JP2017075772A - Concentrator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a concentrator improved in heat utilization efficiency for concertation.SOLUTION: A concentrator 1 comprises: an absorber 10 for heating concentration object fluid W flowing through a concentration object fluid channel 11 with the heat of absorption generated when an absorbent Sa absorbs coolant steam Ve; an evaporator 60 for creating the coolant steam Ve by heating coolant liquid Vf with the heat held by coolant heating fluid he flowing through a coolant heating fluid channel 61; a regenerator 70 for increasing the concentration of absorbent Sw by withdrawing coolant steam Vg after heating the absorbent Sw introduced from the absorber 10; a condenser 80 for creating the coolant liquid Vf by cooling and condensing the coolant steam Vg introduced from the regenerator 70; a gas-liquid separator 91 for separating the concentration object fluid Wm heated by the absorber 10 into departure vapor Wv and concentrated liquid Wc; and heating parts 69 and 79 for heating heated fluids Vf and Sw with the heat of the introduced departure vapor Wv, in which the internal pressure of the absorber 10 is higher than that of the regenerator 70.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a concentrating device, and more particularly to a concentrating device that concentrates a fluid to be concentrated using an absorption heat pump.

  As a device for concentrating concentrated liquids such as fruit juice, saline and milk using an absorption heat pump that transfers heat from a low-temperature heat source to a high-temperature heat source, an absorber, a resolver, and a condenser of a heat-increased type 1 absorption heat pump The cooling water that has passed through the condenser is led to a concentrator outside the absorption heat pump to concentrate the liquid to be concentrated, and the vapor generated by the concentration of the liquid to be concentrated is introduced into the evaporator and the desorber of the absorption heat pump ( For example, see Patent Document 1.)

JP 2004-257705 A

  However, in the absorption heat pump concentration apparatus described in Patent Document 1, a driving heat source having a temperature higher than the temperature at which the liquid to be concentrated evaporates must be input to the regenerator, and the temperature of the steam input to the evaporator Is difficult to raise.

  In view of the above problems, an object of the present invention is to provide a concentrating device in which the temperature of steam generated with the concentration of a fluid to be concentrated is increased to improve the heat utilization efficiency for concentration.

  In order to achieve the above object, the concentration apparatus according to the first aspect of the present invention has a concentration target fluid flow path 11 for flowing the concentration target fluid W, for example, as shown in FIG. The absorber 10 that heats the concentration target fluid W that flows through the concentration target fluid flow path 11 with the absorption heat generated when the vapor Ve is absorbed; the refrigerant heating fluid flow path 61; An evaporator 60 that heats the refrigerant liquid Vf with the heat of the flowing refrigerant heating fluid he and generates refrigerant vapor Ve that is supplied directly or indirectly to the absorber 10; The absorption liquid Sw that has absorbed and absorbed the vapor Ve of the refrigerant in the absorber 10 directly or indirectly, and the absorption liquid Sw that flows through the absorption liquid heating fluid flow path 71 is held by the absorption liquid Sw. The refrigerant Vg is heated from the absorbing liquid Sw A regenerator 70 for separating and increasing the concentration of the absorbing liquid Sw; introducing the refrigerant vapor Vg desorbed from the absorbing liquid Sw in the regenerator 70; cooling and condensing the introduced refrigerant vapor Vg; A condenser 80 that generates a refrigerant liquid Vf to be supplied to the refrigerant; a concentration target fluid Wm heated by the absorber 10 is introduced, and a separation steam Wv separated from the concentration target fluid Wm, and a separation steam Wv from the concentration target fluid Wm A gas-liquid separator 91 that separates into the concentrated liquid Wc after being separated; a heating unit 69 and 79 that introduces the separation steam Wv and heats the fluids Vf and Sw to be heated by the heat of the introduced separation steam Wv; Provided: The internal pressure of the absorber 10 is configured to be higher than the internal pressure of the regenerator 70.

  If comprised in this way, while the temperature of the separation | steaming vapor | steam produced | generated by concentration of the concentration object fluid can be made higher than the temperature of a refrigerant | coolant heating fluid and an absorption liquid heating fluid, a to-be-heated fluid is made into a separation | steam vapor | steam. It can heat and can improve the heat utilization efficiency of the concentrating device when concentrating the fluid to be concentrated.

  Further, the concentrating device according to the second aspect of the present invention supplies the separated steam Wv to the heating parts 69 and 79 in the concentrating device 1 according to the first aspect of the present invention as shown in FIG. Heating unit separation steam flow paths 99A and 99B; heating unit separation steam flow rate adjusting devices 99Va and 99Vb for adjusting the flow rate of separation steam Wv flowing through the heating unit separation steam flow paths 99A and 99B; An external detachment steam flow path 99C for supplying Wv; and an external detachment steam flow rate adjusting device 99Vc for adjusting the flow rate of the detachment steam Wv flowing through the external detachment steam flow path 99C.

  If comprised in this way, separation | steaming vapor | steam can be utilized with external vapor | steam utilization equipment, and the heat utilization efficiency of the system containing a concentrating apparatus can be improved.

  Further, the concentrating device according to the third aspect of the present invention is, for example, as shown in FIG. 1, in the concentrating device 1 according to the first aspect of the present invention described above, the detachment flowing through the heating unit separation steam flow paths 99A and 99B. The heating unit detachment steam flow rate adjustment devices 99Va and 99Vb and the external detachment steam flow rate adjustment device 99Vc are set so that the flow rate of the steam Wv and the flow rate of the detachment steam Wv flowing through the external detachment steam flow path 99C become a predetermined ratio.

  If comprised in this way, the improvement of the heat utilization efficiency in a concentrating device and the expansion of steam utilization outside can be distributed appropriately.

  In addition, the concentrating device according to the fourth aspect of the present invention is the same as the concentrating device 1 according to any one of the first to third aspects of the present invention, as shown in FIG. Portions 69 and 79 are provided in at least one of the evaporator 60 and the regenerator 70.

  If comprised in this way, separation | steam vapor | steam can be utilized as a heating source of at least one of an evaporator and a regenerator.

  Further, the concentrating apparatus according to the fifth aspect of the present invention is, for example, as shown in FIG. 1, in the concentrating apparatus 1 according to the fourth aspect of the present invention, the heating units 69 and 79 are provided in the evaporator 60. When arranged in the regenerator 70, it is arranged below the absorbent heating fluid channel 71.

  If comprised in this way, the heat exchange efficiency in a heating part can be made high.

  Further, the concentrating device according to the sixth aspect of the present invention is, for example, as shown in FIG. 2, the concentrating device 1 </ b> A according to the first aspect of the present invention has a low-temperature absorber whose operating pressure is lower than that of the absorber 10. 50, which has a heating target fluid flow channel 51 through which the heating target fluid flows, and directly or indirectly introduces the absorbing liquid Sb that has absorbed the refrigerant vapor Va in the absorber 10, and the introduced absorbing liquid Sc is the refrigerant. The low temperature absorber 50 which heats the heating object fluid which flows through the heating object fluid flow path 51 with the absorption heat generated when the vapor | steam Vc of this was absorbed is provided.

  If comprised in this way, the temperature difference of detachment | desorption vapor | steam and an absorption liquid heating fluid can be enlarged.

  In addition, the concentrating device according to the seventh aspect of the present invention is the same as the concentrating device 2 according to any one of the first to sixth aspects of the present invention, as shown in FIG. A low-temperature concentration tank 191 having a portion 193 therein, the concentration target fluid Wdx being introduced as the fluid to be heated in the heating portion 193, and the concentration target fluid Wdx being heated by the heat of the separated steam Wv A low-temperature concentration tank 191 is provided.

  If comprised in this way, the increase of the processing amount of the concentration object fluid or the raise of the concentration rate of a concentrate can be aimed at.

  Further, the concentrating device according to the eighth aspect of the present invention is separated from the concentration target fluid Wdx in the low-temperature concentrating tank 191 in the concentrating device 2A according to the seventh aspect of the present invention, for example, as shown in FIG. The low-temperature desorption steam Wvx, which is steam, is converted into an evaporator additional heating unit 69 provided in the evaporator 60, a regenerator additional heating unit 79 provided in the regenerator 70, a refrigerant heating fluid channel 61, and an absorption liquid heating fluid flow Introducing portions 69p and 79p leading to at least one of the paths 71 are provided.

  If comprised in this way, the drain of the vapor | steam generate | occur | produced in the low temperature concentration tank can be utilized as a heating source of at least one of an evaporator and a regenerator, and the heat utilization efficiency of the concentrating device when concentrating the concentration target fluid is further increased. Can be improved.

  Further, the concentrating device according to the ninth aspect of the present invention supplies the low-temperature desorption steam Wvx to the introducing portions 69p and 79p in the concentrating device 2A according to the eighth aspect of the present invention, for example, as shown in FIG. Introducing section low temperature desorption steam flow paths 199A, 199B; introducing section low temperature desorption steam flow rate adjusting devices 199Va, 199Vb for adjusting the flow rate of the low temperature desorption steam Wvx flowing through the introduction section low temperature desorption steam flow paths 119A, 119B; An external low-temperature desorption steam flow path 199C for supplying the low-temperature desorption steam flow Wvx to the outside; and an external low-temperature desorption steam flow rate adjustment device 199Vc for adjusting the flow rate of the low-temperature desorption steam Wvx flowing through the external low-temperature desorption steam flow path 199C.

  If comprised in this way, low-temperature separation | steam vapor | steam can be utilized with external vapor | steam utilization equipment, and the heat utilization efficiency of the system containing a concentrator can be improved.

  Further, the concentrating device according to the tenth aspect of the present invention flows through the introduction part low temperature desorption steam flow paths 199A and 199B in the concentrating device 2A according to the ninth aspect of the present invention as shown in FIG. 4, for example. The introduction low-temperature desorption steam flow control devices 199Va and 199Vb and the external low-temperature desorption steam flow rate adjustment so that the flow rate of the low-temperature desorption steam Wvx and the flow rate of the low-temperature desorption steam Wvx flowing through the external low-temperature desorption steam flow path 199C become a predetermined ratio. Set the device 199Vc.

  If comprised in this way, the improvement of the heat utilization efficiency in a concentrating device and the expansion of steam utilization outside can be distributed appropriately.

  Moreover, the concentrating apparatus according to the eleventh aspect of the present invention is the same as the concentrating apparatus 1 according to any one of the first to tenth aspects of the present invention, as shown in FIG. Heat exchange for exchanging heat between the drain Wq of the separated steam Wv after the heated fluids Vf and Sw are heated by the sections 69 and 79 and the refrigerant liquid Vf supplied from the condenser 80 to the evaporator 60. A container 98D is provided.

  If comprised in this way, the heat | fever discharged | emitted can be collect | recovered.

  According to the present invention, it is possible to make the temperature of the separated steam generated by concentration of the fluid to be concentrated higher than the temperatures of the refrigerant heating fluid and the absorption liquid heating fluid, and the heated fluid with the separated steam. It can heat and can improve the heat utilization efficiency of the concentrating device when concentrating the fluid to be concentrated.

It is a typical systematic diagram of the concentration apparatus which concerns on the 1st Embodiment of this invention. It is a typical systematic diagram of the concentration apparatus which concerns on the modification of the 1st Embodiment of this invention. It is a typical systematic diagram of the concentration apparatus which concerns on the 2nd Embodiment of this invention. It is a typical systematic diagram of the concentration apparatus which concerns on the modification of the 2nd Embodiment of this invention.

  Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or similar members are denoted by the same or similar reference numerals, and redundant description is omitted.

  First, with reference to FIG. 1, the concentration apparatus 1 which concerns on the 1st Embodiment of this invention is demonstrated. FIG. 1 is a schematic system diagram of the concentrating device 1. The concentration device 1 is a device that heats and concentrates the non-concentrated liquid Wd as a concentration target fluid in the absorption heat pump unit, and includes an absorption heat pump unit and a concentration tank 91. The absorption heat pump unit constituting the concentrating device 1 is a temperature rising type second-type absorption heat pump. As main components, the absorber 10, the evaporator 60, the regenerator 70, and the condenser 80 are provided. I have.

In the following description, regarding the absorption liquid (also referred to as “solution”) circulated in the absorption heat pump unit, in order to facilitate the distinction on the heat pump cycle, “ Although referred to as “high-concentration solution Sa”, “dilute solution Sw”, etc., when the properties are not questioned, they are collectively referred to as “absorbing liquid S”. Similarly, regarding the refrigerant, in order to easily distinguish on the heat pump cycle, “evaporator refrigerant vapor Ve”, “regenerator refrigerant vapor Vg”, “refrigerant liquid Vf”, etc., depending on the properties and the position on the heat pump cycle. However, when the properties and the like are not asked, they are collectively referred to as “refrigerant V”. In the present embodiment, an LiBr aqueous solution is used as the absorbing liquid S (a mixture of the absorbent and the refrigerant V) circulated in the absorption heat pump unit, and water (H ₂ O) is used as the refrigerant V. Further, as the concentration of the non-concentrated liquid Wd is increased, the concentrated liquid Wc is concentrated, the liquid separated from the non-concentrated liquid Wd is separated steam Wv, and the mixture of the concentrated liquid Wc and the separated steam Wv is mixed liquid. It is called Wm, and these are collectively referred to as the concentration-related substance W.

  The absorber 10 includes therein a heat transfer tube 11 that forms a flow path of the concentration-related substance W and a high concentration solution spray nozzle 12 that sprays the high concentration solution Sa. The heat transfer tube 11 corresponds to a concentration target fluid flow path. The high-concentration solution spray nozzle 12 is disposed above the heat transfer tube 11 so that the sprayed high-concentration solution Sa falls on the heat transfer tube 11. The high temperature absorber 10 sprays the high concentration solution Sa from the high concentration solution spray nozzle 12 and generates heat of absorption when the high concentration solution Sa absorbs the evaporator refrigerant vapor Ve. The concentrated related substance W flowing through the heat transfer tube 11 receives this absorbed heat, and the concentrated related substance W is heated. In the lower part of the absorber 10, a storage part 13 for storing the dilute solution Sw is formed. The dilute solution Sw is an absorbing solution S whose concentration is reduced from the high concentration solution Sa as the high concentration solution Sa sprayed from the high concentration solution spray nozzle 12 absorbs the evaporator refrigerant vapor Ve. The heat transfer tube 11 is disposed above the storage unit 13 so as not to be immersed in the dilute solution Sw. If it does in this way, the absorbed heat which generate | occur | produced will be rapidly transmitted to the concentration related substance W which flows through the inside of the heat exchanger tube 11, and recovery | restoration of absorption capability can be accelerated.

  The evaporator 60 includes an evaporator heat source pipe 61 as a refrigerant heating fluid flow path that constitutes a flow path of the evaporator heat source hot water he as a refrigerant heating fluid, a refrigerant liquid spray nozzle 62 that sprays the refrigerant liquid Vf, and separation steam. It has an evaporator heating tube 69 constituting the Wv flow path. The evaporator heating pipe 69 is disposed below the evaporator heat source pipe 61. The refrigerant liquid spray nozzle 62 is disposed above the evaporator heat source pipe 61 so that the sprayed refrigerant liquid Vf falls on the evaporator heat source pipe 61 and the evaporator heating pipe 69. One end of a refrigerant liquid pipe 88 that allows the refrigerant liquid Vf to flow therein is connected to the evaporator 60. One end of a low-temperature refrigerant liquid pipe 65 that guides the refrigerant liquid Vf stored in the lower part of the evaporator 60 to the refrigerant liquid spray nozzle 62 is connected to the lower part (typically the bottom part) of the evaporator 60. The other end of the low-temperature refrigerant liquid pipe 65 is connected to the refrigerant liquid spray nozzle 62. The low-temperature refrigerant liquid pipe 65 is provided with a low-temperature refrigerant liquid pump 66 that pumps the refrigerant liquid Vf flowing inside. In the evaporator 60, the refrigerant liquid Vf is sprayed from the refrigerant liquid spraying nozzle 62, and the sprayed refrigerant liquid Vf flows in the evaporator heat source pipe 61 and flows in the evaporator heating pipe 69. The evaporator refrigerant vapor Ve is generated by evaporating with the heat of the vapor Wv. That is, in the present embodiment, the evaporator heating pipe 69 corresponds to a heating unit that heats the refrigerant liquid Vf with the heat of the introduced separation steam Wv, and the refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 62 is heated by the evaporator. This corresponds to the heated fluid heated by the tube 69.

  The absorber 10 and the evaporator 60 are in communication with each other. The absorber 10 and the evaporator 60 communicate with each other so that the evaporator refrigerant vapor Ve generated in the evaporator 60 can be supplied to the absorber 10. The absorber 10 and the evaporator 60 typically communicate with each other above the high concentration solution spray nozzle 12 and above the refrigerant liquid spray nozzle 62.

  The regenerator 70 includes a regenerator heat source pipe 71 as an absorption liquid heating fluid flow path that constitutes a flow path of the regenerator heat source hot water hg as an absorption liquid heating fluid, a dilute solution spray nozzle 72 that sprays the dilute solution Sw, And a regenerator heating pipe 79 constituting the flow path of the separation steam Wv. The regenerator heating tube 79 is disposed below the regenerator heat source tube 71. The regenerator heat source hot water hg flowing through the regenerator heat source pipe 71 may be the same hot water as the evaporator heat source hot water he flowing through the evaporator heat source pipe 61. In this case, after flowing through the evaporator heat source pipe 61, the regenerator It is good to be connected by piping (not shown) so that it may flow through the heat source pipe 71. Different heat source media may flow through the evaporator heat source pipe 61 and the regenerator heat source pipe 71. The dilute solution spray nozzle 72 is disposed above the regenerator heat source tube 71 so that the sprayed dilute solution Sw falls on the regenerator heat source tube 71 and the regenerator heat tube 79. In the regenerator 70, the sprayed dilute solution Sw is heated by the regenerator heat source hot water hg and the separated steam Wv, whereby the refrigerant V evaporates from the dilute solution Sw to generate a high concentration solution Sa having an increased concentration. . That is, in this embodiment, the regenerator heating tube 79 corresponds to a heating unit that heats the dilute solution Sw with the heat of the introduced separation steam Wv, and the dilute solution Sw sprayed from the dilute solution spray nozzle 72 is heated by the regenerator. This corresponds to the heated fluid heated by the pipe 79. The regenerator 70 is configured such that the generated high concentration solution Sa is stored in the lower part.

  The condenser 80 has a cooling water pipe 81 that forms a cooling medium flow path. The cooling water c as a cooling medium flows through the cooling water pipe 81. The condenser 80 is configured to introduce the regenerator refrigerant vapor Vg, which is the vapor of the refrigerant V generated in the regenerator 70, and to cool and condense it with the cooling water c. The cooling water pipe 81 is disposed so that the regenerator refrigerant vapor Vg is not immersed in the condensed refrigerant liquid Vf so that the regenerator refrigerant vapor Vg can be directly cooled. One end of a refrigerant liquid pipe 88 that sends the condensed refrigerant liquid Vf toward the evaporator 60 is connected to the condenser 80. The other end of the refrigerant liquid pipe 88 is connected to the evaporator 60. The refrigerant liquid pipe 88 is provided with a condensing refrigerant pump 89 for pumping the refrigerant liquid Vf.

  The regenerator 70 and the condenser 80 are in communication with each other. By connecting the regenerator 70 and the condenser 80, the regenerator refrigerant vapor Vg generated in the regenerator 70 can be supplied to the condenser 80. The regenerator 70 and the condenser 80 communicate with each other in the upper gas phase portion. In the present embodiment, the regenerator 70 and the condenser 80 are provided below the absorber 10 and the evaporator 60.

  The portion of the regenerator 70 where the high concentration solution Sa is stored and the high concentration solution spray nozzle 12 of the absorber 10 are connected by a high concentration solution tube 75. The high concentration solution pipe 75 is provided with a high concentration solution pump 76 that pumps the high concentration solution Sa in the regenerator 70 to the high concentration solution spray nozzle 12. The storage unit 13 of the high-temperature absorber 10 and the dilute solution spray nozzle 72 of the regenerator 70 are connected by the absorber outflow solution pipe 15. A high temperature heat exchanger 18 is disposed in the absorber outflow solution tube 15 and the high concentration solution tube 75. The high temperature heat exchanger 18 is a device that exchanges heat between the dilute solution Sw flowing through the absorber outflow solution tube 15 and the high concentration solution Sa flowing through the high concentration solution tube 75.

  The concentration tank 91 is a device that introduces the mixed liquid Wm generated by heating the unconcentrated liquid Wd in the heat transfer tube 11 of the absorber 10 and separates it into the concentrated liquid Wc and the separated vapor Wv. It corresponds to. The lower part of the side surface of the concentration tank 91 and one end of the heat transfer tube 11 of the absorber 10 are connected by an unconcentrated liquid tube 92 that guides the unconcentrated liquid Wd to the heat transfer tube 11. The side surface of the concentrating tank 91 whose inside is a gas phase portion and the other end of the heat transfer tube 11 are connected by a mixed liquid pipe 94 that guides the mixed liquid Wm to the concentrating tank 91. The non-concentrated liquid pipe 92 is connected to a non-concentrated liquid supply pipe 95 for introducing the non-concentrated liquid Wd from outside the system. A supply pump 96 that pumps the non-concentrated liquid Wd toward the concentration tank 91 is disposed in the non-concentrated liquid supply pipe 95. The concentration tank 91 is connected to an upper part (typically the top) of a separation steam pipe 99 that flows out the separation steam Wv, and a concentration liquid pipe 97 that flows out the concentrate Wc is below (typically). Connected to the bottom). In addition, the connection part of the non-concentrated liquid pipe 92 with respect to the concentration tank 91 may be the lower part (typically the lowermost part) of the concentration tank 91, similarly to the concentrated liquid pipe 97. The non-concentrated liquid supply pipe 95 and the concentrated liquid pipe 97 have a concentrated liquid heat exchanger that exchanges heat between the non-concentrated liquid Wd flowing through the non-concentrated liquid supply pipe 95 and the concentrated liquid Wc flowing through the concentrated liquid pipe 97. 98S is disposed.

  The other end of the separation steam pipe 99 having one end connected to the concentrating tank 91 is branched into an evaporator separation steam pipe 99A, a regenerator separation steam pipe 99B, and an external separation steam pipe 99C. A part of the evaporator separation steam pipe 99 </ b> A passes through the inside of the evaporator 60 as an evaporator heating pipe 69. A part of the regenerator leaving steam pipe 99 </ b> B passes through the inside of the regenerator 70 as a regenerator heating pipe 79. The evaporator detachment steam pipe 99A on the upstream side of the evaporator heating pipe 69 is a flow path for supplying the detachment steam Wv to the evaporator heating pipe 69 in the system (in the concentrator 1). It corresponds to. An evaporator detachment steam valve 99Va for adjusting the flow rate of the detachment steam Wv flowing inside is provided in the evaporator detachment steam pipe 99A on the upstream side of the evaporator heating pipe 69. The regenerator separation steam pipe 99B on the upstream side of the regenerator heating pipe 79 is a flow path for supplying the separation steam Wv to the regenerator heating pipe 79 in the system (in the concentrator 1). It corresponds to. A regenerator detachment steam valve 99Vb for adjusting the flow rate of the detachment steam Wv flowing inside is provided in the regenerator detachment steam pipe 99B on the upstream side of the regenerator heating pipe 79. The evaporator detachment steam valve 99Va and the regenerator detachment steam valve 99Vb correspond to a heating unit detachment steam flow rate control device. The evaporator detachment steam pipe 99A and the regenerator detachment steam pipe 99B are connected at a junction 99j on the downstream side of the evaporator heating pipe 69 and on the downstream side of the regenerator heating pipe 79, respectively. It becomes. The separation steam pipe 99 and the refrigerant liquid pipe 88 on the downstream side of the junction 99j are separated so that heat is exchanged between the separation drain Wq flowing through the separation steam pipe 99 and the refrigerant liquid Vf flowing through the refrigerant liquid pipe 88. A drain heat exchanger 98D is provided. The leaving drain Wq is a drain of the leaving steam Wv. The external detachment steam pipe 99C is a flow path for supplying the detachment steam Wv outside the system (outside the concentrator 1), and corresponds to an external detachment steam flow path. The external separation steam pipe 99C is connected to a device (not shown) that uses the separation steam Wv outside the system. The external detachment steam pipe 99C is provided with an external detachment steam valve 99Vc for adjusting the flow rate of the detachment steam Wv flowing inside. The external detachment steam valve 99Vc corresponds to an external detachment steam flow control device. The evaporator detachment steam valve 99Va, the regenerator detachment steam valve 99Vb, and the external detachment steam valve 99Vc typically have a target ratio between the flow rate of the evacuation steam Wv used in the system and the flow rate used outside the system. The opening degree is adjusted so as to obtain the usage flow rate ratio.

  With continued reference to FIG. 1, the operation of the concentration apparatus 1 will be described. First, the cycle on the refrigerant side of the absorption heat pump unit will be described. The condenser 80 receives the regenerator refrigerant vapor Vg generated in the regenerator 70, cools the regenerator refrigerant vapor Vg with the cooling water c flowing through the cooling water pipe 81, and condenses it into a refrigerant liquid Vf. The condensed refrigerant liquid Vf is pumped toward the evaporator 60 by the condensed refrigerant pump 89. The refrigerant liquid Vf pressure-fed by the condensing refrigerant pump 89 flows through the refrigerant liquid pipe 88 and is introduced into the evaporator 60 after the temperature rises in the separation drain heat exchanger 98D. The refrigerant liquid Vf introduced into the evaporator 60 is pumped by the low-temperature refrigerant liquid pump 66 to the refrigerant liquid spray nozzle 62 and sprayed from the refrigerant liquid spray nozzle 62 toward the evaporator heat source pipe 61. The refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 62 is heated and evaporated by the evaporator heat source hot water he that flows in the evaporator heat source pipe 61 and the separated steam Wv that flows in the evaporator heating pipe 69, and becomes the evaporator refrigerant vapor Ve. Become. The evaporator refrigerant vapor Ve generated in the evaporator 60 moves to the absorber 10 communicating with the evaporator 60. Thus, in this Embodiment, the vapor | steam of the refrigerant | coolant in the evaporator 60 is directly introduce | transduced into the absorber 10 (without passing through another apparatus).

  Next, the cycle on the absorption liquid side of the absorption heat pump unit will be described. In the absorber 10, the high concentration solution Sa is sprayed from the high concentration solution spray nozzle 12, and the sprayed high concentration solution Sa absorbs the evaporator refrigerant vapor Ve that has moved from the evaporator 60. The high-concentration solution Sa that has absorbed the evaporator refrigerant vapor Ve is reduced in concentration to become a dilute solution Sw. In the absorber 10, heat of absorption is generated when the high-concentration solution Sa absorbs the evaporator refrigerant vapor Ve. Due to this absorbed heat, the concentration-related substance W flowing through the heat transfer tube 11 is heated. Here, the operation around the concentration tank 91 for taking out the concentrate Wc will be described.

  The non-concentrated liquid Wd is introduced into the system of the concentration tank 91 from the outside through the non-concentrated liquid supply pipe 95. The non-concentrated liquid Wd is pumped through the non-concentrated liquid supply pipe 95 by the supply pump 96 and is introduced into the non-concentrated liquid pipe 92 after heat is exchanged with the concentrated liquid Wc by the concentrated liquid heat exchanger 98S and is heated. Is done. The non-concentrated liquid Wd introduced into the non-concentrated liquid pipe 92 merges with the concentration-related substance W flowing from the lower side of the concentration tank 91 and flows into the heat transfer pipe 11 of the absorber 10 by the action of the bubble pump. Here, when it is difficult for the non-concentrated liquid Wd to flow into the heat transfer tube 11 due to high viscosity or the like, a pump for pushing the non-concentrated liquid Wd into the heat transfer tube 11 may be provided. The unconcentrated liquid Wd that has flowed into the heat transfer tube 11 is heated by the above-described absorption heat in the absorber 10. The unconcentrated liquid Wd heated by the heat transfer tube 11 flows through the mixed liquid tube 94 toward the concentration tank 91 as a mixed liquid Wm in which a part of the unconcentrated liquid Wd is evaporated and the separated vapor Wv and the concentrated liquid Wc are mixed. In the mixed liquid Wm introduced into the concentration tank 91, the concentrated liquid Wc and the separated vapor Wv are separated. The separated concentrated liquid Wc is stored in the lower part of the concentration tank 91, and what exists above the connection portion of the non-concentrated liquid pipe 92 is sent again to the heat transfer pipe 11 of the absorber 10, and the non-concentrated liquid pipe 92 Those existing below the connecting portion flow into the concentrated liquid tube 97. On the other hand, the separated detachment steam Wv flows into the detachment steam pipe 99, and is divided into an evaporator detachment steam pipe 99A, a regenerator detachment steam pipe 99B, and an external detachment steam pipe 99C. The separated steam Wv separated into the evaporator leaving steam pipe 99A and the regenerator leaving steam pipe 99B other than flowing into the external leaving steam pipe 99C passes through the evaporator 60 and the regenerator 70, and then merges again. Then, it flows into the detachment drain heat exchanger 98D as the detachment drain Wq, exchanges heat with the refrigerant liquid Vf, and flows out of the system after the temperature is lowered. On the other hand, the separation steam Wv flowing into the external separation steam pipe 99C flows toward a steam utilization device (not shown) provided outside the system.

  In the present embodiment, each flow rate of the separation steam Wv flowing into the evaporator 60 and the regenerator 70 and the flow rate of the separation steam Wv flowing out toward the steam utilization device (not shown) outside the system are separated from the evaporator. It is adjusted by the opening degree of the steam valve 99Va, the regenerator detachment steam valve 99Vb, and the external detachment steam valve 99Vc. The opening degree of each of these valves 99Va, 99Vb, 99Vc takes into consideration the heat utilization efficiency when concentrating the unconcentrated liquid Wd, the steam utilization method when utilizing the separated steam Wv outside the system, and the like. The target usage flow rate ratio of the separated steam Wv to the inside is set, and a predetermined fixed opening degree is set so as to become the set target usage flow rate ratio, or the opening degree is set so as to become a predetermined target usage flow rate ratio. Control is sufficient. Setting of the target utilization flow rate ratio of the separated steam Wv outside and inside the system is not only the adjustment of the opening degree of each valve 99Va, 99Vb, 99Vc, but also the opening degree adjustment of the automatic valve using a touch panel, a switch, etc. Any means capable of setting the flow rate ratio both inside and outside the system, such as an adjustable manual valve or orifice, may be used. When the separated steam Wv is not used outside the system, if the separated steam Wv supplied to the outside of the system is introduced into the evaporator 60 or the regenerator 70, the heat utilization efficiency when the unconcentrated liquid Wd is concentrated can be improved. In addition, when there is a device that can use the separation steam Wv outside the system, the use of the steam can be expanded by supplying the separation steam Wv outside the system. Thus, the steam utilization ratio of the separated steam Wv in the system ranges from 100% in which the total amount of the separated steam Wv separated in the concentration tank 91 is used to 0% in which it is not used at all. It can be set to any ratio according to the driving situation. When the opening degree of each valve 99Va, 99Vb, 99Vc is constant depending on the equipment in which the concentrating device 1 is placed, an orifice may be used instead of each valve 99Va, 99Vb, 99Vc. In this manner, the valves 99Va, 99Vb, and 99Vc are set to predetermined opening degrees (flow rate utilization ratio between outside and inside the system) in consideration of the improvement of the overall thermal efficiency and the steam utilization as the concentrator 1.

  Returning to the description of the cycle on the absorption liquid side of the absorption heat pump unit again. The high-concentration solution Sa that has absorbed the evaporator refrigerant vapor Ve by the absorber 10 is reduced in concentration to become a dilute solution Sw, and is stored in the storage unit 13. The dilute solution Sw in the reservoir 13 flows through the absorber effluent solution tube 15 toward the regenerator 70 due to the difference between gravity and internal pressure, and heat exchange with the high-concentration solution Sa in the high-temperature heat exchanger 18 causes the temperature to decrease. Later, it reaches the dilute solution spray nozzle 72. As described above, in the present embodiment, the absorbing liquid S in the absorber 10 is directly introduced into the regenerator 70 (without passing through another absorber).

  The dilute solution Sw sent to the regenerator 70 is sprayed from the dilute solution spray nozzle 72. The dilute solution Sw sprayed from the dilute solution spray nozzle 72 is heated and sprayed by the regenerator heat source hot water hg (for example, around 80 ° C.) flowing through the regenerator heat source pipe 71 and the separated steam Wv flowing through the regenerator heating pipe 79. The refrigerant in the diluted solution Sw evaporates to become a high concentration solution Sa and is stored in the lower part of the regenerator 70. On the other hand, the refrigerant V evaporated from the dilute solution Sw moves to the condenser 80 as the regenerator refrigerant vapor Vg. The high concentration solution Sa stored in the lower part of the regenerator 70 is pumped by the high concentration solution pump 76 to the high concentration solution spray nozzle 12 of the absorber 10 through the high concentration solution tube 75. The high-concentration solution Sa flowing through the high-concentration solution pipe 75 exchanges heat with the dilute solution Sw in the high-temperature heat exchanger 18 and rises in temperature, and then flows into the absorber 10 and sprayed from the high-concentration solution spray nozzle 12. . Thereafter, the same cycle is repeated.

  As described above, in the concentrating device 1 according to the present embodiment, since the absorption heat pump unit is a temperature rising type second-type absorption heat pump, when the unconcentrated liquid Wd is concentrated to the concentrated liquid Wc. The temperature of the separation steam Wv generated as a secondary can be higher than the temperatures of the evaporator heat source hot water he and the regenerator heat source hot water hg that are input as heat sources, and the separation steam generated as the concentrate Wc is generated. It is possible to heat the refrigerant liquid Vf in the evaporator 60 and the dilute solution Sw in the regenerator 70 with a part of the heat of Wv, and the heat utilization efficiency of the concentrating device 1 when concentrating the unconcentrated liquid Wd Can be improved. Further, since the unconcentrated liquid Wd can be heated and concentrated at a temperature higher than the temperatures of the evaporator heat source hot water he and the regenerator heat source hot water hg, the operating pressure in the concentration tank 91 is atmospheric pressure or a pressure exceeding atmospheric pressure. It is not necessary to reduce the pressure in the concentration tank 91 to a pressure lower than the atmospheric pressure, which is performed when the unconcentrated liquid Wd is concentrated by evaporating the liquid at a low temperature. . When the operation is performed so that the concentration tank 91 has a pressure exceeding the atmospheric pressure, the use of the separation steam Wv can be expanded and the utilization of the separation steam Wv outside the system can be promoted. Moreover, since it is not necessary to reduce the pressure in the concentration tank 91 to a pressure lower than the atmospheric pressure, the internal volume of the concentration tank 91 can be reduced in size. The operating pressure in the concentration tank 91 and the flow rate of the unconcentrated liquid Wd introduced into the concentration tank 91 are the evaporator heat source that flows into the evaporator heat source pipe 61 in order to achieve the target concentration and flow rate of the concentrated liquid Wc to be extracted. The temperature and flow rate of the hot water he, the temperature and flow rate of the regenerator heat source hot water hg flowing into the regenerator heat source tube 71, the temperature and flow rate of the cooling water c flowing into the cooling water tube 81, the heat utilization efficiency of the concentrator 1, and outside the system It is preferable to make adjustments by comprehensively considering how to use the separated steam Wv.

  Next, referring to FIG. 2, a concentrating device 1A according to a modification of the first embodiment of the present invention will be described. FIG. 2 is a schematic system diagram of the concentration apparatus 1A. The concentrating device 1A is a concentrating device 1 provided with a heat pump part of a second-stage absorption heat pump of a single-stage temperature rising type in that the absorption heat pump part is a three-stage temperature rising type second-type absorption heat pump (see FIG. 1). ) Is different. The concentrating device 1A includes a high temperature evaporator 20, an intermediate temperature absorber 30, an intermediate temperature evaporator 40, and a low temperature absorber 50 in addition to the configuration of the concentrating device 1 (see FIG. 1). In the concentration device 1A, the configuration corresponding to the absorber 10 in the concentration device 1 (see FIG. 1) is referred to as a “high temperature absorber 10” in order to distinguish it from the intermediate temperature absorber 30 and the low temperature absorber 50. In order to distinguish the configuration corresponding to the evaporator 60 in the apparatus 1 (see FIG. 1) from the high temperature evaporator 20 and the intermediate temperature evaporator 40, it is referred to as a “low temperature evaporator 60”.

  The high-temperature evaporator 20 is a component that supplies the high-temperature refrigerant vapor Va to the high-temperature absorber 10. The high-temperature evaporator 20 includes a refrigerant gas-liquid separation cylinder 21 that stores the refrigerant liquid Vf and the high-temperature refrigerant vapor Va, a high-temperature refrigerant liquid supply pipe 22, and a high-temperature refrigerant vapor receiving pipe 24. The high-temperature refrigerant liquid supply pipe 22 is a pipe constituting a flow path that guides the refrigerant liquid Vf to the heating pipe 31 of the intermediate temperature absorber 30. The high-temperature refrigerant vapor receiving pipe 24 represents the refrigerant gas-liquid mixed phase of the high-temperature refrigerant vapor Va generated by the refrigerant liquid Vf being heated by the heating pipe 31 of the intermediate temperature absorber 30 or the high-temperature refrigerant vapor Va and the refrigerant liquid Vf. It is a tube constituting a flow path for guiding to the separation cylinder 21. A baffle plate (not shown) that collides and separates the droplets of the refrigerant V contained in the high-temperature refrigerant vapor Va is provided in the refrigerant gas-liquid separation cylinder 21. In the present embodiment, the inner surface of the heating tube 31 of the intermediate temperature absorber 30 is used as the heat transfer surface of the high temperature evaporator 20. The high temperature evaporator 20 is connected to a refrigerant liquid pipe 82 for introducing the refrigerant liquid Vf. A flow rate adjustment valve 83 is disposed in the refrigerant liquid pipe 82 connected to the high temperature evaporator 20. One end of the high-temperature refrigerant liquid supply pipe 22 is connected to the portion of the refrigerant gas-liquid separation cylinder 21 where the refrigerant liquid Vf is stored, and the other end is connected to one end of the heating pipe 31. The high temperature refrigerant vapor receiving pipe 24 has one end connected to the refrigerant gas-liquid separation cylinder 21 and the other end connected to the other end of the heating pipe 31. In the high-temperature evaporator 20, the refrigerant liquid Vf changes to steam inside the heating pipe 31 and the density is greatly reduced. Therefore, the refrigerant in the refrigerant gas-liquid separation cylinder 21 is assumed to function as the bubble pump. A pump for sending the liquid Vf to the heating pipe 31 is omitted. A pump (not shown) that sends the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 21 to the heating pipe 31 may be disposed in the high-temperature refrigerant liquid supply pipe 22.

  The high-temperature absorber 10 is connected to the evaporator 60 via the flow path of the evaporator refrigerant vapor Ve in the concentrator 1 (see FIG. 1), but in the concentrator 1A according to this modification, the high-temperature refrigerant vapor flow path. Is connected to the high-temperature evaporator 20 through a high-temperature refrigerant vapor pipe 29. One end of the high-temperature refrigerant vapor pipe 29 is connected to the upper part (typically the top) of the refrigerant gas-liquid separation cylinder 21, and the other end is absorbed at a high temperature above the high-concentration solution spray nozzle 12. Connected to the vessel 10. With such a configuration, the high-temperature refrigerant vapor Va generated by the high-temperature evaporator 20 can be supplied to the high-temperature absorber 10 through the high-temperature refrigerant vapor pipe 29.

  The intermediate temperature absorber 30 has a heating pipe 31 as a refrigerant heating pipe constituting a flow path for the refrigerant liquid Vf and the high temperature refrigerant vapor Va, and an intermediate concentration solution spray nozzle 32 inside. As described above, the heating pipe 31 has one end connected to the high-temperature refrigerant liquid supply pipe 22 and the other end connected to the high-temperature refrigerant vapor receiving pipe 24. The medium concentration solution spray nozzle 32 sprays the medium concentration solution Sb in the present embodiment. The medium concentration solution spray nozzle 32 is disposed above the heating tube 31 so that the sprayed medium concentration solution Sb falls on the heating tube 31. One end of an absorber outflow solution tube 15 for flowing the intermediate concentration solution Sb is connected to the intermediate concentration solution spray nozzle 32. In the concentrator 1 (see FIG. 1), the absorber outflow solution pipe 15 is connected to the dilute solution spray nozzle 72 in the regenerator 70 and is configured to flow the dilute solution Sw. The apparatus 1A is connected to the medium concentration solution spray nozzle 32 and is configured to flow the medium concentration solution Sb. The intermediate temperature absorber 30 heats the refrigerant liquid Vf flowing through the heating pipe 31 by absorption heat generated when the intermediate concentration solution Sb is applied from the intermediate concentration solution spray nozzle 32 and the intermediate concentration solution Sb absorbs the intermediate temperature refrigerant vapor Vb. Thus, the high-temperature refrigerant vapor Va can be generated. The intermediate temperature absorber 30 is configured to operate at a pressure (dew point temperature) lower than that of the high temperature absorber 10, and the operating temperature is lower than that of the high temperature absorber 10. A storage part 33 for storing the low-concentration solution Sc is formed in the lower part of the intermediate temperature absorber 30. The low-concentration solution Sc is an absorbing solution S whose concentration is lowered by the medium-concentration solution Sb sprayed from the medium-concentration solution spray nozzle 32 absorbing the intermediate temperature refrigerant vapor Vb. The heating tube 31 is disposed above the storage unit 33.

  The intermediate temperature evaporator 40 is a component that supplies the intermediate temperature refrigerant vapor Vb to the intermediate temperature absorber 30. The intermediate temperature evaporator 40 includes a refrigerant gas-liquid separation cylinder 41 that stores the refrigerant liquid Vf and the intermediate temperature refrigerant vapor Vb, an intermediate temperature refrigerant liquid supply pipe 42, and an intermediate temperature refrigerant vapor receiving pipe 44. The intermediate temperature refrigerant liquid supply pipe 42 is a pipe that constitutes a flow path that guides the refrigerant liquid Vf to the heating pipe 51 of the low temperature absorber 50. The intermediate-temperature refrigerant vapor receiving pipe 44 is a refrigerant gas-liquid that represents an intermediate-temperature refrigerant vapor Vb generated by heating the refrigerant liquid Vf in the heating pipe 51 of the low-temperature absorber 50 or a refrigerant gas-liquid mixed phase of the intermediate-temperature refrigerant vapor Vb and the refrigerant liquid Vf. It is a tube constituting a flow path for guiding to the separation cylinder 41. The refrigerant gas-liquid separation cylinder 41 is configured in the same manner as the refrigerant gas-liquid separation cylinder 21 of the high-temperature evaporator 20. In the present embodiment, the inner surface of the heating tube 51 of the low temperature absorber 50 is used as the heat transfer surface of the intermediate temperature evaporator 40. In addition, a refrigerant liquid pipe 84 for introducing the refrigerant liquid Vf is connected to the intermediate temperature evaporator 40. The refrigerant liquid pipe 84 branches from the refrigerant liquid pipe 82. A flow rate adjustment valve 85 is disposed in the refrigerant liquid pipe 84 connected to the intermediate temperature evaporator 40. The intermediate temperature refrigerant liquid supply pipe 42 has one end connected to the portion of the refrigerant gas-liquid separation cylinder 41 where the refrigerant liquid Vf is stored, and the other end connected to one end of the heating pipe 51. The intermediate temperature refrigerant vapor receiving pipe 44 has one end connected to the refrigerant gas-liquid separation cylinder 41 and the other end connected to the other end of the heating pipe 51. In the intermediate temperature evaporator 40, since the refrigerant liquid Vf changes to steam inside the heating pipe 51 and the density is greatly reduced, the refrigerant in the refrigerant gas-liquid separation cylinder 41 is assumed to function as the bubble pump. A pump for sending the liquid Vf to the heating pipe 51 is omitted. A pump (not shown) that sends the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 41 to the heating pipe 51 may be disposed in the intermediate temperature refrigerant liquid supply pipe 42.

  The intermediate temperature evaporator 40 and the intermediate temperature absorber 30 are connected by an intermediate temperature refrigerant vapor pipe 49 as an intermediate temperature refrigerant vapor channel. One end of the intermediate temperature refrigerant vapor pipe 49 is connected to the upper part (typically the top) of the refrigerant gas-liquid separation cylinder 41, and the other end is above the intermediate concentration solution spray nozzle 32 and absorbs the intermediate temperature. Connected to the container 30. With such a configuration, the intermediate temperature refrigerant vapor Vb generated by the intermediate temperature evaporator 40 can be supplied to the intermediate temperature absorber 30 via the intermediate temperature refrigerant vapor pipe 49.

  The low-temperature absorber 50 has a heating pipe 51 as a refrigerant heating pipe constituting a flow path for the refrigerant liquid Vf and the medium-temperature refrigerant vapor Vb, and a low-concentration solution spray nozzle 52 inside. As described above, the heating pipe 51 is connected to the intermediate temperature refrigerant liquid supply pipe 42 at one end and the intermediate temperature refrigerant vapor receiving pipe 44 at the other end. The low concentration solution spray nozzle 52 sprays the low concentration solution Sc in the present embodiment. The low concentration solution spray nozzle 52 is disposed above the heating tube 51 so that the sprayed low concentration solution Sc falls on the heating tube 51. The low concentration solution spray nozzle 52 is connected to one end of a low concentration solution pipe 35 that allows the low concentration solution Sc to flow inside. The low-temperature absorber 50 sprays the low-concentration solution Sc from the low-concentration solution spray nozzle 52, and heats the refrigerant liquid Vf flowing through the heating pipe 51 by heat absorbed when the low-concentration solution Sc absorbs the low-temperature refrigerant vapor Vc. Thus, the intermediate temperature refrigerant vapor Vb can be generated. Therefore, the heating pipe 51 corresponds to a heating target fluid flow path, and the refrigerant V flowing through the heating pipe 51 corresponds to a heating target fluid. The low temperature absorber 50 is configured to operate at a pressure (dew point temperature) lower than that of the intermediate temperature absorber 30, and the operating temperature is lower than that of the intermediate temperature absorber 30. A storage part 53 for storing the dilute solution Sw is formed below the low-temperature absorber 50. The dilute solution Sw is an absorbing solution S whose concentration is lowered by absorbing the low-temperature refrigerant vapor Vc by the absorbing solution S (low concentration solution Sc in the present embodiment) sprayed from the low concentration solution spray nozzle 52. The dilute solution Sw contains more refrigerant V than the high concentration solution Sa and the medium concentration solution Sb. The heating tube 51 is disposed above the storage unit 53.

  In the concentrator 1 (see FIG. 1), the absorber 10 and the evaporator 60 are in communication with each other. However, in the concentrator 1A according to this modification, the low-temperature absorber 50 and the low-temperature evaporator 60 are in communication with each other. ing. The low temperature absorber 50 and the low temperature evaporator 60 communicate with each other so that the low temperature refrigerant vapor Vc generated in the low temperature evaporator 60 can be supplied to the low temperature absorber 50. In the concentrator 1A according to the present modification, the refrigerant vapor generated in the low-temperature evaporator 60 is not the evaporator refrigerant vapor Ve called by the evaporator 60 in the concentrator 1 (see FIG. 1) for convenience. The low-temperature refrigerant vapor Vc is called. The low-temperature absorber 50 and the low-temperature evaporator 60 typically communicate with each other above the low-concentration solution spray nozzle 52 and above the refrigerant liquid spray nozzle 62. In addition, the pipe connected to the dilute solution spray nozzle 72 of the regenerator 70 is an absorber effluent solution pipe 15 for flowing the dilute solution Sw stored in the storage unit 13 of the absorber 10 in the concentration device 1 (see FIG. 1). However, in the concentrating device 1A according to the present modification, the dilute solution tube 55 is used to flow the dilute solution Sw stored in the storage unit 53 of the low-temperature absorber 50. Further, the high-temperature heat exchanger 18 is a device that performs heat exchange between the dilute solution Sw and the high-concentration solution Sa in the concentration device 1 (see FIG. 1), but in the concentration device 1A according to the present modification, the medium concentration This is a device that exchanges heat between the solution Sb and the high-concentration solution Sa.

  Further, the concentration device 1A according to the present modification is different from the concentration device 1 (see FIG. 1) in the following points. The absorber outflow solution pipe 15 is provided with a medium concentration solution pump 16 that pumps the medium concentration solution Sb in the high temperature absorber 10 to the medium temperature absorber 30. The storage unit 33 of the intermediate temperature absorber 30 and the low concentration solution spray nozzle 52 of the low temperature absorber 50 are connected by a low concentration solution tube 35. The low concentration solution pipe 35 is provided with a low concentration solution pump 36 that pumps the low concentration solution Sc in the intermediate temperature absorber 30 to the low temperature absorber 50. The storage unit 53 of the low-temperature absorber 50 and the dilute solution spray nozzle 72 of the regenerator 70 are connected by a dilute solution tube 55. An intermediate temperature heat exchanger 38 is disposed in the low concentration solution tube 35 and the high concentration solution tube 75. The intermediate temperature heat exchanger 38 is a device that exchanges heat between the low concentration solution Sc flowing through the low concentration solution tube 35 and the high concentration solution Sa flowing through the high concentration solution tube 75. A low temperature heat exchanger 58 is disposed in the dilute solution tube 55 and the high concentration solution tube 75. The low-temperature heat exchanger 58 is a device that performs heat exchange between the dilute solution Sw flowing through the dilute solution tube 55 and the high concentration solution Sa flowing through the high concentration solution tube 75. Further, the other end of the refrigerant liquid pipe 88 connected at one end to the condenser 80 is connected to the evaporator 60 in the concentrating device 1 (see FIG. 1), but in the concentrating device 1A according to the present modification, the temperature is high. The refrigerant liquid pipe 82 connected to the evaporator 20 and the refrigerant liquid pipe 86 connected to the low-temperature evaporator 60 are connected, and the refrigerant liquid Vf in the condenser 80 is transferred to the high-temperature evaporator 20, the intermediate-temperature evaporator 40, and the low-temperature evaporator. It can be distributed to the evaporator 60. The refrigerant liquid pipe 86 is provided with a flow rate adjusting valve 87 for adjusting the flow rate of the refrigerant liquid Vf introduced into the low temperature evaporator 60. The configuration of the concentrator 1A other than that described so far is the same as that of the concentrator 1 (see FIG. 1).

  With continued reference to FIG. 2, the operation of the concentration apparatus 1A will be described. First, regarding the cycle on the refrigerant side of the absorption heat pump unit, the condenser 80 receives the regenerator refrigerant vapor Vg generated in the regenerator 70 and cools the regenerator refrigerant vapor Vg with the cooling water c flowing through the cooling water pipe 81. Condensate to make refrigerant liquid Vf. The condensed refrigerant liquid Vf is pumped toward the high temperature evaporator 20, the medium temperature evaporator 40, and the low temperature evaporator 60 by the condensation refrigerant pump 89. The refrigerant liquid Vf pressure-fed by the condensing refrigerant pump 89 flows through the refrigerant liquid pipe 88 and is divided into the refrigerant liquid pipe 82 and the refrigerant liquid pipe 86 after the temperature rises in the separation drain heat exchanger 98D. A part of the refrigerant liquid Vf flowing through the refrigerant liquid pipe 82 flows into the refrigerant liquid pipe 84 in the middle, and the rest flows through the refrigerant liquid pipe 82 as it is and is introduced into the high-temperature refrigerant liquid supply pipe 22. The refrigerant liquid Vf flowing through the refrigerant liquid pipe 84 is introduced into the intermediate temperature refrigerant liquid supply pipe 42. The refrigerant liquid Vf flowing through the refrigerant liquid pipe 86 is introduced into the low temperature evaporator 60.

  In the low temperature evaporator 60, the same operation as the evaporator 60 in the concentrating device 1 (see FIG. 1) is performed, and the low temperature refrigerant vapor Vc is generated. The low-temperature refrigerant vapor Vc generated in the low-temperature evaporator 60 moves to the low-temperature absorber 50 that communicates with the low-temperature evaporator 60. On the other hand, the refrigerant liquid Vf introduced into the intermediate temperature refrigerant liquid supply pipe 42 flows into the heating pipe 51 of the low temperature absorber 50 by the action of the bubble pump. The refrigerant liquid Vf flowing into the heating pipe 51 is heated by the absorption heat generated when the low-temperature refrigerant vapor Vc moved from the low-temperature evaporator 60 is absorbed by the low-concentration solution Sc in the low-temperature absorber 50. Evaporates to medium temperature refrigerant vapor Vb. The intermediate temperature refrigerant vapor Vb generated in the heating pipe 51 flows through the intermediate temperature refrigerant vapor receiving pipe 44 and reaches the refrigerant gas-liquid separation cylinder 41. The intermediate temperature refrigerant vapor Vb flowing into the refrigerant gas-liquid separation cylinder 41 moves to the intermediate temperature absorber 30 communicating with the intermediate temperature evaporator 40 via the intermediate temperature refrigerant vapor pipe 49. The refrigerant liquid Vf introduced into the high-temperature refrigerant liquid supply pipe 22 flows into the heating pipe 31 of the intermediate temperature absorber 30 by the action of the bubble pump. The refrigerant liquid Vf flowing into the heating pipe 31 is heated by the absorption heat generated when the intermediate temperature refrigerant vapor Vb moved from the intermediate temperature evaporator 40 is absorbed by the intermediate concentration solution Sb in the intermediate temperature absorber 30, and this heating is performed. Evaporates to a high-temperature refrigerant vapor Va. The high-temperature refrigerant vapor Va generated in the heating pipe 31 flows through the high-temperature refrigerant vapor receiving pipe 24 and reaches the refrigerant gas-liquid separation cylinder 21. The high-temperature refrigerant vapor Va flowing into the refrigerant gas-liquid separation cylinder 21 moves to the high-temperature absorber 10 that communicates with the high-temperature evaporator 20 via the high-temperature refrigerant vapor pipe 29.

  Next, in the high-temperature absorber 10, the high-concentration solution Sa is sprayed from the high-concentration solution spray nozzle 12 for the cycle on the absorption liquid side of the absorption heat pump unit of the concentrator 1 </ b> A. The high-temperature refrigerant vapor Va that has moved from the vessel 20 is absorbed. The high-concentration solution Sa that has absorbed the high-temperature refrigerant vapor Va is reduced in concentration to become a medium-concentration solution Sb. In the high-temperature absorber 10, heat of absorption is generated when the high-concentration solution Sa absorbs the high-temperature refrigerant vapor Va. Due to this absorbed heat, the concentration-related substance W flowing through the heat transfer tube 11 is heated. The concentration-related substance W heated by the heat transfer tube 11 is introduced into the concentration tank 91, and the same action as that around the concentration tank 91 in the concentration apparatus 1 (see FIG. 1) is performed, so that the concentrated liquid Wc becomes the concentrated liquid pipe 97. The separated steam Wv flows out into the detached steam pipe 99. The separation steam Wv that has flowed out of the concentration tank 91 into the separation steam pipe 99 is divided into a part that is used inside the system and a part that is used outside the system, similarly to the concentration device 1 (see FIG. 1). The evacuated steam Wv used in the system is divided into two parts, an evaporator detachment steam pipe 99A and a regenerator detachment steam pipe 99B, as in the concentrator 1 (see FIG. 1). After passing through the inside 70, they merge again, flow into the detachment drain heat exchanger 98D as detachment drain Wq, exchange heat with the refrigerant liquid Vf, and then flow out of the system.

  The high-concentration solution Sa that has absorbed the high-temperature refrigerant vapor Va by the high-temperature absorber 10 is reduced in concentration to become a medium-concentration solution Sb and stored in the storage unit 13. The intermediate concentration solution Sb in the reservoir 13 flows through the intermediate concentration solution tube 15 toward the intermediate temperature absorber 30 by the operation of the intermediate concentration solution pump 16, and exchanges heat with the high concentration solution Sa in the high temperature heat exchanger 18. After the decrease, the medium concentration solution spray nozzle 32 is reached. Thus, in the concentration apparatus 1A according to the present modification, the absorbing liquid S in the high temperature absorber 10 is directly introduced into the intermediate temperature absorber 30 (without passing through other absorbers). It should be noted that the internal pressure of the high temperature absorber 10 is higher than the internal pressure of the intermediate temperature absorber 30, and even if the intermediate concentration solution pump 16 is not operating, the medium concentration solution in the high temperature absorber 10 is caused by the difference between the internal pressures of both. When Sb can be conveyed to the intermediate temperature absorber 30, the intermediate concentration solution pump 16 may be stopped.

  In the intermediate temperature absorber 30, the intermediate concentration solution Sb is dispersed from the intermediate concentration solution spray nozzle 32, and the dispersed intermediate concentration solution Sb absorbs the intermediate temperature refrigerant vapor Vb moved from the intermediate temperature evaporator 40. The medium concentration solution Sb that has absorbed the intermediate temperature refrigerant vapor Vb is reduced in concentration to become a low concentration solution Sc and stored in the storage unit 33. In the intermediate temperature absorber 30, heat of absorption is generated when the intermediate concentration solution Sb absorbs the intermediate temperature refrigerant vapor Vb. As described above, the refrigerant liquid Vf flowing through the heating pipe 31 is heated by this absorbed heat. The low-concentration solution Sc in the reservoir 33 flows through the low-concentration solution pipe 35 toward the low-temperature absorber 50 by the operation of the low-concentration solution pump 36, and exchanges heat with the high-concentration solution Sa in the intermediate temperature heat exchanger 38. After the decrease, the low concentration solution spray nozzle 52 is reached. Thus, in the present embodiment, the absorbing liquid S in the high temperature absorber 10 is indirectly introduced into the low temperature absorber 50 via the intermediate temperature absorber 30. The internal pressure of the intermediate temperature absorber 30 is higher than the internal pressure of the low temperature absorber 50, and even if the low concentration solution pump 36 is not operating, the low concentration solution Sc in the intermediate temperature absorber 30 is caused by the difference in internal pressure between the two. Can be transported to the low temperature absorber 50, the low concentration solution pump 36 may be stopped.

  In the low temperature absorber 50, the low concentration solution Sc that has flowed into the low concentration solution spray nozzle 52 is sprayed toward the heating pipe 51. The dispersed low-concentration solution Sc absorbs the low-temperature refrigerant vapor Vc that has moved from the low-temperature evaporator 60. The low-concentration solution Sc that has absorbed the low-temperature refrigerant vapor Vc is reduced in concentration to become a dilute solution Sw. In the low-temperature absorber 50, absorption heat is generated when the low-concentration solution Sc absorbs the low-temperature refrigerant vapor Vc. As described above, the absorbed heat heats the refrigerant liquid Vf flowing through the heating pipe 51 to generate the intermediate temperature refrigerant vapor Vb. The dilute solution Sw in the low-temperature absorber 50 flows through the dilute solution tube 55 toward the regenerator 70 by gravity. At this time, the dilute solution Sw is introduced into the regenerator 70 after the low temperature heat exchanger 58 exchanges heat with the high concentration solution Sa to lower the temperature. Thus, in the concentration apparatus 1A according to the present modification, the absorbing liquid S in the high temperature absorber 10 is indirectly introduced into the regenerator 70 via the intermediate temperature absorber 30 and the low temperature absorber 50. In the regenerator 70, the same operation as the regenerator 70 in the concentrator 1 (see FIG. 1) is performed, the regenerator refrigerant vapor Vg moves to the condenser 80, and the high concentration solution Sa becomes the high concentration solution pump 76. By operation, it flows out to the high concentration solution tube 75.

  As described above, in the concentrating device 1A according to the present modification, the absorption heat pump unit is a multistage temperature rising type second type absorption heat pump, and therefore when the unconcentrated liquid Wd is concentrated to the concentrated liquid Wc. The temperature of the separation steam Wv generated as a secondary can be made higher than in the case of the concentrator 1 (see FIG. 1). Alternatively, the concentrator 1A uses the heat source having a temperature lower than that of the heat source (evaporator heat source hot water he, regenerator heat source hot water hg) used in the concentrator 1 (see FIG. 1). Can be obtained. That is, the temperature difference between the separated steam Wv and the heat source can be made larger than in the case of the concentrator 1. Further, when the boiling temperature for removing the vapor is high when the fluid to be concentrated is a chemical liquid or a high pressure fluid, the fluid to be concentrated is heated to the high boiling temperature in order to concentrate the fluid to be concentrated. Even in that case, according to the concentration device 1A, the fluid to be concentrated can be heated to a high temperature from the heat source having the same temperature as that used in the concentration device 1 (see FIG. 1) and concentrated. Can do. In other words, when the concentration target fluid is a chemical liquid or a high-pressure fluid and the boiling temperature for releasing steam is high, the concentration device according to this modification adopting the second-stage absorption heat pump of the multistage temperature increase type 1A is suitable.

  In the above description, the absorption heat pump unit of the concentrating device 1 is a single-stage heating type, and the absorption heat pump unit of the concentrating device 1A is a three-stage heating type. Good. In the case of the two-stage temperature rising type, the structure around the intermediate temperature absorber 30 and the intermediate temperature evaporator 40 is omitted from the structure of the absorption heat pump unit of the three-stage temperature rising type concentrator 1A, and the high-temperature refrigerant liquid supply of the high-temperature evaporator 20 is omitted. The pipe 22 and the high-temperature refrigerant vapor receiving pipe 24 are connected to the heating pipe 51 of the low-temperature absorber 50, the medium-concentration solution pipe 15 is connected to the low-concentration solution spray nozzle 52, and the medium-concentration solution Sb in the high-temperature absorber 10 is directly supplied. What is necessary is just to comprise so that it may introduce into the low-temperature absorber 50 (without going through another absorber).

  Next, with reference to FIG. 3, a concentrating device 2 according to a second embodiment of the present invention will be described. FIG. 3 is a schematic system diagram of the concentrating device 2. The concentration device 2 is different from the concentration device 1 (see FIG. 1) in the following points. The concentrating device 2 includes an absorber 10, an evaporator 60A, a regenerator 70A, and a condenser 80 as main components of the absorption heat pump unit. The absorber 10 and the condenser 80 are the same as those of the concentrating device 1 (see FIG. 1). The evaporator 60A is different from the evaporator 60 (see FIG. 1) in that the evaporator heating tube 69 (see FIG. 1) is not provided. The regenerator 70A differs from the regenerator 70 (see FIG. 1) in that the regenerator heating tube 79 (see FIG. 1) is not provided.

  Further, the concentrating device 2 includes a low-temperature concentrating tank 191 separately from the concentrating tank 91. The low-temperature concentration tank 191 is a device that introduces the concentrated liquid Wdx and heats it to generate the concentrated liquid Wcx whose concentration has increased from the concentrated liquid Wdx. The liquid to be concentrated Wdx corresponds to the fluid to be concentrated, and is the same as the non-concentrated liquid Wd flowing through the non-concentrated liquid supply pipe 95 in the present embodiment. The low-temperature concentration tank 191 has a separation steam circulation pipe 193 that flows the separation steam Wv generated in the concentration tank 91 inside. The separation steam flow pipe 193 is configured to heat the concentrated liquid Wdx with the heat of the introduced separation steam Wv, and corresponds to a heating unit. In the concentrating device 2, the liquid to be concentrated Wdx corresponds to the fluid to be heated. To the low-temperature concentration tank 191, a concentrated liquid supply pipe 195 provided with a concentrated liquid pump 196, a concentrated liquid pipe 197, and a low temperature concentrated steam pipe 199 are connected. In many cases, the concentrated liquid Wcx has a higher specific gravity than the concentrated liquid Wdx, and therefore the concentrated liquid Wcx tends to settle in the low-temperature concentration tank 191. Therefore, the concentrated liquid supply pipe 195 is connected to the side surface of the low-temperature concentration tank 191 at a height corresponding to the upper part of the separation steam circulation pipe 193 or a height above the upper end of the separation steam circulation pipe 193. In addition, the concentrate pipe 197 from which the concentrate Wcx flows out is connected to the lower part (typically the lowermost part) of the low-temperature concentration tank 191. Note that, when the concentrate Wdx and the concentrate Wcx have a viscosity that does not hinder the flow in the low-temperature concentration tank 191, the concentrate supply pipe 195 may be connected to the lower side of the low-temperature concentration tank 191. Good. In the present embodiment, the non-concentrated liquid supply pipe 95 and the concentrated liquid supply pipe 195 are connected in parallel, and the non-concentrated liquid Wd (the concentrated liquid Wdx) is parallel to the concentrating tank 91 and the low-temperature concentrating tank 191. Configured to be supplied. The concentrated liquid pipe 197 is connected to a portion where the concentrated liquid Wcx at the bottom or lower part of the low temperature concentration tank 191 is stored. The low temperature concentration steam pipe 199 is connected to the upper part (typically the top) of the low temperature concentration tank 191. The concentrated liquid supply pipe 195 and the concentrated liquid pipe 197 include a concentrated liquid heat exchanger that exchanges heat between the concentrated liquid Wdx that flows through the concentrated liquid supply pipe 195 and the concentrated liquid Wcx that flows through the concentrated liquid pipe 197. 198S is provided. In the concentrating device 2, the separation steam pipe 99 has the separation steam circulation pipe 193 disposed in the flow path, and passes through the separation drain heat exchanger 98D without passing through the evaporator 60A and the regenerator 70A. In addition, although illustration is abbreviate | omitted, separation | steam vapor flow control apparatuses, such as a separation | steam steam valve which can adjust the flow volume of the separation | steaming steam Wv which flows through the separation | steaming steam pipe 99 between the concentration tank 91 and the low temperature concentration tank 191 inside. And one end of an external detachment steam pipe 99C (see FIG. 1) provided with an external detachment steam valve 99Vc (see FIG. 1) is connected to the detachment steam pipe 99 upstream of the detachment steam flow control device. Thus, the separation steam Wv may be supplied to a steam utilization apparatus (not shown) outside the system. The other configuration of the concentrating device 2 is the same as that of the concentrating device 1 (see FIG. 1).

  In the concentrating device 2 configured as described above, the absorption liquid and refrigerant cycle in the absorption heat pump unit and the operation in the concentrating tank 91 are the same as those in the concentrating device 1 (see FIG. 1). Then, the separated steam Wv separated from the non-concentrated liquid Wd in the concentration tank 91 flows into the separated steam pipe 99 and flows into the detached steam circulation pipe 193 in the low-temperature concentration tank 191. On the other hand, the concentrated liquid Wdx is pumped through the concentrated liquid supply pipe 195 to the low temperature concentration tank 191 by the operation of the concentrated liquid pump 196 and exchanged with the concentrated liquid Wcx in the concentrated liquid heat exchanger 198S. After the temperature rises, it is introduced into the low-temperature concentration tank 191. The liquid to be concentrated Wdx introduced into the low-temperature concentration tank 191 is heated by the heat of the separation steam Wv flowing through the separation steam flow pipe 193, part of it is evaporated to become the low-temperature steam Wvx, and the rest is concentrated from the liquid to be concentrated Wdx. As a result, the concentrated liquid Wcx is raised, and both are separated. The separated concentrated liquid Wcx is stored in the lower part of the low-temperature concentration tank 191, flows into the concentrated liquid pipe 197, and is transported to the use place. The low-temperature steam Wvx separated in the low-temperature concentration tank 191 and flowing out from the low-temperature concentration tank 191 through the low-temperature concentration steam pipe 199 may be applied outside the concentration apparatus 2. On the other hand, the separation steam Wv that has given heat to the liquid Wdx to be concentrated in the separation steam flow pipe 193 decreases in temperature and becomes separation drain Wq, flows into the separation drain heat exchanger 98D, and exchanges heat with the refrigerant liquid Vf. After the temperature further decreases, it flows out of the system. It should be noted that the evaporator 60A and / or the regenerator 70A are connected to the evaporator heating tube 69 and / or the regenerator heating tube provided in the regenerator 70 in the concentrator 1 (see FIG. 1). 79 may be provided so that the separation drain Wq flowing out of the separation steam flow pipe 193 is guided to the evaporator 60A and / or the regenerator 70A. Since the separation drain Wq is higher than the evaporator heat source hot water he and the regenerator heat source hot water hg, the separated drain Wq is guided to the evaporator 60A and / or the regenerator 70A, so that the refrigerant liquid Vf in the evaporator 60A and / or the regenerator. The dilute solution Sw in 70A can be heated.

  As described above, the concentration device 2 according to the present embodiment supplies the unconcentrated liquid Wd (the liquid to be concentrated Wdx) in parallel to the concentration tank 91 and the low-temperature concentration tank 191, The throughput can be increased. In the description of the concentration device 2 described above, the non-concentrated liquid supply pipe 95 and the concentrated liquid supply pipe 195 are connected in parallel, and the non-concentrated liquid Wd (concentrated liquid Wdx) is concentrated in the concentration tank 91 and the low-temperature concentration. Although it was configured to be supplied to the tank 191 in parallel, the concentrated liquid pipe 197 connected to the low-temperature concentration tank 191 was connected to the non-concentrated liquid supply pipe 95 and flowed out of the low-temperature concentration tank 191. The concentrated liquid Wcx may be configured to be supplied to the concentration tank 91 as the unconcentrated liquid Wd. When the concentrate Wcx flowing out from the low temperature concentration tank 191 is configured to be supplied to the concentration tank 91, the concentration rate of the concentrate can be increased.

  Alternatively, the low temperature steam Wvx flowing out from the low temperature concentration tank 191 may be guided to the evaporator 60 and the regenerator 70 as in the concentration device 2A according to the modification shown in FIG. The concentrator 2A is different from the concentrator 2 (see FIG. 3) in that the configuration of the evaporator 60 and the regenerator 70 is the same as that of the concentrator 1 (see FIG. 1). In the concentrating device 2A, the evaporator heating tube 69 corresponds to an evaporator additional heating unit, and the regenerator heating tube 79 corresponds to an additional regenerator heating unit. In the concentrating device 2A, the low-temperature concentration steam pipe 199 is divided into an evaporator low-temperature concentration steam pipe 199A, a regenerator low-temperature concentration steam pipe 199B, and an external low-temperature concentration steam pipe 199C, and the evaporator heating pipe 69 is an evaporator. The evaporator low temperature is disposed in the flow path of the low temperature concentrated steam pipe 199A, and the regenerator heating pipe 79 is disposed in the flow path of the regenerator low temperature concentrated steam pipe 199B and flows into the external low temperature concentrated steam pipe 199C. The low-temperature steam Wvx divided into the concentrated steam pipe 199A and the regenerator low-temperature concentrated steam pipe 199B is introduced from the low-temperature concentrated steam introduction section 69p to the evaporator 60 and from the low-temperature concentrated steam introduction section 79p to the regenerator 70, respectively. It differs from the concentration apparatus 2 (refer FIG. 3) also in the point comprised. Note that the low-temperature steam Wvx introduced into the evaporator 60 and the regenerator 70 is discharged as a low-temperature drain Wqx. The evaporator low-temperature concentration steam pipe 199A provided with the evaporator low-temperature concentration steam valve 199Va corresponds to the evaporator release steam pipe 99A provided with the evaporator release steam valve 99Va in the concentration apparatus 1 (see FIG. 1). . The regenerator low-temperature concentration steam pipe 199B provided with the regenerator low-temperature concentration steam valve 199Vb corresponds to the regenerator release steam pipe 99B provided with the regenerator release steam valve 99Vb in the concentrator 1 (see FIG. 1). . The evaporator low-temperature concentration steam pipe 199A and the regenerator low-temperature concentration steam pipe 199B correspond to the introduction part low-temperature desorption steam flow path, and the evaporator low-temperature concentration steam valve 199Va and the regenerator low-temperature concentration steam valve 199Vb adjust the introduction part low-temperature desorption steam flow rate. It corresponds to a device. Further, the external low-temperature concentration steam pipe 199C provided with the external low-temperature concentration steam valve 199Vc corresponds to the external release steam pipe 99C provided with the external release steam valve 99Vc in the concentrator 1 (see FIG. 1). The external low-temperature concentrated steam pipe 199C corresponds to an external low-temperature desorption steam flow path, and the external low-temperature concentrated steam valve 199Vc corresponds to an external low-temperature desorption steam flow control device.

  The concentrating device 2A configured as described above can use the low-temperature steam Wvx generated in the low-temperature concentrating tank 191 as a heating source for the evaporator 60 and the regenerator 70, thereby improving the heat utilization efficiency of the device. it can. Further, the low-temperature steam Wvx can be used in a steam utilization apparatus (not shown) outside the system, the use of the low-temperature steam Wvx can be expanded, and the use of the low-temperature steam Wvx outside the system can be promoted. In the above description of the concentrating device 2A, the low-temperature steam Wvx used in the system is introduced into both the evaporator heating pipe 69 and the regenerator heating pipe 79, but is introduced into either one of them. Alternatively, instead of or together with these, it may be introduced into the evaporator heat source pipe 61 and / or the regenerator heat source pipe 71. That is, the low temperature steam Wvx may be introduced into at least one of the evaporator heating pipe 69, the regenerator heating pipe 79, the evaporator heat source pipe 61, and the regenerator heat source pipe 71. When it is set as the structure which introduce | transduces the low temperature vapor | steam Wvx into the evaporator heat source pipe | tube 61 and the regenerator heat source pipe | tube 71, it is good to provide branch parts, such as cheese, in each, and let this be an introduction part. Similarly, in the concentrators 1 and 1A (see FIGS. 1 and 2), instead of introducing the separated steam Wv into the evaporator heating pipe 69 and / or the regenerator heating pipe 79, or these At the same time, it may be introduced into the evaporator heat source pipe 61 and / or the regenerator heat source pipe 71. Similarly, when the drainage drain Wq flowing out of the stripping steam flow pipe 193 in the concentrating device 2 (see FIG. 3) is led to the evaporator 60A and / or the regenerator 70A, the evaporator heat source pipe 61 and / or the regenerator heat source pipe 71 are similarly used. It is good also as introducing the leaving drain Wq. Further, when the concentrating devices 1, 1A, 2, 2A do not supply the disengagement steam Wv outside the system, it is not necessary to provide the external disengagement steam pipe 99C provided with the external disengagement steam valve 99Vc. When Wvx is not supplied outside the system, it is not necessary to provide the external low-temperature concentrated steam pipe 199C provided with the external low-temperature concentrated steam valve 199Vc.

  In the above description of the concentrators 2 and 2A, the case where the absorption heat pump unit is a single stage has been described. However, as in the concentrator 1A (see FIG. 2), a three-stage temperature rise type or a two-stage temperature rise type may be used. It is good also as a multistage temperature rising type.

  In the above description, the non-concentrated liquid Wd that has flowed into the heat transfer tube 11 of the absorber 10 is heated by the absorption heat in the absorber 10, so that part of it evaporates and the separated vapor Wv and the concentrated liquid Wc are mixed. The mixed liquid tube 94 flows as the mixed liquid Wm in a state where the liquid to be concentrated is crystallized. However, when there is a possibility that the fluid to be concentrated may crystallize, the mixed liquid pipe 94 is kept in the unconcentrated liquid Wd state by pressurizing with a pump or the like. It may be configured to flow so that when the non-concentrated liquid Wd flows into the concentration tank 91, a part of the non-concentrated liquid Wd evaporates and the separated vapor Wv and the concentrated liquid Wc are generated.

1, 1A, 2, 2A Concentrator 10 Absorber 11 Heat transfer tube 60, 60A Evaporator 61 Evaporator heat source tube 69 Evaporator heating tube 69p Low temperature drain introduction part 70, 70A Regenerator 71 Regenerator heat source tube 79 Regenerator heating tube 79p Low-temperature drain introduction part 80 Condenser 91 Concentration tank 99A Evaporator detachment steam pipe 99B Regenerator detachment steam pipe 99C External detachment steam pipe 99Va Evaporator detachment steam valve 99Vb Regenerator detachment steam valve 99Vc External detachment steam valve 98D Removal drain heat exchange 191 Low temperature concentrating tank 193 Departure steam flow pipe 199A Evaporator low temperature concentration steam pipe 199B Regenerator low temperature concentration steam pipe 199C External low temperature concentration steam pipe 199Va Evaporator low temperature concentration steam valve 199Vb Regenerator low temperature concentration steam valve 199Vc External low temperature concentration steam valve he evaporator heat source hot water hg regenerator heat source hot water Sa high concentration solution Sw dilute solution Ve evaporator Medium steam Vf refrigerant liquid W concentrated target fluid Wc concentrate Wm mixture Wv leaving vapor Wdx the concentrate Wvx cryogen vapor

Claims (11)

An absorber having a concentration target fluid flow path for flowing the concentration target fluid, and heating the concentration target fluid flowing in the concentration target fluid flow path with absorption heat generated when the absorbing liquid absorbs the vapor of the refrigerant;
A refrigerant heating fluid channel is provided, and the refrigerant liquid is heated with heat held by the refrigerant heating fluid flowing through the refrigerant heating fluid channel to generate refrigerant vapor to be supplied directly or indirectly to the absorber. With an evaporator;
An absorption liquid heating fluid flow path is provided, and the absorption liquid that has absorbed the refrigerant vapor in the absorber is directly or indirectly introduced, and the introduced absorption liquid flows through the absorption liquid heating fluid flow path. A regenerator that heats with heat held by the absorption liquid heating fluid to release the refrigerant from the absorption liquid to increase the concentration of the absorption liquid;
A condenser that introduces a refrigerant vapor separated from the absorbing liquid in the regenerator, cools and condenses the introduced refrigerant vapor, and generates a refrigerant liquid to be supplied to the evaporator;
A gas-liquid separator that introduces the concentration target fluid heated by the absorber and separates the separated vapor separated from the concentration target fluid and the concentrated liquid after the separated vapor is separated from the concentration target fluid; ;
A heating unit that introduces the desorption steam and heats the fluid to be heated with the heat of the introduced desorption vapor;
The internal pressure of the absorber was configured to be higher than the internal pressure of the regenerator;
Concentrator. A heating part separation steam channel for supplying the separation steam to the heating part;
A heating unit detachment steam flow rate adjusting device for adjusting a flow rate of the detachment steam flowing through the heating unit detachment steam channel;
An external desorption steam channel for supplying the desorption steam to the outside of the concentrator;
An external detachment steam flow rate adjusting device for adjusting a flow rate of the detachment steam flowing through the external detachment steam flow path;
The concentration apparatus according to claim 1. The heating unit detachment steam flow rate adjusting device and the external detachment so that the flow rate of the detachment steam flowing through the heating unit detachment steam channel and the flow rate of the detachment steam flowing through the external detachment steam channel become a predetermined ratio. Set the steam flow regulator;
The concentration apparatus according to claim 2. The heating unit is provided in at least one of the evaporator and the regenerator;
The concentrator according to any one of claims 1 to 3. The heating unit is disposed below the refrigerant heating fluid channel when provided in the evaporator, and is disposed below the absorbent heating fluid channel when provided in the regenerator;
The concentration apparatus according to claim 4. A low-temperature absorber having an operating pressure lower than that of the absorber, having a heating target fluid passage for flowing a heating target fluid, and directly or indirectly receiving the absorbing liquid that has absorbed the refrigerant vapor in the absorber. A low-temperature absorber that introduces and heats the heating target fluid that flows through the heating target fluid flow path with absorption heat generated when the introduced absorbing liquid absorbs the vapor of the refrigerant;
The concentrator according to any one of claims 1 to 5. A low-temperature concentration tank having the heating unit therein, wherein a concentration target fluid is introduced as a fluid to be heated in the heating unit, and the introduced concentration target fluid is heated by the heat of the separated steam to generate a concentrate With a concentration tank;
The concentrator according to any one of claims 1 to 6. In the low-temperature concentration tank, low-temperature desorption steam, which is vapor desorbed from the fluid to be concentrated, is supplied to an evaporator additional heating unit provided in the evaporator, a regenerator additional heating unit provided in the regenerator, and the refrigerant heating fluid. A flow path, and an introduction portion leading to at least one of the absorption liquid heating fluid flow path;
The concentration apparatus according to claim 7. An introduction portion low temperature desorption steam flow path for supplying the low temperature desorption vapor to the introduction portion;
An introduction unit low temperature desorption steam flow rate adjusting device for adjusting a flow rate of the low temperature desorption vapor flowing through the introduction unit low temperature desorption vapor channel;
An external low temperature release steam flow path for supplying the low temperature release steam to the outside of the concentrator;
An external low-temperature desorption steam flow rate adjusting device for adjusting a flow rate of the low-temperature desorption steam flowing through the external low-temperature desorption steam flow path;
The concentrating device according to claim 8. The introduction portion low temperature desorption steam flow rate adjustment so that the flow rate of the low temperature desorption steam flowing through the introduction portion low temperature desorption vapor flow path and the flow rate of the low temperature desorption steam flowing through the external low temperature desorption vapor flow path become a predetermined ratio. Setting the device and the external low temperature desorption steam flow control device;
The concentration apparatus according to claim 9. A heat exchanger that exchanges heat between the drained steam drained after the heated fluid is heated by the heating unit and the refrigerant liquid supplied from the condenser to the evaporator;
The concentrator according to any one of claims 1 to 10.

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