the liquid supply tube 2 may be simply placed in a bucket or the like.
A cleaning liquid recovery bag FB is also connected to the other end of the connecting tube 9. A waste liquid bag DB may be connected to the other end of the connecting tube 9, or the other end of the connecting tube 9 may be simply placed in a bucket or the like.
Furthermore, a cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid supply tube 6 instead of the cleaning liquid bag SB, and the cleaning liquid bag SB is connected to the other end of the cleaning liquid recovery tube 7 instead of the cleaning liquid recovery bag FB. A waste liquid bag DB may be connected to the other end of the cleaning liquid supply tube 6, or the other end of the cleaning liquid supply tube 6 may be simply placed in a bucket or the like.

Then, the flow rate adjustment means 2c and the flow rate adjustment means 9c are used to allow the cleaning liquid to flow through the liquid supply tube 2 and the connecting tube 9.

In the above state, the concentrated liquid tube delivery unit 4p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the concentrated liquid tube 4 to the concentrated liquid 20. Then, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the concentrated liquid tube 4 to the concentrator 20 through the concentrated liquid tube 4. After passing through the concentrator 20, the supplied cleaning liquid passes through the filtrate supply tube 3 and the connecting tube 9 and is collected in the cleaning liquid recovery bag FB connected to the connecting tube 9. If the waste liquid tube delivery unit 5p is operated so that the liquid flows from the concentrator 20 to the cleaning liquid recovery bag FB, a portion of the cleaning liquid can be collected in the cleaning liquid recovery bag FB connected to the other end of the waste liquid tube 5 through the waste liquid tube 5.

The cleaning liquid recovery tube delivery unit 7p is also operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the cleaning liquid recovery tube 7 to the filter 10. Then, a portion of the cleaning liquid is supplied from the cleaning liquid bag SB connected to the cleaning liquid recovery tube 7 to the filter 10 through the cleaning liquid recovery tube 7. The cleaning liquid supplied to the filter 10 passes through the filter 10, then passes through the filtrate supply tube 3 and the connecting tube 9, and is collected in the cleaning liquid recovery bag FB connected to the connecting tube 9. In addition, by operating the cleaning liquid supply tube delivery unit 6p, a portion of the cleaning liquid supplied to the filter 10 can also be flowed into the cleaning liquid supply tube 6. Furthermore, a portion of the cleaning liquid is collected from the cleaning liquid recovery tube 7 through the supply tube 2 to the cleaning liquid recovery bag FB connected to the supply tube 2.

This allows the cleaning liquid to flow through the filter 10, the concentrator 20, and all the tubes, so that the entire raw liquid processing device 1C of the third embodiment can be cleaned.

<Filtration and concentration work>
Once the preparatory cleaning process is completed, the filtration and concentration process is carried out.

As shown in Figure 11, in the filtration and concentration operation of the raw liquid treatment device 1C of the third embodiment, from the state of the preparatory cleaning operation, a concentrate bag CB is connected to the other end of the concentrate tube 4 instead of the cleaning liquid bag SB, and a waste liquid bag DB is connected to the other end of the waste liquid tube 5 instead of the cleaning liquid recovery bag FB.
On the other hand, a stock solution bag UB is connected to the other end of the liquid supply tube 2 in place of the cleaning liquid recovery bag FB.
Also, the flow rate adjusting means 2c is opened to maintain a state in which liquid can flow through the liquid supply tube 2, while the flow rate adjusting means 9c is used to close the connecting tube 9 so that liquid does not flow through the connecting tube 9. In addition, the cleaning liquid recovery tube sending part 7p and the cleaning liquid supply tube sending part 6p are not operated and function as clamps.

In the above state, the concentrate tube delivery unit 4p is operated to flow the concentrate from the concentrator 20 to the concentrate bag CB, and the waste liquid tube delivery unit 5p is operated to flow the waste liquid from the concentrator 20 to the waste liquid bag DB.

The raw liquid is then supplied from the raw liquid bag UB to the filter 10 through the liquid supply tube 2. The supplied raw liquid is filtered by the filter 10, and the filtrate produced is supplied to the concentrator 20 through the filtrate supply tube 3. The filtrate supplied to the concentrator 20 is then concentrated by the concentrator 20, and the concentrate produced is collected in the concentrate bag CB through the concentrate tube 4. Meanwhile, the water separated from the concentrate is collected in the waste liquid bag DB through the waste liquid tube 5.

<About filtration and concentration operations>
Here, in the filtration and concentration operation, the operation of the concentrated liquid tube sending section 4p and the waste liquid tube sending section 5p is controlled so that the concentration ratio falls within a predetermined range. However, as described below, the operation of the concentrated liquid tube sending section 4p and the waste liquid tube sending section 5p, that is, the flow rate of the liquid in the concentrated liquid tube 4 and the waste liquid tube 5, may be controlled by utilizing the filter transmembrane pressure difference and the concentrator transmembrane pressure difference. In this way, the capacity of the filter 10 and the concentrator 20 can be effectively utilized to perform filtration and concentration, so that the time required to produce a concentrated liquid can be shortened and the efficiency of the concentration operation can be increased.
In the following, the operation of filtering and concentrating by controlling the operation of the concentrated liquid tube sending section 4p and the waste liquid tube sending section 5p using the filter transmembrane pressure difference and the concentrator transmembrane pressure difference will be described.

The filter transmembrane pressure and the concentrator transmembrane pressure can be calculated by measuring the pressure inside the tubes connected to the filter 10 and the concentrator 20. For example, if a pressure gauge is provided in the liquid supply tube 2 and the filtrate supply tube 3 and the signal is supplied to the control unit 106, the control unit 106 can calculate the filter transmembrane pressure. As shown in FIG. 10, even if a pressure gauge is provided in the port 11c (or the tube connected to this port 11c) to which the filtrate supply tube 3 is not connected, the control unit 106 can calculate the filter transmembrane pressure. Also, if a pressure gauge is provided in the filtrate supply tube 3 and the waste liquid tube 5 and the signal is supplied to the control unit 106, the control unit 106 can calculate the concentrator transmembrane pressure. If there is a port 20c to which the waste liquid tube 5 is not connected, the control unit 106 can calculate the concentrator transmembrane pressure even if a pressure gauge is provided in this port 20c (or the tube connected to this port 20c).

In addition, in the filter 10 or the concentrator 20, if either the liquid supply side or the liquid discharge side is close to being open to the atmosphere, the control unit 106 can calculate the filter transmembrane pressure or the concentrator transmembrane pressure by simply measuring the pressure inside the tube connected to the side of the liquid supply side or the liquid discharge side that is not open to the atmosphere. In other words, instead of the filter transmembrane pressure or the concentrator transmembrane pressure, the control unit 106 can control the operation of the liquid delivery unit by using only the pressure inside the tube connected to the side that is not open to the atmosphere. For example, if the tube connected to the filter 10 or the concentrator 20 is connected to a bag and is not blocked by the liquid delivery unit or the flow rate adjustment means, the tube can be considered to be close to being open to the atmosphere. In the state of FIG. 12, the liquid supply tube 2 connected to the raw liquid bag UB of the tubes 2 and 3 connected to the filter 10 can also be considered to be open to the atmosphere. In addition, the liquid discharge tube 5 connected to the waste liquid bag DB of the tubes 3 and 5 connected to the concentrator 20 can also be considered to be open to the atmosphere. In this case, in the state shown in FIG. 12, the control unit 106 can control the operation of the liquid delivery unit using only the internal pressure of the filter supply tube 3.

The flow rate of the liquid flowing through the concentrate tube 4 and the waste liquid tube 5 may be estimated from the operation of the concentrate tube delivery section 4p and the waste liquid tube delivery section 5p, or the flow rate may be measured directly by providing a flow meter in the concentrate tube 4, concentrate tube delivery section 4p, waste liquid tube 5, or waste liquid tube delivery section 5p.

<Explanation of filtration and concentration using the filter transmembrane pressure difference and the concentrator transmembrane pressure difference>
When performing a filtration and concentration operation using a filter transmembrane pressure difference or a concentrator transmembrane pressure difference, an allowable pressure difference is set in advance. That is, a pressure difference (allowable pressure difference) that the filter 10 and the concentrator 20 can tolerate is set according to the filter 10 and the concentrator 20, respectively. This allowable pressure difference may have a predetermined range, or may be set to a specific value. In the following, a case where the allowable pressure difference has a predetermined range will be described as a representative example.

When performing filtration and concentration using the filter transmembrane pressure difference or the concentrator transmembrane pressure difference, it is desirable to set an allowable flow rate in advance. That is, it is desirable to set an allowable flow rate (allowable flow rate) of the raw liquid in the liquid supply tube 2. This allowable flow rate may have a predetermined range or may be set to a specific value. Such an allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the liquid supply tube 2 becomes too low, the time required for filtration and concentration becomes too long. Therefore, in order to prevent the processing time of the raw liquid from becoming too long, it is desirable to set an allowable flow rate.
Furthermore, when performing filtration and concentration work using the filter transmembrane pressure difference or the concentrator transmembrane pressure difference, it is desirable to set an allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the raw liquid in the liquid supply tube 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 (allowable concentration ratio). This allowable concentration ratio may have a predetermined range or may be set to a specific value. Such an allowable concentration ratio does not necessarily have to be set. However, if the concentration ratio, which is the ratio of the flow rate of the raw liquid in the liquid supply tube 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4, is too low (i.e., if the flow rate of the concentrated liquid becomes too large), the concentration efficiency will deteriorate. Moreover, there is a risk that the amount of concentrated liquid increases and a large amount of the filtered concentrated liquid is reinfused intravenously, which may cause an increase in blood pressure and an exacerbation of cardiac failure or respiratory failure. For this reason, if the amount of concentrated liquid becomes too large, a reconcentration process must be added, which takes time. When the concentrated liquid is reconcentrated, the reconcentration process takes time, so the total time for processing the raw liquid will be long. Therefore, in order to prevent the concentration ratio from decreasing too much, it is desirable to set an allowable concentration ratio.

At the start of filtration and concentration, the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p are operated to increase the amount of raw liquid sent to the filter 10. At this time, the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p are operated so that the concentrated liquid is at a predetermined concentration ratio. For example, when producing a concentrated liquid with a concentration ratio of 10 times, the flow rate of the concentrated liquid flowing through the concentrated liquid tube 4 and the flow rate of the waste liquid flowing through the waste liquid tube 5 are adjusted to 1:9. In addition, the operation of the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p may be adjusted so that the filter transmembrane pressure or the concentrator transmembrane pressure becomes a set value within the allowable pressure difference (or is maintained within the allowable pressure difference) instead of the concentration ratio of the concentrated liquid or while maintaining the concentrated liquid at a predetermined concentration ratio. Note that while the amount of raw liquid sent to the filter 10 is being increased, the operation of the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p is controlled so that one of the above states is achieved.

As filtration and concentration progresses, clogging of the filter 10 and concentrator 20 gradually occurs. This causes the filter transmembrane pressure difference and the concentrator transmembrane pressure difference to rise. However, the concentrate tube delivery section 4p and waste liquid tube delivery section 5p operate to increase the amount of raw liquid delivered to the filter 10 until the filter transmembrane pressure difference and the concentrator transmembrane pressure difference fall within the allowable pressure difference range.

<First Method>
Here, the increase in the amount of the stock solution sent to the filter 10 continues until the filter transmembrane pressure falls within the allowable pressure difference of the filter 10. Then, when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10, the operation of the concentrated solution tube sending unit 4p and the waste solution tube sending unit 5p is controlled so that the flow rate of the stock solution in the liquid supply tube 2 is maintained at the flow rate when the filter transmembrane pressure falls within the allowable pressure difference of the filter 10.

Here, when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the operation of the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p is controlled so that the amount of filtrate sent to the concentrator 20, in other words, the amount of raw liquid sent to the filter 10, is maintained. Then, the filtration by the filter 10 and the concentrated state by the concentrator 20 can be maintained in a predetermined state. If the amount of raw liquid sent to the filter 10 is increased or decreased according to the value of the filter transmembrane pressure difference, the amount of raw liquid sent to the filter 10 can be increased while maintaining the filter transmembrane pressure difference within the allowable pressure difference of the filter 10. In other words, there is a possibility that the efficiency of the filtration and concentration work can be improved. In particular, if the filter transmembrane pressure difference is maintained to be the maximum allowable pressure difference PM of the filter 10, the amount of raw liquid sent to the filter 10 can be increased to the maximum, so that the effect of shortening the time of the filtration work can be further improved.

On the other hand, when the filter transmembrane pressure difference becomes greater than the maximum allowable differential pressure PM of the filter 10, the operation of the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p is controlled so that the amount of raw liquid sent to the filter 10 is reduced. Even if the amount of raw liquid sent to the filter 10 is constant, if clogging of the hollow fiber membrane or the like occurs, the filter transmembrane pressure difference may increase and filtration may not be able to continue. However, if the amount of raw liquid sent to the filter 10 is reduced, the filter transmembrane pressure difference can be reduced, so that filtration work can be continued even if clogging of the filter 10 occurs. Moreover, by reducing the amount of raw liquid sent to the filter 10, clogging of the hollow fiber membrane or the like may be slightly reduced, making it easier to continue filtration work and shortening the time for filtration work. In particular, if the filter transmembrane pressure difference becomes greater than the maximum allowable pressure difference PM of the filter 10, the effect of reducing clogging of the hollow fiber membrane, etc. may be enhanced by temporarily stopping the supply of the raw liquid to the filter 10 and then resuming the supply after a certain period of time.

In addition, when the filter membrane pressure difference becomes smaller than the minimum allowable pressure difference PL of the filter 10 by, for example, reducing the amount of stock solution sent to the filter 10, the operation of the concentrated liquid tube sending section 4p and the waste liquid tube sending section 5p is controlled so that the amount of stock solution sent to the filter 10 is increased. This increases the amount of filtration by the filter 10, which may shorten the filtration time. If the amount of stock solution sent to the filter 10 is increased until the filter membrane pressure difference becomes within the allowable pressure difference of the filter 10, particularly the maximum allowable pressure difference PM, the filtering capacity of the filter 10 can be used effectively, thereby further enhancing the effect of shortening the filtration time.

In addition, when the amount of the raw liquid fed to the filter 10 is reduced when the filter transmembrane pressure becomes larger than the maximum allowable pressure difference PM of the filter 10, the amount of the raw liquid fed may be gradually reduced, or the amount of the raw liquid fed may be reduced in a stepwise manner. In addition, when the filter transmembrane pressure becomes larger than the maximum allowable pressure difference PM of the filter 10, the feed of the raw liquid to the filter 10 may be stopped for a certain period of time, and then the feed of the raw liquid to the filter 10 may be started (see FIG. 24). In this case, the amount of the raw liquid fed to the filter 10 may be adjusted while checking the filter transmembrane pressure. For example, as in pattern 1 of FIG. 24, when the feed of the raw liquid to the filter 10 is stopped for a certain period of time and then the feed of the raw liquid to the filter 10 is started, the feed is first started at a flow rate of about 1/2 the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is checked. In this state, if the filter transmembrane pressure is smaller than the minimum allowable pressure PL (PL in FIG. 24), the flow rate is increased by about 1/2 the difference between the current flow rate and the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is confirmed. In this state, if the filter transmembrane pressure is still smaller than the minimum allowable pressure PL, the flow rate is further increased by about 1/2 the difference between the current flow rate and the maximum allowable flow rate LM, and the filter transmembrane pressure at that time is confirmed. This operation is repeated, and when the filter transmembrane pressure becomes equal to or greater than the minimum allowable pressure PL and equal to or less than the maximum allowable pressure PM of the filter 10 (or becomes equal to the maximum allowable pressure PM), the increase in the flow rate is stopped. In addition, if the filter transmembrane pressure is within the allowable pressure of the filter 10 but does not reach the maximum allowable flow rate LM, the amount of raw liquid sent to the filter 10 may be increased in the same manner while checking the filter transmembrane pressure until it reaches the maximum allowable flow rate LM.
When the amount of the stock solution fed to the filter 10 is increased when the filter transmembrane pressure becomes smaller than the minimum allowable pressure difference PL of the filter 10, the amount of the stock solution fed may be increased gradually. For example, the amount of the stock solution fed to the filter 10 may be increased by a method similar to the above-mentioned method of increasing the flow rate, that is, the method of increasing the flow rate after stopping the feed of the stock solution to the filter 10 for a certain period of time.

In addition, when the filter transmembrane pressure difference is maintained within the allowable pressure difference of the filter 10, the amount of raw liquid sent to the filter 10 may be maintained, but if the flow rate is smaller than the maximum allowable flow rate LM, the amount of raw liquid sent to the filter 10 may be increased until it reaches the maximum allowable flow rate LM.

In addition, if the filter transmembrane pressure difference becomes equal to or exceeds the minimum allowable pressure difference PL of the filter 10, but the amount of raw liquid sent to the filter 10 does not reach the minimum allowable flow rate LL (pattern 3 in Figure 24), it is determined that the hollow fiber membrane 16 or the like is clogged, and the filtration and concentration operation may be stopped and a cleaning operation may be started.

Now, in a state where the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10 and the flow rate of the raw liquid in the liquid supply tube 2 is maintained at the flow rate when the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the concentrated liquid tube liquid delivery section 4p can be controlled as follows based on the concentrator transmembrane pressure difference.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the concentrate tube delivery unit 4p is operated to reduce the amount of concentrate delivered to the concentrate bag CB. In other words, the operation of the concentrate tube delivery unit 4p is controlled to increase the concentration of the concentrate. At this time, the waste liquid tube delivery unit 5p may be maintained in an operating state so that the amount of waste liquid flowing through the waste liquid tube 5 is maintained.
Conversely, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the operation of the waste liquid tube delivery section 5p may be controlled so as to increase the amount of waste liquid flowing through the waste liquid tube 5, thereby maintaining the amount of concentrated liquid delivered to the concentrator 20.

<Step 2>
Then, the amount of concentrate sent to the concentrate bag CB is reduced until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the concentrate tube sending unit 4p is controlled to maintain the flow rate of the concentrate in the concentrate tube 4 at the flow rate in the state in which the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. At this time, the operation of the waste liquid tube sending unit 5p may also be controlled to maintain the sending amount of the waste liquid flowing in the waste liquid tube 5.

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrated liquid tube sending unit 4p is controlled to increase the amount of concentrated liquid sent to the concentrated liquid bag CB. Note that as the amount of concentrated liquid sent increases, the concentration ratio decreases, but the operation of the concentrated liquid tube sending unit 4p is controlled so that the concentration ratio decreases (so that the concentration of the concentrated liquid decreases) while satisfying the allowable concentration ratio. At this time, the waste liquid tube sending unit 5p may be maintained in an operating state so that the amount of waste liquid flowing through the waste liquid tube 5 is maintained.
Conversely, when the concentrator transmembrane pressure difference is greater than the maximum allowable pressure difference of the concentrator 20, the operation of the waste liquid tube delivery unit 5p is controlled to reduce the amount of waste liquid flowing through the waste liquid tube 5. When the amount of waste liquid delivered decreases, the concentration ratio decreases, but the operation of the waste liquid tube delivery unit 5p is controlled to reduce the concentration ratio (to reduce the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.

When the amount of concentrated liquid sent to the concentrated liquid bag CB increases (or the amount of waste liquid sent through the waste liquid tube 5 decreases), the concentrator transmembrane pressure difference decreases. When the concentrator transmembrane pressure difference falls below the minimum allowable pressure difference of the concentrator 20, the concentrated liquid tube sending section 4p is again operated to decrease the amount of concentrated liquid sent to the concentrated liquid bag CB (or the operation of the waste liquid tube sending section 5p is controlled to increase the amount of waste liquid sent through the waste liquid tube 5).

That is, while the filter transmembrane pressure difference is within the allowable pressure difference of the filter 10, the above steps 1 to 3 are repeated. By adopting this method, it is possible to ensure the maximum filtration flow rate (i.e., the above-mentioned maximum allowable flow rate LM) and the maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the filter 10 and the concentrator 20, which is impossible when the amount of liquid sent to the filter 10 and the concentrated liquid bag CB is constant, and according to the state of the raw liquid (concentration of the substance causing the clogging of the filter or concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated liquid from the raw liquid can be shortened, and re-concentration work can be prevented or the time required for re-concentration work can be shortened.
Moreover, by operating as described above, it becomes possible to quickly remove the cleaning liquid filled in the filter 10, concentrator 20, and the circuit at the start of filtration and concentration, and the cleaning liquid in the filter 10 and the circuit immediately after cleaning the filter 10, as waste liquid from the concentrator 20. In other words, it is possible to efficiently prevent dilution of the concentrated liquid by the cleaning liquid at the start and immediately after cleaning the filter, as described above.

In addition, in the above method (first method), when the filter transmembrane pressure difference is greater than the maximum allowable pressure difference PM, when the filter transmembrane pressure difference is less than the minimum allowable pressure difference PL, and further when the amount of raw liquid sent to the filter 10 is constant regardless of the filter transmembrane pressure difference, the above steps 1 to 3 may be repeated to adjust the amount of concentrated liquid sent to the concentrator 20.
Furthermore, the above method (first method) may be employed throughout the entire period of filtration and concentration, or may be employed only for a certain period, such as at the start of filtration and concentration or immediately after cleaning of the filter, and the solution may be concentrated at a set concentration ratio during other periods.

<About cleaning the filter>
In the raw liquid treatment device 1C of the third embodiment, when the above-mentioned filtration and concentration work is performed, the filter transmembrane pressure becomes larger than the maximum allowable pressure PM of the filter 10 due to clogging of the filter 10. In this case, if the flow rate of the raw liquid in the liquid supply tube 2 is reduced, the filter transmembrane pressure can be made smaller than the maximum allowable pressure PM of the filter 10, and the filter transmembrane pressure can be maintained within the allowable pressure (a range from the minimum allowable pressure PL to the maximum allowable pressure PM). However, if the clogging of the filter 10 becomes severe, the flow rate of the raw liquid in the liquid supply tube 2 is reduced in order to maintain the filter transmembrane pressure within the allowable pressure of the filter 10, and the flow rate of the raw liquid in the liquid supply tube 2 may become smaller than the minimum allowable flow rate LL. In such a state, the filter 10 is cleaned during the filtration and concentration work of the raw liquid treatment device 1C of the third embodiment.

As shown in FIG. 23, the flow rate adjustment means 2c blocks the liquid supply tube 2 so that no liquid flows through it. In addition, the operation of the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p is stopped and they function as clamps. If the filter cleaning is performed during the filtration and concentration work, after the completion of the preparatory cleaning work, a cleaning liquid bag SB is connected to the other end of the cleaning liquid supply tube 6 instead of the cleaning liquid recovery bag FB, and a cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid recovery tube 7 instead of the cleaning liquid bag SB.

In the above state, the cleaning liquid supply tube delivery unit 6p is operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 to the filter 10, and the cleaning liquid recovery tube delivery unit 7p is operated to flow the cleaning liquid from the filter 10 to the cleaning liquid recovery bag FB connected to the cleaning liquid recovery tube 7. This allows the cleaning liquid to flow inside the hollow fiber membrane 16 in the opposite direction to the direction in which the raw liquid flows during filtration and concentration, so that the inside of the hollow fiber membrane 16 can be cleaned with the cleaning liquid.

After the preparatory cleaning operation is completed, a cleaning liquid bag SB is connected to the other end of the connecting tube 9 instead of the cleaning liquid recovery bag FB. Then, by opening the flow rate adjustment means 9c to allow liquid to flow through the connecting tube 9, in addition to the above state, cleaning liquid can be supplied to the filter 10 from the cleaning liquid bag SB connected to the connecting tube 9. Then, the cleaning liquid supplied through the connecting tube 9 permeates the hollow fiber membrane 16 in the opposite direction to the direction in which the filtrate permeates the hollow fiber membrane 16, so clogging of the hollow fiber membrane 16 can be eliminated. In this case, cleaning liquid is supplied to the filter 10 from both the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 and the cleaning liquid bag SB connected to the connecting tube 9, so that the flow rate of the cleaning liquid flowing through the cleaning liquid recovery tube 7 by the cleaning liquid recovery tube liquid delivery part 7p is adjusted to be greater than the flow rate of the cleaning liquid flowing through the cleaning liquid supply tube 6 by the cleaning liquid supply tube liquid delivery part 6p.

When the flow rate adjustment means 9c is used to allow liquid to flow through the connecting tube 9, the cleaning liquid recovery tube sending section 7p may be operated while the cleaning liquid supply tube sending section 6p is stopped. In this case, cleaning liquid is supplied to the filtrate 10 only from the cleaning liquid bag SB connected to the connecting tube 9. In this case, too, the cleaning liquid permeates the hollow fiber membrane 16 in the opposite direction to the direction in which the filtrate permeates the hollow fiber membrane 16, so clogging of the hollow fiber membrane 16 can be eliminated.

When a filter having a hollow fiber membrane 16 as shown in FIG. 5 is used as the filter 10, it is desirable for the control unit 106 to adjust the amount and timing of the cleaning liquid supplied to the filter 10 so that the filter 10 is cleaned as described above. In other words, it is desirable to adjust the amount and timing of the cleaning liquid supplied to the filter 10 so that the cleaning liquid permeates the hollow fiber membrane 16 while filling the hollow space 12h of the body 12 up to the area of the hollow fiber membrane 16 where cleaning is to be performed.

<Filtrate recovery>
On the other hand, when the filter is washed by the above method, the filtrate remaining in the internal space 12h of the main body 11 of the filter 10 is mixed with the washing liquid and discharged, which reduces the amount of the active ingredient recovered by filtration and concentration.

Therefore, when cleaning the filter, it is preferable to first send the filtrate present in the internal space 12h of the main body 11 of the filter 10 to the concentrator 20 and then perform the filter cleaning.

<Recovery using cleaning fluid (outside)>
As shown in FIG. 10, the cleaning solution bag SB is connected to the port 11c (the port 11c to which the filtrate supply tube 3 is not connected, hereinafter referred to as the cleaning port 11c) of the main body 11 of the filter 10 via a tube. Then, the flow rate adjustment means 3c maintains the state in which the liquid flows in the filtrate supply tube 3, and the flow rate adjustment means 2c closes the liquid supply tube 2 while the concentrated liquid tube sending section 4p and/or the waste liquid tube sending section 5 are continued to operate. In this state, if the cleaning solution is supplied from the cleaning solution bag SB to the filter 10 by the pump provided on the tube, the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20, and instead the cleaning solution is supplied from the cleaning solution bag SB to the internal space 12h. Eventually, when the filtrate in the internal space 12h is completely replaced with the cleaning solution, the flow rate adjustment means 3c closes the filtrate supply tube 3, and the operation of the concentrated liquid tube sending section 4p and/or the waste liquid tube sending section 5 is stopped. After this state has been reached, by cleaning the filter 10 using the cleaning method for the filter 10 as described above, it is possible to prevent the filtrate discharged together with the cleaning liquid from being reconcentrated.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the internal space 12h has been replaced with the cleaning liquid can be determined theoretically by counting the amount of pumping provided in the tube connected to the cleaning port 11c, or by measuring the concentration of the concentrated liquid. It can also be determined by looking at the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a hydrometer.

In addition, the tube connected to the cleaning port 11c of the main body 11 of the filter 10 does not necessarily need to be provided with a pump. Even in this case, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be replaced with cleaning liquid by operating the concentrated liquid tube delivery unit 4p or the waste liquid tube delivery unit 5p.

<Recovery using air or other gas>
In addition, in the above explanation, a case was described in which the cleaning solution bag SB was connected to the cleaning port 11c of the main body 11 of the filter 10 via a tube, but a gas such as air may also be supplied to the cleaning port 11c of the main body 11 of the filter 10 via a tube.

In this case, the flow rate adjustment means 3c maintains the state in which liquid flows in the filtrate supply tube 3, and the flow rate adjustment means 2c closes the liquid supply tube 2 while continuing the operation of the concentrated liquid tube delivery section 4p and/or the waste liquid tube delivery section 5p. In this state, if a gas such as air is supplied to the filter 10 from a tube connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be supplied to the concentrator 20. When all of the filtrate in the internal space 12h is eventually discharged, the flow rate adjustment means 3c closes the filtrate supply tube 3, and the operation of the concentrated liquid tube delivery section 4p and/or the waste liquid tube delivery section 5p is stopped. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the internal space 12h has been discharged can be determined by installing a liquid detector or air bubble detector in the filtrate supply tube 3, measuring the pressure in the filtrate supply tube 3, or theoretically calculating the amount of water pumped out by counting the amount of water pumped out.

In addition, when the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the internal space 12h of the main body 11 of the filter 10 is filled with a gas such as air. Therefore, when performing a cleaning operation after collecting the filtrate, it is desirable to first fill the hollow space 12h of the body 12 up to the area to be cleaned in the hollow fiber membrane 16 (or the entire hollow space 12h of the body 12) with cleaning liquid before performing the cleaning operation.

<Collecting in a bag>
In the above example, the filtrate is sent to the concentrator 20 and collected in a concentrated state, but the filtrate may be collected as it is. For example, a bag for collecting the filtrate is connected to the filtrate supply tube 3 upstream of the flow rate adjustment means 3c (i.e., the filter 10 side). In this state, if the flow rate adjustment means 3c makes the filtrate supply tube 3 in a state where liquid does not flow, and a cleaning liquid or a gas such as air is supplied to the filter 10 from the cleaning port 11c as described above, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be collected in the bag. In this case, the filtrate can be collected in a short time compared to the case where the filtrate is sent to the concentrator 20 and collected in a concentrated state, so that the transition to the cleaning operation can be performed quickly.

<Recovery using cleaning fluid (inside)>
In the above description, the raw liquid is supplied into the through-flow passages 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15 of the filter 10, and the filtrate is discharged into the internal space 12h of the trunk 12 of the main body 11 of the filter 10. However, the raw liquid may be supplied from the filtrate discharge port 11c into the internal space 12h of the trunk 12 of the main body 11, and the filtered filtrate may be discharged into the through-flow passages 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15, and then discharged to the outside from the raw liquid supply port 11a.

In this case, the tubes are connected as follows.
First, the filtrate supply tube 3 is connected to the raw liquid supply port 11a, the supply tube 2 is connected to the port 11c (i.e., the above-mentioned cleaning port 11c), the cleaning liquid supply tube 6 is connected to the port 11c (i.e., the above-mentioned filtrate discharge port 11c) to which the supply tube 2 is not connected, and the cleaning liquid bag SB that was connected to the cleaning port 11c is connected to the cleaning liquid supply port 11b.

Then, the flow rate adjustment means 3c maintains the state in which the liquid flows in the filtrate supply tube 3, and the flow rate adjustment means 2c closes the liquid supply tube 2 while continuing the operation of the concentrated liquid tube delivery section 4p and/or the waste liquid tube delivery section 5p. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by the pump provided on the tube connected to the cleaning liquid supply port 11b, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20, and instead, the cleaning liquid is supplied from the cleaning liquid bag SB to the through flow path 16h. When the filtrate in the through flow path 16h is completely replaced with the cleaning liquid, the flow rate adjustment means 3c closes the filtrate supply tube 3, and the operation of the concentrated liquid tube delivery section 4p and/or the waste liquid tube delivery section 5p is stopped. After this state is reached, if the filter 10 is washed by the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the internal space 12h has been replaced with the cleaning liquid can be determined theoretically by counting the amount of pumping provided in the tube connected to the cleaning port 11c, or by measuring the concentration of the concentrated liquid. It can also be determined by looking at the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a hydrometer.

<Recovery using air or other gas>
In addition, in the above explanation, a case was described in which the cleaning solution bag SB was connected to the cleaning solution supply port 11b of the main body 11 of the filter 10 via a tube, but a gas such as air may also be supplied to the cleaning solution supply port 11b of the main body 11 of the filter 10 via a tube.

In this case, the flow rate adjustment means 3c maintains the state in which liquid flows in the filtrate supply tube 3, and the flow rate adjustment means 2c closes the liquid supply tube 2 while continuing the operation of the concentrated liquid tube delivery section 4p and/or the waste liquid tube delivery section 5p. In this state, if a gas such as air is supplied to the filter 10 from the tube, the filtrate in the through flow passage 16h of the hollow fiber membrane 16 of the filter 10 can be supplied to the concentrator 20. When all of the filtrate in the through flow passage 16h of the hollow fiber membrane 16 is eventually discharged, the flow rate adjustment means 3c closes the filtrate supply tube 3, and the operation of the concentrated liquid tube delivery section 4p and/or the waste liquid tube delivery section 5p is stopped. After this state is reached, if the filter 10 is washed using the above-mentioned method for washing the filter 10, re-concentration of the filtrate discharged together with the washing liquid can be suppressed.

In the above example, the liquid supply tube 2 was blocked by the flow rate adjustment means 2c to perform the recovery, but the liquid supply tube 2 may be left open to perform the recovery. In other words, it is possible to recover the filtrate in the filter 10 while continuing the filtration and concentration.

Whether or not all of the filtrate in the through-flow passage 16h of the hollow fiber membrane 16 has been discharged can be determined by providing a liquid detector or air bubble detector in the filtrate supply tube 3, measuring the pressure in the filtrate supply tube 3, or theoretically calculating the amount of pump feed by counting the amount of pump feed.

In addition, when the filtrate in the through passage 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the through passage 16h of the hollow fiber membrane 16 of the filter 10 is filled with a gas such as air. Therefore, when performing a cleaning operation after collecting the filtrate, it is desirable to first fill the through passage 16h with cleaning liquid up to the area of the hollow fiber membrane 16 to be cleaned (or the entire hollow fiber membrane 16) before performing the cleaning operation.

<Collecting in a bag>
In the above example, the filtrate is sent to the concentrator 20 and collected in a concentrated state, but the filtrate may be collected as it is. For example, a bag for collecting the filtrate is connected to the filtrate supply tube 3 upstream of the flow rate adjustment means 3c (i.e., the filter 10 side). In this state, if the flow rate adjustment means 3c makes the filtrate supply tube 3 in a state where no liquid flows, and the cleaning liquid or gas such as air is supplied to the filter 10 from the cleaning liquid supply port 11b as described above, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be collected in the bag. In this case, the filtrate can be collected in a short time compared to the case where the filtrate is sent to the concentrator 20 and collected in a concentrated state, so that the transition to the cleaning operation can be performed quickly.

<Example of method for recovering liquid from filter 10>
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated liquid, it is desirable to adjust the flow rate when sending the filtrate to the concentrator 20 based on the transmembrane pressure of the concentrator 20. By adopting such a method, even if the concentrator 20 should become clogged, an increase in the transmembrane pressure of the concentrator can be suppressed and processing can be prevented from being stopped, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate when sending liquid to the concentrator 20 based on the concentrator transmembrane pressure of the concentrator 20, the flow rate can be adjusted as follows. First, when the concentrator transmembrane pressure of the concentrator 20 is within a set differential pressure range, the operation of the concentrate tube sending unit 4p and/or the waste liquid tube sending unit 5p is controlled so as to maintain the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the concentrator transmembrane pressure of the concentrator 20 is greater than the maximum set pressure difference, the operation of the concentrated liquid tube sending section 4p and/or the waste liquid tube sending section 5p is controlled so as to reduce the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set pressure difference and being unable to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrated liquid tube sending section 4p and/or the waste liquid tube sending section 5p is controlled so as to increase the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference and the concentrated liquid becoming diluted.

The set differential pressure of the concentrator transmembrane pressure when recovering the filtrate from the filter 10 may be the same as the allowable differential pressure in the filtration and concentration work, or the set differential pressure may be a value different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the set differential pressure range may be wider than the allowable differential pressure range. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the set differential pressure range is narrower than the allowable differential pressure range, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, there may be a discrepancy between the allowable differential pressure range and the set differential pressure range.

<Reconcentration process>
When the concentrate obtained by the filtration and concentration process is to be further concentrated, a re-concentration process is carried out.

As shown in FIG. 12, in the re-concentration operation of the stock solution treatment device 1C of the third embodiment, the other end of the connection tube 9 is detached from the cleaning solution bag SB, and a concentrate bag CB is connected to the other end of the connection tube 9.
Also, the flow rate adjusting means 3c maintains a state in which liquid can flow through the filtrate supply tube, and the flow rate adjusting means 9c maintains a state in which liquid can flow through the connecting tube 9, while the cleaning liquid supply tube sending section 6p and the cleaning liquid recovery tube sending section 7p are not operated and function as clamps. In addition, the flow rate adjusting means 2c closes the liquid supply tube 2 so that no liquid flows through it. This brings about a state in which no liquid flows through the filter 10.

In the above state, the concentrate tube delivery unit 4p and the waste liquid tube delivery unit 5p are operated so that the concentrate flows from the concentrator 20 through the concentrate tube 4 to the concentrate bag CB.

Then, the concentrated liquid is supplied from the concentrated liquid bag CB connected to the connecting tube 9 to the concentrator 20 through the connecting tube 9, and the re-concentrated liquid further concentrated by the concentrator 20 is collected in the concentrated liquid bag CB through the concentrated liquid tube 4. Meanwhile, the water separated from the concentrated liquid is collected in the waste liquid bag DB through the waste liquid tube 5. In other words, a concentrated liquid (re-concentrated liquid) with a higher concentration rate can be obtained.

<Explanation of reconcentration using transmembrane pressure difference in concentrator>
In the reconcentration operation, the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, i.e., the reconcentration rate, may be adjusted based on the transmembrane pressure of the concentrator 20. This method has the effect of suppressing an increase in the transmembrane pressure of the concentrator, while at the same time shortening the time required to produce a highly concentrated liquid.

In this case, when performing reconcentration work using the concentrator transmembrane pressure difference in advance, it is desirable to set an allowable pressure difference. In other words, a pressure difference (allowable pressure difference) that the concentrator 20 can tolerate is set according to the concentrator 20. This allowable pressure difference may have a predetermined range, or may be set to a specific value. In the following, a case where the allowable pressure difference has a predetermined range will be described as a representative example.

When performing reconcentration using the transmembrane pressure difference of the concentrator, it is desirable to set an allowable flow rate in advance. In other words, it is desirable to set the allowable flow rate (allowable flow rate) of the concentrated liquid in the connecting tube 9. This allowable flow rate may have a predetermined range, or may be set to a specific value. Such an allowable flow rate does not necessarily have to be set. However, if the flow rate of the concentrated liquid in the connecting tube 9 becomes too low, the time required for reconcentration becomes too long. Therefore, in order to prevent the reconcentration processing time from becoming too long, it is desirable to set an allowable flow rate. Also, the allowable flow rate in the reconcentration operation may be the same as the allowable flow rate in filtration concentration, or may be different from the allowable flow rate in filtration concentration.

Furthermore, when performing reconcentration using the transmembrane pressure difference of the concentrator, it is desirable to set an allowable concentration ratio in advance. In other words, it is desirable to set the ratio of the flow rate of the concentrate flowing through the concentrate tube 4 to the flow rate of the concentrate in the connecting tube 9 (allowable concentration ratio). This allowable concentration ratio may have a predetermined range or may be set to a specific value. Such an allowable concentration ratio does not necessarily have to be set. However, if the concentration ratio, which is the ratio of the flow rate of the concentrate flowing through the concentrate tube 4 to the flow rate of the concentrate in the connecting tube 9, drops too much (i.e., if the flow rate of the concentrate becomes too large), the concentration efficiency will deteriorate, and the reconcentration process will take time. Therefore, in order to prevent the concentration ratio from dropping too much, it is desirable to set an allowable concentration ratio. In addition, the allowable concentration ratio in the reconcentration work may be the same as the allowable flow rate in filtration concentration, or may be different from the allowable concentration ratio in filtration concentration.

At the start of reconcentration, the concentrate tube delivery section 4p and the waste liquid tube delivery section 5p are operated to increase the amount of concentrate sent to the concentrator 20 (i.e., the flow rate of the concentrate in the connecting tube 9). At this time, the concentrate tube delivery section 4p and the waste liquid tube delivery section 5p are operated so that the concentrate reaches a predetermined concentration ratio. For example, when producing a concentrate with a concentration ratio of 10 times, the flow rate of the concentrate flowing through the concentrate tube 4 and the flow rate of the waste liquid flowing through the waste liquid tube 5 are adjusted to 1:9. In addition, the operation of the concentrate tube delivery section 4p and the waste liquid tube delivery section 5p may be adjusted so that the concentrator transmembrane pressure difference reaches a set value. Note that while the amount of concentrate sent from the concentrator 20 is being increased, the operation of the concentrate tube delivery section 4p and the waste liquid tube delivery section 5p is controlled so that one of the above states is reached.

As the reconcentration progresses, clogging of the concentrator 20 gradually occurs. This causes the concentrator transmembrane pressure difference to rise. However, the concentrated liquid tube delivery section 4p and the waste liquid tube delivery section 5p operate to increase the amount of concentrated liquid delivered to the concentrator 20 until the concentrator transmembrane pressure difference falls within the allowable pressure difference.

<First Method>
Here, the increase in the amount of concentrated liquid sent to the concentrator 20 continues until the concentrator transmembrane pressure becomes equal to the allowable pressure difference of the concentrator 20. Then, when the concentrator transmembrane pressure becomes within the allowable pressure difference of the concentrator 20, the operation of the concentrated liquid tube sending unit 4p and the waste liquid tube sending unit 5p is controlled as follows based on the concentrator transmembrane pressure so that the flow rate of the concentrated liquid in the connecting tube 9 is maintained at the flow rate when the concentrator transmembrane pressure becomes within the allowable pressure difference of the concentrator 20.

<Step 1>
First, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the concentrate tube delivery unit 4p is operated to reduce the amount of concentrate delivered to the concentrate bag CB. In other words, the operation of the concentrate tube delivery unit 4p is controlled to increase the concentration of the concentrate. At this time, the waste liquid tube delivery unit 5p may be maintained in an operating state so that the amount of waste liquid flowing through the waste liquid tube 5 is maintained.
Conversely, when the concentrator transmembrane pressure difference is smaller than the minimum allowable pressure difference of the concentrator 20, the operation of the waste liquid tube delivery section 5p may be controlled so as to increase the amount of waste liquid flowing through the waste liquid tube 5, thereby maintaining the amount of concentrated liquid delivered to the concentrator 20.

<Step 2>
Then, the amount of concentrate sent to the concentrate bag CB is reduced until the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. When the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20, the concentrate tube sending unit 4p is controlled to maintain the flow rate of the concentrate in the concentrate tube 4 at the flow rate in the state in which the concentrator transmembrane pressure falls within the allowable pressure difference of the concentrator 20. At this time, the operation of the waste liquid tube sending unit 5p may also be controlled to maintain the sending amount of the waste liquid flowing in the waste liquid tube 5.

<Step 3>
When the concentrator transmembrane pressure difference becomes greater than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrated liquid tube sending unit 4p is controlled to increase the amount of concentrated liquid sent to the concentrated liquid bag CB. Note that as the amount of concentrated liquid sent increases, the concentration ratio decreases, but the operation of the concentrated liquid tube sending unit 4p is controlled so that the concentration ratio decreases (so that the concentration of the concentrated liquid decreases) while satisfying the allowable concentration ratio. At this time, the waste liquid tube sending unit 5p may be maintained in an operating state so that the amount of waste liquid flowing through the waste liquid tube 5 is maintained.
Conversely, when the concentrator transmembrane pressure difference is greater than the maximum allowable pressure difference of the concentrator 20, the operation of the waste liquid tube delivery unit 5p is controlled to reduce the amount of waste liquid flowing through the waste liquid tube 5. When the amount of waste liquid delivered decreases, the concentration ratio decreases, but the operation of the waste liquid tube delivery unit 5p is controlled to reduce the concentration ratio (to reduce the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.

When the amount of concentrated liquid sent to the concentrated liquid bag CB increases (or the amount of waste liquid sent through the waste liquid tube 5 decreases), the concentrator transmembrane pressure difference decreases, so when the concentrator transmembrane pressure difference falls below the minimum allowable differential pressure of the concentrator 20, the concentrated liquid tube sending section 4p is again operated to decrease the amount of concentrated liquid sent to the concentrated liquid bag CB (or the operation of the waste liquid tube sending section 5p is controlled to increase the amount of waste liquid sent through the waste liquid tube 5).

In other words, steps 1 to 3 are repeated as long as the concentrator transmembrane pressure difference is within the allowable pressure difference of the concentrator 20. By adopting this method, it is possible to ensure the maximum circulation flow rate and maximum concentration ratio according to the membrane area and clogging state of the filtration membrane of the concentrator 20, which is not possible when the amount of liquid sent to the concentrate bag CB is constant, and according to the state of the concentrate (concentration of the substance causing the clogging of the concentrator, concentration of the useful substance to be recovered, viscosity of the liquid, etc.). In other words, by improving the circulation efficiency and concentration efficiency, the time required to produce a highly concentrated concentrate can be shortened, and the time required for re-concentration work can be shortened.

The allowable pressure difference of the concentrator transmembrane pressure during reconcentration may be the same as the allowable pressure difference during the filtration and concentration work, or may be a value (range) different from the allowable pressure difference during the filtration and concentration work. For example, when the allowable pressure difference during the filtration and concentration work has a certain range, the allowable pressure difference during the reconcentration may be wider than that range. In this case, when treating a stock solution that is prone to clogging the filter 10, the filtration and concentration work is performed slowly so as not to apply pressure to the filter 10, but instead a highly concentrated solution can be produced, which is desirable in that the time required for the reconcentration work can be shortened. In addition, when the allowable pressure difference during reconcentration is narrower than the allowable pressure difference during the filtration and concentration work, when treating a stock solution that is prone to clogging the concentrator 20, the filtration and concentration work is performed in a short time without applying pressure to the concentrator 20, which is desirable in that a highly concentrated solution can be produced in the reconcentration work. Furthermore, there may be a difference between the allowable pressure difference during the filtration and concentration work and the allowable pressure difference during the reconcentration work.
The allowable concentration ratio in reconcentration may be the same as the allowable concentration ratio in the filtration and concentration work, or may be a value (range) different from the allowable concentration ratio in the filtration and concentration work. For example, when the allowable concentration ratio in the filtration and concentration work has a certain range, the range of the allowable concentration ratio in the reconcentration may be wider than that range. In this case, it is desirable in that the time of the reconcentration work can be shortened instead of concentrating the filtration and concentration work for a long time. In addition, when the range of the allowable concentration ratio in the reconcentration is narrower than the range of the allowable concentration ratio in the filtration and concentration work, it is desirable in that the filtration and concentration work can be completed quickly instead of concentrating the reconcentration work for a long time. Furthermore, there may be a difference between the range of the allowable concentration ratio in the filtration and concentration work and the range of the allowable concentration ratio in the reconcentration.

<Example of method for recovering liquid from filter 10>
Before carrying out the above-mentioned reconcentration operation, the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as a concentrated liquid. In this case, it is desirable to adjust the flow rate when sending the filtrate to the concentrator 20 based on the transmembrane pressure of the concentrator 20. By adopting such a method, even if the concentrator 20 becomes clogged, the increase in the transmembrane pressure of the concentrator can be suppressed and the process can be prevented from being stopped, so that the filtrate in the filter 10 can be effectively recovered.

For example, when adjusting the flow rate when sending liquid to the concentrator 20 based on the concentrator transmembrane pressure of the concentrator 20, the flow rate can be adjusted as follows. First, when the concentrator transmembrane pressure of the concentrator 20 is within a set differential pressure range, the operation of the concentrate tube sending unit 4p and/or the waste liquid tube sending unit 5p is controlled so as to maintain the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure significantly deviating from the set differential pressure range from occurring.
On the other hand, when the concentrator transmembrane pressure of the concentrator 20 is greater than the maximum set pressure difference, the operation of the concentrated liquid tube sending section 4p and/or the waste liquid tube sending section 5p is controlled so as to reduce the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to rise above the maximum set pressure difference and being unable to continue processing.
Conversely, when the concentrator transmembrane pressure of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrated liquid tube sending section 4p and/or the waste liquid tube sending section 5p is controlled so as to increase the amount of liquid sent from the filter 10 to the concentrator 20. This makes it possible to prevent problems such as the concentrator transmembrane pressure continuing to decrease below the minimum set pressure difference and the concentrated liquid becoming diluted.

The set differential pressure of the concentrator transmembrane pressure when recovering the filtrate from the filter 10 may be the same as the allowable differential pressure in the filtration and concentration work, or the set differential pressure may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the set differential pressure range may be wider than the allowable differential pressure range. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the set differential pressure range is narrower than the allowable differential pressure range, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, there may be a discrepancy between the allowable differential pressure range and the set differential pressure range.

<Recovery of concentrator 20>
When recovering the concentrate in the concentrator 20 after recovering the raw liquid or filtrate in the filter 10, the recovery of the concentrate may be performed by simply passing a fluid such as a cleaning liquid or a gas (hereinafter simply referred to as a fluid) through the concentrator 20. However, as in the above-mentioned case, the flow rate of the fluid supplied to the concentrate 20 may be adjusted while measuring the concentrator transmembrane pressure difference. This can prevent problems such as the concentrator transmembrane pressure increasing and the inability to continue the treatment from occurring. If the concentrator transmembrane pressure of the concentrator 20 becomes greater than the maximum set pressure difference, the flow of liquid (including the flow of gas) from the filter 10 to the concentrator 20 can be stopped to prevent problems such as the concentrator transmembrane pressure continuing to increase.

The set differential pressure (second set differential pressure) of the concentrator transmembrane pressure when recovering the concentrated liquid from the concentrator 20 may be the same as the allowable differential pressure in the filtration concentration operation or the set differential pressure (first set differential pressure) when recovering the filtrate from the filter 10, or may be a different value. For example, when the allowable differential pressure or the first set differential pressure has a certain range, the range of the second set differential pressure may be wider than the range of the allowable differential pressure or the first set differential pressure. In this case, it is desirable in that the concentrated liquid can be recovered to the end as much as possible even if it is in a diluted state. In addition, when the range of the second set differential pressure is narrower than the range of the allowable differential pressure or the first set differential pressure, it is desirable in that the concentrated liquid can be recovered to the end as much as possible without diluting it, even if it takes time. Furthermore, the range of the second set differential pressure may deviate from the range of the allowable differential pressure or the first set differential pressure.

<Recovery of liquid in filtrate supply tube 3>
After the above-mentioned recovery of the concentrated liquid in the concentrator 20 is performed, if the concentrator transmembrane pressure difference reaches a set pressure difference or a specified amount of liquid has been recovered, the liquid transfer (including the flow of gas) from the filter 10 to the concentrator 20 may be stopped and then a gas such as air may be supplied to the filtrate supply tube 3. This makes it possible to prevent recovery leakage of the concentrated liquid in the concentrator 20 or the concentrated liquid flow path 4, and the liquid in the flow path downstream of the filtrate supply tube 3. If the concentrator transmembrane pressure difference has not reached the set pressure difference, the liquid transfer from the filter 10 to the concentrator 20 does not necessarily have to be stopped.

The liquid treatment device of the present invention is suitable as a device for filtering and concentrating pleural and ascites fluids containing cells, blood obtained during surgery or bloodletting to obtain concentrated liquids, and as a device for purifying and reusing plasma such as waste plasma from plasma exchange.

REFERENCE SIGNS LIST 1 Raw liquid treatment device 2 Supply tube 2c Flow rate adjustment means 2p Supply tube delivery section 3 Filtrate supply tube 3c Flow rate adjustment means 3p Filtrate supply tube delivery section 4 Concentrated liquid tube 4p Concentrated liquid tube delivery section 5 Waste liquid tube 5c Flow rate adjustment means 6 Cleaning liquid supply tube 6c Flow rate adjustment means 6p Cleaning liquid supply tube delivery section 7 Cleaning liquid recovery tube 7c Flow rate adjustment means 7p Cleaning liquid recovery tube delivery section 9 Connecting tube 9c Flow rate adjustment means 9f Flow rate adjustment means 9p Connecting tube delivery section 10 Filter 10B Filter 11 Main body 11a Raw liquid supply port 11b Cleaning liquid supply port 11c Filtrate discharge port 12 Body 12h Internal space 15 Hollow fiber membrane bundle 16 Hollow fiber membrane 16h Through flow path 16w UB
17a Holding member 17b Filtration membrane 17h Space 17f Space 20 Concentrator 20a Filtrate supply port 20b Concentrate discharge port 20c Waste liquid discharge port 100 Main body 103 Hanging portion 106 Control portion 110 Roller pump 120 Roller pump 150 Tube holder 155 Holding portion 152 Connection portion 153 Engagement member 160 Tube positioning member 161 Holding member 165 Connection member UB Stock solution bag CB Concentrate bag DB Waste solution bag SB Washing solution bag FB Washing solution recovery bag GB Concentrator washing solution recovery bag P1 Pressure gauge P2 Pressure gauge

Claims (10)

1. A method of operating an apparatus for concentrating a stock solution to form a concentrate, comprising the steps of:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
supplying a gas or liquid to a space in the filter separated from the raw liquid supply port of the filter by the filtering member before cleaning the filter;
A method for operating a raw liquid treatment device, comprising recovering filtrate and/or concentrate within the device while adjusting the flow rate of the concentrate flow path and/or the waste liquid flow path based on the pressure within a space separated from the waste liquid outlet by a water separation member in the concentrator or within a flow path connected to said space. 1. A method of operating an apparatus for concentrating a stock solution to form a concentrate, comprising the steps of:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
supplying a gas or liquid to a space in the filter separated from the raw liquid supply port of the filter by the filtering member before cleaning the filter;
The filtrate and/or the concentrate in the device is recovered while adjusting the flow rate of the concentrate flow path or the waste liquid flow path and the flow rate of the filtrate supply flow path based on the pressure in a space separated from the waste liquid outlet by a water separating member in the concentrator or in a flow path communicating with the space.
2. A method for operating a raw liquid treatment apparatus comprising the steps of: 1. A method of operating an apparatus for concentrating a stock solution to form a concentrate, comprising the steps of:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
When recovering the filtrate and/or the concentrated liquid in the apparatus, a liquid is supplied to a space in the filter separated from the raw liquid supply port of the filter by the filtering member,
The flow rate of liquid supplied to the flow path of the filtrate supply flow path and/or the space separated from the raw liquid supply port of the filter is adjusted based on the pressure in a space separated from the waste liquid discharge port by a water separating member in the concentrator or in a flow path connected to the space.
2. A method for operating a raw liquid treatment apparatus comprising the steps of: 1. A method of operating an apparatus for concentrating a stock solution to form a concentrate, comprising the steps of:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
a flow path branched from the filtrate supply flow path;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
Before cleaning the filter, the filtrate in the device is collected from a flow path branched off from the filtrate supply flow path.
2. A method for operating a raw liquid treatment apparatus comprising the steps of: 5. The method for operating a raw liquid treatment device according to claim 4, further comprising the step of: supplying a gas or a liquid to a space in the filter separated from the raw liquid supply port of the filter by the filtering member when recovering the filtrate and/ or the concentrated liquid in the device. 1. An apparatus for concentrating a stock solution to form a concentrate, comprising:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
a flow path for supplying a gas or a liquid to a space in the filter separated from a raw liquid supply port of the filter by the filtering member;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
The control unit:
Before cleaning the filter, the operation of the liquid delivery unit is controlled to supply the gas or liquid from the flow path that supplies the gas or liquid to a space in the filter separated from the raw liquid supply port by the filtering member, and the filtrate and/or the concentrated liquid in the device is recovered by adjusting the flow rate of the concentrated liquid flow path and/or the waste liquid flow path based on the pressure in the space separated from the waste liquid discharge port by the moisture separating member in the concentrator or in the flow path that communicates with the space.
A raw liquid treatment device comprising: 1. An apparatus for concentrating a stock solution to form a concentrate, comprising:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
a flow path for supplying a gas or a liquid to a space in the filter separated from a raw liquid supply port of the filter by the filtering member;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
The control unit:
Before cleaning the filter, the operation of the liquid delivery unit is controlled to supply gas or liquid from a flow path that supplies the gas or liquid to a space in the filter separated from the raw liquid supply port by the filtering member, and the filtrate and/or concentrated liquid in the device is recovered by adjusting the flow rate of the concentrated liquid flow path or the waste liquid flow path and the flow rate of the filtrate supply flow path based on the pressure in a space separated from the waste liquid discharge port by a water separating member in the concentrator or in a flow path that communicates with the space.
A raw liquid treatment device comprising: 1. An apparatus for concentrating a stock solution to form a concentrate, comprising:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
a flow path for supplying a gas or a liquid to a space in the filter separated from a raw liquid supply port of the filter by the filtering member;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
The control unit:
Before cleaning the filter, the operation of the liquid delivery unit is controlled to adjust the flow rate of the liquid supplied to the flow path of the filtrate supply flow path and/or the space separated from the raw liquid supply port of the filter based on the pressure in the space separated from the waste liquid discharge port by the water separation member in the concentrator or in the flow path communicated with the space, so that the gas or liquid is supplied from the flow path supplying the gas or liquid to the space separated from the raw liquid supply port of the filter by the filtering member in the filter and the filtrate and/or concentrated liquid in the device is recovered.
A raw liquid treatment device comprising: 1. An apparatus for concentrating a stock solution to form a concentrate, comprising:
The device,
A filter having a filtering member for filtering the raw liquid;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrate;
A raw liquid supply unit that supplies the raw liquid to the filter;
a liquid supply flow path communicating the raw liquid supply unit with a raw liquid supply port of the filter;
a filtrate supply flow path communicating a filtrate outlet of the filter with a filtrate supply port of the concentrator;
a concentrated liquid flow path connected to a concentrated liquid outlet of the concentrator;
a waste liquid flow path connected to a waste liquid outlet through which a waste liquid separated from the concentrated liquid in the concentrator is discharged;
a flow path for supplying a gas or a liquid to a space in the filter separated from a raw liquid supply port of the filter by the filtering member;
A liquid delivery unit that delivers liquid to each flow path;
A control unit that controls the operation of the liquid delivery unit,
A collection container is connected to the filtrate supply flow path,
The control unit:
Before cleaning the filter, the operation of the liquid delivery unit is controlled so that the filtrate is supplied to the collection container.
A raw liquid treatment device comprising: a flow path for supplying a gas or a liquid to a space in the filter separated from a raw liquid supply port of the filter by the filtering member;
The control unit:
The raw liquid treatment device according to claim 9, characterized in that, during an operation of recovering the filtrate and/or concentrated liquid within the device , the operation of the liquid delivery unit is controlled so that the gas or liquid is supplied from the flow path that supplies the gas or liquid to a space separated from the raw liquid supply port by the filtering member in the filter.

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