JP5495404B2 - Accompanying water concentration system and accompanying water concentration method - Google Patents

Description

  The present invention relates to an accompanying water concentrating system and an accompanying water concentrating method, and more particularly to an accompanying water concentrating system and an accompanying water concentrating system characterized by a circulating system of cooling water required when processing accompanying water generated during coal mining by an evaporation method. Regarding the method.

  In recent years, coal seam methane gas existing in the coal seam has attracted attention as a new natural gas. Since coal seam methane gas is dissolved in the accompanying water contained in the coal seam, the coal water is obtained by pumping up the accompanying water with a screw pump installed in the well and then separating the methane gas from the accompanying water (see Non-Patent Document 1).

  Since the accompanying water after separation of methane gas contains salt, it cannot be used for irrigation or greening or drained into rivers in an untreated state. A process of reducing the volume, concentrating with a reverse osmosis membrane apparatus, storing in a pond and reducing the volume by natural evaporation has been performed.

  However, the method of temporarily storing accompanying water in a reservoir causes a problem that a large reservoir is required as mining of coal bed methane gas continues, making continuous implementation of the coal bed methane gas mining business difficult. In addition, even when concentration is reduced by using a reverse osmosis membrane device, the required power of the reverse osmosis membrane device increases as the salt concentration increases, so a high concentration rate can be obtained in terms of processing costs. It becomes difficult and a similar problem occurs.

  On the other hand, when desalinating seawater, there is a desalination device that supplies the concentrated water of the reverse osmosis membrane treatment to an evaporation method concentration device such as a multi-effect evaporation method or a multistage flash method to reduce the total amount of concentrated water (for example, Patent Document 1). In addition, there is an evaporation method concentration apparatus that can efficiently evaporate and concentrate an aqueous solution at low cost (see, for example, Patent Document 2). Since the required power and required energy of the evaporation method concentrator are less affected by the salt concentration, it is practically possible to obtain a high concentration ratio by using such a desalting apparatus.

JP 2008-100219 A JP 2010-46571 A Shigeki Sakamoto, Yasunobu Ohno, "Oil and Natural Gas Review", Independent Administrative Agency, Japan Oil, Gas and Metals National Corporation, November 2008, Vol.42, No.6, pp.31-49

If the technique of patent document 1 and 2 mentioned above is used, it will become possible to reduce the volume of the accompanying water after methane gas separation.
However, in order to operate the condensing device of the evaporation method concentrating device, for example, it is necessary to take in and supply cooling water from a river or the sea, and to discharge the warm waste water after heat exchange back to the river or the sea. Become. If the cooling water used in the evaporation method concentrator is returned to the river or sea after use, the water temperature is higher than that at the time of water intake or chemicals are added to the components. May have adverse effects.

  In order to suppress these adverse effects, when seawater or river water is used as cooling water and returned to the sea or river after use, environmental regulations regarding water temperature differences and contained substances are often applied. In order to comply with this environmental regulation, equipment for cooling the cooling water after use and equipment for removing chemicals are required, and there is a problem that equipment costs and running costs increase.

  The present invention has been made based on the above-mentioned matters, and its purpose is to reduce the accompanying water generated when obtaining coal-bed methane gas, and to use the accompanying method using an evaporation method concentrating device capable of reducing the amount of concentrated water stored in the reservoir. In the water concentration system, an accompanying water concentration system and an accompanying water concentration method that do not require special equipment for treating cooling water after being used in an evaporation method concentration apparatus are provided.

In order to achieve the above object, the first invention is an accompanying water concentration system including an evaporation method concentrating device for concentrating accompanying water discharged together with coal bed gas from a coal bed, wherein the evaporation method concentrating device is provided. The cooling system for cooling includes an indirect heat exchanger for cooling the evaporation method concentrator, a cooling water supply means for taking cooling water used for cooling from a well or a reservoir, and supplying the cooling water to the indirect heat exchanger, It shall be comprised with the closed circuit which consists of a waste warm water return means which returns waste warm water to the said well or the said pond.

Moreover, 2nd invention is provided with the electric power generation equipment which can utilize waste heat as a heat source of the said evaporation method concentration apparatus, and a waste heat recovery boiler in 1st invention.

Furthermore, the third invention is the first or second invention , further comprising a reverse osmosis membrane type concentrator in the previous stage of the evaporation method concentrator, and the concentrated water from the reverse osmosis membrane type concentrator is concentrated by the evaporation method. It is characterized by being supplied as raw water for the device.

Moreover, 4th invention is a water temperature measurement means which measures the water temperature of the said waste warm water discharged | emitted after cooling with the said indirect heat exchanger in any one of the 1st thru | or 3rd invention, and is measured with the said water temperature measurement means. And a control device for controlling the flow rate of the cooling water supply means and / or the flow rate of the waste warm water return means so that the temperature of the waste hot water becomes equal to or lower than a predetermined value set in advance.

Furthermore, a fifth invention is the fourth invention, wherein, in order to control the flow rate of the cooling water supply means and / or the flow rate of the waste hot water return means, the cooling water supply means according to the output of the control device. And / or using the inverter which outputs motive power to the said waste warm water return means.

Further, a sixth invention is characterized in that, in any one of the first to fifth inventions, a cooling means for cooling the cooling water is provided in a previous stage to be supplied to the evaporation method concentrating device.

Furthermore, a seventh invention is characterized in that, in any one of the first to sixth inventions, a predetermined water depth range is provided in the pond, and a cooling water intake is provided below the water depth range.

In addition, an eighth invention is characterized in that, in any one of the first to seventh inventions, an electric immersion pump is used as a device for taking the cooling water from the well.

Further, a ninth invention is based on the eighth invention, wherein the in-liquid particle detector detects the amount of solid particles in the accompanying water liquid, and the solid particle signal which is an output of the in-liquid particle detector. And an electric immersion pump control device for stopping the electric immersion pump or reducing the suction flow rate.

According to a tenth aspect , in the eighth aspect , the submerged bubble detector that detects the amount of bubbles in the accompanying water liquid, and the bubble signal that is an output of the submerged bubble detector, An electric immersion pump control device that stops the electric immersion pump or reduces the suction flow rate is provided.

Furthermore, the eleventh invention is an accompanying water concentration method by an evaporation method concentrating device for concentrating accompanying water discharged together with coal bed gas from a coal bed, wherein the cooling step for cooling the evaporation method concentrating device is used for cooling. A cooling water supply process for taking cooling water from a well or a reservoir and supplying it to an indirect heat exchanger that cools the evaporative concentration apparatus, and a waste hot water returning process for returning the waste warm water after cooling to the well or the reservoir. Shall have.

  According to the present invention, the volume of the accompanying water can be reduced by the evaporation method, so that the accompanying water can be easily discarded. In addition, when cooling water from an evaporation method concentrator taken from a well or pond is returned to the source, no cooling or chemical treatment is required. Running costs can be reduced.

It is a system configuration figure showing a 1st embodiment of the accompanying water concentration system of the present invention. It is a schematic sectional drawing which shows the intake part of a basin in 1st Embodiment of the accompanying water concentration system of this invention. It is a system block diagram which shows 2nd Embodiment of the accompanying water concentration system of this invention. It is a system block diagram which shows 3rd Embodiment of the accompanying water concentration system of this invention. It is a system block diagram which shows 4th Embodiment of the accompanying water concentration system of this invention. It is a system block diagram which shows 5th Embodiment of the accompanying water concentration system of this invention.

<First Embodiment>
Hereinafter, a first embodiment of an accompanying water concentration system of the present invention will be described with reference to the drawings. FIG. 1 is a system configuration diagram showing a first embodiment of an accompanying water concentration system of the present invention, and FIG. 2 is a schematic cross-sectional view showing a water intake portion of a pond in the first embodiment of the accompanying water concentration system of the present invention. It is.

  In FIG. 1, the accompanying water which became unnecessary after taking water from a coal bed and isolate | separating coal bed gas turns into the raw water 10 for the accompanying water concentration system. The raw water 10 flows into the reverse osmosis membrane type concentrator 12 and is separated into fresh water 14 and concentrated water 16. Although the use of the fresh water 14 is not specified, it can be used as river discharge or irrigation water because the salt concentration is low.

  The concentrated water 16 of the reverse osmosis membrane type concentrator 12 is supplied to an evaporation method concentrator 18. The evaporation method concentrator 18 is supplied with steam 24 from an exhaust heat recovery boiler 26 that converts exhaust heat of the exhaust gas 22 of the power generation facility 20 into steam 24. Indirect heat that is provided in the evaporation method concentrator 18 using the heat energy of the steam 24 and cools the evaporation method concentrator 18 without changing the water quality of the cooling water 36 so as not to affect the groundwater layer. The concentrated water 16 of the reverse osmosis membrane type concentrator 12 is separated into fresh water 30 and highly concentrated water 32 by the exchanger 28.

  Since the highly concentrated water 32 having a high salt concentration cannot be used as river discharge or irrigation water, it is discarded in the pond 34 or supplied to a crystallization apparatus (not shown) for recovering valuable materials. In the present embodiment, since the amount of highly concentrated water 32 discharged from the associated water concentration system is small, the capacity of the basin 34 can be reduced or the crystallization apparatus (not shown) can be downsized.

  The cooling water 36 required by the indirect heat exchanger 28 is taken from the reservoir 34 by the cooling water supply means 38. Note that the cooling water supply unit 38 may be specifically configured by an electric pump or the like, for example.

  In the irrigation pond 34, water is constantly evaporating from the water surface, so the heat of vaporization reduces the water temperature of the pond 34. However, sufficient cooling may not be possible due to the effects of solar radiation and temperature. For this reason, the cooling means 42 for lowering the water temperature of the cooling water 36 is provided on the downstream side of the cooling water supply means 38, and the cooling water 36 whose water temperature has been lowered is supplied to the indirect heat exchanger 28. As the cooling means 42, a method using a heat pump, a method of electronically cooling by a Peltier element, or a part of the cooling water 36 is vaporized by a spraying device or the like, and the remaining cooling water 36 is further cooled by the overheating. There are a method, a method using an absorption refrigerator, a method using cold heat previously stored in ice or the like with surplus power, and any of them may be used. In addition, when the water temperature of the cooling water 36 can be cooled by the pond 34 or the like, the cooling means 42 may not be provided.

  In the indirect heat exchanger 28, the cooling water 36 receives heat energy and becomes waste hot water 44. The waste hot water 44 is circulated to the reservoir 34 by the waste hot water return means 40 to form a closed circuit. Unlike the river and the ocean, the pond 34 has no restriction on the difference between the intake temperature and the disposal temperature, and therefore it is not necessary to provide a special cooling facility.

  When the cooling water 36 is taken from a pond, a temporal fluctuation in water temperature occurs due to the influence of solar radiation and temperature. Even when the cooling water 36 is taken from the well, the time constant is larger than in the case of the pond, but the water temperature fluctuates with time. Although the concentration capacity of the indirect heat exchanger 28 is affected by the water temperature of the cooling water 36, this capacity can be evaluated by the water temperature of the waste hot water 44. The temperature of the waste hot water 44 is measured by the water temperature sensor 46 and given to the control device 50 as a water temperature signal 48. The control device 50 controls the flow rate of the cooling water supply means 38 or the flow rate of the waste hot water return means 40 based on the preset waste hot water temperature target value 52 and the water temperature signal 48, and the cooling capacity of the cooling means 42. Control. At this time, the control device 50 calculates the operating condition that minimizes the sum of the operating cost of the cooling water supply means 38 or the waste hot water return means 40 and the operating cost of the cooling means 42, and realizes the condition. Control of the cooling water supply means 38, the waste warm water return means 40, and the cooling means 42 is performed.

  These flow rates are controlled by outputting operation signals 60 and 64 from the control device 50 to the cooling water supply means inverter 54 or the waste hot water return means inverter 56, respectively, thereby pumping the cooling water supply means 38 and the waste hot water return means 40. The cooling water supply means power 62 and the waste hot water return means power 66, which are power to the electric motor or the like, are controlled. As compared with the case where a valve is used for the flow rate control, the pressure loss that is wasted can be reduced, and the running cost can be further reduced.

  When the cooling means 42 is not provided, only the cooling water supply means 38 or the waste hot water return means 40 is controlled by the control device 50. Even in this case, the flow rate of each means is controlled via the cooling water supply means inverter 54 or the waste hot water return means inverter 56 based on the waste warm water temperature signal 48 and the waste warm water temperature target value 52. The running cost can be reduced.

  FIG. 2 is a schematic view showing the intake portion of the pond in the first embodiment of the accompanying water concentration system of the present invention. In FIG. 2, the same reference numerals as those shown in FIG.

  When the cooling water 36 is taken from the pond 34, the water near the water surface of the pond 34 is affected by solar radiation and temperature, so the water temperature is high. On the other hand, when water evaporates from the water surface of the pond 34, heat is removed as heat of vaporization, so that a physical phenomenon that lowers the water temperature also occurs simultaneously. In addition, when the air temperature around the pond is lower than the water temperature, heat escapes from the water surface to the air, so the water temperature decreases. The density of water varies with the water temperature and is maximum at about 4 ° C. Since there is no stirrer in the pond 34, water having a low water temperature generally moves toward the bottom of the pond 34.

  In the present embodiment, paying attention to the difference in water temperature with respect to the water depth of the pond, a water intake 70 for the cooling water 36 is provided at a location deeper than a predetermined water depth, and the cooling water 36 is taken. Thereby, the cooling water 36 whose water temperature is lower can be obtained.

  According to the first embodiment of the accompanying water concentration system of the present invention described above, the volume of the accompanying water can be reduced by the evaporation method, so that the accompanying water can be easily discarded. In addition, cooling and chemical treatments are not required when returning the cooling water from the evaporative concentration device taken from the pond to the water source, so equipment costs and running costs are reduced compared to returning cooling water to rivers and seawater. Can be reduced.

  In addition, according to the first embodiment of the accompanying water concentration system of the present invention described above, in the well 68 for collecting coal seam gas that is generally located far from rivers and oceans, the cooling water is supplied from the reservoir 34. By taking water 36, it is possible to reduce the cost of pipe laying and the operating cost.

  Moreover, according to 1st Embodiment of the accompanying water concentration system of this invention mentioned above, since the water intake 70 of the pond was provided in the location deeper than the predetermined water depth D, the cooling water 36 with low water temperature can be obtained. Thus, it is possible to reduce the amount of the cooling water 36 necessary for obtaining the cold heat necessary for the indirect heat exchanger 28. As a result, the capacity and power cost of the cooling water supply means 38 or the waste hot water return means 40 can be reduced.

<Second Embodiment>
Hereinafter, a second embodiment of the accompanying water concentration system of the present invention will be described with reference to the drawings. FIG. 3 is a system configuration diagram showing a second embodiment of the accompanying water concentration system of the present invention. In FIG. 3, the same reference numerals as those shown in FIGS. 1 and 2 are the same parts, and detailed description thereof is omitted.

  In FIG. 3, the cooling water supply means 38 in the first embodiment is omitted. When there is no free water surface in the middle of the piping of the cooling water 36, water can be taken in by the waste hot water returning means 40, and the cooling water supply means 38 can be omitted. When the cooling water 36 is taken from the reservoir 34 by the waste warm water returning means 40, the water temperature in the waste hot water returning means 40 is increased, so that the viscosity resistance of the water is lowered and the running cost can be reduced. Specifically, the waste warm water returning means 40 may be constituted by, for example, an electric pump or the like.

<Third Embodiment>
Hereinafter, a third embodiment of the accompanying water concentration system of the present invention will be described with reference to the drawings. FIG. 4 is a system configuration diagram showing a third embodiment of the accompanying water concentration system of the present invention. In FIG. 4, the same reference numerals as those shown in FIGS. 1 to 3 are the same parts, and detailed description thereof is omitted.

  In FIG. 4, the waste warm water returning means 40 in the first embodiment is omitted. When there is no free water surface in the middle of the piping of the cooling water 36, it is possible to take / return water only by the cooling water supply means 38, and the waste warm water returning means 40 can be omitted.

<Fourth embodiment>
Hereinafter, a fourth embodiment of the accompanying water concentration system of the present invention will be described with reference to the drawings. FIG. 5 is a system configuration diagram showing a fourth embodiment of the accompanying water concentration system of the present invention. In FIG. 5, the same reference numerals as those shown in FIGS. 1 to 4 are the same parts, and detailed description thereof is omitted.

  In FIG. 5, the accompanying water which became unnecessary after taking water from a coal bed and isolate | separating coal bed gas turns into the raw water 10 for the accompanying water concentration system. This raw water 10 flows into the reverse osmosis membrane type concentrator 12 and is separated into fresh water 14 and concentrated water 16. Of these, the use of fresh water 14 is not specified, but it can be used as river discharge or irrigation water because of its low salt concentration.

  The concentrated water 16 of the reverse osmosis membrane type concentrator 12 is supplied to an evaporation method concentrator 18. The evaporation method concentrator 18 is supplied with steam 24 from an exhaust heat recovery boiler 26 that converts exhaust heat of the exhaust gas 22 of the power generation facility 20 into steam 24. Using the heat energy of the steam 24, the concentrated water 16 of the reverse osmosis membrane type concentrator 12 is separated into fresh water 30 and highly concentrated water 32 by an indirect heat exchanger 28 provided in the evaporation method concentrator 18.

  Since the highly concentrated water 32 having a high salt concentration cannot be used for discharge or irrigation, it is discarded in the pond 34 or supplied to a crystallizer (not shown) for recovering valuable materials. In the present embodiment, since the amount of highly concentrated water 32 discharged from the associated water concentration system is small, the capacity of the basin 34 can be reduced or the crystallization apparatus (not shown) can be downsized.

  The cooling water 36 required by the indirect heat exchanger 28 is taken from the well 68 by the cooling water supply means 38 or the waste hot water return means 40. Since the well from which the coal seam gas is collected is generally located at a location far from the river or the ocean, the cooling water 36 can be taken from the well 68 to reduce the cost of piping installation and the operation cost.

  Well water taken from the well 68 is generally suitable as the cooling water 36 because the water temperature is generally stable and is not affected by temperature or solar radiation. However, when sufficient cooling cannot be performed, the cooling means 42 is provided on the downstream side of the cooling water supply means 38, and the cooling water 36 with the water temperature lowered is supplied to the indirect heat exchanger 28. As the cooling means 42, a method using a heat pump, a method of electronically cooling with a Peltier element, or a part of the cooling water 36 is vaporized by a spraying device or the like, and the remaining cooling water 36 is further cooled by the heat of vaporization. There are a method, a method using an absorption refrigerator, a method using cold heat previously stored in ice or the like with surplus power, and any of them may be used. If the water temperature of the cooling water 36 can be cooled by the well 68, the cooling means 42 need not be provided.

  In the indirect heat exchanger 28, the cooling water 36 receives heat energy and becomes waste hot water 44. The waste hot water 44 is circulated to the well 68 by the waste hot water returning means 40 to form a closed circuit. Unlike the river and the ocean, the well 68 has no restriction on the difference between the water intake temperature and the disposal temperature, and therefore there is no need to provide a special cooling facility. Further, since the cooling water 36 only changes in temperature in the indirect heat exchanger 28 and does not change in chemical properties, there is no problem even if it is circulated to the well 68 as the waste hot water 44.

  Although FIG. 5 shows a flow of returning the waste hot water 44 after taking water from the well 68 and using it for cooling to the well 68, the waste hot water 44 may be returned to the reservoir 34.

  Although the concentration capacity of the indirect heat exchanger 28 is affected by the water temperature of the cooling water 36, this capacity can be evaluated by the water temperature of the waste hot water 44. The temperature of the waste hot water 44 is measured by the water temperature sensor 46 and given to the control device 50 as a water temperature signal 48. The control device 50 controls the flow rate of the cooling water supply means 38 or the flow rate of the waste hot water return means 40 based on the preset waste hot water temperature target value 52 and the water temperature signal 48, and the cooling capacity of the cooling means 42. Control. At this time, the control device 50 calculates the operating condition that minimizes the sum of the operating cost of the cooling water supply means 38 or the waste hot water return means 40 and the operating cost of the cooling means 42, and realizes the condition. Control of the cooling water supply means 38, the waste warm water return means 40, and the cooling means 42 is performed.

  These flow rates are controlled by outputting operation signals 60 and 64 from the control device 50 to the cooling water supply means inverter 54 or the waste hot water return means inverter 56, respectively, thereby pumping the cooling water supply means 38 and the waste hot water return means 40. The cooling water supply means power 62 and the waste hot water return means power 66, which are power to the electric motor or the like, are controlled.

  When the cooling means 42 is not provided, only the cooling water supply means 38 or the waste hot water return means 40 is controlled by the control device 50. Even in this case, the flow rate of each means is controlled via the cooling water supply means inverter 54 or the waste hot water return means inverter 56 based on the waste warm water temperature signal 48 and the waste warm water temperature target value 52. The running cost can be reduced.

  According to the 4th Embodiment of the accompanying water concentration system of this invention mentioned above, since the volume of accompanying water can be reduced by an evaporation method, disposal of accompanying water becomes easy. In addition, cooling and chemical treatment are not required when returning the cooling water from the evaporative concentration device taken from the well to the water source, so equipment costs and running costs are reduced compared to returning cooling water to rivers and seawater. Can be reduced.

  Further, according to the above-described fourth embodiment of the accompanying water concentration system of the present invention, in the well 68 that collects coal seam gas that is generally located far from rivers and oceans, the cooling water is supplied from the well 68. By taking water 36, it is possible to reduce the cost of pipe laying and the operating cost.

<Fifth embodiment>
Hereinafter, a fifth embodiment of the accompanying water concentration system of the present invention will be described with reference to the drawings. FIG. 6 is a system configuration diagram showing a fifth embodiment of the accompanying water concentration system of the present invention. In FIG. 6, the same reference numerals as those shown in FIGS. 1 to 5 are the same parts, and detailed description thereof is omitted.

  In FIG. 6, an electric immersion pump 72 is used as the cooling water supply means 38 for taking the cooling water 36 from the well 68 of the coal seam in the fourth embodiment described above. When the electric immersion pump 72 is used when pumping the accompanying water contained in the coal seam, the ratio of mechanical loss is reduced as compared with a screw pump conventionally used, and maintenance is facilitated. As a result, the running cost can be reduced.

  On the other hand, when the solid water that clogs the electric submersible pump 72 is included in the accompanying water to be pumped, the performance of the electric submerged pump 72 is deteriorated or the worst case occurs. When the pump breaks down, the electric immersion pump 72 is provided below the well 68, so that time and cost are spent for lifting and maintenance.

  As solid matter that can be included in the accompanying water, for example, coal powder, rock particles, sand particles, and the like can be considered. When these particles become fine particles, they are likely to be mixed between the pump components and induce a failure.

  Therefore, in the present embodiment, the submerged particle detector 74 that detects the amount of solid particulates in the accompanying water liquid, and the electric immersion pump 72 is stopped based on the detection signal of the submerged particle detector 74. And an electric dipping pump control device 82 for reducing the suction flow rate. When the amount of solid particulates in the accompanying water increases, the suction flow rate of the electric dipping pump 72 is reduced or stopped to wait for these solid particulates to sink downward, and then pumped up. By starting the operation, it is possible to suppress the performance degradation of the electric immersion pump 72 and the like.

  In addition, when the accompanying water to be pumped contains a large amount of gas such as methane in the form of bubbles, the electric immersion pump 72 runs idle, resulting in a performance degradation or worst case failure. When the pump breaks down, the electric immersion pump 72 is provided below the well 68, so that time and cost are spent for lifting and maintenance.

  Therefore, in the present embodiment, the submerged bubble detector 78 that detects the amount of bubbles in the liquid of the accompanying water, and the electric immersion pump 72 is stopped based on the detection signal of the submerged bubble detector 78, And an electric immersion pump controller 82 for reducing the suction flow rate.

  According to the fifth embodiment of the accompanying water concentration system of the present invention described above, the same effect as that of the fourth embodiment described above can be obtained, and the electric immersion pump 72 is used instead of the screw pump. Therefore, the rate of mechanical loss is reduced, and maintenance is facilitated. As a result, the running cost can be reduced.

  Further, according to the fifth embodiment of the accompanying water concentration system of the present invention described above, since the in-liquid particle detector 74, the in-liquid bubble detector 78, and the electric immersion pump control device are provided, the accompanying water It is possible to suppress deterioration in performance or failure of the electric immersion pump 72 caused by solid fine particles or bubbles therein at an early stage. As a result, it is possible to reduce the time and cost spent for the lifting operation and maintenance of the electric immersion pump 72.

  In addition, in embodiment of this invention, although the evaporation method concentration apparatus 18 to which the concentrated water 16 concentrated with the reverse osmosis membrane type concentration apparatus 12 was supplied was demonstrated, it is not restricted to this. For example, the evaporation method concentration apparatus 18 to which the accompanying water is directly supplied as the raw water 10 may be used.

DESCRIPTION OF SYMBOLS 10 Raw water 12 Reverse osmosis membrane type concentrator 14 Fresh water 16 Concentrated water 18 Evaporation method concentrator 20 Power generation equipment 22 Exhaust gas 24 Steam 26 Waste heat recovery boiler 28 Indirect heat exchanger 30 Fresh water 32 Highly concentrated water 34 Reservoir 36 Cooling water 38 Cooling water Supply means 40 Waste warm water return means 42 Cooling means 44 Waste hot water 46 Water temperature sensor 48 Water temperature signal 50 Control device 52 Waste warm water temperature target value 54 Cooling water supply means inverter 56 Waste warm water return means inverter 58 Cooling means operation signal 60 Cooling water Supply means operation signal 62 Cooling water supply means power 64 Waste warm water return means operation signal 66 Waste warm water return means power 68 Well 70 Water intake 72 Electric dipping pump 74 Liquid particle detector 76 Particle signal 78 Liquid bubble detector 80 Bubble signal 82 Electric immersion pump controller 84 Electric immersion pump power

Claims (11)

An associated water concentration system comprising an evaporation method concentration device (18) for concentrating associated water discharged together with coal bed gas from a coal bed,
The cooling system for cooling the evaporation method concentrator (18) includes an indirect heat exchanger (28) for cooling the evaporation method concentrator (18), and
Cooling water supply means (38) for taking cooling water (36) used for cooling from the well (68) or the reservoir (34) and supplying the cooling water (36) to the indirect heat exchanger (28);
An associated water concentration system comprising a closed circuit comprising waste warm water returning means (40) for returning the waste warm water (44) after cooling to the well (68) or the reservoir (34). The accompanying water concentration system according to claim 1 ,
An accompanying water concentration system comprising: a power generation facility (20) that can use exhaust heat as a heat source of the evaporation method concentration device (18); and an exhaust heat recovery boiler (26). The accompanying water concentration system according to claim 1 or 2 ,
A reverse osmosis membrane type concentrating device (12) is provided in front of the evaporation method concentrating device (18), and the concentrated water (16) from the reverse osmosis membrane type concentrating device (12) is supplied to the evaporation method concentrating device (18). An accompanying water concentration system, characterized in that it is supplied as raw water (10). In the accompanying water concentration system according to any one of claims 1 to 3 ,
Water temperature measuring means (46) for measuring the water temperature of the waste warm water (44) discharged after cooling by the indirect heat exchanger (28);
The flow rate of the cooling water supply means (38) and / or the waste warm water return means (40) so that the water temperature of the waste warm water (44) measured by the water temperature measuring means (46) is below a predetermined value set in advance. And a control device (50) for controlling the flow rate of the adjoining water. The accompanying water concentration system according to claim 4 ,
In order to control the flow rate of the cooling water supply means (38) and / or the flow rate of the waste warm water return means (40), the cooling water supply means (38) and / or the output of the control device (50) is controlled. Or the accompanying water concentration system using the inverters (54) and (56) which output motive power to the said waste warm water return means (40). The accompanying water concentration system according to any one of claims 1 to 5 ,
A companion water concentration system comprising cooling means (42) for cooling the cooling water (36) in a previous stage to be supplied to the evaporation method concentration device (18). The accompanying water concentration system according to any one of claims 1 to 6 ,
The associated water concentration system, wherein a predetermined water depth range is provided in the pond (34), and a water intake (70) for the cooling water (36) is provided below the water depth range. The accompanying water concentration system according to any one of claims 1 to 7 ,
An accompanying water concentration system using an electric dipping pump (72) as an apparatus for taking the cooling water (36) from the well (68). The accompanying water concentration system according to claim 8 ,
An in-liquid particle detector that detects the amount of solid particles in the accompanying water liquid, and an electric motor that stops or reduces the suction flow rate based on a solid particle signal that is an output of the in-liquid particle detector. An accompanying water concentration system comprising an immersion pump control device. The accompanying water concentration system according to claim 8 ,
A submerged bubble detector for detecting the amount of bubbles in the liquid of the accompanying water, and an electric submerged pump for stopping the electric submersible pump or reducing the suction flow rate based on a bubble signal that is an output of the submerged bubble detector An accompanying water concentration system comprising: a control device. An accompanying water concentration method by an evaporation method concentration device (18) for concentrating accompanying water discharged from a coal bed together with coal bed gas,
The cooling step of cooling the evaporation method concentration device (18)
A cooling water supply step of taking cooling water (36) used for cooling from the well (68) or the reservoir (34) and supplying the cooling water (36) to the indirect heat exchanger (28) for cooling the evaporation method concentrator (18);
A method for concentrating waste water, comprising a step of returning the waste warm water (44) after cooling to the well (68) or the reservoir (34).

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