JP2016073961A - Concentration system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a concentration system devised to prevent a decrease in efficiency of heat transfer to an evaporation surface and dirt of heat-radiating heat exchanger while aiming at an improvement in thermal efficiency.SOLUTION: A concentration system comprises a concentrator 2 that evaporates a solvent component to concentrate a treatment target liquid by being contacted to the treatment target liquid with an evaporation face 221a heated by vapor, a capacitor 4 that cools solvent vapor, an evaporator 3 that produces vapor by heating drain, a heat pump 5 having a heat-absorbing heat exchanger 51 and a heat-radiating heat exchanger 52, a first circulation flow passage 61 that is a cooling water passage and couples the capacitor 4 with the heat-absorbing heat exchanger 51, and a second circulation flow passage 2 that is a heated water passage and couples the heat-radiating heat exchanger 52 with the evaporator 3. The evaporator 3 is separately provided with a cylinder side S3 where the heated water passes within a production space S4 that produces vapor from supplied drain to heat the drain within the production space S4 with the heated water passing through the cylinder side S3.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a concentration system having an evaporation surface heated by steam and having a concentration device for concentrating the liquid to be processed by evaporating a solvent component by bringing the liquid to be processed into contact with the evaporation surface.

  Concentration systems that concentrate various liquids such as enzymes, antibiotic extracts, aqueous protein solutions, fermentation liquids, various seasonings, various extracts, oils and fats, vitamins, synthetic chemical products, and drainage are known. Hereinafter, the liquid concentrated in the concentration system may be referred to as a liquid to be processed.

  A concentration system generally includes a concentrator that evaporates the solvent component of the liquid to be processed, a condenser that cools the solvent evaporated from the liquid to be processed, and the like. The concentrator has an evaporation surface that is heated by steam supplied from a boiler or the like, and causes the liquid to be treated to come into contact with the heated evaporation surface to evaporate the solvent component. The liquid to be processed concentrated by evaporation of the solvent component is collected from the concentrator to a tank or the like. Hereinafter, the solvent evaporated from the liquid to be treated may be referred to as solvent vapor, as distinguished from vapor that heats the evaporation surface.

  By the way, various types of concentrators such as a liquid film ascending type, a flowing down type, and a centrifugal type are employed. The liquid film raising type concentrator includes a heating can and an evaporator. The heating can is, for example, a shell and tube heat exchanger (multi-tubular cylindrical heat exchanger), and a large number of heat transfer tubes extending in the vertical direction are provided in the casing. These heat transfer tubes are used to receive the liquid to be processed. In the liquid film raising type concentrator, the heat transfer tube is heated by supplying steam into the casing, and the solvent component is evaporated from the liquid to be treated flowing into the heat transfer tube. That is, the liquid film rising type concentrator evaporates the solvent component from the liquid to be processed by bringing the liquid to be processed into contact with the inner peripheral surface of the heat transfer tube heated by the steam, and the inner peripheral surface of the heat transfer tube. Becomes the evaporation surface. The solvent vapor and the liquid to be treated are blown into the evaporator, and the solvent vapor and the liquid to be treated are separated in the evaporator.

  A flow-down type concentrator has an evaporation plate disposed in a casing at a predetermined angle with respect to the horizontal direction, for example, and heats the evaporation plate by supplying steam to the lower surface side of the evaporation plate. . The solvent component is evaporated from the liquid to be processed by flowing the liquid to be processed onto the upper surface of the heated evaporation plate. That is, the flow down type concentrator evaporates the solvent component from the liquid to be processed by bringing the liquid to be processed into contact with the upper surface of the evaporation plate heated by steam, and the upper surface of the evaporation plate becomes the evaporation surface.

  The centrifugal concentrator has, for example, an evaporation plate that rotates at high speed around a rotation axis extending in the horizontal direction in a casing, and this evaporation plate is formed in a mortar shape, for example. . In the centrifugal concentrator, the evaporation plate is heated by supplying steam to the jacket part on the outer peripheral surface side of the evaporation plate while rotating the evaporation plate, and is processed toward the rotation center side on the inner surface of the evaporation plate. Supply liquid. The supplied liquid to be treated flows on the inner surface of the heated evaporation plate while maintaining the liquid film state toward the outer side due to the centrifugal force generated by the high-speed rotation of the evaporation plate. The solvent component effectively evaporates during the flow. That is, the centrifugal concentrator evaporates the solvent component from the liquid to be processed by bringing the liquid to be processed into contact with the inner surface of the evaporation plate that rotates at high speed while being heated by steam. It becomes an evaporation surface.

  In the concentration system including these concentration devices, the solvent vapor is cooled with cooling water in the condenser. The cooling water whose temperature has been increased by exchanging heat with the solvent vapor is generally cooled by a cooling tower, and the heat transferred from the solvent vapor to the cooling water is released to the atmosphere. In some cases, the cooling water whose temperature has risen is cooled by a refrigerator. In this case, energy is consumed and cooling is performed. Moreover, the drain obtained by condensing the vapor | steam supplied from the boiler etc. may be drained as it is, without collect | recovering heat | fever. As described above, in the conventional concentration system, a large amount of heat is discarded, and there is room for improvement in terms of thermal efficiency.

  Then, the concentration system which aims at the improvement of thermal efficiency by utilizing the heat | fever of solvent vapor | steam and drain is proposed (for example, refer patent document 1 etc.). The concentration system described in Patent Document 1 includes a centrifugal concentration device, a condenser, a heat pump, and a water tank. The heat pump has a heat-absorbing heat exchanger connected to the capacitor and a heat-dissipating heat exchanger connected to the water tank. The concentrator is connected to each of the condenser and the water tank. The solvent evaporated from the liquid to be treated by the concentrator is sent to the condenser and cooled by the cooling water supplied to the condenser from the heat absorption heat exchanger. As a result, the solvent vapor condenses, the sensible heat of the solvent vapor and the latent heat when condensing move to the cooling water, and the temperature of the cooling water rises. The cooling water whose temperature has risen is supplied to an endothermic heat exchanger, and the heat transferred from the solvent vapor is recovered by the endothermic heat exchanger. The drain obtained by condensing in the concentrator is once stored in the water tank, and then supplied from the water tank to the heat dissipation heat exchanger. In the heat dissipation heat exchanger, the temperature of the drain rises using the heat recovered by the heat absorption heat exchanger. Steam is generated by spraying the drain having the increased temperature into the water tank. This vapor is supplied to the evaporation plate of the concentrator and the evaporation surface is heated. Thus, the concentration system described in Patent Document 1 attempts to improve the thermal efficiency by utilizing the heat of the solvent vapor and drain.

JP 2012-206035 A

  However, in the concentration system described in Patent Document 1, droplets (mist) are generated when steam is generated by spraying drain into a water tank, and these droplets enter the concentrator together with the steam. May end up. If the droplets that have entered the concentrator adhere to the evaporation plate, the efficiency of heat transfer to the evaporation surface will be reduced. Moreover, in the concentration system described in Patent Document 1, the drain collected from the concentrator and temporarily stored in the water tank is used as the heat medium of the heat exchanger for heat dissipation. There is a possibility that various contaminants typified by dust (hereinafter abbreviated as dust) may be mixed in the drain from the concentrator or in the water tank, and that drain is used as a heat medium. The heat exchanger for heat dissipation may get dirty.

  In view of the above circumstances, an object of the present invention is to provide a concentrating system that is devised to prevent a decrease in heat transfer efficiency to an evaporation surface and contamination of a heat-dissipating heat exchanger while improving heat efficiency.

The concentrating system of the present invention that solves the above-described object has a concentrating device that has an evaporation surface heated by steam and that concentrates the liquid to be processed by evaporating the solvent component by contacting the liquid to be processed with the evaporation surface.
A condenser for cooling the solvent evaporated from the liquid to be treated;
An evaporator for supplying the drain obtained by condensing the steam in the concentrator, and heating the supplied drain to generate the steam;
A heat pump having a heat exchanger for heat absorption and a heat exchanger for heat dissipation;
A flow path of a first heat medium whose temperature is increased by heat exchange with the solvent in the capacitor, and a first circulation flow path connecting the capacitor and the heat-absorbing heat exchanger;
A flow path of a second heat medium whose temperature has increased in the heat-dissipating heat exchanger, the heat-dissipating heat exchanger comprising a second circulation flow path connecting the heat-dissipating heat exchanger and the evaporator;
The evaporator is provided with a separate passage for the second heat medium to pass through in the generation space for generating the steam from the supplied drain, and the second heat medium passing through the passage passes through the generation space. The drain is heated.

  Here, the evaporator has a storage space for storing drain in addition to the generation space, and the passage route may be separately provided in the generation space and the storage space. Good. The term "separate" here means that the generation space and the storage space are separate systems (independent systems) provided in a partitioned manner. The concentrating device may be of a liquid film rising type, and the evaporation surface may be an inner peripheral surface of a heat transfer tube of the concentrating device. Further, the concentrating device may be a flow-down type, and the evaporation surface may be an upper surface of an evaporation plate that allows the liquid to be processed to flow down. The evaporator may be a shell and tube heat exchanger.

  According to the concentration system of the present invention, in the condenser, heat exchange is performed between the solvent and the first heat medium, and sensible heat of the solvent and latent heat when the solvent condenses move to move the first heat medium. One heating medium rises in temperature. The first heat medium whose temperature has risen flows through the first circulation channel and is supplied to the heat absorption heat exchanger, and the heat transferred from the solvent is recovered by the heat absorption heat exchanger. In the heat dissipation heat exchanger, the temperature of the second heat medium rises due to the heat recovered from the solvent. The second heat medium whose temperature has risen flows through the second circulation channel and is supplied to the evaporator. In the evaporator, the steam is generated by heating the drain by the second heat medium. Thus, the heat efficiency can be improved by generating the vapor using the heat of the solvent and the heat of the drain. Further, since the drain in the evaporator is heated by the second heat medium passing through the passage path to generate the vapor, liquid droplets are hardly generated as in the concentration system described in Patent Document 1, A drop in heat transfer efficiency to the evaporation surface due to the adhesion of the droplets is greatly suppressed. Furthermore, since the passage path that is a part of the flow path of the second heat medium is provided separately in the generation space, the flow path of the second heat medium is connected to the passage path and the first passage. It becomes a closed flow path composed of two circulation flow paths, and dust or the like is hardly mixed into the second heat medium, and the heat-radiating heat exchanger can be prevented from becoming dirty.

  In the concentrating system of the present invention, the concentrating device is such that the evaporation surface rotates, the processing liquid is supplied toward the rotation center side of the evaporation surface, and the supplied processing liquid is Further, the liquid may flow toward the outside in the form of a liquid film by centrifugal force generated by the rotation of the evaporation surface.

  By doing so, the solvent component can be evaporated from the liquid to be processed while the liquid to be processed flows in the form of a liquid film, which is particularly suitable when concentrating the liquid to be processed that is susceptible to thermal denaturation. is there. Note that, in the configuration in which droplets are generated when generating steam as in the concentration system described in Patent Document 1, the droplets adhere to the members constituting the evaporation surface, and the evaporation surface is There is a case where the balance of rotation at the time of rotation is lost. As described above, since the concentration system of the present invention does not generate droplets when generating the vapor, there is no inconvenience even if the evaporation surface rotates.

  Furthermore, the concentration system of the present invention may further include a decompression unit that decompresses a space from the generation space until the vapor is supplied to the evaporation surface.

  By depressurizing the space from the production space to supplying the vapor to the evaporation surface by the decompression means, the boiling point of the drain is lowered in the production space, and the vapor is easily generated at a low temperature.

  The concentration system of the present invention may further include a compressor that compresses the steam generated by the evaporator before being supplied to the evaporation surface.

  By compressing the steam by the compressor, the temperature of the steam can be increased, and the evaporation surface can be heated by a higher temperature steam.

  ADVANTAGE OF THE INVENTION According to this invention, the improvement system which made the device which prevents the fall of the heat transfer efficiency to an evaporation surface and the contamination of the heat exchanger for thermal radiation was achieved, improving a thermal efficiency can be provided.

It is a systematic diagram showing an example of a concentration system corresponding to one embodiment of the present invention. (A) is a figure which expands and shows the concentration apparatus shown in FIG. 1, (b) is a figure which shows typically the internal structure of the evaporator shown in FIG. (A) is a figure showing typically the 1st modification of a concentration device, and (b) is a figure showing typically the 2nd modification of a concentration device. It is a systematic diagram which shows 2nd Embodiment in the concentration system of this invention.

  Embodiments of the present invention will be described below with reference to the drawings. The concentration system according to one embodiment of the present invention treats various liquids such as enzymes, antibiotic extracts, aqueous protein solutions, fermentation broth, various seasonings, various extracts, fats and oils, vitamins, synthetic chemical products, and drainage. The liquid to be treated is concentrated as a liquid.

  FIG. 1 is a system diagram showing an example of a concentration system corresponding to an embodiment of the present invention.

  As shown in FIG. 1, the concentrating system 10 includes a concentrating device 2, an evaporator 3, a condenser 4, a heat pump 5, a liquid tank T1, a condensate tank T2, and a distillate tank T3. In the concentration system 10, the liquid to be processed is supplied from the liquid tank T 1 to the concentration device 2 via the heat exchanger 8, and the supplied liquid to be processed is heated by the vapor supplied from the evaporator 3. The solvent component evaporates. The to-be-processed liquid which the solvent component evaporated and concentrated is collect | recovered by the concentrate tank T2. Hereinafter, the liquid to be treated in which the solvent component is evaporated and concentrated may be referred to as a concentrated liquid. The solvent (solvent vapor) evaporated from the liquid to be treated is cooled and condensed in the condenser 4 by the cooling water supplied from the heat pump 5. The condensed solvent is collected in the distillate tank T3 as a distillate. The drain obtained by condensing in the concentrator 2 is heated by the heated water supplied from the heat pump 5 in the evaporator 3. As a result, steam is generated, and the generated steam is supplied to the concentrating device 2.

  Next, the concentration apparatus 2 will be described in detail with reference to FIG.

  FIG. 2A is an enlarged view of the concentrating device shown in FIG. In FIG. 2A, the internal structure of the concentrating device 2 is shown. In FIG. 2A, the left side of the concentration device 2 may be referred to as the front side, the right side of the concentration device 2 may be referred to as the back side, and the direction connecting the front side and the back side may be referred to as the front-rear direction.

  As shown in FIG. 2A, the concentration device 2 includes a casing 21, a rotating body 22, a liquid to be processed supply pipe 23, a concentrated liquid recovery pipe 24, and a drain recovery pipe 25. The casing 21 has a hollow cylindrical shape, and an exhaust part 211 is provided on the back side portion thereof. The exhaust part 211 is a part for discharging the solvent vapor from the casing 21. In addition, the casing 21 can be divided | segmented into the front-back direction in the connection part 212, and the inspection window 213 for visually confirming an inside is provided in the front side part.

  The rotating body 22 includes an evaporation plate 221, a jacket portion 222, a dam portion 223, a shaft member 224, and a scattering prevention member 225, and is accommodated in the casing 21. The shaft member 224 extends in the front-rear direction and is rotationally driven by a motor M connected to the back side portion thereof. The evaporating plate 221 has a mortar shape that is spread toward the front side by, for example, forming a thin steel plate by squeezing, and is fixed to the shaft member 224 with the shaft member 224 penetrating through the center portion thereof. ing. Thus, when the motor M is driven to rotate the shaft member 224, the evaporation plate 221 also rotates. The jacket portion 222 is provided in a jacket shape on the back side of the evaporation plate 221, and a jacket space S <b> 1 is formed between the evaporation plate 221 and the jacket portion 222. The jacket portion 222 is provided with a steam supply port 2221 and a drain discharge port 2222. The evaporator 3 (see FIG. 1) is connected to the steam supply port 2221, and the steam generated by the evaporator 3 is supplied from the steam supply port 2221 to the jacket space S1. The dam portion 223 is provided in a posture facing the rotation center side of the evaporation plate 221 from the front end of the evaporation plate 221, and a circumferential connection portion 2213 is formed between the dam portion 223 and the evaporation plate 221. ing.

  The liquid supply pipe 23 to be processed has a discharge port 23a at the tip, and discharges the liquid to be processed supplied from the liquid tank T1 (see FIG. 1) from the discharge port 23a. The discharge port 23 a is disposed toward the connection portion of the shaft member 224 with the evaporation plate 221. As will be described later, when the liquid to be processed is discharged from the liquid supply pipe 23 to be processed while the shaft member 224 and the evaporation plate 221 are rotated, the discharged liquid to be processed is caused by the centrifugal force generated by the rotation of the evaporation plate 221. Then, it flows in a liquid film shape on the front surface of the evaporation plate 221 toward the outside. That is, the surface on the front side of the evaporation plate 221 corresponds to an example of the evaporation surface in the present invention, and is hereinafter referred to as an evaporation surface 221a. The evaporation surface 221a corresponds to the inner surface of the evaporation plate 221 formed in a mortar shape. In addition, the scattering prevention member 225 which prevents the to-be-processed liquid discharged from the discharge outlet 23a from scattering is provided in the vicinity of the discharge outlet 23a.

  The concentrated liquid recovery tube 24 has a suction port 24a at the tip, and sucks the concentrated liquid from the suction port 24a. The suction port 24 a is open toward the tangential direction in the connection portion 2213 between the evaporation plate 221 and the dam portion 223. The drain collection pipe 25 has a drain suction port 25a at the tip, and sucks the drain obtained by condensing the steam supplied to the jacket space S1 from the drain suction port 25a. The drain suction port 25a is disposed in the front end region of the jacket space S1. Further, the drain recovery pipe 25 is connected to the drain discharge port 2222, and the drain sucked from the drain suction port 25 a is discharged from the drain discharge port 2222.

  In the concentrating device 2, the motor M is driven to rotate the shaft member 224 and the evaporation plate 221, and steam is supplied from the steam supply port 2221 to the jacket space S <b> 1. In a state where the evaporation plate 221 is heated by this vapor, the processing liquid is discharged from the processing liquid supply pipe 23 toward the rotation center side of the evaporation plate 221. The discharged liquid to be processed flows in a liquid film shape toward the outside on the evaporation surface 221a, and is blocked by the dam portion 223. For example, the solvent component evaporates from the liquid to be processed, and the solvent vapor evaporated from the liquid to be processed is exhausted from the exhaust unit 211 in about 1 second, for example, when the liquid to be processed flows on the evaporation surface 221a. The concentrated liquid blocked by the weir part 223 is sucked into the concentrated liquid recovery pipe 24 opened to the connection part 212. On the other hand, the steam supplied to the jacket space S1 is condensed by heating the evaporation plate 221 to generate drain. This drain is sucked into the drain recovery pipe 25 and discharged from the drain discharge port 2222. A part of the steam supplied to the jacket space S <b> 1 is sucked into the drain recovery pipe 25 without being condensed, and is discharged together with the drain from the drain discharge port 2222.

  Next, the apparatus and apparatus connected to the concentration apparatus 2 will be described. As shown in FIG. 1, a liquid tank T <b> 1 is connected to the liquid supply pipe 23 via a pump P and a heat exchanger 8. The liquid to be processed that is concentrated by the concentration device 2 is stored in the liquid tank T1 to be processed. The heat exchanger 8 is also connected with a condenser 4 and a distillate tank T3. To the heat exchanger 8, the liquid to be processed is supplied from the liquid tank T1 to be processed, and the distilled liquid generated in the condenser 4 is supplied as will be described later. In the heat exchanger 8, heat exchange is performed between the liquid to be treated and the distilled liquid, the temperature of the liquid to be treated rises, and the temperature of the distilled liquid drops. The liquid to be processed whose temperature has risen is supplied to the liquid supply pipe 23 to be processed, and the distillate whose temperature has decreased is collected in the distillate tank T3. Thus, in the concentration system 10 of this embodiment, the temperature of the to-be-processed liquid is raised using the heat | fever of a distillate, and the aspect which accelerates | stimulates the evaporation of a solvent component in the concentration apparatus 2 is employ | adopted.

  A concentrated liquid tank T2 is connected to the concentrated liquid recovery pipe 24 via a pump P. The concentrated liquid is sucked into the concentrated liquid recovery pipe 24 by the action of the pump P and is recovered in the concentrated liquid tank T2.

  The condenser 4 has a solvent vapor receiving port 41, a distillate discharge port 42, a cooling water supply port 43, a cooling water discharge port 44 and an exhaust port 45. The exhaust unit 211 of the concentrator 2 is connected to the solvent vapor receiving port 41 of the condenser 4, and the solvent vapor discharged from the exhaust unit 211 is received by the capacitor 4 from the solvent vapor receiving port 41. The solvent vapor received in the condenser 4 is cooled by the cooling water supplied from the cooling water supply port 43. The cooled solvent vapor is condensed to be a distillate and is discharged from the distillate outlet 42. The distillate discharged from the distillate discharge port 42 is supplied to the heat exchanger 8 by the pump P, and as described above, after exchanging heat with the liquid to be treated in the heat exchanger 8, it is recovered in the distillate tank T3. The Further, a vacuum pump VP1 is connected to the exhaust port 45, and by driving the vacuum pump VP1, solvent vapor is sucked from the concentrating device 2 to the condenser 4, and air in the casing 21 of the concentrating device 2 is discharged. The inside of the casing 21 is evacuated. Thereby, the boiling point of the solvent component in the liquid to be processed is lowered, and the solvent is easily evaporated from the liquid to be processed flowing on the evaporation surface 221a.

  The heat pump 5 includes an endothermic heat exchanger 51, a heat radiating heat exchanger 52, a compressor 53, and an expansion valve 54. In the heat pump 5 of the present embodiment, carbon dioxide is used as the refrigerant, and this refrigerant flows from the heat absorption heat exchanger 51 through the compressor 53 to the heat dissipation heat exchanger 52 and expands from the heat dissipation heat exchanger 52. It flows through the valve 54 to the endothermic heat exchanger 51.

  The condenser 4 and the heat absorption heat exchanger 51 are connected by a first circulation flow path 61 having a pump P. The first circulation flow path 61 allows the cooling water to pass between the condenser 4 and the heat absorption heat exchanger 51. It becomes a circulating flow path. In addition, a cushion tank 72 that temporarily stores cooling water supplied from the condenser 4 to the heat absorption heat exchanger 51 is disposed in the first circulation flow path 61. The cushion tank 72 is provided with an electric heater, a heating steam pipe from a boiler, or a waste heat recovery pipe through which waste water from which waste heat is recovered from a device that generates heat is passed. As will be described later, the cooling water stored in the cushion tank 72 is heated to a predetermined temperature by the electric heater or the like when the driving of the concentration system 10 is started. Instead of the cushion tank 72, an electric heater may be directly wound around the piping of the first circulation channel 61 in a ribbon shape to heat the cooling water flowing through the first circulation channel 61. Moreover, it is good also as an aspect which stores the waste water which collect | recovered waste heat from the apparatus which generate | occur | produces heat in a tank, and heat-exchanges this waste water and cooling water with a heat exchanger.

  As described above, the cooling water whose temperature has risen to about 20 ° C., for example, by recovering heat from the solvent vapor in the condenser 4 is discharged from the cooling water discharge port 44, and the heat absorption heat exchanger via the cushion tank 72. 51. In the heat absorption heat exchanger 51, the heat recovered from the solvent vapor is absorbed from the cooling water and recovered by the refrigerant. The cooling water whose temperature has been lowered to about 15 ° C. by being absorbed in the heat absorption heat exchanger 51 is supplied to the condenser 4 from the cooling water supply port 43 and used for cooling the solvent vapor. That is, the cooling water corresponds to an example of the first heat medium in the present invention. On the other hand, in the heat-absorbing heat exchanger 51, the refrigerant that has recovered heat from the cooling water is compressed by the compressor 53 to become high-pressure and high-temperature gas and flows to the heat-dissipating heat exchanger 52.

  Next, the evaporator 3 and the second circulation passage 62 connecting the evaporator 3 and the heat dissipation heat exchanger 52 will be described. The evaporator 3 has a drain receiving port 31, a steam discharge port 32, a heating water supply port 33, and a heating water discharge port 34. The second circulation flow path 62 is connected from the heat dissipation heat exchanger 52 to the heating water supply port 33 of the evaporator 3, and is connected from the heating water discharge port 34 to the heat dissipation heat exchanger 52 via the pump P. . The second circulation channel 62 is a channel through which the heated water circulates between the heat exchanger 52 for heat dissipation and the evaporator 3. This heated water corresponds to an example of the second heat medium in the present invention. The heating water, for example, of about 80 ° C. supplied to the heat exchanger 52 for heat dissipation rises in temperature to, for example, about 90 ° C. by recovering heat from the refrigerant. To the evaporator 3.

  FIG.2 (b) is a figure which shows typically the internal structure of the evaporator shown in FIG.

  As shown in FIG. 2B, a heating member 35 is disposed inside the evaporator 3. The heating member 35 has a pair of upper and lower tube plates 352 and a plurality of heat transfer tubes 351 extending in the vertical direction. Each of the plurality of heat transfer tubes 351 has an upper end portion inserted into a hole 352a provided in the upper tube plate 352 and a lower end portion inserted into a hole 352a provided in the lower tube plate 352. They are arranged at predetermined intervals in the lateral direction. The drain received from the drain receiving port 31 flows into the tube interior S2 of the plurality of heat transfer tubes 351, and the heated water supply port on the lower side of the heat transfer tube 351 is inserted into the trunk side S3 (the outer surface side of the heat transfer tube 351). Heated water is supplied from 33 and discharged from a heated water discharge port 34 on the upper side of the heat transfer tube 351. As shown by the dots in FIG. 2B, the trunk side S3 is almost filled with heated water. For example, the drain of about 80 ° C. received from the drain receiving port 31 into the evaporator 3 flows into the tube interior S <b> 2 from the lower end of each heat transfer tube 351. The drain that has flowed into the tube interior S2 of the heat transfer tube 351 is heated and evaporated by the heated water flowing through the trunk side S3. As a result, the drain received by the evaporator 3 becomes steam mainly in the tube interior S2 of the heat transfer tube 351. In the present embodiment, the region where the steam is generated and the tube interior S2 of the heat transfer tube 351 and the trunk side S3 are combined (the region partitioned by the pair of upper and lower tube plates 352 in the evaporator 3). This is equivalent to an example of the generation space in FIG. The inside of the evaporator 3 is depressurized by the vacuum pump VP2 so that the boiling point of the drain is about 80 ° C. to 90 ° C. Detailed description of the pressure reduction by the vacuum pump VP2 will be described later. Moreover, trunk | drum side S3 is a path | route through which heated water was separately provided in production | generation space S4, and is equivalent to an example of the passage path | route in this invention. Thus, in the evaporator 3, steam is generated by heating the drain with the heating water flowing through the trunk side S <b> 3. For this reason, unlike the aspect which produces | generates a vapor | steam by spraying drain in a water tank like the concentration system of patent document 1, a vapor | steam can be produced | generated without producing a droplet. Further, the heated water supplied to the heat dissipation heat exchanger 52 circulates in a closed path composed of the second circulation channel 62 and the trunk side S3. For this reason, dirt, such as dust, is hard to mix into heating water, and it can prevent that heat dissipation heat exchanger 52 gets dirty compared with the mode which supplies drain directly to heat dissipation heat exchanger 52. On the other hand, the evaporator 3 that is in contact with the drain can have a heat cleaning tube 351 that can be easily cleaned, and is excellent in maintainability as a system.

  As shown in FIG. 1, the evaporator 3 is connected to the concentrating device 2 by a third circulation channel 63. The third circulation channel 63 connects the vapor discharge port 32 of the evaporator 3 and the vapor supply port 2221 of the concentration device 2, and connects the drain discharge port 2222 of the concentration device 2 and the drain reception port 31 of the evaporator 3. The separator 71, the solenoid valve SV, and the pump P are connected. In addition, a vacuum pump VP2 is connected to the separator 71 via an exhaust passage. When the vacuum pump VP2 is driven, the steam generated in the generation space S4 of the evaporator 3 is discharged from the steam discharge port 32, and the discharged steam is supplied from the steam supply port 2221 into the jacket space S1. Moreover, the area | region of jacket space S1 from the production | generation space S4 of the evaporator 3 is pressure-reduced. Thereby, vapor | steam becomes easy to be produced | generated when the boiling point of drain falls in production | generation space S4. Further, as described above, since the droplets are not easily generated in the evaporator 3, there is a disadvantage that the heat transfer efficiency to the evaporation surface 221 a decreases due to the droplets adhering to the evaporation plate 221, Inconveniences such as adhesion and loss of the balance of rotation when the evaporation plate 221 rotates at high speed are unlikely to occur.

  The drain obtained by condensing steam in the jacket space S1 and the steam not condensed in the jacket space S1 are discharged together from the drain discharge port 2222, and then drained in the separator 71 and the third circulation channel. Air leaking from the outside of 63 is separated. The air separated by the separator 71 is exhausted by the vacuum pump VP2. On the other hand, the drain is received in the evaporator 3 from the drain receiving port 31 by the pump P, and as described above, the drain is heated by the heated water that has recovered the heat of the solvent vapor, thereby generating steam. Thus, the heat efficiency can be improved by generating the steam using the heat of the solvent vapor and the heat of the drain.

  Next, an example of the operating state of the concentration system 10 will be described. First, the vacuum pump VP1 connected to the capacitor 4 is driven, and the air in the casing 21 of the concentrating device 2 is discharged to make the inside of the casing 21 in a vacuum state. Next, the motor M and the pump P of the first circulation flow path 61 are driven to circulate the cooling water through the first circulation flow path 61 and drive a heater or the like disposed in the cushion tank 72 so that the inside of the cushion tank 72 The cooling water stored in is heated. As a result, when the concentration system 10 is activated, the heated cooling water in the cushion tank 72 is supplied to the heat-absorbing heat exchanger 51, so that the time until the system reaches a steady state can be shortened. . Next, the pump P of the second circulation channel 62 is driven to circulate the heating water through the second circulation channel 62 and to drive the heat pump 5. As a result, the heat recovered from the heat absorption heat exchanger 51 is recovered by the heat dissipation heat exchanger 52 into heated water, whereby the drain in the evaporator 3 is heated and the temperature rises to about 90 ° C., for example. Further, the vacuum pump VP2 connected to the separator 71 is driven to depressurize the region of the jacket space S1 from the generation space S4 of the evaporator 3. Thereby, the boiling point of the drain falls in the generation space S4, and the evaporation of the drain starts actively in the generation space S4 of the evaporator 3. The steam generated in the generation space S4 is discharged from the steam discharge port 32, and the discharged steam is supplied from the steam supply port 2221 into the jacket space S1.

  After the steam starts to be supplied into the jacket space S1, the pump P connected to the liquid tank T1 to be processed and the pump P connected to the concentrate tank T2 are driven. Thus, the evaporation plate 221 rotates while being heated by the steam, and the liquid to be processed is discharged from the liquid supply pipe 23 to be processed toward the rotation center of the evaporation plate 221. While the discharged liquid to be processed flows in the form of a liquid film toward the outside on the evaporation surface 221a, the solvent component is evaporated, and the evaporated solvent vapor is exhausted from the exhaust unit 211. The concentrated liquid blocked by the weir part 223 is sucked into the concentrated liquid recovery pipe 24 opened in the connection part 2213 and recovered in the concentrated liquid tank T2.

  Next, a modified example of the concentration apparatus in the concentration system 10 shown in FIGS. 1 and 2A will be described.

  Fig.3 (a) is a figure which shows typically the 1st modification of a concentration apparatus. In the first modification, instead of the centrifugal concentration device 2 shown in FIG. 1 and FIG. 2A, a liquid film raising type concentration device 2 'is adopted.

  As shown in FIG. 3A, the concentrating device 2 ′ has a heating can 26, an evaporator 27, a blow pipe 281 and a conduit 282. The heating can 26 includes a hollow cylindrical casing 261, a steam supply port 2611 and a drain discharge port 2612 provided in the casing 261, and a plurality of second heat transfer tubes 262 accommodated in the casing 261. . Each of the plurality of second heat transfer tubes 262 is arranged in a state extending in the vertical direction. The evaporator 27 has a hollow cylindrical shape in which a lower side portion is formed in an inverted conical shape, an outlet 271 is provided at a lower end portion, and an exhaust portion 272 is provided at an upper end side portion. The blowing pipe 281 connects the upper end side portion of the heating can 26 and the evaporator 27, and the inside of the evaporator 27 is in communication with the second heat transfer pipe 262 through the blowing pipe 281. Further, the blowing pipe 281 is connected to the evaporator 27 toward the tangential direction of the evaporator 27. The conduit 282 connects the outlet 271 of the evaporator 27 and the lower end side portion of the heating can 26, and the second heat transfer tube 262 communicates from the inside of the evaporator 27 via the conduit 282. Yes. The conduit 282 is provided with a concentrate discharge port 2821. A processing liquid supply pipe 273 is connected to the evaporator 27. The upstream portion of the liquid supply pipe 273 to be processed is connected to the liquid tank T1 (see FIG. 1) via a solenoid valve (not shown).

  In the concentration device 2 ′ of the first modified example, when the liquid to be processed is supplied from the liquid supply pipe 273 to the evaporator 27, the liquid to be processed is supplied from the outlet 271 to the second through the conduit 282. It flows into the heat transfer tube 262. In the heating can 26, steam generated by the evaporator 3 (see FIG. 1) is supplied from a steam supply port 2611, and the second heat transfer pipe 262 is heated by this steam, and the inside of the second heat transfer pipe 262 is inside. The solvent component evaporates from the liquid to be processed that is in contact with the surface 262a. That is, the tube inner surface 262a of the second heat transfer tube 262 corresponds to an example of the evaporation surface in the present invention. The concentrated solution obtained by evaporating the solvent component is pulled up by the solvent vapor rising in the second heat transfer tube 262, and the concentrated solution and the solvent vapor flow through the blowing tube 281 and are blown into the evaporator 27. The concentrate and the solvent vapor blown into the evaporator 27 are swirled in the evaporator 27, whereby the concentrate and the solvent vapor are separated. The separated solvent vapor is discharged from the exhaust section 272 and received by the condenser 4 (see FIG. 1). The separated concentrated liquid is mixed with the liquid to be processed supplied from the liquid to be processed supply pipe 273, flows through the conduit 282, and is supplied to the heating can 26. By repeating such an operation and opening the solenoid valve (not shown) when the concentrate reaches a desired concentration, the concentrate is discharged from the concentrate discharge port 2821 and the concentrate tank T2 (see FIG. 1). To collect. On the other hand, the steam supplied into the heating can 26 is condensed by heating the second heat transfer tube 262 to generate a drain, and the steam state is maintained without condensing a part of the steam. These drains and steam are discharged from a drain outlet 2612.

  FIG.3 (b) is a figure which shows typically the 2nd modification of a concentration apparatus. In the second modification, a flow down type concentrator 2 '' is employed.

  As shown in FIG. 3B, the concentrating device 2 ″ includes a casing 29, a heater 291, an evaporation plate 292, a concentrated liquid storage tank 293, and a liquid nozzle 294 to be processed provided in the casing 29. Have. The casing 29 is provided with a steam supply port 295, a drain discharge port 296, a concentrate discharge port 297, and an exhaust unit 298.

  The heater 291 is a member having a rectangular shape in plan view that can flow steam therein, and is provided in a state where an evaporation plate 292 is overlapped on the upper surface of the heater 291. Further, the heater 291 and the evaporation plate 292 are arranged such that the upper surface 292a of the evaporation plate 292 is inclined downward as it goes from right to left in FIG. 3B. Hereinafter, in the heater 291 and the evaporation plate 292, the upper end side may be referred to as an upstream side, and the lower end side may be referred to as a downstream side. A liquid nozzle 294 to be processed is disposed above the upstream end of the evaporation plate 292. In addition, a concentrated liquid storage tank 293 is disposed in the vicinity of the downstream end of the evaporation plate 292. The concentrate storage tank 293 is connected to the concentrate discharge port 297. A steam supply port 295 is connected to an upstream end portion of the heater 291, and a drain discharge port 296 is connected to a downstream end portion of the heater 291.

  In the concentrating device 2 '' of the second modified example, the evaporation plate 292 is heated by supplying the steam taken from the vapor supply port 295 to the heater 291, and the liquid nozzle to be processed is placed on the upper surface 292a of the heated evaporation plate 292. A liquid to be processed is supplied from 294. The supplied liquid to be processed flows down in contact with the upper surface 292a of the heated evaporation plate 292, whereby the solvent component evaporates. That is, the upper surface 292a of the evaporation plate 292 corresponds to an example of the evaporation surface in the present invention. The concentrated liquid obtained by evaporating the solvent component is stored in the concentrated liquid storage tank 293, then discharged from the concentrated liquid discharge port 297, and collected in the concentrated liquid tank T2 (see FIG. 1). Note that a circulation structure may be provided in which the concentrated liquid stored in the concentrated liquid storage tank 293 is sprayed again on the upper surface 292a of the evaporation plate 292. The solvent vapor evaporated from the liquid to be treated is discharged from the exhaust unit 298 and received by the capacitor 4 (see FIG. 1). On the other hand, the steam supplied into the heater 291 is condensed by heating the evaporation plate 292 to generate a drain, and a part of the steam is not condensed and the state of the steam is maintained. These drains and steam are discharged from a drain outlet 296.

  Next, a second embodiment of the concentration system of the present invention will be described. In description of 2nd Embodiment, it demonstrates centering around difference with 1st Embodiment of the concentration system shown in FIG.1 and FIG.2, and in the component of the same name as the name of the component demonstrated so far, The description will be given with the reference numerals used so far, and redundant description may be omitted.

  FIG. 4 is a system diagram showing a second embodiment in the concentration system of the present invention.

  As shown in FIG. 4, in the concentration system 11 of the second embodiment, the compressor 9 is provided between the evaporator 3 and the concentration device 2 in the third circulation flow path 63. In this embodiment, a roots type compressor is adopted as the compressor 9. The inside of the evaporator 3 is depressurized by the compressor 9, and the pressure is adjusted so that, for example, the boiling point of the drain is about 80 ° C. For example, the steam of about 80 ° C. supplied to the compressor 9 from the steam outlet 32 of the evaporator 3 is heated by the compressor 9 to rise in temperature to, for example, about 100 ° C. It is supplied from the supply port 2221 to the jacket space S1. Thereby, the evaporation surface 221a is heated to a higher temperature, and the solvent component can be more efficiently evaporated from the liquid to be processed flowing through the evaporation surface 221a.

  In the present embodiment, an auxiliary steam supply pipe 631 is connected between the compressor 9 and the concentrating device 2 in the third circulation flow path 63. The auxiliary steam supply pipe 631 is provided in place of the cushion tank 72 in the concentration system 10 of the first embodiment, but may be provided together with the cushion tank 72. In this embodiment, when the concentration system 11 starts to be driven, surplus steam or the like generated in other devices in the factory is supplied from the auxiliary steam supply pipe 631 to the third circulation flow path 63, and in particular, the concentration system 11. The time until the system reaches a steady state can be shortened by being actively supplied to the third circulation flow path 63 at the time of activation. The third circulation channel 63 is provided with a check valve in order to prevent the auxiliary steam supplied from the auxiliary steam supply pipe 631 to the third circulation channel 63 from flowing back to the compressor 9 side. The separator 71 is connected to a pump P that is driven and controlled by a level control LC. In the present embodiment, the liquid amount (water amount) circulating through the third circulation flow path 63 increases by the amount of the steam supplied from the auxiliary steam supply pipe 631. For this reason, when the level control LC detects that the drain stored in the separator 71 exceeds a predetermined amount, the pump P is driven to drain the drain. Furthermore, the vacuum pump VP2 connected to the separator 71 can be omitted if the path from the compressor 9 to the separator 71 is maintained at a pressure higher than the atmospheric pressure. Instead of the pump P interlocking with the above, as a configuration for discharging the drain of the separator 71, a simple drain valve may be opened or closed, or an overflow port may be provided in the separator 71. The drain obtained by condensing the steam in the jacket space S1 and the steam maintained without being condensed are discharged from the drain discharge port 2222, and the drain 71 separates the air leaking from the outside by the separator 71. . The separated air is exhausted from the vacuum pump VP2, and the separated drain is supplied to the evaporator 3 by the pump P. In the present embodiment, the distillate discharge pump P1 is connected to the distillate discharge port 42 of the condenser 4, and the distillate discharged from the distillate discharge port 42 is distillate tank T3 by the distillate discharge pump P1. To be recovered.

  According to the concentration systems 10 and 11 described above, it is possible to prevent deterioration of the heat transfer efficiency to the evaporation surface and contamination of the heat dissipation heat exchanger while improving the heat efficiency.

  The present invention is not limited to the above-described embodiments, and various modifications can be made within the scope described in the claims. For example, in the above-described embodiment, liquid is used as the heat medium flowing through the first circulation channel 61 and the second circulation channel 62, but gas may be used as one of the heat media, or A gas such as air may be used as the heat medium flowing in both the first circulation channel 61 and the second circulation channel 62. In this case, the first circulation channel 61 and the second circulation channel 62 are sucked and discharged using a fan or a blower. Further, instead of the cushion tank 72 of the first circulation channel 61 and the cooling water stored in the tank, for example, a container body incorporating an electric heater is provided in the first circulation channel 61 to heat the air in the container body. Then, a mode in which the heat absorption heat exchanger 51 is supplied using a fan or a blower may be employed. Alternatively, if high-temperature air is always obtained from other than the concentration system 10, the high-temperature air is appropriately dust-removed and then supplied to the heat-absorbing heat exchanger 51, cooled by the heat-absorbing heat exchanger 51, and then the condenser 4 After being discharged from the condenser 4, it may be discharged to the atmosphere without being circulated.

  In addition, even if it is the structural requirement contained only in each description of each embodiment and each modification demonstrated above, you may apply the structural requirement to another embodiment and another modification.

DESCRIPTION OF SYMBOLS 10,11 Concentration system 2 Concentrator 21 Casing 221 Evaporating plate 221a Evaporating surface 3 Evaporator 35 Heating member 4 Condenser 5 Heat pump 51 Endothermic heat exchanger 52 Heat dissipating heat exchanger 61 1st circulation path 62 2nd circulation path 63 3rd circulation flow path 9 Compressor S1 Jacket space S2 Pipe inside S3 Body side S4 Generation space VP1, VP2 Vacuum pump

Claims (4)

A concentrating device having an evaporation surface heated by steam and concentrating the treatment liquid by evaporating the solvent component by bringing the treatment liquid into contact with the evaporation surface;
A condenser for cooling the solvent evaporated from the liquid to be treated;
An evaporator for supplying the drain obtained by condensing the steam in the concentrator, and heating the supplied drain to generate the steam;
A heat pump having a heat exchanger for heat absorption and a heat exchanger for heat dissipation;
A flow path of a first heat medium whose temperature is increased by heat exchange with the solvent in the capacitor, and a first circulation flow path connecting the capacitor and the heat-absorbing heat exchanger;
A flow path of a second heat medium whose temperature has increased in the heat-dissipating heat exchanger, the heat-dissipating heat exchanger comprising a second circulation flow path connecting the heat-dissipating heat exchanger and the evaporator;
The evaporator is provided with a separate passage for the second heat medium to pass through in the generation space for generating the steam from the supplied drain, and the second heat medium passing through the passage passes through the generation space. A condensing system characterized by heating the drain of the water.   The concentrating device is such that the evaporation surface rotates, the liquid to be processed is supplied toward the rotation center side of the evaporation surface, and the supplied liquid to be processed is subjected to centrifugal force due to the rotation of the evaporation surface. The concentration system according to claim 1, wherein the concentration system flows in the form of a liquid film toward the outside.   The concentration system according to claim 1, further comprising a decompression unit configured to decompress a space from the generation space until the vapor is supplied to the evaporation surface.   The concentration system according to claim 1, further comprising a compressor that compresses the steam generated by the evaporator before being supplied to the evaporation surface.