JPS5827993B2 - Method and apparatus for recovering clean water and solids from aqueous solids - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method and apparatus for recovering clean water and solids from aqueous solids.

In summary of the invention, the aqueous solids are relatively volatile with low viscosity to maintain a fluid and pumpable mixture even after substantially all of the water has been removed. mixed with a light fluidizing oil that is immiscible with water.

The mixture of solids, water and fluidized oil is subjected to a dehydration step by thermal evaporative action, whereby substantially all of the water and at least some of the light oils are evaporated and then recovered.

The light fluidized oil is then largely separated from the solids.

The solid content carrying the residual light fluidized oil is then steamed (
From now on, it will be called ``blow steam.''

) come into direct contact with. The presence of blown steam reduces the boiling point of the water-immiscible light fluidizing oil, making it effective for removal from the solids.

The effluent blown steam and the light oil vapor removed from the solids can be used to supply heat to the entire process.

The economical treatment of waste solids and the recovery of clean water from aqueous solutions and dispersions of the solids are well known problems in the art.

Also, the need to recover clean water and valuable solid materials from aqueous solutions and dispersions of solid materials is also a common concern.

Ideally, an apparatus and method for recovering water from aqueous solids would be easy to treat all components, non-polluting, economical to operate, and hygienic to handle. In addition, it should produce clean water.

In addition, when recovering the clean water, by-products, which either have an exciting value in themselves or can be used to make the process more economical, i.e.
It is desirable to obtain both liquid and solid by-products.

As used herein, the phrase "water/solids" generally encompasses suspensions, dispersions, solutions, mixtures, and various forms of fluids in which the solids are associated with water. used in

No. 3,855,079 (“Pro
Cess and Apparatus forRe
covering Re5idual Oil fr
om 5olidsDehydrated in
an Oil Medium and Grossly
[) eoi led 〃) describes a method and apparatus in which an aqueous solid is mixed with a relatively non-volatile fluidizing oil to form a mixture that is dehydrated by thermal evaporation.

The solids in the substantially anhydrous fluidized oil thus formed are then separated into an oil phase and a solids phase.

However, the solids have sorbed some amount of fluidizing oil thereon, which contaminates the solids and is also a loss to the process and economically uneconomical if not recovered. That's not a good thing.

The fluidized oil-borne solids are therefore subsequently subjected to an extraction step using relatively volatile, water-immiscible light oils.

The light oil-supported solids are then brought into direct contact with blown steam.

The presence of blown steam lowers the boiling point of the residual water-immiscible light oil, making its removal from the solids more effective.

The method and apparatus according to the invention consists of a series of steps and a systematic arrangement of equipment for recovering clean water and fractions from aqueous solids.

The aqueous solids are slurried with a light fluidizing oil of low viscosity, relatively volatile, and immiscible in water;
The mixture is then dehydrated by thermal evaporation.

Substantially all the water and a portion of the light fluidized oil are thereby vaporized.

The mixed vapor is condensed and separated into a clean water portion and a recovered light oil portion.

The resulting slurry of substantially anhydrous solids in a molded light fluidized oil is separated into an oil phase and a solids phase.

The solid phase carries residual light fluidizing oil.

Separation of the oil phase and solids phase can be carried out, for example, by gravity separation or by a pressurizing device, which pressurizing device may be static, dynamic, or both. .

The method and apparatus according to the invention can economically remove residual light oil from the separated dry solids without the need for extraction L8.

It is therefore an object of the present invention to provide a method and apparatus for dewatering aqueous solids in a light fluidized oil medium.

``The first objective is to provide a method and apparatus for recovering clean water from water and NTG solids'' in the song ``Ki-ni [1]''.

The purpose of the present invention is to recover dehydrated water in a fluidized oil medium from solids to substantially dry fluid-free solids. and equipment.

Yet another feature of the present invention is to substantially dry the heavy oil-containing aqueous solids, which have a reduced heavy oil content as compared to the raw heavy oil content of the raw feedstock system based on a water-free condition. An object of the present invention is to provide a process and apparatus for recovering solids.

Yet another object of the present invention is to recover substantially dry solids from heavy oil-containing aqueous solids having substantially the same heavy oil content as a feedstock system based on water-free conditions. An object of the present invention is to provide a method and apparatus for doing so.

These and other objects are accomplished by practicing the present invention.

An overview of the present invention from one of its important aspects:
The present invention comprises a method for recovering clean water and substantially dry fluidizing oil-free solids from aqueous solids that are dehydrated in a light fluidizing oil medium, the method comprising: , mixing the aqueous solids with a low viscosity, relatively volatile, water-immiscible light fluidizing oil to obtain a pumpable mixture that remains fluid after removal of water; 2. Dewatering the oil-containing mixture by means of a heated evaporator, thereby vaporizing substantially all of the water and some of the light fluidized oil to produce a substantially anhydrous solid in the form of an oil slurry: 3. A one-liter scale 44 for condensing the resulting mixture of water and light oil vapor. Separating the condensate produced in the above step into a clean water portion and a light oil portion; 5. The substance in the form of an oil slurry. (+4) Step of separating at least some of the light fluidizing oil that is relatively volatile and immiscible with water from the solids of the water: 6. contact with blown steam, thereby efficiently removing the light oil from the substantially anhydrous solids by thermal evaporation.
It is characterized by comprising various processes consisting of culm.

The process involves the use of dehydrated water in a light fluidized oil medium.
FjJ t! 1. v The tank 2 which receives the IjjτI type flow and is equipped with a stirring or mixing mechanism, the small C-quality fluid fluid storage tank 3, and the fluidized oil from the high-quality oil storage tank to the tank. Means adapted to feed and mix said light fluidized RB oil and aqueous solids: 4. Evaporator 5 extending from said tank to said evaporator and delivering a stream of aqueous solids mixed with light fluidized oil. a conduit for providing flow from the tank to the evaporation zone of the evaporator; 6. a condenser near, extending from the evaporator to the condenser and formed by heating the aqueous solids and light fluidized oil mixture; A conduit for flowing a mixture of water vapor and light oil vapor: 8. Oil/water separation means 9, a conduit extending from the condenser to the oil/water separation means and allowing a mixed condensate of water and light oil to flow; 10. Means for separately recovering light oil and clean water from the water separation means; 11. Liquid/solid separation means 12. Extending from the smoke evaporator to the liquid/solid separation means; a conduit for flowing a substantially anhydrous solids slurry stream; 13. deoiling means;

14. A conduit extending from the liquid/solid separation means to the deoiling means and allowing the light fluidized oil-carrying solids to flow, and 15. The light fluidized oil in the evaporator and the deoiling means. Systematically installing means consisting of a combustion device associated with said evaporator and deoiling means to supply heat of vaporization to the blown steam brought into direct contact with the supported solid cedar fraction.
It is composed of

Accordingly, the present invention provides a method and apparatus for recovering solids and clean water from an aqueous stream dehydrated in a light fluidized oil medium.

The present invention is characterized in that not only clean water is recovered from aqueous solids dehydrated in a light oil medium, but also residual light oil is recovered from the solids.

The aqueous solids are mixed with a low viscosity, relatively volatile, water-immiscible light fluidizing oil, and the mixture is heated to remove substantially all of the water and some of the light oil. It undergoes a dehydration process by evaporation.

The remainder of the light fluidized oil is then separated from most of the solids.

After that, the solid content for light fluidized oil is removed by steam (hereinafter referred to as ``blown steam'').

) can come into direct contact with or come into contact with.

Since light oils are immiscible with water, direct contact with blown steam is essentially equivalent to steam distillation; in the presence of blown steam, the light oil boils at a temperature below its normal boiling point.

The aspects and advantages as well as the nature and content of the invention will become more clearly apparent in the detailed description taken in conjunction with the drawings.

Therefore, the clean water and solids sheet method according to the present invention applied to aqueous solids is characterized in that the residual light oil is recovered from the solids which have been substantially dehydrated in advance in a light fluidized oil medium.

In this method, the aqueous solids are mixed with a light fluidizing oil of low viscosity, relatively volatile, and water-repellent;
This results in a pumpable mixture that remains fluid even after virtually all water has been removed, after which the synthetic mixture of solids, water and oil is subjected to a dehydration step by thermal evaporation, thereby substantially all of the water and at least a portion of the light fluidized oil are evaporated;
It will be collected next.

Very dilute aqueous solids can also be concentrated by evaporation prior to mixing with light oils.

Steam from the subsequent oil dewatering step can be used to replenish the fluidized oil-free condensing stage of the evaporator system.

After the dehydration step, the light oil is largely separated from the solids.

The solids carrying residual light flow oil are brought into direct contact with the blown steam, whereby the light oil is removed by thermal evaporation.

The solid content is insoluble in water and originally includes heavy oil, and in an embodiment of the present invention in which the oil is extracted with light fluidized oil, light fluidized oil The supported solid content is slurried with water.

The slurry is contacted directly with steam, thereby vaporizing substantially all of the light oil and at least an amount of water.

The solids are then removed from the remaining water, for example by a settling tank.

An important step of the present invention is to contact the solids in the light fluidizing oil directly with blown steam, thereby causing the light oil to evaporate.

Therefore, if the blown steam is superheated steam,
The blown steam supplies the latent heat of vaporization of the light oil, and further the blown steam supplies the light oil with water at a temperature below the boiling point of the higher boiling point of the liquid. Since it is a well-known scientific fact that light fluidizing oil boils at This results in a state of evaporation.

On the other hand, light oil-supported solids have a temperature of approximately 212"F (100°C) at atmospheric pressure if the heat of vaporization of the light oil is supplied through a device such as a heating jacket. direct contact with saturated blown steam is also possible.

If the contact of the light oil-supported solids with the blown steam is carried out under reduced pressure and the heat of vaporization of the light oil is provided by an external heat source, for example by a heating jacket,
Lower temperature steam in the range of about 150''F (65.6C) or lower may also be used.

It will be appreciated that as a result of the heating by an external heat source, the solids are in each case at the specified pressure and at a temperature above the boiling point of water.

Light fluidizing oil refers to a fluid that is immiscible with water, relatively fluid, and relatively volatile.

Accordingly, a relatively volatile fluidizing oil is mixed with the aqueous solids prior to their dewatering.

Substantially all the water is removed by dehydration through heating and evaporation.
Some light fluidized oil is removed.

The remaining light oil is largely separated from the solids and thereby removed from the solids carrying residual flow oil.

When heated by an external heat source, it would otherwise be extremely high, e.g.
Light oils boiling at temperatures such as 87.8° C.) can be used as fluidizing oils in the dewatering process in the practice of this invention.

Contacting the light fluidized oil-supported solids with direct blown steam in accordance with the present invention effectively results in steam distillation, which otherwise would be from about 150 below (65,6°C) to about 550'F.
Light oil that boils in the range of (287,8℃) is about 70″
It is distilled at a temperature within the range of 21,1°C to about 400"F (204,4°C).

In the practice of this invention, a substantially anhydrous slurry of solids in a light fluidized oil is separated to recover the oil and solids.

The solids are mostly dry but contain sorbed light flow oil.

This applies either statically varying mechanical pressures, dynamically varying mechanical pressures, or both pressures to the anhydrous slurry by the action of gravity, thereby causing most of the oil to This is achieved by separating the solids from the solids.

For example, when processing food products, sewage sludge, raw materials or abattoir waste, the material itself contains some oil separate from the light fluidizing oil added prior to the dewatering step. Contains.

If the kernel oil is a light oil, the oil is substantially reduced to a portion of the light fluidized oil and is evaporated during the dehydration process and subsequently recovered or solids and added fluidization during the dehydration process. It will be transported along with most of the oil and will be separated from the slurry, which is subjected to dewatering, along with the added oil.

If a substantially water-free slurry is subjected to a very efficient separating action, oil will be produced in an amount or proportion equal to or greater than the amount of oil previously added to the anhydrous solids. It will happen.

If the oil contained in the anhydrous solids is a heavy, relatively non-volatile oil, then the oil is actually reduced to a lighter fluidized oil during the separation process, e.g. during the application of pressure, thereby substantially drying the oil. The extracted solids are separated from the light oil and recovered.

Alternatively, if the extracted heavy oil is not separated from the light fluidized oil and the entire oil mixture is recycled as fluidized oil, an equilibrium condition will occur, resulting in a substantially dry solid state. The heavy oil content of the output will be substantially the same as the content of the raw feedstock in the absence of moisture.

Generally, it is desirable that all oil separation and deoiling steps yield enough oil for reuse in the dewatering step, and that the process be self-sufficient with respect to light fluidized oil requirements.

More desirably, for example, when the aqueous solids initially contain light oils, somewhat more light oils than are required for the dewatering step are added in the overall process of oil separation and deoiling. oil, so there will be a net oil production in the process.

Also, if the aqueous solids originally contained heavy oil, the kernel oil could be extracted with light fluidized oil and then recovered as described above.

No matter how severe the separation action, e.g. pressurization action, is on the substantially anhydrous solids slurry in the light oil, the recovered solids will still have absorbed some of the light oil; If so, the light oil will be lost to the process.

The liquid-solid separation means for separating the light fluidized oil from the solids may be, for example, a settling tank in which the separation is effected by gravity.

Alternatively, the separating action may be a static mechanical pressure varying means, such as a reciprocating filter press;
Further preferred is a dynamic separation device such as a centrifuge.

However, it is also possible to use presses of both static and dynamic nature.

Therefore, most light oils are pressurized with solids, for example in a centrifuge, and the oil is collected in a suitable storage tank and available for reuse in the process if desired.

If the aqueous solids initially contain heavy oil, the oil can be separated from the substantially anhydrous solids by extraction with a light fluidized oil during the liquid-solid separation step. Probably.

If the separated oil were to be divided into light and heavy oil components, the result would be a reduction in the heavy oil content of the dry solids.

On the other hand, if the separated total amount of oil consisting of light fluidized oil and extracted heavy oil is recycled as fluidized oil, an equilibrium condition is obtained and the heavy oil is the total amount of recycled oil. The same amount is refluxed into the dry solids as is removed by the fluidizing oil.

The net result is a substantially dry solids having substantially the same heavy oil content as the raw feedstock in the absence of moisture.

Since light fluidizing oils have low viscosity and low specific gravity, such as light oils in petroleum systems, the dewatered slurry from the evaporator can be transferred to a settling tank, thereby The solids of the more concentrated oil phase are separated as a thick slurry, and an amount of oil is retained in the upper part of the tank from which it can be recycled to the process.

The gravity separation action does not require any mechanical pressure fluctuations, static or dynamic.

The concentrated thick oil-solids slurry or oil-absorbed solids is then brought into direct contact with blown steam.

The blown steam, if superheated, provides latent heat for vaporization of the light oil.

Alternatively, saturated blown steam at about 212"F (100'C) is used in conjunction with external heat, such as from a steam jacket, to provide heat for light oil evaporation.

Since light oils are immiscible with water, direct contact of the kernel oil with blown steam essentially means steam distillation, causing the light oil to boil below its normal boiling point.

Light oils therefore require less thermal energy than is required for blown steam alone or for blown steam in conjunction with an external heat source, such as steam in a steam jacket or indirect heat transfer with other heat transfer fluids. Not only is it more easily evaporated from the solids by
Enables the use of light oil with a higher boiling point.

However, the heavy oil present on the dry solids is not substantially evaporated.

As mentioned above, direct contact of the yuzu solids or concentrated oil-solids slurry with blown steam allows evaporation of the light oil at temperatures below its normal boiling point.

However, when used for deoiling temperature-sensitive materials such as human food or animal feed,
A 111 leather oil with a very low evaporation temperature is desired.

This is accomplished by contacting the oil solids with blown steam at subatmospheric pressure.

Removal of the light oil from the solids by direct contact with the blown steam can be conveniently carried out in a deoiler.

The deoiling device is preferably connected to a settling tank or to the discharge of a Kada device, such as a centrifuge, and is operated at atmospheric pressure or below atmospheric pressure.

If desired, the deoiling device can be heated externally, for example by a steam jacket.

The blown steam flows into a deoiler with a concentrated oil-solids slurry or oil-supported solids.

It is preferable to use the blown steam discharged from the deoiling equipment and the vaporized light oil as heat sources in the process.

The vaporized light oil is eventually condensed and reused in the dehydration process.

Any heavy oil present on the solids is not substantially evaporated.

In one embodiment of the invention, the aqueous solids initially contain a heavy oil that is water-insoluble and is substantially extracted by the light fluidizing oil, and then the light fluidizing oil and the extracted heavy oil. Separated from quality oil.

The light fluid oil-borne solids are slurried with water and the slurry is directed to the evaporation zone of an evaporator where at least a portion of the water is converted to steam.

The steam is a blown steam that is in direct contact with the light oil-carrying solids and causes the evaporation of the water-insoluble light oil to occur in the same manner as the evaporation effect performed in the deoiling equipment described in -.

Some of the water in the aqueous slurry is also evaporated as described above.

The solids are then separated from the residual water by means such as filters or settling tanks.

The recovered solids not only contain no light fluidizing oil, but also substantially contain the heavy oil that it initially contained.
do not have.

The residual solids after light oil has been removed by direct contact with blown steam can often be used for other purposes than those of the process itself and can therefore be considered an output of the process. .

The process and apparatus of the present invention converts aqueous solids from a variety of sources, whether the solids are waste or solids with inherent value, into clean water and substantially dry water. It can be used to recover solids.

Thus, for example, the present invention can be used in aqueous solutions, in aqueous dispersions or in other embodiments associated with water, such as powdered coal, food products, animal feed and waste, cement, old lime, mineral salts, sewage, sewage, etc. Sludge, abattoir effluent and generated substances, ooze, black liquor from the paper industry, bark consisting of, right machine effluent from garbage treatment plants, drugs and pharmaceutical waste, Ganzume factory effluent, chemicals, etc. It can be used to collect clean water and solids from the limbs of humans.

Depending on the source of the feed, the solids recovered by blown steam contact, catalysis can therefore be used as fertilizer, as animal feed or as human food, e.g. in dehydrated, fat-free food. It is available as.

Also, since the solids are often combustible, the steam required to operate the evaporator component of the device, the concentrated oil-solids slurry or the blown steam to contact the oil-borne solids. It can also be used as a fuel for producing auxiliary equipment such as steam-driven pumps, or indirectly in the case of motor-driven pumps, to operate auxiliary equipment such as these pumps. It is used as fuel for the necessary steam generation, and the steam is also used to directly drive the turbine generator.

Heavy oil remaining on substantially dry solids may also have value as a fuel.

The process is therefore at least partially self-sufficient in terms of fuel requirements.

Accordingly, the method and apparatus of the present invention provide a means for recovering substantially clean water and valuable solid product from aqueous solids.

Additionally, the present invention provides that residual light fluidizing oil from the dewatering process that is sorbed onto or otherwise associated with the solids is efficiently recovered for reuse. It has characteristics in points.

Materials processed by the method of the present invention should generally contain solid particulates smaller than 10 inches (6.35 mm).

However, larger granules, such as bones for gelatin production, are also possible if the air gaps between the heat transfer surfaces are correspondingly enlarged.

Large granules may be crushed or subdivided by existing techniques to size.

The oil used to mix with the aqueous solids prior to dehydration is inert and immiscible with water.

In addition, the light oil is volatile and volatile to the extent that it is vaporized by direct contact with blown steam at a temperature within the range of about 70"F (21,1°C) to about 400'F (204,4°C). Should have 11.

Generally from about 150 below (65,6°C) to about 550 below (2
87.8°C), preferably 300'F (1
Light oils boiling within the range of 48.9'C to about 450F (232.2C) are believed to be effective in this regard.

For example, from about 325'F (162,8'C) to about 40
Light oils, such as hydrocarbon oils that boil in the 0"F (204,4C) range, must be boiled within their boiling range when processing animal feed and human food. This is particularly preferred since it can be almost completely removed from the dry and refined solids.

The type of light oil that is usually preferred is the light hydrocarbon oil.

The light hydrocarbon oil may be normal paraffinic, isoparaffinic, aromatic hydrocarbon, or naphthenic.

Examples of suitable light hydrocarbon oils include n-pentane, isopentane, n-hexane, cyclohexane, benzene, isooctane, eicosane, about 300 or less (148,9
Petroleum fractions, isohexane, xylene, octadecane, I
Examples include toluene, n-hebutane, cyclopentane, and mixtures thereof.

Another class of suitable light oils are fatty alcohols which are immiscible with water.

Examples of suitable alcohols include n-hexyl alcohol, n-hexyl alcohol, isohedityl alcohol, n-z)r'7f alcohol, isooctyl alcohol, n-/nyl alcohol, and n-decyl alcohol. It will be done.

Fatty acids such as caproic acid and capric acid can also be used as light oils.

In food and animal feed processing processes, for example, HumbleOil and Refining Company under the trade name
FDA, such as a range of isoparaffinic oils manufactured by Refining Company
Approved light oils may be used.

I 5o, especially when processing animal feed and human food.
par H is preferred.

It has a flash point of 3.5 l5 oparH, which is suitable for safe work, and a boiling point of 15 oparH of about 325”F.
(162,8°C) to 400"F (204"C), the oil is almost completely removed from the altameni dried food and meets FDA regulations.

In general, materials that are solid at operating temperatures, preferably oily, and relatively volatile and substantially immiscible with water can be used.

using light oils that allow the process to operate efficiently, i.e. those that can add value to solid products, such as waste oils normally found in F-water or industrial wastewater, or fuel oils;
Alternatively, as mentioned above, it is often desirable to use oil produced in the process itself to minimize cost factors.

The amount of fluidizing oil is such that the proportion in the system ranges from about 2 to about 20 parts by weight or more per part of solids that are not fats or oils.

This refers to the total oil, ie the total oil that is added, also including the oil produced from the process for reuse.

This amount of oil provides a fluid pumpable material even in the absence of water.

As used herein, the term "fluid" refers to "liquid";
That is, it is used synonymously with a "liquid" that assumes the shape of a container when the mixture is filled into the container.

Although the dehydration process of the present invention can be carried out in single-stage or single-effect can evaporators known in the art, it is preferred that the process is carried out in a plurality of consecutive heated evaporation stages.

In the continuous heating evaporation steps, the temperature in each continuous evaporation step increases successively, and the degree of concentration of the resulting solids stream increases sequentially due to the increasing dehydration effect; The steam released from each evaporation step will supply half of the heat requirements of the preceding evaporation step.

Therefore, a plurality of continuous heating regimes means at least two steps.

The temperature, pressure and concentration at each step in the evaporation sequence will depend on the equipment and oil used and will largely depend on experience.

Typical processing temperatures for the dewatering of light fluid oil/aqueous solids mixtures are approximately 70"F (2
1,1"°C) to about 250 below (121,1°C), and in the second, third, or final stages about 100"F (37,8°C) to about 250°F (121,1°C) 400”F (204
, 4°C).

The preferred processing temperature is about 90'''F (32,2°
C) to approximately 175”F (79.4°C);
The second, third or final stage ranges from about 125 below (51-7'C) to about 350'F (176,7'C).

The temperature range and its progress are determined by the temperature range and its progress.
This is reasonable for a J-type evaporator in which the flow through the evaporator and the heating or drying steam are substantially countercurrent; (
backward flow (backward flow) is called the evaporator.

The temperature also depends on the desired quality of the final product and the economy of fuel utilization;
Depends on cooling water right dexterity, capital investment, etc.

In the foregoing description, the expression "first stage" refers to that part of the evaporator apparatus in which the light fluidizing oil/aqueous solids mixture is subjected to the first stage of a plurality of successive evaporation stages; When there are two or three or more steps, a "second stage", "third stage", etc. are provided correspondingly.

On the other hand, the expression "effect can", for example in the expression "multi-effect can" or "multi-effect can", relates to the flow and action of the heating medium, usually steam, of the evaporator device.

If the stream of light fluidizing oil/aqueous solids mixture to be heated and vaporized is in a countercurrent relationship (countercurrent condition) to the stream of heating steam, the first stage of the evaporator is in its last effect vessel. will be the same as

Pressure is controlled by temperature to achieve the desired evaporation rate for a given design.

Therefore, the pressure in the first stage is about + inch (12,'7 mm
) Hg (absolute) to approximately atmospheric pressure is advantageous.

The pressure then increases in the subsequent stages in response to the temperature in the case of countercurrent flow.

Preferably, the first stage operates under reduced Efx conditions, and the final stage operates near atmospheric pressure.

The benefits of a continuous evaporation process will become clear from the discussion below.

For example, in a two-effect evaporator where the feed enters at 80°C (26,7°C), the material enters the evaporator at 225°C.
Approximately 1.5 to 1.75 ″F (107,2°C) to 250″F (121,1°C) can leave and evaporate.
Approximately 1 pound (0.68-0.79 kg) of water
lb. (0.45 kg) of steam rate is used, but in normal single-effect can operation, approximately 1.5 kg. 5 bonds (0,68 kg) of steam is required.

If three or more effect can evaporators are used,
Further savings in fuel consumption would be possible.

The steam released from each heating evaporation step after the first step is
It should be understood that in the case of a countercurrent evaporator, a significant portion of the desired heat of the pre-heated evaporation step or stage is provided.

The small amount of external heat required is the amount of heat required to raise the temperature of the components to the vaporization temperature and provide the heat of vaporization and compensate for heat losses.

The final product from the dehydration step is generally a substantially anhydrous oil solids containing about 5 to 10 weight percent water based on the non-fat base.

Any type of evaporator can be used, although countercurrent evaporators are preferred.

Therefore, a countercurrent evaporator, a forward flow (downflow) evaporator, a combination countercurrent-downflow evaporator, or any combination thereof can be used.

Various types of evaporators are available on the market that are considered preferred.

For example, examples of these evaporators are those manufactured by Mojonnier Bros, Co. and Blow-Knox Food &C.
Chemical Equipment, Inc.
)'s Buflovac Div.
Multi-effect can evaporators, such as the Mojonier type or Pufflobac type evaporators manufactured and sold by Ision), recompression type evaporators, such as the thermal or mechanical recompression type, and others.

Functionally, the evaporator device may be of the forced circulation type, flash type, fallen film recirculation type, single flow type, rotating wiped film type, plate type or any type of device.

The separation of solids from the light flow oil may conveniently be carried out by gravity separation or by liquid-solid separation means, preferably by dynamic pressure action, such as a centrifuge.

recovered by liquid/solid separation means, such as a centrifuge,
The surface contains solids or concentrated oil that sorbs residual light oil.
The solids slurry is then contacted directly with blown steam to remove residual light oil.

Residual heavy oil present on the solids is not substantially removed by contact with the steam.

In the embodiment of the invention illustrated in FIG. is brought into direct contact with the blown steam.

It may be advantageous for the deoiling device to be heated externally, for example by flowing steam through a surrounding heating jacket.

The blown steam is preferably saturated steam at a temperature in the vicinity of 21.2'F (100°C) and atmospheric pressure, but may range from about 250°F (121.1°C) to 500'F (100°C) or below.
It is also possible to overheat in the range (260° C.).

The light oil is evaporated at a temperature below its normal boiling point by blown steam that is brought into contact with the light oil-bearing solids in the deoiler.

As mentioned above, the residual heavy oil of the oil-bearing solids is not evaporated to an appreciable extent.

The vaporized light oil and effluent blown steam are preferably introduced from the deoiler, and their energy is recovered as useful work.

It is then used, for example, as a heat source in the evaporation zone of the system.

In the embodiment illustrated in FIG. 2, the deoiling device is connected directly to a drying evaporator operating at reduced pressure, ie, subatmospheric pressure.

As a result, the deoiling equipment is also under reduced pressure.

Accordingly, the deoiler requires less blown steam and can operate at lower temperatures.

This is useful when deoiling temperature sensitive materials such as human food or animal feed.

The deoiling device can be heated externally, for example by a steam jacket, to provide latent heat.

In the embodiment illustrated in FIG. 3, the aqueous solids initially contain heavy oil, the heavy oil is extracted with light flow oil, and then the light flow oil and the extracted heavy oil are combined. are separated.

Light fluidizing oil is recycled through the system.

As shown in FIG. 1, which is a modified version of FIG. 3, the oil-loaded solids are brought into direct contact with blown steam in a deoiler to remove residual light flow oil.

By initially extracting the heavy oil contained in the aqueous solids with a light flowing oil, the heavy oil content of the resulting substantially dry solids has been reduced.

In the embodiment illustrated in FIG. 4, the aqueous solids are water-insoluble and initially contain heavy oil, which is allowed to be extracted by light flow (arsenic oil).

Light slaked 2-solid content pulping (re-pulp mixing)
It is made into a slurry with water in a tank.

The water slurry is introduced into the evaporation zone of the evaporator where at least a portion of the water is converted to steam, the steam directly contacts the slurry and a portion of the light oil and water is evaporated.

The solids are then separated from the water.

The heavy oil initially associated with the aqueous solids is extracted by the light flow oil, resulting in a significant reduction in the heavy oil content of the recovered solids.

In the embodiment illustrated in FIG. 5, a substantially anhydrous solids slurry in a light fluidized oil is separated by gravity into an oil phase and a thickened light oil/solids slurry in a settling tank.

Separated oil is removed from the top of the settling tank and recycled into the system.

The concentrated light solids slurry is pumped to a deoiling unit where it is brought into direct contact with blown steam to vaporize the haze oil at temperatures below the normal boiling point.

Although the deoiling apparatus illustrated in FIG. 5 operates at substantially atmospheric pressure, it will be appreciated that it could alternatively operate under reduced fields.

In the embodiment illustrated in FIG. 6, the apparatus uses a single stage evaporator in which a substantially anhydrous solids slurry in a stream of concentrated oil is separated by gravity into a light oil phase and a concentrated light oil/solids slurry. It can be said that it is relatively simple and compact in that it is separated into a slurry and does not require a pressurizing device.

The separated light oil is recycled into the system, while the concentrated light oil/solids slurry is pumped to the deoiler.

The effluent blown steam and vaporized light oil from the deoiler are introduced directly into the first stage evaporator of the system.

In such a single-stage evaporator, it is important to use the steam blown out from the deoiling device and the vaporized light oil in order to utilize the steam for right movement within the system.

BRIEF DESCRIPTION OF THE DRAWINGS The invention will be clearly understood with reference to the preferred embodiments which will be described in more detail in connection with the flow diagrams illustrated in the drawings.

In the embodiment illustrated in FIG. 1, a meandering stream of water in the form of a solution or dispersion enters the fluidization tank 10 via line 12. In the embodiment illustrated in FIG.

Light fluidizing oil flows into fluidizing tank 10 via line 14 .

The fluid mixture in the fluidization tank 10 is agitated by an agitator 16 and then removed from the fluidization tank by a pump 18.

Pump 18 delivers the mixture via line 20 to the evaporative working area of the first stage of the all-dry evaporator assembly or evaporator array, ie to the third effect can evaporator 22 .

In the evaporator 22, water and a portion of the light oil are under reduced pressure,
For example, typically about 2 to 10 inches (50,8 to 254
mm) Boiled at Hg (absolute).

The temperature of the partially dehydrated and partially deoiled output of the influent aqueous solids mixture mixed into the light oil is about 70-250 below depending on the evaporator pressure (2). 1-1
21.1°C), preferably about 90-175 below (32,
2 to 79.4°C).

The system is heated by a mixture of steam and light oil vapor to a temperature approximately 30-40"F above the temperature of the aqueous solids that are partially dehydrated within the oil mixture. It is said that

The steam and light oil vapor mixture also comes from the steam chamber of the subsequent or second stage of the evaporator.

The heated steam condensate is recovered via line 26, which is connected to line 28 at a "T" joint.

The condensate is introduced via line 28 into an oil/water separator 30.

The steam/light oil vapor mixture formed by partially dewatering the incoming aqueous solids mixture in the light oil is transferred to the evaporator 2.
2 steam chamber is fed via line 34 to surface condenser 36 .

The interior of the condenser is maintained in a partial vacuum state by a vacuum pump 38.

The vacuum pump is connected to the rain condenser 36 via a vacuum line 40.
connected to.

The water and light oil vapor mixture entering the surface condenser 36 via line 34 is cooled by cooling water entering the condenser via line 42 and exiting the condenser via line 44. Condensed.

The condensate mixture of warm water and light oil is sent from the condenser via line 46 to oil/water separator 30 .

In the oil/water separator 30, the water and light oil mixture is separated into light oil and partially purified water containing some light oil.

The separated light oil is recovered through the oil/water separator 30 and the pipe 48 and introduced into the light oil storage tank 50.

Partially purified water is introduced from the oil/water separator 30 via line 54 to a coalescer 56.

In the condenser 56, partially purified water containing some amount of light oil is separated into a light oil and a clean water product.

The separated light oil is recovered from the condenser via line 58.

The pipe 58 is connected to the pipe 48 at a "T" joint, and the light oil is eventually introduced into the light oil storage tank 50.

Clean water output is recovered from the flocculator 56 via line 60.

If desired, a portion of the output water can be reused within the system.

Alternatively, all recovered water can be stored for later use in applications where substantially clean water is required.

The partially dehydrated aqueous isomorphic mixture in the light oil is transferred to the evaporator 2.
2 through the line 62 by the force of the pump 64.

The partially dehydrated mixture is forced through line 62 to the evaporation zone of the second stage 66 of the evaporator.

In the second stage evaporator, a procedure similar to that of the first stage continues, except that the mocha is elevated.

The pressure in each subsequent evaporator stage is somewhat higher than the pressure in the preceding stage, and approaches near atmospheric pressure in the final stage.

The temperature of the further dehydrated output of the second stage evaporator is approximately 100-400"F (37.8-20"F) depending on the evaporator pressure.
4. ．． 4°C) preferably below about 125-350°C (51,7
~176.7°C).

The heating medium is a mixture of steam and light oil vapor, which is approximately 30-40F (16,7-22.2'C) above the temperature of the aqueous solids slurry exiting the further dehydrated second stage evaporator.
) is the highest temperature.

The mixed heated steam is provided via line 68 from the steam chamber of the third or subsequent evaporator stage.

The condensate of the mixed heated steam is recovered from the second stage evaporator 66 via line 28 and fed to the oil/water separator 30.

As mentioned above, the steam/light oil vapor mixture formed by further dehydrating the aqueous solid content mixture in the partially dehydrated light oil is sent from the steam chamber of the second stage evaporator 66 through the pipe 24 to and is used as a heating medium for the first stage evaporator 22.

The aqueous solids slurry in the further dehydrated light oil recovered from the second stage evaporator 66 is transferred to a pipe 74 by a pump 70.
released through.

The further dehydrated mixture is introduced via line 74 into the evaporation zone of the third stage 76 of the evaporator.

The pressure in the third stage is higher than the pressure in the second stage, preferably approximately atmospheric pressure.

The temperature of the output of the third stage evaporator 76, a slurry of solids in light oil containing about 1% water by weight based on the total slurry, is greater than the temperature of the second stage evaporator 66, about 10
It is within the range of 0 to below 400°C (37.8 to 204.4°C), preferably about 150 to 350'P (65.6 to 1767°C).

The heating medium for the third stage evaporator 76 is approximately 30 to
The steam temperature is 50°C (16.7~27.8°C) higher.

The steam is generated in the boiler/furnace γ7, and is passed through the pipe 78.
to the third stage 76 of the evaporator.

The heated steam condensate is collected via line 80 and returned to the boiler/furnace.

As previously described, the steam/light oil vapor mixture formed by further dewatering the solids slurry in light oil is removed from the vapor chamber of the third stage evaporator 76 via line 68 and transferred to the second stage evaporator 76. It is used as a heating medium for the stage evaporator 66.

A substantially anhydrous solids-in-light slurry is recovered from the third stage evaporator 76 and forced by a pump 82 through line 84 to a continuous centrifuge 86 .

The light oil is separated from the solids in a centrifuge 86 and introduced from the centrifuge through a line 88 into the light oil storage tank 50 .

The recovered light fluidizing oil is transferred to the pipe 14 by a pump 90.
to the fluidization tank 10 and recycled into the system.

If the process produces net oil, that oil can be recovered from tank 50 and stored for use outside the system.

Solids sorbing residual light oil also exit the continuous centrifuge 86 and flow via conduit 96 into a container (reservoir) 94.

The container 94 is a container equipped with a conveying means such as a screw conveyor at the bottom thereof, and is generally referred to as an "active bottom container (1iv)".
e bottom bin) 1 is a well-known storage and transport means.

Thus, the bottom of the container 94 with the screw conveyor, ie the talking bottom, advances the solids charged in the container to the outlet of the container.

The solids are then transferred from the outlet ``J'' to the categorizer (
Lumps) are introduced into the deoiling device 100 by gravity.

The deoiling device 100 generates steam in a boiler/furnace 77 as desired, and supplies steam to the jacket 10 via a pipe 104 1-.
It can be heated externally by steam flowing into 2.

Steam jacket condensate is collected via line 106 and returned to the boiler/furnace.

The blown steam generated in the boiler/furnace 77 is transferred to pipe 1
04 to a pipe 108 connected at a T-1 joint, and from the pipe 108 to the deoiling apparatus 100.

In the deoiling device, the steam is brought into direct contact with the light oil-carrying solids, and the light oil is vaporized at a purity above its normal boiling point.

Effluent blown steam and vaporized light oil exit the deoiler via line 110.

The solid content, which has lost its sorbed light oil, is transferred by gravity from the deoiling device 100 via a conduit 114 to an active bottom container (reservoir) 116 having the same structure as the active bottom container 94.
sent to.

The screw conveyor bottom of vessel 116 guides the solids to the outlet, where the solids, which are substantially anhydrous and free of fluidizing oil, are passed via line 118 to a grinder or pulverizer 119. is sent out.

A grinder 119 subdivides the solid content into powder or particles.

The solids then flow from the grinder via line 120 to a rotary selection valve 121 and are directed by the rotary selection valve 121 into either line 122 or line 123. .

Conduit 122 is guided to a collection or bagging machine, from which it is removed and reused outside the system shown.

According to the setting of valve 121 as actually shown in the diagram, line 1
23 is introduced into the suction section of the blower 124.

The blower delivers the crushed solids via line 125 to the combustion zone of the boiler/furnace 77.

The effluent blown steam and vaporized light oil coming from the deoiler 100 are introduced by line 110 into the second stage evaporator 66 .

In the evaporator, the mixed vapor supplies heat of vaporization to the second stage evaporator.

The second stage evaporator is operated below atmospheric pressure, and a valve 126 equipped with a pressure sensor is disposed on the line 110 to maintain the pressure within the deoiling apparatus 100 at somewhat less than atmospheric pressure. Operate.

Therefore, the deoiling process is carried out at substantially atmospheric pressure.

Thus, in the illustrated embodiment, the energy of the effluent blown steam and vaporized light oil is effectively recovered by providing heat to the second stage evaporator 66.

Heated steam and vaporized light oil condensate are recovered from the second stage evaporator via line 28 and sent to oil/water separator 30.
sent to.

The steam blown into the deoiling apparatus 100 and the vaporized light oil are shown in FIG. 1 as supplying heat of evaporation to the second stage evaporator 66, but the energy of the mixed steam is It can also be recovered by supplying it to the first stage evaporator 22.

The energy of the steam mixture is also such that the oil it contains will contaminate the condensate which is returned to the boiler/furnace 77 via line 80 and the temperature of the steam will be sufficient to cover the required amount of heat transfer. is not high enough, it can be recovered by supplying it to any evaporation stage in the system except for the shell side of the third stage evaporator 76.

Alternatively, the effluent blown steam and vaporized light oil can be removed from the aqueous solids by being delivered to the fluidization tank 10, or anywhere else in the system where the efficiency of the process can be increased by recovering its energy. minutes can be utilized to preheat the light fluidized oil mixture.

The foregoing discussion with respect to FIG. 1 applies when the aqueous solids do not initially contain heavy, relatively non-volatile oils.

If a relatively non-volatile heavy oil had originally been present in conjunction with the aqueous solids, it would have been extracted by the light fluidizing oil during the pressurization operation.

In the embodiment illustrated in FIG. 1, all oil portions from the pressurization operation are recycled as fluidizing oil.

Therefore, if heavy oil is present, an equilibrium condition is immediately obtained, in which the heavy oil is replaced by the fluidizing oil in the same proportion as the oil is replaced by recirculated oil. ″L is extracted from solid matter.

The result is a deliberately dry solid product with a heavy oil content that is substantially the same as the haze oil content of the raw feedstock based on a moisture-free condition. Probably.

FIG. 2 illustrates a portion of the apparatus used in a modified embodiment of the apparatus of FIG. 1, in which the deoiling device is connected directly to a drying evaporator operating at reduced distance. .

Therefore, the deoiling equipment is also under reduced pressure.

The apparatus of FIG. 2 is primarily configured without a valve 126 equipped with a pressure sensor in the line 110 and with a first rotary valve in the line 98 between the active bottom vessel 94 and the deoiling apparatus 100. or the equivalent is provided and further includes a deoiling device 100 and an active bottom vessel 116.
The apparatus differs from that of FIG. 1 in that a second rotary valve or equivalent is provided in the conduit 114 between the two.

The advantage of operating the deoiling equipment under reduced pressure is that less blown steam is required for the deoiling process, and the process can be carried out at lower temperatures, e.g. This is useful when deoiling sensitive materials.

In FIG. 2, light oil-bearing solids discharged from continuous centrifuge 86 via conduit 96 enters active bottom vessel 94. In FIG.

The active bottom of the vessel 94 carries the solids to the outlet through which it enters a conduit 98 and is conveyed by rotary valve 12γ to a deoiler 100.

As illustrated in FIG. 1, deoiling apparatus 100 may be heated externally by steam entering steam jacket 102 via line 104, if desired.

Jacket steam condensate is collected via line 106.

The blown steam generated in the boiler/furnace is passed through the pipe 108
The light oil flows into the deoiling device 100 through the 100, directly contacts the light oil-carrying solid content, and vaporizes the light oil.

The solids, depleted of residual light oil, are discharged from the deoiler 100 via conduit 114 (-) and pumped by rotary valve 128 to an active bottom vessel.

The solid valve, free of fluidized light oil and substantially dry, is ultimately discharged from the active bottom vessel 116 via conduit 118.

However, as discussed in connection with Figure 1, if the aqueous solids initially contained heavy oil, the substantially dry solid output would be It will contain substantially the same proportion of heavy oil as the proportion of heavy oil in the feedstock.

Outflow blown steam and vaporized light oil are transferred to a deoiling device 10
0 via line 110.

Line 110 is connected to an evaporator stage operating under reduced pressure;
The energy of the effluent blown steam and vaporized light oil is thereby effectively recovered by supplying heat to the evaporator stage.

As mentioned above, line 110 is not provided with a valve equipped with a strength detector, so that deoiling device 100 is directly connected to the evaporator stage operating under reduced pressure.

The rotary valves 127 and 128 are substantially gas-tight so that the deoiler 100 is not under reduced pressure even if the active bottom vessels 94 and 116 connected to the deoiler are at substantially atmospheric pressure. It will be placed.

Figure 3 shows a part of the equipment modified from Figure 1, in which the aqueous solids contain heavy oil from the beginning, and the heavy oil is converted into light fluid during the liquid/solid separation process. Extracted by oil.

The light fluidizing oil and extracted heavy oil are then separated and the light components are recycled as fluidizing oil.

The result is a net reduction in the heavy oil content of the substantially dry solid product.

For example, if the aqueous solids normally contain 10 to 15% by weight of heavy oils and fats, such as beef tallow and other animal fats, extraction with light fluidized oils removes such heavy oils and fats. This results in an output containing only about 6-7% fat by weight.

Examples of other aqueous solids containing heavy oils and fats include bark such as fir, fir, pine, and pine bark.

Upon dehydration by the method illustrated in FIG. 3, a valuable wax similar to carnauba wax is recovered from the bark.

Yet another example of aqueous solids containing heavy oils is organic fluids from waste treatment plants.

The materials typically contain about 5% by weight heavy oil in the form of polyethylene and polyvinyl chloride, among other things.

These recovered polymer substances can be recycled and used.

Additionally, removing polyvinyl chloride from the dried sludge means that no corrosive hydrogen chloride is released when the sludge is burned.

In FIG. 3, a mixture of light fluidized oil and heavy oil extracted from the solids by the light oil is guided from a centrifuge 86 through a line 88 to a light oil/heavy oil storage tank 130. .

The light oil supported solid content, which contains less heavy oil compared to the amount of raw heavy oil ore as the raw material based on a moisture-free state, is transferred to conduit 9.
6 from the centrifuge, and then the
Processed according to any of the procedures described above in connection with the figures.

A mixture of light oil and heavy oil is also removed from tank 130 and is pumped via line 132 by a pump 134 provided therein.

Steam is introduced into line 132 via line 136, which is connected to line 132 at the ITJ joint.

A mixture of light and heavy oil and live steam is provided in pipe 132.
and into the stripping evaporator 138.

Indirect steam is introduced from the boiler/furnace via line 140 to the stripping evaporator 138 to provide latent heat for vaporizing the light oil fractions.

Indirect steam condensate is returned from the stripping evaporator 138 via line 146 to the boiler/furnace.

The light oil is vaporized in a stripping evaporator 138.

The dissolved oil vapor mixed with the direct steam introduced via line 136 is discharged from the steam chamber of evaporator 138 via steam duct 148 which is joined to line 68 at the ITJ joint.

As mentioned above, line 68 conveys the steam/light oil vapor mixture from third stage evaporator 76 to second stage evaporator 66 to replenish the second stage evaporator with heat of vaporization.

The light oil and steam mixture in steam conduit 148 is then delivered to line 68, which vapor mixture passes through second stage evaporator 6.
6 is used as an evaporation heat source.

Extracted heavy oil not vaporized in evaporator 138 is recovered from stripping evaporator 138 and passed through line 150.
The water is delivered via a pump 152 provided in the pipe.

The heavy oil is transferred to a heavy oil storage tank 154 via a pipe 150.
will be introduced to.

The heavy oil may be used as a fuel or as having other commercial value by virtue of its composition in raw aqueous solids feedstock or whether the material is useful other than animal feed, human food or food products. can be used.

As mentioned above in the description of FIG. 1, condensate of mixed heated steam is recovered from the second stage generator 66 via line 28;
It is introduced into an oil/water separator 30.

Inside the oil/water separator 30, the mixture is separated into a light oil fraction and partially purified water containing some light oil.

The separated light oil is delivered from the oil/water separator 30 via line 48 to a light oil recirculation tank 156.

Partially purified water is removed from the oil/water separator 30 via line 54 and introduced into a condenser 56 where it is separated into light oil and a clean water product. Separated.

The separated light oil is recovered from the condenser 56 via line 58, which is connected to line 48 at a "T" joint, so that the light oil is ultimately used for light oil recirculation. It is fed to tank 156.

The light oil is transferred to the light oil recirculation tank 15 by a pump 158.
6 and delivered via line 160 to fluidization tank 10.

Since the light oil is separated from the extracted heavy oil before being recycled to the fluidization tank 10, an equilibrium condition is not achieved and as a result, the light fluidization oil is separated from the solids in the centrifuge 86. The net gain is the amount of heavy oil extracted.

Therefore, the heavy oil extraction action substantially reduces the final oil content of the dry solids, thereby reducing the commercial value of the solids as fertilizer, animal feed and human food, and for other uses. This will result in an increase.

It will be appreciated by those skilled in the art that the modified embodiment of FIG. 1 illustrated in FIG. 3 can equally be applied to FIG. will be understood.

In either case, a substantially dry solid product with a low content of heavy oil is obtained.

Figure 4 shows that the water-insoluble solids originally contain heavy oil;
A flow diagram of an apparatus according to another embodiment of the present invention is shown, in which the heavy oil is extracted with a light fluidizing oil and then the light fluidizing oil and the extracted heavy oil are separated. ing.

The water-insoluble solids carried in light fluid oil are made into a slurry with water, and the slurry is introduced into an evaporator.

In the evaporator, at least a portion of the water is converted to steam, thereby directly contacting the aqueous slurry of light oil-supported solids and promoting evaporation of the light oil.

In an embodiment of the process using the apparatus illustrated in FIG. 4, a stream of water-insoluble solids in a water dispersion with heavy oil enters fluidization tank 164 via line 166. do.

Light fluidized oil enters the fluidized tank 164 via line 168.

The liquid mixture in fluidization tank 164 is agitated by an agitator and then withdrawn from the fluidization tank by pump 174.

Pump 174 delivers the mixture via line 176 to the evaporation region of the second stage generator of the entire three-stage evaporator assembly or evaporator bank.

In the evaporator 178, the water and a portion of the light oil are typically about 2 to 10 inches (50.8 to 254 mm) l.
: It is boiled at a pressure between absolute and atmospheric pressure.

The temperature of the partially dehydrated and partially deoiled product of the aqueous solids inlet mixture in the light fluidized oil is approximately 10°C depending on the evaporator pressure.
It is within the range of 0 to 400 below (37.8 to 204.4°C), preferably about 125 to 350 below (51.7 to 176.7°C).

The system includes steam L-'f from a pipe or steam duct 180.
F=heated by the oil vapor mixture.

The steam mixture in steam line 180 is approximately 30 to 40'F (16
, 7-22.2°C), and the subsequent, i.e.
It comes from the evaporation chamber of the third stage evaporator.

The heated steam condensate is collected via line 182.

Conduit 182 is connected to conduit 184 at an rTl joint.

The mixed condensate is passed through line 184 to oil/water separator 1.
86 will be introduced.

Steam formed by partially dewatering an aqueous solids inlet mixture in a light oil.

The light oil vapor mixture is recovered from the vapor chamber of evaporator 178 via line 188 to first stage evaporator 190 where it acts as a heat source for the first stage evaporator. do.

Condensate of the mixed heated steam is recovered from the evaporator 190 via line 192 .

The line 192 connects to line 184 at an ITJ joint and is ultimately delivered to an oil/water separator 186 via line 184.

The partially dehydrated water-in-oil solids mixture is continuously removed from evaporator 178 via line 194 with the aid of pump 196.

The partially dehydrated mixture is delivered via line 194 to the third stage of the evaporator assembly, ie, the evaporation region of first effect can 198 .

In the third stage evaporator, the same process as the second stage continues, except that the pressure is higher.

The pressure in each subsequent evaporator stage is typically somewhat higher than the pressure in the preceding stage, and approaches approximately atmospheric pressure in the third or final stage.

The temperature of the output from the third stage evaporator 198 is between the light fluidized oil and the heavy oil initially included and based on the total slurry (~1% The humidity of the water-impregnated solids slurry is higher than that of the output of the second stage evaporator 178, about 1.00 to 4001' (37.8 to
204.4°C), preferably about 150-350”F (
65, (3 to 176.7'C).

The heating medium is approximately 30 to 50'F (16
, 7 to 27.8°C).

The steam is generated in the boiler/furnace 200 and fed via line 204 to the third stage 198 of the evaporator.

The heated steam condensate is collected via line 206 and returned to boiler/furnace 200.

The substantially anhydrous solids slurry in oil is passed through the third stage evaporator 1.
98 and pumped into line 21 by pump 208.
Sent via 0.

The slurry is fed via line 210 to a continuous centrifuge 212.

The light fluidized oil and the extracted heavy oil are separated from the solids in a centrifuge 212 and introduced from the centrifuge through a line 214 into a light/heavy oil tank 216 .

A mixture of light and heavy oils is withdrawn from tank 216 and pumped through line 218 by a pump 220 provided therein.

Steam is introduced through line 222 into line 218 which is connected to line 222 at an ITJ joint.

A mixture of light and heavy oils and live steam are introduced via line 218 to stripping evaporator 224 .

Indirect steam is introduced from the boiler/furnace via line 226 to the stripping evaporator to provide latent heat for vaporization of the light oil fractions.

Indirect steam condensate is returned from the stripping evaporator 224 via line 228 to the boiler/furnace.

The light oil is vaporized in a stripping evaporator 224.

The vaporized light oil and direct steam introduced via line 222 are delivered from the evaporation chamber of evaporator 224 via steam conduit 230 which is connected to steam conduit 180 at the ITJ joint.

-1- As mentioned above, the steam conduit 180 transports the steam/light oil vapor mixture from the third stage evaporator 198 to the second stage evaporator 17.
8 and replenish the heat of evaporation.

The mixture of light oil vapor and steam in steam conduit 230 is then introduced into line 180, where the mixed vapor is used as an evaporative heat source in second stage evaporator 178 and in 1° stripping evaporator 224. The extracted heavy oil that has not been vaporized is removed from the evaporator and pumped through line 234 by a pump 236 provided therein.

Heavy oil is introduced via line 234 to heavy oil storage tank 238 .

Heavy oil can be utilized for fuel or other purposes as a component of the raw aqueous solids feed.

The water-insoluble solids that have sorbed the remaining light oil are discharged from the centrifuge 212 and introduced via conduit 240 into a pulp mixing tank 242.

Water is introduced to repulping mixing tank 242 via line 244 .

The mixture in the repulped mixing tank 242 consisting of water and solids containing residual light oil is agitated by an agitation device 246 .

The fluid mixture is then withdrawn from the nuclear repulp mixing tank by pump 248.

Pump 248 delivers the aqueous mixture via line 250 to first stage evaporator 190 in a total three stage evaporator assembly.

In the evaporator, a portion of the water is converted to steam, thereby directly contacting the light oil-carrying solids and facilitating the evaporation of the light oil from the solids.

Therefore, in the evaporator 190, the remaining light oil and a portion of the water are typically about 2 to 10 inches (50.8 to 254 mm).
) Boils at 1E force between Hg absolute.

The incoming mixture of water and solids containing residual light oil is delivered to the evaporator 190 at a temperature of approximately 70 to 250 ml, depending on the pressure of the evaporator.
”F (21,1-121.1°C), preferably about 4
Heat to a temperature within the range of 0-175'F (32,2-79.4°C).

As mentioned above, the first stage evaporator 190 is heated by a vapor mixture of steam and vaporized light oil from line 188.

The vapor is at a temperature of about 30-40'F (16.7-22.2C) above the temperature of the solids mixture in the deoiled water.

As previously discussed, heated steam condensate is withdrawn from evaporator 190 via line 192.

The water vapor and light oil vapor formed as a result of evaporating the incoming mixture of water and solids containing residual light oil are
90 is removed via line 252 and introduced into a surface condenser 254.

The interior of the condenser is maintained at a partial vacuum by a vacuum pump 256 connected to the condenser 254 via a vacuum line 258.

Surface condenser 254 is cooled by cooling water entering the condenser via line 260 and exiting the condenser via line 266.

A mixed vapor of steam and vaporized light oil entering condenser 254 via line 252 is condensed in the condenser and a mixed condensate of water and light oil flows from the condenser to line 184. is then introduced into an oil/water separator 186.

The substantially completely deoiled solids slurry in water from the first stage generator 190 is continuously removed via line 268 with the assistance of pump 270 .

Pump 2γ0 pumps the solids slurry in water to settling tank 212 via line 268.

The solid content settles to the bottom of the settling tank 272, and the precipitate is transferred as a wet solid to the line 27 by the action of the pump 276.
4.

Surface water is withdrawn from the top of settling tank 242 via line 244 and pumped by pump 278 to repulping mixing tank 242.

In the tank the water is mixed with solids containing residual light oil and recycled into the system.

In the oil/water separator 186, the water and light oil mixture is separated into light oil and partially purified water containing some light oil.

The light oil phase is removed from the oil/water separator 186 via line 282 and pumped to a light oil recirculation tank 286 by pump 284 and then to fluidization tank 164 via line 168 by pump 288. and thus recycled into the system.

If the process produces a net production of light oil, the net production is recovered from tank 286 and stored for off-system use.

Partially purified water flows from the oil/water separator 186 to a pipe 290.
is introduced into the condenser 292 via the condenser 292.

In the condenser 292, partially purified water containing some light oil is separated into light oil and clean produced water.

The separated light oil is recovered from the condenser 292 via line 294.

Line 294 connects to line 282 at an rTJ joint and ultimately introduces light oil to light oil recirculation tank 286.

Clean output water is withdrawn from the flocculator 292 via line 296.

The clean output water can be used within the system or recovered for storage for use outside the paternity.

Since the light oil is separated from the extracted heavy oil before being recycled to the fluidization tank 164, no equilibrium occurs.

Therefore, in the end, a heavy oil is obtained which is extracted from the water-insoluble solids using a light fluidizing oil in a centrifuge.

Extraction of the heavy oil therefore reduces the heavy oil content of the final solid product.

As a result, the commercial value of solids used in various applications is often increased.

FIG. 5 shows a portion of the device according to a modified embodiment of FIG.

In this apparatus, a solid slurry in a substantially anhydrous light fluidized oil is separated by gravity into a light oil phase and a thick light oil/solid slurry, and the thick light oil/solid slurry is passed through a deoiling apparatus. directly introduced into the

Due to the separation action of gravity, no pressurized equipment, such as a centrifuge, is required to separate the substantially anhydrous solids slurry in the light fluidized oil into its component parts.

In FIG. 5, a substantially anhydrous light fluidized solids-in-oil mixture is recovered from the third stage generator 76 and pumped 8
2 to the settling tank 300 via line 84.

The solids settle to the bottom of settling tank 300 under the action of gravity and are removed from the bottom via line 302 as a concentrated pumpable oil-solids slurry.

A pump 304 disposed in the conduit 302 feeds the thick oil/solid slurry to the deoiling device 100 via the conduit 302 .

The deoiling device 100 can be equipped with a steam jacket +
Heating can also be done externally by 102.

The blown steam generated in the boiler/furnace 77 flows into the pipe line 1.
08 into the deoiling apparatus 100.

In the deoiler, steam is brought into direct contact with the concentrated light oil/solids slurry, causing the light oil to vaporize at a temperature below its boiling point.

Effluent blown steam and vaporized light oil exit the deoiler via line 110 and are directed to an evaporator stage operating under reduced pressure as illustrated in FIG.

Valve 12 comprising a pressure sensor and disposed in line 110
6 functions to maintain the deoiling device 100 at a pressure somewhat lower than atmospheric pressure, that is, at substantially atmospheric pressure.

The solid content that does not contain light oil is transferred from the deoiling device 100 to the conduit 1.
14 and processed according to the procedure described in FIG.

Light fluidized oil from the oil/water separator and condenser is piped into line 48.
is introduced into settling tank 300 via.

The collected light fluidized oil is transferred from the settling tank 300 to the pipe line 3.
06 and is pumped by a pump 308 in the line to a fluidization tank and recirculated into the system.

If the process produces a net oil production, the producing country may also recover settling tanks 300 and store them for off-system use.

In the discussion above with respect to Figure 5, if the aqueous solids initially contain heavy, relatively non-volatile oil, the heavy oil will not be completely extracted by the light fluidizing oil. There probably wasn't.

The thick light oil/solids slurry pumped from settling tank 300 to the deoiler will contain some non-volatile oil fraction that is not removed by the deoiler.

Thus, a substantially dry solid product will contain at least some heavy, non-volatile oils.

Fifth, the deoiling device operates at substantially atmospheric pressure.
It will be appreciated by those skilled in the art that the modified embodiment of FIG. 1 illustrated in the figure is equally applicable when the deoiling device is operated under reduced pressure as illustrated in FIG. It will be understood.

In either case a substantially dry solid product is obtained.

FIG. 6 depicts the apparatus of one embodiment of the present invention, which uses a compact and relatively simple system.

The equipment features a single stage evaporator and a settling tank to separate the substantially anhydrous solids slurry in the cracked fluidized oil by gravity into an oil phase and a thick oil/solids slurry. The point is that

The thick slurry is pumped to a deoiler where it is brought into direct contact with blown steam.

Outflow blown steam from the deoiling device and vaporized light oil are introduced into the single-stage evaporator to replenish the heat of evaporation.

This is a necessary means for effective steam utilization in compact systems.

In FIG. 6, a stream of aqueous solids enters fluidization tank 310 via line 312.

The light fluidized oil is transferred to the fluidized tank 310 via a pipe 314.
flows into.

The fluid mixture in fluidization tank 310 is agitated by stirring means 316 and then removed from the tank by pump 318.

Pump 318 delivers the mixture via line 320 to the evaporation region of single stage evaporator 326 .

In the evaporator 326 substantially all of the water and a portion of the light oil are boiled under reduced pressure.

The temperature of the output from the single stage evaporator 326, i.e., the solids slurry in light oil containing about 1% water by weight based on the total slurry, is about 100% depending on the evaporator pressure.
~400 below (39,8 to 204,4'C), preferably about 150 to 350 below (65,6 to 176,7'
C) is within the range.

The heating medium for evaporator 326 is a mixture of steam and light oil vapor, the temperature of which is approximately 30° below the temperature of the output, i.e., a solids slurry in substantially anhydrous light oil.
The temperature is ~50°C (16.7-27.8°C) higher.

Steam for the evaporator is generated in boiler/furnace 328 and introduced to evaporator 326 via line 330.

A mixture of steam and light oil vapor is also introduced from deoiler 332 to evaporator 326 via line 334 .

The heated steam condensate is collected via line 336 and introduced into an oil/water separator 338.

The steam-light oil vapor mixture formed as a result of substantially complete dewatering of the water-in-light oil solids valve inlet mixture is withdrawn from the vapor chamber of evaporator 326 via line 340 and transferred to a surface condenser. 342.

The inside of the condenser is connected to the surface condenser 34 via a vacuum line 346.
A partial vacuum is maintained by a vacuum pump 344 connected to 2.

A mixture of steam and light oil vapor entering surface condenser 342 is condensed by cooling water that enters the condenser via line 348 and exits the condenser via line 350.

The condensed mixture of hot water and light oil is discharged from the condenser via line 352 to oil/water separator 338 .

In the oil/water separator 338, the mixture of water and light oil is separated into light oil and partially purified water containing some light oil.

The separated light oil is passed from the oil/water separator 338 to the pipe 354.
and is introduced into settling tank 356.

Partially purified water flows from the oil/water separator 338 to the pipe 358.
is introduced into the condenser 360 via.

In the condenser 360, the partially purified water containing some light oil is separated into light oil and clean produced water.

The separated light oil is recovered from the condenser 360 via line 362.

Line 362 is connected to line 354 at an rTl joint so that the light oil is eventually introduced into settling tank 356.

Clean output water is recovered from the condenser 360 via line 364.

If desired, a portion of the clean output water can be recovered from the condenser 360 via line 366 and introduced into the boiler furnace 328 for reuse within the system.

Alternatively, all recovered clean water may be recovered via line 364 and introduced into a storage tank for subsequent use in applications requiring substantially clean water. It is Noh.

The substantially anhydrous light fluidized solids-in-oil mixture is recovered from the single stage evaporator 326 and delivered by pump 368 via line 370 to settling tank 356 .

The solids settle by gravity to the bottom of settling tank 356 from which they are removed via line 372 as a condensed pumpable light oil/solids slurry.

A pump 374 disposed in line 372 delivers the thick oil/slurry through line 372 to deoiling device 332 .

The deoiling device 332 is provided with steam generated in a boiler/furnace 328 and sent to a steam jacket via a line 378 as desired.
It can also be heated externally by steam flowing into the -376.

Jacket steam condensate is collected via line 380.

The line 380 connects to line 366 at the rTJ joint and the condensate is eventually returned to the boiler/furnace.

The blown steam generated in the boiler/furnace 328 is introduced via a line 378 into a line 382 connected to the line 378 by an IT, J joint;
2 to the deoiling device 332.

In the deoiler, the blown steam is brought into direct contact with the concentrated light oil solids slurry, causing the light oil to evaporate at a temperature f above its normal boiling point.

Effluent blown steam and vaporized light oil exit the deoiler via line 334 and are introduced into single stage evaporator 326 .

Heat of vaporization is supplied to the evaporator by the mixed vapor.

Since the evaporator 326 is operated below atmospheric pressure, a valve 383 equipped with a pressure sensor is disposed in the line 334 and serves to maintain the deoiling device 332 at a pressure somewhat less than atmospheric pressure. .

Accordingly, in the illustrated embodiment, the deoiling process is operated at substantially atmospheric pressure.

Alternatively, the effluent blown steam and vaporized light oil may be injected into the fluidization tank 310 or at any point in the system where process efficiency may be compromised by energy capture. It can also be used to preheat aqueous solids/light fluidized oil mixtures.

The use of the mixed vapor to supply heat of vaporization to the single stage evaporator or elsewhere in the system is necessary for efficient steam utilization in the compact apparatus shown in the embodiment of FIG. That's true.

Light fluidized oil-free solids are pumped by gravity from the deoiler 332 via conduit 384 to active bottom vessel 386.

The screw conveyor bottom of vessel 386 directs the solids to an outlet from which the solids, free of light fluidizing oil and substantially anhydrous, are transferred via line 388 to a grinder. 390.

The solids are broken down into powder or particulate form by a grinder 390 and then flowed from the grinder via line 392 to a rotary selection valve 394 .

The fine solids are directed to either line 396 or line 398 by the selection valve.

Conduit 396 leads to a collection or bagging device through which the solids are recovered for use outside the illustrated system.

Line 398 , following the settings of valve 394 as shown, remains at the suction of blower 400 , which delivers fine solids via line 402 to the combustion zone of boiler/furnace 328 .

As mentioned above, the substantially anhydrous light fluidized solids-in-oil mixture in settling tank 356 is separated by gravity into a lower solids phase and a light oil phase floating on the surface.

The solids are recovered from the settling tank as a concentrated eaves oil-solids slurry and introduced into the deoiler 332.

The light fluidized oil on the surface flows from the settling tank 356 to the pipe 314.
A pump 404 provided in the conduit 314
to the fluidization tank 310 and recycled into the system.

If the process produces a net oil output, the net oil output can be recovered from the settling tank 356 and stored for use outside the system.

As discussed above in connection with the discussion of Figure 5, if the aqueous solids initially contained heavy, relatively non-volatile oil, the heavy oil would be completely replaced by the light flowing oil. would not have been extracted.

As a result, the substantially dry solids output of the embodiment of the invention illustrated in FIG. 6 will contain at least some heavy, non-volatile oil.

The flow diagrams illustrated in the drawings generally relate to the dewatering of aqueous solids and the subsequent deoiling, so that the present invention can be used to Those skilled in the art will appreciate that it is useful to dehydrate aqueous solids in a light oil medium followed by deoiling.

Examples of the aqueous solids mentioned above include sewage sludge,
Slaughterhouse effluents and fat refining materials, inorganic salts, pharmaceutical industry outputs, various barks, organic fluids from waste treatment plants,
Various water-based chemicals and their mixtures, animal feed, human food, etc. are listed.

Accordingly, the present invention provides a method and apparatus for recovering clean water and solids from dewatered aqueous solids in a light fluidized oil medium that is immiscible with water.

The feature of this method is that after the solid matter dewatering step, residual light fluidized oil is recovered from the solid matter.

After the dewatering step, the concentrated light oil/solids slurry or light oil-supported solids is brought into direct contact with direct blown steam.

The blowing steam! Well, if it's overheated,
Direct contact with blown steam is essentially equivalent to steam distillation, providing latent heat for vaporization of residual light fluidized oil, and also because light oils are immiscible with water, direct contact with blown steam is essentially equivalent to steam distillation; Light oils boil at temperatures below their normal boiling point.

Light fluidizing oils can be evaporated from the solids at fairly low temperatures by being brought into contact with blown steam at subatmospheric pressures.

As a result of this reduced pressure, light oils are more easily evaporated from the solids, requiring less heat energy, and also permitting the use of light fluidizing oils with higher boiling points. .

Furthermore, in accordance with the present invention, solids can be obtained that are not only dehydrated, but also deoiled to a greater extent than is normally obtainable by mechanical means.

Furthermore, if the aqueous solids feed initially contains heavy and relatively non-volatile oil, embodiments of the present invention remove the heavy oil from the solids output. If the heavy oil is of value, it could be considered for off-site use.

On the other hand, if the heavy oil, which is initially associated with aqueous solids, is not separated from the light flowing oil before recycling the light oil into the system, an equilibrium condition is achieved;
The heavy oil content of the dewatered product will thereby be substantially the same as the content of the water-free feedstock.

While certain embodiments of the invention have been illustrated and described in detail to illustrate the manner in which the principles of the invention may be utilized, the drawings and description are presented by way of example only.
It should be understood that this is not a limitation of the present invention.

[Brief explanation of the drawing]

FIG. 1 depicts an apparatus according to one embodiment of the present invention, in which blown steam is brought into direct contact with the light fluid oil phase solids in a deoiler operating at substantially atmospheric pressure, whereby said light oil is configured to facilitate the removal of. FIG. 2 shows a portion of another embodiment modified from the device of FIG. 1, in which the deoiling device is configured to operate under reduced pressure. FIG. 3 represents a portion of another embodiment modified from the apparatus of FIG. The extracted heavy oil is configured to be separated from the extracted heavy oil. FIG. 4 represents another embodiment of the invention, in which the water-insoluble solids initially contain heavy oil, which is extracted with light fluidizing oil, and then with light fluidizing oil and extracted heavy oil. It is configured to be separated from quality oil. The water-insoluble solids carried in light fluidizing oil are made into a slurry with water, and the slurry is introduced into an evaporator. The evaporator is configured to convert at least a portion of the water into steam, thereby directly contacting the light oil-carrying solids and promoting evaporation of the light oil. FIG. 5 depicts a portion of a modified embodiment of FIG. 1 in which a substantially anhydrous solids slurry in a light fluidized oil is separated by gravity into an oil phase and a thickened light oil/solids slurry;
The thick light oil/solids slurry is configured to be introduced into a deoiler. FIG. 6 depicts yet another embodiment of the present invention, wherein the apparatus uses a single stage evaporator and a substantially anhydrous light fluidized solids-in-oil slurry is separated by gravity from the oil phase and the concentrated oil/solids. The structure is relatively simple and compact in that it is separated from the slurry, thereby eliminating the need for a pressurizing device. 10: Fluidization tank, 12: Aqueous solid content, 16: Stirring device, 22, 66.76: Evaporator (effective can), 30: Oil
Water separator, 36: Condenser, 50: Light oil storage tank, 5
6: Concentrator, 77: Boiler/Furnace, 86: Centrifuge, 94,
116: Active bottom container, 100: Deoiling device, 119: Grinder, 121: Rotary selection valve, 130: Light/heavy oil tank, 138 Varnish dripping evaporator, 154: Heavy oil storage tank, 156: Light Oil recirculation tank, 164:
Fluid tank, 166: Aqueous solids, 178.190,1
98: Evaporator, 186: Oil/water separator, 200: Boiler/furnace, 212: Centrifuge, 216: Light/heavy oil tank,
224 Varnish dripping evaporator, 238: Heavy oil storage tank, 242: Repulping mixing tank, 254: Condenser, 272.300: Sedimentation tank, 286: Light oil recirculation tank, 292: Concentrator, 310: Fluidization tank, 31
2: aqueous solid content, 326: evaporator, 328: boiler/furnace, 332: oil removal equipment, 338: oil/water separator, 342:
Condenser, 356: Sedimentation tank, 360: Condenser, 386
: active bottom, 390: grinder.

Claims (1)

[Scope of Claims] 1. A method for recovering pure water and substantially dry fluidizing oil-free solids from aqueous solids dehydrated in a light fluidizing oil medium. (1) The aqueous solids content is reduced to about 150% to obtain a pumpable mixture that remains fluid even after water is removed.
(2) mixing with a light fluidizing oil of low viscosity, relatively volatile, water-immiscible boiling in the range from 656 °C to about 550 °C (287,8 °C); (2) The oil-containing mixture produced in the step is dehydrated by thermal evaporation, whereby substantially all the water and some of the light fluidized oil is vaporized, leaving a vapor mixture of water and light oil and a substance in the form of an oil slurry. (3) condensing the vapor mixture of water and light oil; (4) separating the condensate produced in the step into a clean water portion and a light oil portion; (5) separating at least some relatively volatile, water-immiscible, light fluidized oil from said substantially anhydrous solid in the form of an oil slurry; directly contacting the solids carrying residual light fluidized oil with blown steam, thereby removing the light oil from the substantially anhydrous solids by thermal evaporation;
The method characterized in that it comprises the following steps. 2. The method according to claim 1, wherein the solid content carrying the residual light fluidized oil is brought into direct contact with blown steam supplied from a source outside the system. 3. In the method according to claim 2, the step (
The above-mentioned method, wherein the outflow blown steam produced in step 6) is used as a part of the heat supply source in the heating evaporation step (2). 4. The method of claim 3, wherein the solids carrying residual light fluidized oil are brought into direct contact with the blown steam at substantially atmospheric pressure. 5. The method according to claim 3, wherein the solid content carrying the residual light fluidized oil is brought into direct contact with the blown steam under reduced pressure.6. The method of claim 1, wherein the thermal evaporation step (2) is carried out at a salinity within the range of about 70"F (21,1C) to below 400"F (204,4C). In the method of item 1, the residual light fluidized solid content is about 70″F (21,1
8. The method of claim 1, wherein the residual light fluidized 9. A method according to claim 1, in which the oil-supported solids are brought into direct contact with superheated blown steam. 10. The method of claim 1, wherein at least a portion of the oil-free solids from step (6) is utilized. 11. The method of claim 10, wherein the light oil fraction is mixed with fresh aqueous solids and thereby recycled as fluidized oil.
The aqueous solid content subjected to the dehydration action initially contains heavy, relatively non-volatile oil, and the heavy oil is purified by the light fluidized oil in the liquid/solid separation step (5). Equilibrium is established by recycling all oil extracted and thereby separated from the solids as fluidizing oil, with heavy oil being added to said aqueous solids in substantially the same proportion as it was extracted. The said method comprising recontaining. 12. In the method according to claim 1, the aqueous solids subjected to dehydration initially contain heavy, relatively non-volatile oil, and the heavy oil is removed in the separation step (5). ), the separated light oil and the extracted heavy oil are separated into a light oil portion and a heavy oil portion, and the light oil portion and the heavy oil portion are separated into a light oil portion and a heavy oil portion. , the light oil fraction separated in step (4) is combined and mixed with fresh aqueous solids and recycled as fluidized oil, whereby the substantially anhydrous solids of step (6) are Said method consisting in reducing the content of heavy oil. 13. The method according to claim 1, wherein the separation step (5) is separation by gravity. 14 4′! The method of claim 1, wherein the light fluidizing oil is a hydrocarbon oil boiling within the range of about 325'F (162,8°C) to 400'P (204,4°C). Certain said methods. 15. In the method according to claim 14,
The above method, wherein the light hydrocarbon fluidizing oil is an isoparaffinic oil. 16 from water-insoluble aqueous solids that initially contain heavy, relatively non-volatile oils and are dehydrated in an oil medium; 7. pure water and substantially free of fluidizing oils; (1) converting the aqueous solids slurry into a low viscosity, relatively (2) dewatering the oil-containing mixture resulting from said step by thermal evaporation, thereby removing substantially all the water and some light fluidizing oil; the fluidized oil is vaporized to produce a vapor mixture of water and light oil and a substantially anhydrous solid in the form of an oil slurry: (3) condensing the vapor mixture of water and light oil: (4) ) separating the condensate produced in said step into a clean water portion and a light oil portion; (5) separating at least some relatively volatile solids from said substantially anhydrous solids in the form of an oil slurry; 1: Squeezing out the light fluidized oil that is immiscible with water and the extracted heavy oil; (6) making the solid content supporting the residual light oil produced in the above step into a slurry with water; (7) the above step; The slurry produced in the process is heated to convert a portion of the water into blown steam, which blown steam directly contacts the remaining light fluidized oil-bearing solids, thereby removing the remaining light fluidized oil-bearing solids. (8) a step of causing the solids in the water/solids slurry produced in the step to be precipitated under the action of gravity; and (9) The method described above comprises the steps of removing upper water from the precipitated solids with reduced heavy oil content. 17 In the method according to claim 16,
The heating evaporation step (2) is carried out at a temperature within the range of about 100°F (37.8°C) to about 400'F (204°4°C), and the heating step (7) is carried out at a temperature of about 70"F. (21,1'C
) to about 250'F (121,1°C). 18 In the method according to claim 16,
The light oil and extracted heavy oil squeezed out by pressurization in step (5) are divided into a light oil portion and a heavy oil portion, and the light oil portion and the light oil separated in step (4) are divided into a light oil portion and a heavy oil portion. Said process in which the oil portion is combined and mixed with fresh aqueous solids, thereby being recycled as fluidized oil. 19 Apparatus for recovering clean water and substantially dry fluidizing oil-free solids from aqueous solids dehydrated in a light fluidizing oil medium, comprising: A tank that receives a divided flow and is equipped with an agitation or mixing mechanism; a tank for supplying light fluidized oil from the light oil storage tank to the tank; an evaporator extending from said tank to a Mrf evaporator and directing a stream of aqueous solids mixed with light fluidized oil from said tank to an evaporation region of said evaporator; a conduit for flowing: a condenser; a conduit extending from said evaporator to said condenser for flowing a mixture of water vapor and light oil vapor formed by heating said aqueous solids and light fluidized oil mixture; ; water separation means; a conduit extending from the condenser to the oil/water separation means and allowing a mixed condensate of water and light oil to flow; separately recovering light oil and clean water from the oil/water separation means; means for; liquid-solid separation means; a conduit extending from said evaporator to said liquid-solid separation means for carrying a stream of substantially anhydrous solids slurry in a light fluidized oil; deoiling means;
and a conduit extending from the liquid/solid separation means to the oil removal means and allowing a flow of solid content carrying residual light fluidized oil to flow. 2042, the apparatus of claim 19, wherein the evaporator is a multi-stage evaporator, the evaporator having a fluid material therein to be heated and evaporated; a vaporous material, wherein the fluid material and the vaporous material are flowed in a countercurrent relationship. 2. The apparatus according to claim 19, wherein the conduit extending from the liquid/solid separation means to the deoiling means is provided with a rotary valve, whereby the liquid/solid separation means and the oil removal means are separated. Said device in which the means can be maintained at separate pressures. 22. The apparatus of claim 19, further comprising a conduit extending from the deoiling means to the evaporator, the effluent blown steam containing light oil vapor acting as part of the evaporative heat source of the evaporator. The device described above is adapted to flow. 23. In the device according to claim 19,
A combustion device is associated with the evaporator and the deoiling means for supplying heat of vaporization to the evaporator and blown steam that is brought into direct contact with the light fluidized oil-bearing solids within the deoiling means. The device is arranged in such a manner that the 24. The device according to claim 22,
Before extending from the deoiling means to the evaporator, the 1e conduit is fitted with a valve with a 1f force detector, so that the deoiling means and the evaporator can be maintained at separate pressures. said device. 25. In the device according to claim 23,
said combustion device associated with said evaporator and said deoiling means comprises a boiler/furnace for producing steam and is provided with conduit means leading from said boiler/furnace to said evaporator and said deoiling means; The apparatus is adapted to flow heated steam and blown steam from the boiler/furnace to the evaporator and the deoiling means, respectively. 3. The apparatus according to claim 25, further comprising means for conveying solids from the deoiling means to the boiler/furnace, and the boiler/furnace is arranged to receive the solids. , and wherein the solids are burned as fuel to provide at least a portion of the heat required by the system. 27 In the device according to claim 19,
The device, wherein the liquid-solid separation means is a continuous centrifuge. 28 In the device according to claim 19,
The device wherein the liquid/solid separation means is a settling tank. 29 An aqueous solid initially containing heavy, relatively non-volatile oil is dehydrated in a light fluidized oil to produce clean water and a substantially dry oil from the aqueous solid. a tank receiving said aqueous solids stream and equipped with an agitation or mixing mechanism;
Light fluidized oil storage tank: means for feeding light fluidized oil to the light oil storage tank or the tank and mix the light fluidized oil and aqueous solids; evaporator for dehydration; a conduit extending to said evaporator and allowing a stream of aqueous solids mixed with light fluidized oil to flow from said tank to the evaporation zone of said dehydration evaporator; condenser: from said dehydration evaporator to said condenser; a conduit for flowing a mixture of steam and light oil vapor formed by heating the aqueous solids and light fluidized oil mixture; an oil/water separation means; a conduit for separating the oil/water from the condenser; Stretching to the means;
A conduit for flowing a mixed condensate of water and light oil; Means for separately recovering light oil and clean water from the oil/water separation means; Liquid/solid separation means; A conduit extending from said liquid-solids separating means to said deoiling means for flowing a stream of substantially anhydrous solids sludge IJ- in a light fluidized oil; a conduit for flowing a stream of solids containing a light fluidizing oil; an oil tank; extending from the liquid/solid separation means to the oil tank and containing a mixture of light fluidizing oil and heavy oil extracted from the solids; a stripping evaporator in which a light fluidizing oil is separated from the oil mixture by thermal evaporation; a conduit extending from the oil tank to the stripping evaporator and flowing the oil mixture; condensing means. extending from the stripping evaporator to the condensing means;
A conduit for flowing light oil vapor formed by heating evaporation of the stripping evaporator; and a conduit extending from the condensing means to the light oil storage tank for flowing the condensed light oil vapor. The device characterized in that. 30. The device according to claim 29,
A combustion device is provided in connection with the dehydration evaporator, the stripping evaporator, and the deoiling means (-), and the solid content carrying residual light fluidized oil is provided in each of the evaporators and the deoiling means. said apparatus for supplying heat of vaporization to the blown steam which is brought into direct contact with the blown steam. an apparatus for recovering clean water and substantially oil-free solids from the aqueous solids by dehydration therein; receiving the aqueous solids flow and comprising an agitation or mixing mechanism; tank; light fluid oil storage tank; means for feeding light fluid oil to the tank, which may be the light oil storage tank, and mixing the light fluid oil and aqueous solids; at least first and second stages; a multistage dehydration evaporator consisting of stages; extending from said tank to the second stage of said multistage dehydration evaporator, and directing a stream of aqueous solids mixed with light fluidizing oil from said tank to said multistage dehydration evaporator; a conduit extending from the second stage steam chamber of the dehydration evaporator to the first stage evaporation region of the dehydration evaporator to flow the aqueous solids and light fluids; A steam duct configured to flow a mixture of water vapor and light oil vapor formed by heating and evaporating a petroleum oil mixture, thereby acting as an evaporation heat source for the first stage; liquid/solid separation means; and the dehydration. a conduit extending from the second stage of the evaporator to said liquid-solid separation means and carrying a flow of a substantially anhydrous water-insoluble solids slurry in a light fluidized oil: an oil tank; said liquid-solid separation means; a conduit extending from the oil tank to flow a mixture of light fluidizing oil and heavy oil extracted from the solids; a stripping evaporator in which the light fluidizing oil is separated from the oil mixture by thermal evaporation; a conduit extending from the oil tank to the stripping evaporator and causing the oil mixture to flow; condensing means; extending from the stripping evaporator to the condensing means and formed by heating evaporation of the stripping evaporator; A conduit for flowing light oil vapor; A conduit extending from the condensing means to the light oil storage tank for flowing the condensed light oil vapor; A repulping mixing tank equipped with a mixing or stirring device; A conduit extending from the separating means to the repulping mixing tank and causing the solid content carrying residual light fluidized oil to flow; Water tank: A conduit extending from the water tank to the repulping mixing tank and inside the repulping mixing tank. A conduit for flowing water such that water mixes with the solid content carrying the residual light fluidized oil; extending from the repulping mixing tank to the first stage of the multi-stage dewatering evaporator and carrying the residual light fluidized oil; a conduit for flowing the aqueous sludge IJ- of the water-insoluble solids carrying fossil oil from the repulping mixing tank to the evaporation zone of the first stage of the dehydration evaporator; a condenser; A conduit extending from the first stage to the condenser for flowing light oil vapor and water vapor formed by heating the aqueous solids slurry carrying residual light fluidized oil;
water separation means; extending from the condenser to the oil/water separation means, causing a mixed condensate of water and light oil to flow from the condenser to the oil/water separation means; The mixed condensate is separated into a clean water product and a light oil; a settling tank; A conduit for flowing an aqueous solids slurry carrying the above from the first stage of the dehydration evaporator to the settling tank, in which the slurry is separated into solids and upper layer water. The device characterized in that it comprises the following. 32. The apparatus according to claim 31, wherein a combustion device is provided in association with the multi-stage dehydration evaporator and the stripping evaporator, and the apparatus supplies heat of vaporization to these evaporators. . 33. The device according to claim 31,
The apparatus, wherein the limb/solid separation means is a continuous centrifuge.