JP2019113259A - Absorption type heat exchange system - Google Patents

Abstract

To provide an absorption type heat exchange system in which an outlet temperature of a heated fluid is higher than an inlet temperature of a heating source fluid.SOLUTION: An absorption type heat exchange system 1 includes first and second absorption portions A1, A2 for increasing a temperature of a first heated fluid RP, first and second condensation portions C1, C2 for increasing a temperature of a second heated fluid GP, first and second evaporation portions E1, E2 for lowering a temperature of a heating source fluid RS, and first and second regeneration portions G1, G2 for lowering a temperature of the heating source fluid RS. Internal pressures and temperatures of the first evaporation portion E1 and the second evaporation portion E2 are respectively higher than those of the first condensation portion C1 and the second condensation portion C2 by absorption heat pump cycle of an absorption liquid and a refrigerant, and a part of the heating source fluid branched from the heating source fluid RA before introduced into the first and second evaporation portions E1, E2 and the first and second regeneration portions G1, G2, is introduced to the first and second absorption portions A1, A2 as the first heated fluid RP.SELECTED DRAWING: Figure 1

Description

  The present invention relates to an absorption heat exchange system, and more particularly to an absorption heat exchange system in which heat is exchanged between two fluids such that the outlet temperature of the temperature raising fluid is higher than the inlet temperature of the temperature decreasing fluid.

  Heat exchangers are widely used as devices for exchanging heat between hot and cold fluids. In a heat exchanger in which direct heat exchange is performed between two fluids, the outlet temperature of the low temperature fluid can not be higher than the inlet temperature of the high temperature fluid (see, for example, Patent Document 1).

Patent 5498809 gazette (refer to figure 11 grade)

  One of the applications of heat exchangers is to recover waste heat. Exhaust heat is heat that is discarded without being used, so the outlet temperature of the fluid that recovers the exhaust heat and raises the temperature is higher than the inlet temperature of the fluid that loses heat including the exhaust heat and lowers the temperature. If the temperature can be raised, the range of utilization will be expanded.

  The present invention has been made in view of the above problems, and an object thereof is to provide an absorption-type heat exchange system capable of making the outlet temperature of the heated fluid raising the temperature higher than the inlet temperature of the heating source fluid decreasing the temperature. Do.

  In order to achieve the above object, in the absorption heat exchange system according to the first aspect of the present invention, for example, as shown in FIG. 1, the absorption heat released when the absorbent Sa absorbs the refrigerant vapor Ve1 A first absorbing portion A1 for raising the temperature of the first heated fluid RP; and raising the temperature of the first heated fluid RP by the absorption heat released when the absorbing liquid Sa absorbs the vapor Ve2 of the refrigerant A second absorbing part A2; a first condensing part C1 for raising the temperature of the second fluid to be heated GP by condensation heat released when the refrigerant vapor Vg1 condenses and becomes the refrigerant liquid Vf1; A second condensation part C2 that raises the temperature of the second fluid to be heated GP by condensation heat released when the vapor Vg2 condenses and becomes the refrigerant liquid Vf2; a first condensation part C1 and a second condensation part Directly or indirectly from at least one of C2 The refrigerant liquid Vf is introduced into the refrigerant source, and the latent heat of evaporation necessary when the introduced refrigerant liquid Vf evaporates and becomes the vapor Ve1 of the refrigerant supplied to the first absorption part A1 is removed from the heat source fluid RS The refrigerant liquid Vf is directly or indirectly introduced from at least one of the first evaporation part E1 for reducing the temperature of the fluid RS; and the first condensation part C1 and the second condensation part C2, and the introduced refrigerant liquid Vf is And a second evaporation unit E2 for reducing the temperature of the heating source fluid RS by depriving the heating source fluid RS of the evaporation latent heat necessary for evaporating the refrigerant to be vapor Ve2 of the refrigerant supplied to the second absorption unit A2. In order to introduce the absorbing solution Sw directly or indirectly from at least one of the first absorbing portion A1 and the second absorbing portion A2 to generate the vapor Vg1 of the refrigerant supplied to the first condensing portion C1, Heated the introduced absorbent Sw and absorbed it? A first regeneration unit G1 that lowers the temperature of the heat source fluid RS by depriving the heat source fluid RS of heat necessary for removing the refrigerant; and at least at least a first absorption unit A1 and a second absorption unit A2 In order to introduce the absorbing solution Sw directly or indirectly from one side and generate the vapor Vg2 of the refrigerant supplied to the second condenser C2, the introduced absorbing solution Sw is heated to separate the refrigerant from the absorbing solution Sw And a second regeneration unit G2 for reducing the temperature of the heating source fluid RS by depriving the heating source fluid RS of heat necessary to cause the first evaporation unit by an absorption heat pump cycle of the absorbing liquid and the refrigerant. E1 is configured such that the internal pressure and temperature become higher than the first condensation part C1, and the second evaporation part E2 is configured such that the internal pressure and temperature becomes higher than the second condensation part C2; Evaporation unit E1, second evaporation unit E2, first As a first heated fluid RP, a part of the heating source fluid branched from the heating source fluid RA before being introduced into the regeneration unit G1 and the second regeneration unit G2 of the first absorption unit A1 and the second absorption unit A1 It is comprised so that it may introduce | transduce into absorption part A2.

  According to this structure, a part of the heat source fluid branched from the heat source fluid before being introduced into the first evaporation unit, the second evaporation unit, the first regeneration unit, and the second regeneration unit is The temperature of the first heated fluid flowing out of the first absorbing portion and the second absorbing portion is introduced into the first absorbing portion and the second absorbing portion as the first heated portion as the first heated portion. , The temperature of the heat source fluid before being introduced to the second evaporation unit, the first regeneration unit, and the second regeneration unit. In addition, since a part of the heating source fluid branched from the heating source fluid is introduced as the first heated fluid into the first absorbing part and the second absorbing part, the first absorbing part is more than the case with one absorbing part. The temperature of the fluid to be heated can be raised.

  The absorption heat exchange system according to the second aspect of the present invention is, for example, as shown in FIG. 1, in the absorption heat exchange system 1 according to the first aspect of the present invention, the first condensation part C1. And the second heated fluid GP flowing out of the second condensing unit C2 flows out of the first evaporating unit E1, the second evaporating unit E2, the first regeneration unit G1, and the second regeneration unit G2 The flow path 58 of the second heated fluid GP is configured to merge with the source fluid RS.

  With this configuration, it is possible to balance the flow rate of the heat source fluid entering and exiting the absorption heat exchange system.

  The absorption heat exchange system according to the third aspect of the present invention is, for example, as shown in FIG. 1, in the absorption heat exchange system 1 according to the first aspect or the second aspect of the present invention, The absorbing solution Sw that has flowed out from at least one of the first absorbing portion A1 and the second absorbing portion A2 flows directly or indirectly into the first regeneration portion G1 and the second regeneration portion G2 in parallel. The absorbent Sa that has flowed out from at least one of the first regeneration unit G1 and the second regeneration unit G2 flows directly or indirectly into the first absorption unit A1 and the second absorption unit A2 in parallel. The flow path of the absorbent S is configured.

  With such a configuration, it is possible to suppress an excessive increase in the concentration of the absorbing solution.

  The absorption heat exchange system according to the fourth aspect of the present invention is, for example, as shown in FIG. 2, in the absorption heat exchange system 2 according to the first aspect or the second aspect of the present invention, The absorbing liquid that has flowed directly or indirectly from at least one of the first absorption section A1 and the second absorption section A2 into the first regeneration section G1 or the second regeneration section G2 is the first regeneration section G1 or the second regeneration section G1. The absorbent flowing in the regeneration unit G2 in series and flowing directly or indirectly from at least one of the first regeneration unit G1 and the second regeneration unit G2 into the first absorption unit A1 or the second absorption unit A2 A flow path of the absorbing liquid is configured to flow in series through the first absorbing portion A1 and the second absorbing portion A2.

  With this configuration, the output difference can be increased by increasing the concentration difference of the absorbing solution.

  The absorption heat exchange system according to the fifth aspect of the present invention is, for example, as shown in FIG. 3, in the absorption heat exchange system 3 according to the first aspect or the second aspect of the present invention, The absorbing solution Sw1 having flowed out of the first absorbing portion A1 flows into the first regeneration portion G1 and the absorbing solution Sa1 having flowed out of the first regeneration portion G1 flows into the first absorbing portion A1. The first absorbent circulation channels 14 and 34 to be circulated between the first absorbent section A1 and the first regeneration section G1; and the absorbent Sw2 having flowed out the second absorbent section A2 is the second regeneration section G2 And the absorbent in the second regeneration section G2 is circulated between the second absorption section A2 and the second regeneration section G2 so that the absorption solution Sa2 flowing out of the second regeneration section G2 flows into the second absorption section A2. And a second absorbent circulation passage 18, 38.

  According to this structure, a plurality of independent paths for the absorption heat pump cycle of the absorbent and the refrigerant can be provided, and the absorption heat pump cycle can be controlled and managed by a plurality of units.

  The absorption heat exchange system according to the sixth aspect of the present invention is, for example, as shown in FIG. 1, an absorption heat according to any one of the first to fifth aspects of the present invention. In the exchange system 1, the flow path of the first heated fluid RP is configured such that the first heated fluid RP flows in series in the first absorbing portion A1 and the second absorbing portion A2.

  According to this structure, the temperature of the first fluid to be heated can be raised in two steps, and the first fluid to be heated having a higher temperature can be taken out.

  The absorption heat exchange system according to the seventh aspect of the present invention is, for example, as shown in FIG. 1, an absorption heat according to any one of the first to sixth aspects of the present invention. In the exchange system 1, the heating source fluid RS first flows into the first regeneration unit G1 or the first evaporation unit E1, and the first regeneration unit G1, the first evaporation unit E1, the second regeneration unit The flow path of the heat source fluid RS is configured to flow in series in an appropriate order in the G2 and the second evaporation portion E2; the first heated fluid RP is a heat source fluid RS that is the first evaporation portion E1. If the heat source fluid RS flows through the second evaporation section E2 so as to flow through the second absorption section A2 after flowing through the second absorption section A2 after flowing through the second evaporation section E2. When flowing through the first evaporation unit E1, after flowing through the first absorption unit A1, the second absorption unit A2 is To form a flow path of the first heated fluid RP; the second heated fluid GP flows in series through the first condenser C1 and the second condenser C2; A flow path of the heating fluid GP is configured.

  According to this structure, when the heating source fluid first flows into the first regeneration unit, the amount of heat transferred from the heating source fluid to the first heated fluid can be increased and the first heating object flows out. The temperature of the fluid can be increased, and when the heat source fluid first flows into the first evaporation section, the heat transfer from the heat source fluid to the first heated fluid increases and the first subject flows out. In addition to raising the temperature of the heating fluid, it is possible to suppress an increase in the concentration of the absorbing solution in the first regeneration unit and the second regeneration unit, and to avoid that the absorbing solution is excessively concentrated and crystallized be able to.

  In addition, an absorption heat exchange system according to an eighth aspect of the present invention relates to any one of the first aspect to the fifth aspect of the present invention as shown in, for example, FIG. 5 and FIG. In the absorption type heat exchange systems 5 and 6, the heat source fluid RS is parallel to at least two of the first evaporation unit E1, the second evaporation unit E2, the first regeneration unit G1, and the second regeneration unit G2. The flow path of the heating source fluid RS is configured to be introduced (see, for example, FIG. 6), and the first heated fluid RP is parallel to the first absorbing portion A1 and the second absorbing portion A2. The flow path of the first heated fluid RP is configured to be introduced (not shown), and the second heated fluid GP is parallel to the first condenser C1 and the second condenser C2. At least one of the flow paths of the second heated fluid GP being introduced into the Tsu is configured to be performed.

  According to this structure, the resistance of at least one flow path of the heating source fluid, the first heated fluid, and the second heated fluid can be reduced.

  The absorption heat exchange system according to the ninth aspect of the present invention is, for example, as shown in FIG. 7, an absorption heat according to any one of the first to eighth aspects of the present invention. In the exchange system 1A, a first regenerated condensing can barrel 30 that accommodates the first regeneration unit G1 and the first condensation unit C1 such that the first regeneration unit G1 and the first condensation unit C1 communicate with each other. And a first absorption evaporation can barrel 10 for housing the first absorption portion A1 and the first evaporation portion E1 such that the first absorption portion A1 and the first evaporation portion E1 communicate with each other; A second regenerating condensing can barrel 40 for housing the second regenerating section G2 and the second condensing section C2 such that the second regenerating section G2 and the second condensing section C2 communicate with each other; a second absorption A second absorption evaporation that accommodates the portion A2 and the second evaporation portion E2 such that the second absorption portion A2 and the second evaporation portion E2 communicate with each other. A first regenerative condenser cylinder 30 and a second regenerative condenser cylinder 40 arranged at different positions in the horizontal direction; a first absorption evaporator cylinder 10 and a second absorption evaporator cylinder 20 are disposed at positions different from each other in the horizontal direction; above the first regenerating condensing can body 30 and the second regenerating condensing can body 40, the first absorbing evaporation can barrel 10 and the second absorbing evaporation can barrel 20 are provided. It is arranged.

  With this configuration, the apparatus can be prevented from increasing in size while securing the flow of the absorbing liquid.

  The absorption heat exchange system according to the tenth aspect of the present invention is, for example, as shown in FIG. 9, an absorption heat according to any one of the first to ninth aspects of the present invention. In the exchange system 7, the third absorbing portion A3 which raises the temperature of the first heated fluid RP by the absorption heat released when the absorbing liquid Sa absorbs the vapor Ve3 of the refrigerant; and the vapor Vg3 of the refrigerant condenses A third condenser C3 for raising the temperature of the second fluid to be heated GP by condensation heat released when the refrigerant liquid Vf3 is introduced; a first condenser C1, a second condenser C2, and a third C3 The refrigerant liquid Vf is introduced directly or indirectly from at least one of the condensers C3 and the refrigerant liquid Vf introduced evaporates and becomes the vapor Ve3 of the refrigerant supplied to the third absorption part A3. Heat source by removing latent heat from heat source fluid RS The absorbent Sw is directly or indirectly introduced from at least one of the third evaporation part E3 for reducing the temperature of the body RS; and the first absorption part A1, the second absorption part A2 and the third absorption part A3. To generate the vapor Vg3 of the refrigerant supplied to the third condenser C3, the heat necessary for heating the introduced absorbent Sw to separate the refrigerant Vg3 from the absorbent Sw is heated with the heat source fluid RS. And the third regeneration unit G3 that lowers the temperature of the heating source fluid RS by depriving the heat source fluid RS; the third evaporation unit E3 is more internal than the third condensation unit C3 by the absorption heat pump cycle of the absorbing liquid and the refrigerant The first evaporator E1, the second evaporator E2, the third evaporator E3, the first regeneration unit G1, the second regeneration unit G2, and the third evaporator Bifurcated from the heating source fluid RA before being introduced into the regeneration unit G3 Some of the heat source fluid to the first absorption part A1 as a first heated fluid RP, and is configured to introduce the second absorption part A2 and the third absorbent portion A3.

  With this configuration, the temperature of the first heated fluid can be further raised.

  According to the present invention, a part of the heating source fluid branched from the heating source fluid before being introduced into the first evaporation unit, the second evaporation unit, the first regeneration unit and the second regeneration unit is The temperature of the first heated fluid flowing out of the first absorbing portion and the second absorbing portion is introduced into the first absorbing portion and the second absorbing portion as the first heated portion as the first heated portion. , The temperature of the heat source fluid before being introduced to the second evaporation unit, the first regeneration unit, and the second regeneration unit.

It is a typical systematic diagram of an absorption-type heat exchange system concerning a 1st embodiment of the present invention. It is a typical systematic diagram of an absorption-type heat exchange system concerning a 2nd embodiment of the present invention. It is a typical systematic diagram of the absorption-type heat exchange system concerning a 3rd embodiment of the present invention. It is a typical systematic diagram of an absorption-type heat exchange system concerning a 4th embodiment of the present invention. It is a typical systematic diagram of the absorption-type heat exchange system concerning a 5th embodiment of the present invention. It is a typical systematic diagram of an absorption-type heat exchange system concerning a 6th embodiment of the present invention. It is a schematic block diagram of the absorption-type heat exchange system which concerns on the modification of the 1st Embodiment of this invention. It is a schematic block diagram of the absorption-type heat exchange system which concerns on another modification of the 1st Embodiment of this invention. It is a typical systematic diagram of the absorption type heat exchange system concerning a 7th embodiment of the present invention. It is a typical systematic diagram of the absorption type heat exchange system concerning an 8th embodiment of the present invention.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings. In each of the drawings, the same or corresponding members are denoted by the same or similar reference numerals, and the redundant description will be omitted.

  First, an absorption heat exchange system 1 according to a first embodiment of the present invention will be described with reference to FIG. FIG. 1 is a schematic system diagram of the absorption type heat exchange system 1. The absorption type heat exchange system 1 utilizes the absorption heat pump cycle of the absorption liquid and the refrigerant, and the temperature of the temperature rising target fluid RP flowing out of the absorption type heat exchange system 1 toward the heat utilization device HCF is a driving heat source It is a system which carries out heat transfer so that it may become higher than temperature of driving heat-source fluid RS which flows into absorption type heat exchange system 1. Here, the temperature raising target fluid RP is a fluid whose temperature is to be raised in the absorption type heat exchange system 1, and corresponds to a first heated fluid. The driving heat source fluid RS is a fluid whose temperature is reduced in the absorption heat exchange system 1 and corresponds to a heating source fluid. The absorption type heat exchange system 1 includes a first absorber A1, a second absorber A2, a first evaporator E1, a second evaporator E2 and a first device constituting main devices in which an absorption heat pump cycle of an absorption liquid and a refrigerant is performed. The first regenerator G1, the second regenerator G2, the first condenser C1, and the second condenser C2 are provided.

In the present specification, in order to facilitate the distinction on the heat pump cycle regarding the absorbing liquid, “dilute solution Sw”, “first dilute solution Sw1”, “concentrated solution Sa” according to the property or the position on the heat pump cycle. And “the second concentrated solution Sa2”, etc., but when the property etc. are unquestioned, it is collectively referred to as “the absorbing solution S”. Similarly, regarding the refrigerant, in order to facilitate the distinction on the heat pump cycle, the “first evaporator refrigerant vapor Ve1”, the “second regenerator refrigerant vapor Vg2”, the refrigerant according to the property or the position on the heat pump cycle The liquid is referred to as “liquid Vf”, “first refrigerant liquid Vf1” or the like, but when the property or the like is irrelevant, it is collectively referred to as “refrigerant V”. In the present embodiment, an LiBr aqueous solution is used as the absorbent S (a mixture of an absorbent and a refrigerant V), and water (H ₂ O) is used as the refrigerant V.

  The first absorber A1 is a device that absorbs the first evaporator refrigerant vapor Ve1 generated in the first evaporator E1 with the concentrated solution Sa, and corresponds to a first absorption unit. The first absorber A1 includes a first absorption heat transfer tube 11 constituting a flow passage of the temperature raising target fluid RP, and a first absorber solution supply device 12 for supplying the concentrated solution Sa to the surface of the first absorption heat transfer tube 11. Internally. In the first absorber A1, the concentrated solution Sa is supplied from the first absorber solution supply device 12 to the surface of the first absorption heat transfer tube 11, and the concentrated solution Sa absorbs the first evaporator refrigerant vapor Ve1 to be a first dilution. The heat of absorption is generated when the solution Sw1 is obtained. The absorption heat is received by the temperature raising target fluid RP flowing through the first absorption heat transfer pipe 11, and the temperature raising target fluid RP is heated. One end of a first concentrated solution introduction pipe 13 for introducing the concentrated solution Sa is connected to the first absorber solution supply device 12. The lower end (typically the bottom) of the first absorber A1 is connected to one end of a first dilute solution outflow pipe 14 for discharging the stored first dilute solution Sw1.

  The first evaporator E1 is a device that evaporates the refrigerant liquid Vf with the heat of the drive heat source fluid RS to generate a first evaporator refrigerant vapor Ve1, and corresponds to a first evaporation unit. The first evaporator E1 has a first evaporation heat source pipe 21 constituting a flow path of the drive heat source fluid RS inside the can body of the first evaporator E1. The first evaporator E1 does not have a nozzle for dispersing the refrigerant liquid Vf inside the can body of the first evaporator E1. Therefore, the first evaporation heat source pipe 21 is disposed so as to be immersed in the refrigerant liquid Vf stored in the can barrel of the first evaporator E1 (full liquid evaporator). In the first evaporator E1, the refrigerant liquid Vf around the first evaporation heat source pipe 21 is evaporated by the heat of the driving heat source fluid RS flowing in the first evaporation heat source pipe 21 to generate the first evaporator refrigerant vapor Ve1. It is configured. One end of a first refrigerant liquid introduction pipe 23 for supplying the refrigerant liquid Vf to the inside is connected to the first evaporator E1.

  The first absorber A1 and the first evaporator E1 are accommodated in a first absorption evaporation can barrel (hereinafter referred to as "first absorption evaporation can barrel 10") so as to be horizontally adjacent to each other. Inside the first absorption evaporator cylinder 10, a first absorption evaporation wall 19 is provided which divides the internal space into two. Inside the first absorption evaporator cylinder 10, a first absorber A1 is provided on one side, and a first evaporator E1 is provided on the other side, with the first absorption / evaporation wall 19 interposed therebetween. The first absorber cylinder 10 on the first evaporator E1 side from the first absorber wall 19 constitutes the can cylinder of the first evaporator E1. The first absorbing and evaporating wall 19 is provided so as not to contact the top surface of the first absorbing and evaporating can barrel 10 so that the first absorber A1 and the first evaporator E1 communicate with each other at the top. That is, the first absorption and evaporation wall 19 is in contact with the first absorption and evaporation can barrel 10 at both side walls and the bottom excluding the top of the first absorption and evaporation can barrel 10. With such a configuration, the first evaporator refrigerant vapor Ve1 can be moved from the first evaporator E1 to the first absorber A1 in the first absorption evaporator cylinder 10.

  The second absorber A2 is a device for absorbing the second evaporator refrigerant vapor Ve2 generated in the second evaporator E2 with the concentrated solution Sa, and corresponds to a second absorption unit. The second absorber A2 includes a second absorption heat transfer pipe 15 that constitutes a flow passage of the temperature raising target fluid RP, and a second absorber solution supply device 16 that supplies the concentrated solution Sa to the surface of the second absorption heat transfer pipe 15. Internally. The second absorber A2 is configured in the same manner as the first absorber A1, and the second absorption heat transfer tube 15 and the second absorber solution supply device 16 respectively correspond to the first absorption heat transfer tube 11 and the first absorber solution. It corresponds to the supply device 12. In the second absorber A2, the concentrated solution Sa is supplied from the second absorber solution supply device 16 to the surface of the second absorption heat transfer tube 15, and the concentrated solution Sa absorbs the second evaporator refrigerant vapor Ve2 to obtain a second dilution. The heat of absorption is generated when the solution Sw2 is obtained. The absorption heat is received by the temperature raising target fluid RP flowing through the second absorption heat transfer pipe 15, and the temperature raising target fluid RP is heated. One end of the second absorption heat transfer pipe 15 and one end of the first absorption heat transfer pipe 11 are connected by a temperature-rising target communication pipe 71. One end of a second concentrated solution introduction pipe 17 for introducing the concentrated solution Sa is connected to the second absorber solution supply device 16. One end of a second dilute solution outflow pipe 18 for flowing out the stored second dilute solution Sw2 is connected to the lower portion (typically, the bottom portion) of the second absorber A2.

  The second evaporator E2 is a device that evaporates the refrigerant liquid Vf with the heat of the drive heat source fluid RS to generate a second evaporator refrigerant vapor Ve2, and corresponds to a second evaporation unit. The second evaporator E2 has a second evaporation heat source pipe 25 constituting a flow path of the drive heat source fluid RS inside the can body of the second evaporator E2. The second evaporator E2 is configured in the same manner as the first evaporator E1, and the second evaporation heat source pipe 25 corresponds to the first evaporation heat source pipe 21. In the second evaporator E2, the refrigerant liquid Vf around the second evaporation heat source pipe 25 is evaporated by the heat of the drive heat source fluid RS flowing in the second evaporation heat source pipe 25 to generate the second evaporator refrigerant vapor Ve2. It is configured. A heat source evaporation connection pipe 72 connects one end of the first evaporation heat source pipe 21 and one end of the second evaporation heat source pipe 25. One end of a second refrigerant liquid introduction pipe 27 for supplying the refrigerant liquid Vf to the inside is connected to the second evaporator E2.

  The second absorber A2 and the second evaporator E2 are accommodated in a second absorbing evaporator can body (hereinafter referred to as "the second absorbing evaporator can 20") so as to be horizontally adjacent to each other. Inside the second absorption evaporator cylinder 20, a second absorption evaporation wall 29 that divides the internal space into two is provided. Inside the second absorption evaporator cylinder 20, a second absorber A2 is provided on one side and a second evaporator E2 is provided on the other side, with the second absorption evaporation wall 29 interposed therebetween. The second absorber cylinder 20 on the side of the second absorber E2 from the second absorber wall 29 constitutes the can cylinder of the second evaporator E2. The second absorbing and evaporating wall 29 is provided not to contact the top surface of the second absorbing and evaporating can barrel 20 so that the second absorber A2 and the second evaporator E2 communicate with each other at the top. That is, the second absorbing and evaporating wall 29 is in contact with the second absorbing and evaporating can barrel 20 at both side walls and the bottom excluding the top of the second absorbing and evaporating can barrel 20. With such a configuration, the second evaporator refrigerant vapor Ve2 can be moved from the second evaporator E2 to the second absorber A2 in the second absorption evaporator cylinder 20.

  The first regenerator G1 is a device that heats and concentrates the dilute solution Sw, which is the absorbing solution S having a relatively low concentration, to concentrate the solution, and corresponds to a first regeneration unit. The first regenerator G1 supplies the first regeneration heat source pipe 31 to flow the driving heat source fluid RS for heating the dilute solution Sw, and the first regenerator solution supply that supplies the dilute solution Sw to the surface of the first regeneration heat source pipe 31. And a device 32. In the first regenerator G1, the dilute solution Sw supplied from the first regenerator solution supply device 32 is heated to the driving heat source fluid RS flowing in the first regeneration heat source pipe 31, whereby the refrigerant V is removed from the dilute solution Sw. It is configured to generate a first concentrated solution Sa1 of which concentration is increased by evaporation. The first regenerator G1 is configured to store the generated first concentrated solution Sa1 in the lower part. The refrigerant V evaporated from the dilute solution Sw is configured to move to the first condenser C1 as the first regenerator refrigerant vapor Vg1. One end of a first dilute solution introduction pipe 33 for introducing the dilute solution Sw is connected to the first regenerator solution supply device 32. The lower end (typically the bottom) of the first regenerator G1 is connected to one end of a first concentrated solution outflow pipe 34 for discharging the stored first concentrated solution Sa1. The first concentrated solution outflow pipe 34 is provided with a first concentrated solution pump 34 p for pressure-feeding the first concentrated solution Sa1.

  The first condenser C1 is a device that cools and condenses the first regenerator refrigerant vapor Vg1 generated in the first regenerator G1 with the low-temperature heat source fluid GP to form the first refrigerant liquid Vf1, and corresponds to the first condenser Do. The first condenser C1 has a first condensation heat transfer pipe 41 through which the low temperature heat source fluid GP flows, inside the can body of the first condenser C1. The first condenser C1 introduces the first regenerator refrigerant vapor Vg1 generated in the first regenerator G1, and condenses the heat of condensation released when it condenses and becomes the first refrigerant liquid Vf1, the first condensation heat transfer pipe The low temperature heat source fluid GP flowing in the heat source 41 receives heat to heat the low temperature heat source fluid GP so that the temperature rises. The low temperature heat source fluid GP corresponds to a second heated fluid. One end of a first refrigerant liquid outflow pipe 44 for flowing out the stored first refrigerant liquid Vf1 is connected to the lower portion (typically the bottom portion) of the first condenser C1. In the first refrigerant liquid outflow pipe 44, a first refrigerant liquid pump 44p for pressure-feeding the first refrigerant liquid Vf1 is disposed.

  The first regenerator G1 and the first condenser C1 are accommodated in a first regenerated condensing can barrel (hereinafter referred to as "first regenerated condensing can barrel 30") so as to be adjacent to each other in the horizontal direction. Inside the first regenerative condensing can body 30, a first regenerative condensing wall 39 which divides the internal space into two is provided. In the first regeneration condenser cylinder 30, a first regenerator G1 is provided on one side and a first condenser C1 is provided on the other side, with the first regeneration condensing wall 39 interposed therebetween. The first regenerative condenser can barrel 30 on the first condenser C1 side from the first regenerative condensing wall 39 constitutes a can barrel of the first condenser C1. The first regeneration condensing wall 39 is provided so as not to contact the top surface of the first regeneration condensing can barrel 30 so that the first regenerator G1 and the first condenser C1 communicate with each other at the top. That is, the first regeneration condensing wall 39 is in contact with the first regeneration condensing can barrel 30 at both side walls and the bottom excluding the top of the first regeneration condensing can barrel 30. With such a configuration, the first regenerator refrigerant vapor Vg1 can be moved from the first regenerator G1 to the first condenser C1 in the first regeneration condenser can barrel 30.

  The second regenerator G2 is a device that heats and concentrates the dilute solution Sw to regenerate in a concentrated manner, and corresponds to a second regenerating unit. The second regenerator G2 supplies the second regeneration heat source pipe 35 for flowing the driving heat source fluid RS for heating the dilute solution Sw and the second regenerator solution supply for supplying the dilute solution Sw to the surface of the second regeneration heat source pipe 35 And an apparatus 36. The second regenerator G2 is configured in the same manner as the first regenerator G1, and the second regeneration heat source pipe 35 and the second regenerator solution supply device 36 are respectively the first regeneration heat source pipe 31 and the first regenerator solution. It corresponds to the supply device 32. In the second regenerator G2, the dilute solution Sw supplied from the second regenerator solution supply device 36 is heated to the driving heat source fluid RS flowing in the second regeneration heat source pipe 35, whereby the refrigerant V is removed from the dilute solution Sw. It is configured to generate a second concentrated solution Sa2 of which concentration is increased by evaporation. The second regenerator G2 is configured to store the generated second concentrated solution Sa2 in the lower part. The refrigerant V evaporated from the dilute solution Sw is configured to move to the second condenser C2 as a second regenerator refrigerant vapor Vg2. One end of the second regeneration heat source pipe 35 and one end of the first regeneration heat source pipe 31 are connected by a heat source regeneration communication pipe 73. One end of a second dilute solution introduction pipe 37 for introducing the dilute solution Sw is connected to the second regenerator solution supply device 36. The lower end (typically the bottom) of the second regenerator G2 is connected to one end of a second concentrated solution outflow pipe 38 for flowing out the stored second concentrated solution Sa2. The second concentrated solution outlet pipe 38 is provided with a second concentrated solution pump 38p for pressure-feeding the second concentrated solution Sa2.

  The second condenser C2 is an apparatus for cooling and condensing the second regenerator refrigerant vapor Vg2 generated in the second regenerator G2 with the low temperature heat source fluid GP to obtain the second refrigerant liquid Vf2, and corresponds to the second condenser Do. The second condenser C2 has a second condensation heat transfer pipe 45 through which the low temperature heat source fluid GP flows, inside the can body of the second condenser C2. The second condenser C2 is configured in the same manner as the first condenser C1, and the second condensation heat transfer pipe 45 corresponds to the first condensation heat transfer pipe 41. The second condenser C2 introduces the second regenerator refrigerant vapor Vg2 generated in the second regenerator G2, and condenses the heat of condensation released when it condenses and becomes the second refrigerant liquid Vf2, a second condensation heat transfer pipe The low temperature heat source fluid GP flowing in the heat source 45 receives the heat, and the low temperature heat source fluid GP is configured to be heated and the temperature rises. One end of the second condensation heat transfer pipe 45 and one end of the first condensation heat transfer pipe 41 are connected by a low temperature heat source connection pipe 74. One end of a second refrigerant liquid outflow pipe 48 for flowing out the stored second refrigerant liquid Vf2 is connected to the lower portion (typically the bottom) of the second condenser C2. A second refrigerant liquid pump 48p for pressure-feeding the second refrigerant liquid Vf2 is disposed in the second refrigerant liquid outflow pipe 48.

  The second regenerator G <b> 2 and the second condenser C <b> 2 are accommodated in a second regeneration condenser can (hereinafter, referred to as “second regeneration condenser can 40”) so as to be horizontally adjacent to each other. Inside the second regenerative condenser cylinder 40, a second regenerative condensing wall 49 is provided which divides the internal space into two. Inside the second regenerative condenser cylinder 40, a second regenerator G2 is provided on one side and a second condenser C2 is provided on the other side, with the second regenerative condensing wall 49 interposed therebetween. The second regenerative condenser cylinder 40 on the second condenser C2 side from the second regenerative condenser wall 49 constitutes the can cylinder of the second condenser C2. The second regeneration condenser wall 49 is provided so as not to contact the top surface of the second regeneration condenser cylinder 40 so that the second regenerator G2 and the second condenser C2 communicate with each other at the top. That is, the second regeneration condensing wall 49 is in contact with the second regeneration condensing can barrel 40 at both side walls and the bottom excluding the top of the second regeneration condensing can barrel 40. With such a configuration, the second regenerator refrigerant vapor Vg2 can be moved from the second regenerator G2 to the second condenser C2 in the second regeneration condenser can 40.

  In the present embodiment, the temperature rising fluid outflow pipe 53 is provided at the end of the first absorption heat transfer pipe 11 of the first absorber A1 opposite to the end to which the one end of the temperature rising communication pipe 71 is connected. Is connected. The temperature rising fluid outflow pipe 53 is a pipe that constitutes a flow path through which the heated temperature raising target fluid RP flows. Further, the temperature rising fluid introduction pipe 51 is connected to the end of the second absorption heat transfer pipe 15 of the second absorber A2 on the opposite side to the end to which the one end of the temperature rising connection pipe 71 is connected. There is. The temperature raising fluid introduction pipe 51 is a pipe that constitutes a flow path through which the temperature raising target fluid RP before being heated flows. Further, an end of the first evaporation heat source pipe 21 of the first evaporator E1 opposite to the end to which one end of the heat source evaporation communication pipe 72 is connected, and a second regeneration heat source pipe 35 of the second regenerator G2. The heat source regenerating communication pipe 73 is connected to the end opposite to the end to which the one end of the heat source regenerating communication pipe 73 is connected via the heat source evaporation regenerating communication pipe 75. A drive heat source outflow pipe 56 is connected to an end of the second evaporation heat source pipe 25 of the second evaporator E2 opposite to the end to which one end of the heat source evaporation connection pipe 72 is connected. The driving heat source outflow pipe 56 is a pipe which constitutes a flow path for flowing the driving heat source fluid RS which is used as a heat source and whose temperature is lowered.

  A drive heat source introduction pipe 52 is connected to an end of the first regeneration heat source pipe 31 of the first regenerator G1 on the opposite side to the end to which one end of the heat source regeneration communication pipe 73 is connected. The driving heat source introduction pipe 52 is a pipe that constitutes a flow path for guiding the driving heat source fluid RS before the temperature is lowered. The drive heat source introduction pipe 52 is provided with a drive heat source valve 52v that adjusts the flow rate of the drive heat source fluid RS flowing inside. The other end of the drive heat source introduction pipe 52 is connected to the heat source fluid inflow pipe 55 together with the other end of the temperature increasing fluid introduction pipe 51. The heat source fluid inflow pipe 55 is a pipe that constitutes a flow path through which the combined heat source fluid RA flows. The combined heat source fluid RA flowing through the heat source fluid inflow pipe 55 is configured to be branched and flow into the temperature raising fluid introduction pipe 51 and the drive heat source introduction pipe 52. That is, the temperature raising target fluid RP flows into the temperature rising fluid introduction pipe 51 of the combined heat source fluid RA, and the driving heat source fluid RS flows into the driving heat source introduction pipe 52 of the combined heat source fluid RA It is a thing. The temperature raising fluid introduction pipe 51 is provided with a temperature raising fluid valve 51v for adjusting the flow rate of the temperature raising target fluid RP flowing inside.

  Further, a flow passage for flowing the low-temperature heat source fluid GP is configured at the end opposite to the end to which the one end of the low-temperature heat source communication tube 74 is connected of the first condensation heat transfer tube 41 of the first condenser C1. One end of the low temperature heat source outflow pipe 58 is connected. The other end of the low temperature heat source outflow pipe 58 is connected to the heat source fluid outflow pipe 59 together with the other end of the drive heat source outflow pipe 56. The heat source fluid outflow pipe 59 is a pipe constituting a flow path through which the combined heat source fluid RA in which the driving heat source fluid RS flowing through the driving heat source outflow pipe 56 and the low temperature heat source fluid GP flowing through the low temperature heat source outflow pipe 58 join . Further, the low temperature heat source fluid GP before being heated is allowed to flow through the end of the second condensation heat transfer pipe 45 of the second condenser C2 on the opposite side to the end to which the end of the low temperature heat source connection pipe 74 is connected. A low temperature heat source introduction pipe 57 which constitutes a flow path is connected.

  Further, in the present embodiment, the other end of the first dilute solution outflow pipe 14 and the other end of the second dilute solution outflow pipe 18 are connected to one end of the dilute solution merging pipe 61. The other end of the first dilute solution introduction pipe 33 and the other end of the second dilute solution introduction pipe 37 are connected to the other end of the dilute solution merging pipe 61. With such a configuration, the first dilute solution Sw1 flowing out of the first absorber A1 and the second dilute solution Sw2 flowing out of the second absorber A2 join together and flow as the dilute solution Sw through the dilute solution merging pipe 61 After that, the dilute solution Sw is configured to flow in parallel to the first regenerator G1 and the second regenerator G2, respectively. Thus, in the present embodiment, each of the first regenerator G1 and the second regenerator G2 is configured to directly introduce the diluted solution Sw from the first absorber A1 and the second absorber A2. . Here, direct introduction means introduction without passing through other devices of the main devices constituting the absorption heat pump cycle.

  Further, in the present embodiment, the other end of the first concentrated solution outflow pipe 34 and the other end of the second concentrated solution outflow pipe 38 are connected to one end of the concentrated solution merging pipe 63. The other end of the first concentrated solution introduction pipe 13 and the other end of the second concentrated solution introduction pipe 17 are connected to the other end of the concentrated solution joining pipe 63. With such a configuration, the first concentrated solution Sa1 flowing out of the first regenerator G1 and the second concentrated solution Sa2 flowing out of the second regenerator G2 join together and flowed through the concentrated solution merging pipe 63 as a concentrated solution Sa After that, the concentrated solution Sa flows in parallel into the first absorber A1 and the second absorber A2. Thus, in the present embodiment, each of the first absorber A1 and the second absorber A2 is configured to directly introduce the concentrated solution Sa from the first regenerator G1 and the second regenerator G2. . The dilute solution merging pipe 61 and the concentrated solution merging pipe 63 are provided with a solution heat exchanger 62 for performing heat exchange between the dilute solution Sw and the concentrated solution Sa.

  Further, in the present embodiment, the other end of the first refrigerant liquid outflow pipe 44 and the other end of the second refrigerant liquid outflow pipe 48 are connected to one end of the refrigerant liquid merging pipe 64. The other end of the first refrigerant liquid introduction pipe 23 and the other end of the second refrigerant liquid introduction pipe 27 are connected to the other end of the refrigerant liquid junction pipe 64. With such a configuration, the first refrigerant liquid Vf1 flowing out of the first condenser C1 and the second refrigerant liquid Vf2 flowing out of the second condenser C merge and flow through the refrigerant liquid merging pipe 64 as the refrigerant liquid Vf After that, the refrigerant liquid Vf flows in parallel to the first evaporator E1 and the second evaporator E2. Thus, in the present embodiment, each of the first evaporator E1 and the second evaporator E2 is configured to directly introduce the refrigerant liquid Vf from the first condenser C1 and the second condenser C2. .

  In the example shown in FIG. 1, the first absorption evaporator cylinder 10, the second absorption evaporator cylinder 20, the first regeneration condenser cylinder 30, and the second regeneration condenser cylinder 40 are vertically arranged in the horizontal state. The first regeneration condensing can barrel 30, the second regeneration condensing can barrel 40, the first absorption evaporation can barrel 10, and the second absorption evaporation can barrel 20 are vertically stacked in a row. It is arranged in order. Actually, the arrangement as shown in FIG. 1 may be used, but since FIG. 1 is a schematic system diagram, the arrangement of each device may be changed as appropriate after leaving the connection relationship of the fluid flow path as it is. . It is sufficient if the above-mentioned piping installation space can be secured between the respective can bodies.

  In the absorption type heat exchange system 1, the pressure and temperature inside the first absorber A1 become higher than the pressure and temperature inside the first regenerator G1 during steady operation, and the pressure and temperature inside the second absorber A2 The temperature is higher than the internal pressure and temperature of the second regenerator G2, the internal pressure and temperature of the first evaporator E1 is higher than the internal pressure and temperature of the first condenser C1, and the second evaporator The pressure and temperature inside E2 will be higher than the pressure and temperature inside the second condenser C2. The absorption type heat exchange system 1 includes a first absorber A1, a first evaporator E1, a second absorber A2, a second evaporator E2, a first regenerator G1, a first condenser C1, a second regenerator G2, The second condenser C2 is a configuration of a type 2 absorption heat pump.

  The heat source fluid inflow pipe 55 and the heat source fluid outflow pipe 59 are connected to the heat source equipment HSF in the present embodiment. The heat source equipment HSF is equipment that recovers the exhaust heat from, for example, a steel mill or a power plant. In the present embodiment, the heat source equipment HSF heats the combined heat source fluid RA taken from the heat source fluid outlet pipe 59 with exhaust heat to raise the temperature, and supplies the heat source fluid inlet pipe 55 with heat. The temperature rising fluid outflow pipe 53 and the low temperature heat source introduction pipe 57 are connected to the heat utilization facility HCF in the present embodiment. The heat utilization facility HCF uses, for example, the introduced heat for heating or as a heat source of other heat source equipment such as an absorption refrigerator or absorption heat pump. In the present embodiment, the heat utilization facility HCF takes advantage of the heat possessed by the temperature raising target fluid RP introduced from the temperature raising fluid outflow pipe 53, and deprives the heat from the temperature raising target fluid RP so that the temperature is lowered. It flows out to the low temperature heat source introduction pipe 57 as the low temperature heat source fluid GP.

  Continuing to refer to FIG. 1, the operation of the absorptive heat exchange system 1 will be described. First, the absorption heat pump cycle on the refrigerant side will be described. In the first condenser C1, the first regenerator refrigerant vapor Vg1 evaporated in the first regenerator G1 is received, and the first regenerator refrigerant vapor Vg1 is cooled by the low temperature heat source fluid GP flowing through the first condensation heat transfer pipe 41 It condenses and it becomes the 1st refrigerant fluid Vf1. At this time, the temperature of the low temperature heat source fluid GP is increased by the heat of condensation released when the first regenerator refrigerant vapor Vg1 is condensed. The condensed first refrigerant liquid Vf1 is pressure-fed to the first refrigerant liquid pump 44p and flows through the first refrigerant liquid outflow pipe 44. In the second condenser C2, the second regenerator refrigerant vapor Vg2 evaporated in the second regenerator G2 is received, and the low temperature heat source fluid GP flowing through the second condensation heat transfer pipe 45 cools the second regenerator refrigerant vapor Vg2 It condenses and it becomes the 2nd refrigerant fluid Vf2. At this time, the temperature of the low temperature heat source fluid GP is increased by the heat of condensation released when the second regenerator refrigerant vapor Vg2 is condensed. In the present embodiment, since the low temperature heat source fluid GP flows through the second condensation heat transfer pipe 45 and then flows through the first condensation heat transfer pipe 41 via the low temperature heat source connection pipe 74, it flows through the first condensation heat transfer pipe 41. The temperature of the first condenser C1 is higher than the temperature of the second condenser heat transfer pipe 45, and the internal pressure of the first condenser C1 is higher than the internal pressure of the second condenser C2. The condensed second refrigerant liquid Vf2 is pressure-fed to the second refrigerant liquid pump 48p and flows through the second refrigerant liquid outflow pipe 48. The first refrigerant liquid Vf1 flowing through the first refrigerant liquid outflow pipe 44 and the second refrigerant liquid Vf2 flowing through the second refrigerant liquid outflow pipe 48 respectively flow into the refrigerant liquid merging pipe 64 and are mixed to become the refrigerant liquid Vf. The refrigerant liquid Vf in the refrigerant liquid junction pipe 64 is branched to the first refrigerant liquid introduction pipe 23 and the second refrigerant liquid introduction pipe 27. The refrigerant liquid flowing through the first refrigerant liquid introduction pipe 23 flows into the first evaporator E1. On the other hand, the refrigerant liquid flowing through the second refrigerant liquid introduction pipe 27 flows into the second evaporator E2.

  The refrigerant liquid Vf which has flowed into the first evaporator E1 is heated by the driving heat source fluid RS flowing through the first evaporation heat source pipe 21 and is evaporated to be the first evaporator refrigerant vapor Ve1. At this time, the driving heat source fluid RS flowing in the first evaporation heat source pipe 21 is deprived of heat by the refrigerant liquid Vf and the temperature is lowered. The first evaporator refrigerant vapor Ve1 generated in the first evaporator E1 moves to a first absorber A1 in communication with the first evaporator E1. On the other hand, the refrigerant liquid Vf which has flowed into the second evaporator E2 is heated by the driving heat source fluid RS flowing through the second evaporation heat source pipe 25 and is evaporated to become the second evaporator refrigerant vapor Ve2. At this time, the driving heat source fluid RS flowing in the second evaporation heat source pipe 25 is deprived of heat by the refrigerant liquid Vf and the temperature is lowered. The second evaporator refrigerant vapor Ve2 generated in the second evaporator E2 moves to a second absorber A2 in communication with the second evaporator E2. Since the drive heat source fluid RS flows through the first evaporation heat source pipe 21 and then flows through the second evaporation heat source pipe 25 via the heat source evaporation communication pipe 72, the temperature when flowing through the first evaporation heat source pipe 21 is The internal pressure of the first evaporator E1 becomes higher than the internal pressure of the second evaporator E2 because the temperature is higher than the temperature when flowing through the second evaporation heat source pipe 25.

  The solution side absorption heat pump cycle will now be described. In the first absorber A1, the concentrated solution Sa is supplied from the first absorber solution supply device 12, and the supplied concentrated solution Sa absorbs the first evaporator refrigerant vapor Ve1 transferred from the first evaporator E1. . The concentrated solution Sa that has absorbed the first evaporator refrigerant vapor Ve1 is reduced in concentration to become the first dilute solution Sw1. In the first absorber A1, absorption heat is generated when the concentrated solution Sa absorbs the first evaporator refrigerant vapor Ve1. By this absorbed heat, the temperature raising target fluid RP flowing through the first absorption heat transfer pipe 11 is heated, and the temperature of the temperature rising target fluid RP rises. The first dilute solution Sw1 in which the concentration is reduced from the first concentrated solution Sa1 by absorbing the first evaporator refrigerant vapor Ve1 is stored in the lower part of the first absorber A1.

  In the second absorber A2, the concentrated solution Sa is supplied from the second absorber solution supply device 16, and the supplied concentrated solution Sa absorbs the second evaporator refrigerant vapor Ve2 transferred from the second evaporator E2. . The concentrated solution Sa that has absorbed the second evaporator refrigerant vapor Ve2 is reduced in concentration to become the second dilute solution Sw2. In the second absorber A2, absorption heat is generated when the concentrated solution Sa absorbs the second evaporator refrigerant vapor Ve2. By this absorbed heat, the temperature raising target fluid RP flowing through the second absorption heat transfer pipe 15 is heated, and the temperature of the temperature rising target fluid RP rises. In the present embodiment, the temperature raising target fluid RP flowing through the second absorption heat transfer pipe 15 is the same combined heat source as the source of the driving heat source fluid RS introduced into the first regenerative heat source pipe 31 of the first regenerator G1. It is fluid RA. Therefore, the heating target fluid RP flowing out of the second absorber A2 and flowing through the heating target communication pipe 71 flows into the first regenerator G1 as much as it is heated by the second absorber A2. The temperature is higher than that. Further, since the temperature raising target fluid RP flows through the second absorption heat transfer pipe 15 and then flows through the first absorption heat transfer pipe 11 via the temperature raising target connection pipe 71, it flows out from the first absorber A1 and raises the temperature The temperature when flowing through the fluid outflow pipe 53 becomes higher than the temperature when flowing through the heating target communication pipe 71, and the temperature raising target fluid RP can be further heated. The second dilute solution Sw2 in which the concentration is reduced from the concentrated solution Sa by absorbing the second evaporator refrigerant vapor Ve2 is stored in the lower part of the second absorber A2.

  The first dilute solution Sw1 generated in the first absorber A1 flows out to the first dilute solution outflow pipe 14, and the second dilute solution Sw2 generated in the second absorber A2 flows out to the second dilute solution outflow pipe 18 Do. The first dilute solution Sw1 flowing through the first dilute solution outflow pipe 14 and the second dilute solution Sw2 flowing through the second dilute solution outflow pipe 18 respectively flow into the dilute solution joining pipe 61 and are mixed to become a dilute solution Sw. The dilute solution Sw flowing through the dilute solution merging pipe 61 exchanges heat with the concentrated solution Sa in the solution heat exchanger 62 to lower its temperature, and then divided into the first dilute solution introduction pipe 33 and the second dilute solution introduction pipe 37. Do. The dilute solution Sw flowing through the first dilute solution introduction pipe 33 is supplied from the first regenerator solution supply device 32 into the first regenerator G1. On the other hand, the dilute solution Sw flowing through the second dilute solution introduction pipe 37 is supplied from the second regenerator solution supply device 36 into the second regenerator G2.

  In the first regenerator G1, the dilute solution Sw supplied from the first regenerator solution supply device 32 is heated by the driving heat source fluid RS flowing through the first regeneration heat source pipe 31, and the refrigerant in the supplied dilute solution Sw is It evaporates and it becomes 1st concentration solution Sa1, and is stored by the lower part of the 1st regenerator G1. At this time, the driving heat source fluid RS flowing in the first regeneration heat source pipe 31 is deprived of heat by the dilute solution Sw and the temperature is lowered. The refrigerant evaporated from the dilute solution Sw moves to the first condenser C1 as the first regenerator refrigerant vapor Vg1. On the other hand, in the second regenerator G2, the dilute solution Sw supplied from the second regenerator solution supply device 36 is heated by the drive heat source fluid RS flowing through the second regeneration heat source pipe 35, and the diluted solution Sw is supplied. The refrigerant evaporates to be the second concentrated solution Sa2, and is stored in the lower part of the second regenerator G2. At this time, the driving heat source fluid RS flowing in the second regeneration heat source pipe 35 is deprived of heat by the dilute solution Sw and the temperature is lowered. The refrigerant evaporated from the dilute solution Sw moves to the second condenser C2 as the second regenerator refrigerant vapor Vg2.

  The first concentrated solution Sa1 generated in the first regenerator G1 flows out to the first concentrated solution outlet pipe 34, and the second concentrated solution Sa2 generated in the second regenerator G2 flows out to the second concentrated solution outlet pipe 38 Do. The first concentrated solution Sa1 which is pumped to the first concentrated solution pump 34p and flows through the first concentrated solution outlet pipe 34 and the second concentrated solution Sa2 which is pumped to the second concentrated solution pump 38p and flows through the second concentrated solution outlet pipe 38 Each flows into the concentrated solution merging pipe 63 and is mixed to form a concentrated solution Sa. The concentrated solution Sa in the concentrated solution merging pipe 63 exchanges heat with the dilute solution Sw in the solution heat exchanger 62 and the temperature rises, and then it is divided into the first concentrated solution introduction pipe 13 and the second concentrated solution introduction pipe 17 Do. The concentrated solution Sa flowing through the first concentrated solution introduction pipe 13 is supplied from the first absorber solution supply device 12 into the first absorber A1, and the above-mentioned cycle is repeated thereafter. On the other hand, the concentrated solution Sa flowing through the second concentrated solution introduction pipe 17 is supplied from the second absorber solution supply device 16 into the second absorber A2, and the above-mentioned cycle is repeated thereafter.

  The changes in the temperatures of the fluid to be heated and the heat source fluid in the process of performing the absorption heat pump cycle as described above by the absorbent S and the refrigerant V will be described by way of specific examples. The 95 ° C. combined heat source fluid RA flowing out of the heat source equipment HSF and flowing through the heat source fluid inflow pipe 55 is 95 ° C. for the temperature-raising target fluid RP and the driving heat source fluid RS respectively divided. The driving heat source fluid RS at 95 ° C. flowing through the driving heat source introduction pipe 52 loses heat by the dilute solution Sw when flowing through the first regeneration heat source pipe 31 of the first regenerator G 1 and reaches the heat source regeneration communication pipe 73 And the temperature drops to 90 ° C. Thereafter, the driving heat source fluid RS flowing through the heat source regeneration communication pipe 73 is deprived of heat by the dilute solution Sw when flowing through the second regeneration heat source pipe 35 of the second regenerator G2, and reaches the heat source evaporation regeneration communication pipe 75 And the temperature drops to 85 ° C. Thereafter, the drive heat source fluid RS flowing through the heat source evaporation regeneration communication tube 75 is deprived of heat by the refrigerant liquid Vf when flowing through the first evaporation heat source pipe 21 of the first evaporator E1 and reaches the heat source evaporation communication tube 72 And the temperature drops to 80 ° C. Thereafter, when the driving heat source fluid RS flowing through the heat source evaporation connection pipe 72 flows through the second evaporation heat source pipe 25 of the second evaporator E2, the refrigerant liquid Vf loses heat and reaches the driving heat source outflow pipe 56 The temperature drops to 75 ° C.

  On the other hand, when the temperature raising target fluid RP flowing through the temperature raising fluid introduction pipe 51 flows through the second absorption heat transfer pipe 15 of the second absorber A2, the concentrated solution Sa absorbs the second evaporator refrigerant vapor Ve2 The temperature rises to 100 ° C. when it reaches the temperature-raising target communication pipe 71 by obtaining the absorbed heat generated. Thereafter, when the temperature raising target fluid RP flowing through the temperature raising target communication pipe 71 flows through the first absorption heat transfer pipe 11 of the first absorber A1, the concentrated solution Sa absorbs the first evaporator refrigerant vapor Ve1. The temperature rises to 105 ° C. when it reaches the temperature rising fluid outlet pipe 53 by obtaining the absorbed heat generated. At this time, since the temperature of the drive heat source fluid RS flowing through the first evaporator E1 is higher than the temperature of the drive heat source fluid RS flowing through the second evaporator E2, the internal pressure of the second evaporator E2 and the second absorber A2 and The temperature becomes lower than the internal pressure and temperature of the first evaporator E1 and the first absorber A1, and when the temperature raising target fluid RP is introduced in order of the second absorber A2 to the first absorber A1, each absorber A2, The temperature of the temperature raising target fluid RP heated and heated in A1 can be sequentially raised. The temperature raising target fluid RP of 105 ° C. flowing through the temperature raising fluid outflow pipe 53 flows into the heat utilization facility HCF, heat is utilized, and the temperature is lowered. The fluid whose temperature has been reduced by the use of heat in the heat utilization facility HCF flows out to the low temperature heat source inlet pipe 57 as a low temperature heat source fluid GP of 32 ° C. When the 32 ° C. low temperature heat source fluid GP flowing through the low temperature heat source introduction pipe 57 flows through the second condensing heat transfer pipe 45 of the second condenser C2, the second regenerator refrigerant vapor Vg2 condenses and becomes the refrigerant liquid Vf The temperature of the low temperature heat source communication pipe 74 is increased to 37 ° C. Thereafter, when the low temperature heat source fluid GP flowing through the low temperature heat source communication pipe 74 flows through the first condensing heat transfer pipe 41 of the first condenser C1, the first regenerator refrigerant vapor Vg1 condenses and becomes the refrigerant liquid Vf. The heat of condensation released to the low temperature heat source outlet pipe 58 is raised to a temperature of 42.degree.

  The 42 ° C. low temperature heat source fluid GP flowing through the low temperature heat source outflow pipe 58 mixes with the 75 ° C. driving heat source fluid RS flowing through the driving heat source outflow pipe 56 to become a 59 ° C. combined heat source fluid RA Flow. In the present embodiment, by mixing the low temperature heat source fluid GP of the low temperature heat source outflow pipe 58 and the driving heat source fluid RS of the driving heat source outflow pipe 56, the heated fluid and the heat source fluid entering and exiting the absorption heat exchange system 1 are We are trying to balance the flow rate. The 59 ° C. combined heat source fluid RA flowing through the heat source fluid outflow pipe 59 flows into the heat source facility HSF, recovers the exhaust heat, and the temperature rises. The combined heat source fluid RA whose temperature has risen in the heat utilization facility HCF flows out to the heat source fluid inflow pipe 55 at 95 ° C., and thereafter the above-described flow is repeated.

  In the absorption type heat exchange system 1, the temperature of the temperature raising target fluid RP that has flowed out of the first absorber A1 is set to a predetermined temperature (at a temperature suitable for use in the heat utilization facility HCF) by establishing the above-described temperature relationship. In the present embodiment, the ratio of the flow rate of the temperature raising target fluid RP flowing through the temperature raising fluid introduction pipe 51 to the flow rate of the driving heat source fluid RS flowing through the driving heat source introduction pipe 52 is determined so as to be 105.degree. It is good to do. In the present embodiment, the flow ratio of the temperature raising target fluid RP and the driving heat source fluid RS is approximately 1: 1. The temperature of the temperature rising fluid RP rises relatively if the flow rate of the temperature rising fluid RP is decreased, and the temperature of the temperature rising fluid RP decreases if the flow rate of the temperature rising fluid RP is increased. Here, the flow rate ratio between the temperature raising target fluid RP flowing through the temperature raising fluid introducing pipe 51 and the driving heat source fluid RS flowing through the driving heat source introducing pipe 52 is a storage device (not shown) provided in the control device (not shown). It may be set in advance, or may be set as needed by an input device (not shown) provided in the control device. In the present embodiment, the flow rate ratio between the temperature raising target fluid RP and the driving heat source fluid RS is adjusted by adjusting the opening degrees of the heating fluid valve 51v and the driving heat source valve 52v. The adjustment of the opening degree of the temperature raising fluid valve 51v and the drive heat source valve 52v is typically performed automatically by a signal from the control device based on the flow ratio set in the above-described control device, but the control device Alternatively, the opening may be adjusted manually. A three-way valve may be provided at the connection between the temperature increasing fluid inlet pipe 51, the driving heat source inlet pipe 52, and the heat source fluid inflow pipe 55 instead of the temperature increasing fluid valve 51v and the driving heat source valve 52v.

  An overview of the flow of the heat source fluid (combined heat source fluid RA) and the fluid to be heated (the temperature raising target fluid RP, the low temperature heat source fluid GP) which flows into and out of the absorption heat exchange system 1 described above In the heat exchange system 1, the combined heat source fluid RA flowing out of the heat source equipment HSF and flowing into the absorption heat exchange system 1 at 95.degree. C. flows out of the absorption heat exchange system 1 at 59.degree. C. and flows into the heat source equipment HSF. The low-temperature heat source fluid GP that has flowed out of the heat utilization facility HCF into the absorption heat exchange system 1 at 32 ° C. flows out from the absorption heat exchange system 1 at 105 ° C. as the temperature rising fluid RP and is used as a heat utilization facility It is flowing into HCF. When the combined heat source fluid RA flowing into and out of the heat source equipment HSF is the heating source fluid, and the temperature raising target fluid RP flowing into and out of the heat utilizing device HCF and the low temperature heat source fluid GP are the heated fluid, absorption is observed. The heat exchange system 1 can be regarded as performing heat exchange between the heat source fluid and the fluid to be heated, and the fluid to be heated is the temperature of the heat source fluid from the temperature of the inflowing fluid to be heated. The amount of heat required to heat to a higher temperature can be viewed as a heat exchange system that flows out after being removed from the heating source fluid. As the temperature of the fluid to be heated (the fluid to be heated RP) flowing out of the absorption heat exchange system 1 is higher, the temperature difference between the inlet and outlet of the heating fluid with respect to the absorption heat exchange system 1 is greater than the temperature difference between the inlet and outlet of the heating source fluid. Can be expanded to reduce the flow rate of the fluid to be heated (the fluid RP to be heated). In the present embodiment, the flow ratio of the fluid to be heated to the heating source fluid is approximately 1: 2. Further, the flow rate of the combined heat source fluid RA flowing out of the absorption type heat exchange system 1 and flowing into the heat source equipment HSF and the flow rate of the combined heat source fluid RA flowing out of the heat source equipment HSF and flowing into the absorption type heat exchange system 1 are equal The flow rate of the temperature rising target fluid RP flowing out of the absorption heat exchange system 1 and flowing into the heat utilization equipment HCF and the flow rate of the low temperature heat source fluid GP flowing out of the heat utilization equipment HCF and flowing into the absorption heat exchange system 1 It is assumed that both the heating source fluid and the fluid to be heated flow into and out of the absorption heat exchange system 1 as an independent system partitioned within the absorption heat exchange system 1. It becomes clearer to see the absorption heat exchange system 1 as a heat exchanger. As shown in the present embodiment, the combined heat source fluid RA that has flowed out of the absorption heat exchange system 1 passes through the heat source equipment HSF and is heated, and then returns to the absorption heat exchange system 1, and the absorption heat exchange system It is preferable that the temperature raising target fluid RP that has flowed out of 1 passes through the heat utilization device HCF and is consumed after the heat is returned to the absorption heat exchange system 1 as the low temperature heat source fluid GP.

  It should be noted that, temporarily, the fluid (heated fluid) flowing into and out of the heat utilization facility HCF does not branch and merge with the fluid (heating source fluid) flowing in and out of the heat source facility HSF, The low temperature heat source fluid GP which has flowed through the second condensation heat transfer pipe 45 of the vessel C2 and the first condensation heat transfer pipe 41 of the first condenser C1 is transferred to the second absorption heat transfer pipe 15 of the second absorber A2 and the first of the first absorber A1. (1) In the case of an independent system so as to flow to the absorption heat transfer tube 11, the low temperature heat source fluid GP flowing through the first condensation heat transfer tube 41 of the first condenser C1 is used as the second absorption heat transfer tube 15 of the second absorber A2. Drive heat source fluid RS flowing out from both evaporators E1, E2 and both regenerators G1, G2 or drive heat source fluid RS before flowing into both evaporators E1, E2 and both regenerators G1, G2 and A heat exchanger is needed to exchange heat, heat and raise the temperature. On the other hand, as in the present embodiment, the fluid (heated fluid) flowing in and out of the heat utilization facility HCF is branched and merged with the fluid (heating source fluid) flowing in and out of the heat source facility HSF. Then, the heat exchanger provided in the case of the above assumption is not necessary, and the system configuration can be simplified. By eliminating the need for the heat exchanger provided in the above assumption, the heat efficiency of the heat exchanger can be avoided by avoiding the heat radiation loss from the heat exchanger and the temperature decrease of the fluid to be heated due to the heat exchange temperature efficiency being smaller than 1. Can be eliminated. Furthermore, the installation space of the heat exchanger, the piping for the fluid in and out of the heat exchanger, and maintenance work of the heat exchanger can be omitted. Furthermore, in the absorption type heat exchange system 1 according to the present embodiment, a fluid (heated fluid) having a temperature lower than the fluid (heating source fluid) flowing out to the heat source equipment HSF is introduced from the heat utilization equipment HCF, and the heat source equipment The fluid (heated fluid) having a temperature higher than the fluid (heating source fluid) introduced from the HSF can be discharged to the heat utilization facility HCF, and effective utilization of heat can be achieved, and the absorption heat exchange system 1 The inlet / outlet temperature difference of the fluid to be heated can be expanded to reduce the flow rate of the fluid to be heated.

  As described above, according to the absorption type heat exchange system 1 according to the present embodiment, the temperature raising target is such that the temperature of the temperature rising target fluid RP flowing out is higher than the temperature of the driving heat source fluid RS introduced. The fluid RP can be heated, and the temperature raising target fluid RP having higher utility value than the driving heat source fluid RS can be supplied to the outside. Further, since the first absorber A1 and the second absorber A2 are provided, it is possible to raise the temperature of the temperature raising target fluid RP compared to the case of one absorber. Also, the low temperature heat source fluid which is heated by the first absorber A1 and the second absorber A2 is branched from the combined heat source fluid RA and is heated by the first condenser C1 and the second condenser C2. Since the GP is joined to the drive heat source fluid RS which has passed both the evaporators E1 and E2 and the two regenerators G1 and G2, heat exchange between the drive heat source fluid RS and the low temperature heat source fluid GP does not occur. The device configuration can be simplified without providing a heat exchanger, and the temperature raising target fluid RP having a relatively high temperature can be supplied (outflowed). Further, the temperature of the low temperature heat source fluid GP flowing into the absorption heat exchange system 1 and the temperature of the temperature rising target fluid RP flowing out of the absorption heat exchange system 1 based on the inlet / outlet temperature difference of the combined heat source fluid RA flowing into and out of the absorption heat exchange system 1 And the flow rate of the temperature raising target fluid RP to be supplied to the heat utilization facility HCF can be reduced by the amount corresponding to the large temperature difference, so that the transfer power can be reduced. It is suitable for long distance transportation.

  Next, with reference to FIG. 2, an absorption heat exchange system 2 according to a second embodiment of the present invention will be described. FIG. 2 is a schematic system diagram of the absorption type heat exchange system 2. The absorption type heat exchange system 2 is compared with the absorption type heat exchange system 1 (see FIG. 1), and the flow of the absorption liquid S and the refrigerant V and the temperature rising target fluid RP, the low temperature heat source fluid GP, The order of the flow of the driving heat source fluid RS is different. Along with this, the configuration of the absorption type heat exchange system 2 is different from the configuration of the absorption type heat exchange system 1 (see FIG. 1) mainly in the following points. In the absorption type heat exchange system 2, the other end of the second dilute solution outflow pipe 18 for flowing the second dilute solution Sw2 flowing out from the second absorber A2 is connected to the first absorber solution supply device 12 of the first absorber A1. The second dilute solution Sw2 is configured to be supplied to the first absorber A1. In addition, the other end of the first dilute solution outflow pipe 14 for flowing the first dilute solution Sw1 having flowed out from the first absorber A1 is connected to the second regenerator solution supply device 36 of the second regenerator G2, The dilute solution Sw1 is configured to be supplied to the second regenerator G2. In addition, the other end of the second concentrated solution outflow pipe 38 for flowing the second concentrated solution Sa2 flowing out of the second regenerator G2 is connected to the first regenerator solution supply device 32 of the first regenerator G1, and the second The concentrated solution Sa2 is configured to be supplied to the first regenerator G1. The second concentrated solution outlet pipe 38 is not provided with the second concentrated solution pump 38p (see FIG. 1), so that the second concentrated solution Sa2 flows from the second regenerator G2 to the first regenerator G1 by gravity. It has become. Further, the other end of the first concentrated solution outflow pipe 34 for flowing the first concentrated solution Sa1 flowing out of the first regenerator G1 is connected to the second absorber solution supply device 16 of the second absorber A2, The concentrated solution Sa1 is configured to be supplied to the second absorber A2. In the absorption heat exchange system 2, the first dilute solution Sw1 has a lower concentration than the second dilute solution Sw2, the second concentrated solution Sa2 has a higher concentration than the first dilute solution Sw1, and the first concentrated solution Sa1 has a second concentration. The concentration of the second dilute solution Sw2 is higher than that of the concentrated solution Sa2, and the concentration of the second dilute solution Sw2 is lower than that of the first concentrated solution Sa1. With such a configuration, the absorbing solution S flows in series in the order of the second absorber A2, the first absorber A1, the second regenerator G2, and the first regenerator G1, and the second absorption is again performed from the first regenerator G1. It returns to the vessel A2 and circulates while changing the concentration. At this time, the absorbing solution S is introduced into the second regenerator G2 directly from the first absorber A1 and indirectly from the second absorber A2 via the first absorber A1. The regenerator G1 is indirectly introduced from the first absorber A1 via the second regenerator G2 and indirectly from the second absorber A2 via the first absorber A1 and the second regenerator G2 It will be done. In addition, the absorbing solution S will be introduced indirectly to the second absorber A2 from the first regenerator G1 directly and from the second regenerator G2 via the first regenerator G1, and thus the first absorption To the unit A1 indirectly from the first regenerator G1 via the second absorber A2 and indirectly from the second regenerator G2 via the first regenerator G1 and the second absorber A2 It will be. Here, introducing indirectly means introducing through the other equipment of the main equipment which constitutes an absorption heat pump cycle.

  Further, in the absorption type heat exchange system 2, the other end of the second refrigerant liquid outflow pipe 48 for flowing the second refrigerant liquid Vf2 flowing out from the second condenser C2 is connected to the first condenser C1, and the second refrigerant The liquid Vf2 is configured to be supplied to the first condenser C1. The second refrigerant liquid outflow pipe 48 is not provided with the second refrigerant liquid pump 48p (see FIG. 1), and the second refrigerant liquid Vf2 flows from the second condenser C2 to the first condenser C1 by gravity. It has become. Further, the other end of the first refrigerant liquid outflow pipe 44 for flowing the first refrigerant liquid Vf1 flowing out of the first condenser C1 is connected to the second evaporator E2, and the first refrigerant liquid Vf1 is the second evaporator E2 Configured to be supplied to Moreover, in the absorption type heat exchange system 2, the evaporator refrigerant liquid introduction pipe 28 which supplies a part of 1st refrigerant liquid Vf1 stored by the 2nd evaporator E2 to the 1st evaporator E1 is provided. With such a configuration, the refrigerant V removes the portions that flow as vapor (Ve1, Ve2) from the first evaporator E1 to the first absorber A1 and from the second evaporator E2 to the second absorber A2, respectively. The condenser C2, the first condenser C1, the second evaporator E2, and the first evaporator E1 flow in series in this order. In the absorption type heat exchange system 2, the first concentrated solution introduction pipe 13, the second concentrated solution introduction pipe 17, the first refrigerant liquid introduction pipe 23, and the second provided in the absorption type heat exchange system 1 (see FIG. 1). The refrigerant liquid introduction pipe 27, the first dilute solution introduction pipe 33, the second dilute solution introduction pipe 37, the dilute solution joining pipe 61, the concentrated solution joining pipe 63, and the refrigerant liquid joining pipe 64 are not provided. Therefore, the solution heat exchanger 62 is not connected to the first dilute solution outflow pipe 14 and the first concentrated solution outflow pipe 34, not to the dilute solution joining pipe 61 (see FIG. 1) and the concentrated solution joining pipe 63 (see FIG. 1). It is provided.

  Furthermore, in the absorption type heat exchange system 2, the end of the temperature raising fluid introduction pipe 51 opposite to the end connected to the heat source fluid inflow pipe 55 and the drive heat source introduction pipe 52 is the second absorber A2. It is connected to one end of the 1st absorption heat transfer tube 11 of 1st absorber A1, not the 2nd absorption heat transfer tube 15 of this. The temperature rising fluid outflow pipe 53 is connected to an end of the second absorption heat transfer pipe 15 of the second absorber A2 on the opposite side to the end to which the heating target communication pipe 71 is connected. With such a configuration, the temperature raising target fluid RP flowing through the temperature rising fluid introduction pipe 51 flows in series in the order of the first absorber A1 and the second absorber A2 and reaches the temperature rising fluid outflow pipe 53. There is. Further, the low temperature heat source introduction pipe 57 is connected not to the second condensation heat transfer pipe 45 of the second condenser C2, but to one end of the first condensation heat transfer pipe 41 of the first condenser C1. One end of a low temperature heat source outflow pipe 58 is connected to the end of the second condensation heat transfer pipe 45 of the second condenser C2 opposite to the end to which the low temperature heat source connection pipe 74 is connected. With such a configuration, the low temperature heat source fluid GP flowing through the low temperature heat source introduction pipe 57 flows in series in the order of the first condenser C1 and the second condenser C2 to reach the low temperature heat source outflow pipe 58. The end of the heat source evaporation / regeneration communication pipe 75 opposite to the end of the second regenerator G2 connected to the second reproduction heat source pipe 35 is the first evaporation heat source pipe 21 of the first evaporator E1. Instead, it is connected to one end of the second evaporation heat source pipe 25 of the second evaporator E2. One end of a drive heat source outflow pipe 56 is connected to an end of the first evaporation heat source pipe 21 of the first evaporator E1 opposite to the end to which the heat source evaporation communication pipe 72 is connected. With such a configuration, the drive heat source fluid RS that has flowed in series sequentially from the drive heat source introduction pipe 52 in the order of the first regenerator G1 and the second regenerator G2 is then added to the second evaporator E2 and the first evaporator E1. It flows in series in order to reach the driving heat source outflow pipe 56. The remaining configuration of the absorptive heat exchange system 2 is the same as that of the absorptive heat exchange system 1 (see FIG. 1).

  Since the temperature of the low temperature heat source fluid GP flowing through the second condenser C2 becomes higher than the temperature of the low temperature heat source fluid GP flowing through the first condenser C1 in the absorption type heat exchange system 2 configured in this way, the second regeneration Since the internal pressure of the first and second condensers G2 and C2 is higher than the internal pressure of the first regenerator G1 and the first condenser C1, a difference in internal pressure occurs between the second regenerator G2 and the first regenerator G1. Is suitable for flowing the absorbent S from the second regenerator G2 to the first regenerator G1. Similarly, it is also suitable for flowing the refrigerant liquid Vf from the second condenser C2 to the first condenser C1. Since the temperature of the absorbing solution S heated by the second regenerator G2 is lower than the temperature of the absorbing solution S heated by the first regenerator G1, the second regenerator G2 having a lower temperature, and then the second higher temperature (1) The flow of the regenerator G1 and the absorbing solution S causes the absorbing solution S to be heated twice in ascending order of temperature, thereby increasing the concentration of the absorbing solution S and increasing the heat output. In addition, since the internal pressure of the second absorber A2 and the second evaporator E2 becomes higher than the internal pressure of the first absorber A1 and the first evaporator E1, between the second absorber A2 and the first absorber A1 A difference in internal pressure occurs, which is suitable for flowing the absorbent S from the second absorber A2 to the first absorber A1. Similarly, it is also suitable for flowing the refrigerant liquid Vf from the second evaporator E2 to the first evaporator E1. Since the temperature of the absorbing solution S cooled by the second absorber A2 is higher than the temperature of the absorbing solution S cooled by the first absorber A1, the second absorber A2 having a high temperature, and then the second temperature having a low temperature The absorption liquid S is cooled twice in descending order of temperature by the flow of the absorber 1 and the absorption liquid S, and the concentration of the absorption liquid S can be lowered to increase the heat output. As described above, in the absorption type heat exchange system 2, the absorption liquid S flows in series from the second absorber A2 to the first absorber A1 and flows in series from the second regenerator G2 to the first regenerator G1. The output can be increased by increasing the difference in concentration of the liquid S.

  Next, with reference to FIG. 3, an absorption heat exchange system 3 according to a third embodiment of the present invention will be described. FIG. 3 is a schematic system diagram of the absorption type heat exchange system 3. The absorption heat exchange system 3 is different from the absorption heat exchange system 1 (see FIG. 1) in terms of the flow of the absorption liquid S and the refrigerant V and the flow order of the driving heat source fluid RS. There is. Accordingly, the configuration of the absorption type heat exchange system 3 is different from the configuration of the absorption type heat exchange system 1 (see FIG. 1) mainly in the following points. In the absorption type heat exchange system 3, the other end of the first dilute solution outflow pipe 14 for flowing the first dilute solution Sw1 flowing out of the first absorber A1 is connected to the first regenerator solution supply device 32 of the first regenerator G1. The first dilute solution Sw1 is configured to be supplied to the first regenerator G1. Further, the other end of the first concentrated solution outflow pipe 34 for flowing the first concentrated solution Sa1 flowing out of the first regenerator G1 is connected to the first absorber solution supply device 12 of the first absorber A1, The concentrated solution Sa1 is configured to be supplied to the first absorber A1. In the absorption type heat exchange system 3, the first dilute solution Sw1 and the first concentrated solution Sa1 circulate between the first absorber A1 and the first regenerator G1 while changing the concentration, and the first dilute solution outflow The pipe 14 and the first concentrated solution outflow pipe 34 cooperate with the first absorber A1 and the first regenerator G1 to constitute a first absorbent circulation path. Further, in the absorption type heat exchange system 3, the other end of the second dilute solution outflow pipe 18 for flowing the second dilute solution Sw2 flowing out from the second absorber A2 is the second regenerator solution supply device 36 of the second regenerator G2. And the second dilute solution Sw2 is supplied to the second regenerator G2. In addition, the other end of the second concentrated solution outflow pipe 38 for flowing the second concentrated solution Sa2 flowing out of the second regenerator G2 is connected to the second absorber solution supply device 16 of the second absorber A2, The concentrated solution Sa2 is configured to be supplied to the second absorber A2. In the absorption type heat exchange system 3, the second dilute solution Sw2 and the second concentrated solution Sa2 circulate between the second absorber A2 and the second regenerator G2 while changing the concentration, and the second dilute solution outflow The pipe 18 and the second concentrated solution outflow pipe 38 cooperate with the second absorber A2 and the second regenerator G2 to constitute a second absorbent circulation channel. Further, in the absorption type heat exchange system 3, instead of the solution heat exchanger 62 (see FIG. 1), the first dilute solution outflow pipe 14 and the first concentrated solution outflow pipe 34 are provided with the first solution heat exchanger 62A. In addition, a second solution heat exchanger 62B is provided in the second dilute solution outflow pipe 18 and the second concentrated solution outflow pipe 38.

  Further, in the absorption type heat exchange system 3, the other end of the first refrigerant liquid outflow pipe 44 for flowing the first refrigerant liquid Vf1 having flowed out of the first condenser C1 is connected to the first evaporator E1, and the first refrigerant The liquid Vf1 is configured to be supplied to the first evaporator E1. Further, the other end of the second refrigerant liquid outflow pipe 48 for flowing the second refrigerant liquid Vf2 flowing out of the second condenser C2 is connected to the second evaporator E2, and the second refrigerant liquid Vf2 is the second evaporator E2 Configured to be supplied to In the absorption-type heat exchange system 3, the refrigerant V changes phases with the first refrigerant liquid Vf1, the first evaporator refrigerant vapor Ve1, and the first regenerator refrigerant vapor Vg1 as a first system, and the first condenser C1 The first evaporator E1, the first absorber A1, and the first regenerator G1 are circulated, and as a second system, the second refrigerant liquid Vf2, the second evaporator refrigerant vapor Ve2, and the second regenerator refrigerant vapor Vg2 And the second condenser C2, the second evaporator E2, the second absorber A2, and the second regenerator G2 while changing phases.

  Furthermore, in the absorption type heat exchange system 3, the end of the drive heat source introduction pipe 52 opposite to the end connected to the heat source fluid inflow pipe 55 and the temperature raising fluid introduction pipe 51 is the first regenerator G1. It is connected to one end of the 1st evaporation heat source pipe 21 of the 1st evaporator E1, not the 1st reproduction | regeneration heat source pipe 31 of this. One end of a heat source first connection pipe 76 is connected to the other end of the first evaporation heat source pipe 21. The other end of the heat source first connection pipe 76 is connected to one end of the first regeneration heat source pipe 31 of the first regenerator G1. One end of the heat source intermediate communication pipe 77 is connected to the other end of the first regeneration heat source pipe 31. The other end of the heat source intermediate communication pipe 77 is connected to one end of the second evaporation heat source pipe 25 of the second evaporator E2. One end of a heat source second connection pipe 78 is connected to the other end of the second evaporation heat source pipe 25. The other end of the heat source second communication pipe 78 is connected to one end of the second regenerative heat source pipe 35 of the second regenerator G2. The other end of the second regeneration heat source pipe 35 is connected to one end of the drive heat source outflow pipe 56, and the other end of the drive heat source outflow pipe 56 is connected to the low temperature heat source outflow pipe 58 and the ends of the heat source fluid outflow pipe 59 It is done. With such a configuration, the drive heat source fluid RS flowing through the drive heat source introduction pipe 52 flows in series in the order of the first evaporator E1, the first regenerator G1, the second evaporator E2, and the second regenerator G2 to drive the heat source. It comes to the outflow pipe 56. In addition, in the absorption type heat exchange system 3, the heat source evaporation communication pipe 72, the heat source regeneration communication pipe 73, and the heat source evaporation reproduction communication pipe 75 which were provided in the absorption type heat exchange system 1 (see FIG. 1) are not provided. The remaining configuration of the absorption-type heat exchange system 3 is the same as that of the absorption-type heat exchange system 1 (see FIG. 1). The absorption type heat exchange system 3 configured in this way has two independent paths of the absorption heat pump cycle of the absorption liquid S and the refrigerant V, and controls and manages the absorption heat pump cycle by a plurality. Can. Such an absorption type heat exchange system 3 further increases the temperature of the fluid to be heated in a situation where there is an existing type 2 absorption heat pump including one absorber, one evaporator, one regenerator, and one condenser. If you want to make it higher, install a second-class absorption heat pump equipped with an absorber, an evaporator, a regenerator, and a condenser, as well as drive heat source fluid RS, temperature increase target fluid RP, and low temperature heat source fluid GP. The piping can be connected as shown in the present embodiment, and the control system can be configured with a slight change.

  Next, with reference to FIG. 4, an absorption heat exchange system 4 according to a fourth embodiment of the present invention will be described. FIG. 4 is a schematic system diagram of the absorption type heat exchange system 4. The absorption-type heat exchange system 4 is different from the absorption-type heat exchange system 3 (see FIG. 3) in the order of the flow of the driving heat source fluid RS when viewed in outline. Along with this, the configuration of the absorption type heat exchange system 4 is different from the configuration of the absorption type heat exchange system 3 (see FIG. 3) mainly in the following points. In the absorption type heat exchange system 4, the end of the drive heat source introduction pipe 52 opposite to the end connected to the heat source fluid inflow pipe 55 and the temperature raising fluid introduction pipe 51 is the first evaporator E1. It is connected to one end of the first regeneration heat source pipe 31 of the first regenerator G1 instead of the first evaporation heat source pipe 21. One end of the heat source intermediate communication pipe 77 is connected to the end of the first evaporation heat source pipe 21 opposite to the end connected to the first heat source communication pipe 76. The other end of the heat source intermediate communication pipe 77 is connected to one end of the second regeneration heat source pipe 35 of the second regenerator G2, not to the second evaporation heat source pipe 25 of the second evaporator E2. One end of the drive heat source outflow pipe 56 is connected to the end of the second evaporation heat source pipe 25 opposite to the end connected to the second heat source connection pipe 78. The other end is connected to the low temperature heat source outflow pipe 58 and the end of the heat source fluid outflow pipe 59. With such a configuration, the drive heat source fluid RS flowing through the drive heat source introduction pipe 52 flows in series in the order of the first regenerator G1, the first evaporator E1, the second regenerator G2, and the second evaporator E2, and the drive heat source It comes to the outflow pipe 56. The remaining configuration of the absorptive heat exchange system 4 is similar to that of the absorptive heat exchange system 3 (see FIG. 3). The absorption type heat exchange system 4 configured in this way has two independent paths for the absorption heat pump cycle of the absorption liquid S and the refrigerant V, as in the absorption type heat exchange system 3, thus absorbing Multiple heat pump cycles can be controlled and managed. Further, in the absorption type heat exchange system 4, the temperature of the driving heat source fluid RS is higher when flowing into the first regenerator G1 than when flowing into the first evaporator E1, and flows into the second regenerator G2. Is higher than when it flows into the second evaporator E2, and the concentration of the absorbent S in each of the first regenerator G1 and the second regenerator G2 is the absorption heat exchange system 3 (see FIG. 3) Depending on the operating conditions, the heat output can be increased by raising the temperature of the temperature raising target fluid RP after the temperature increase, as compared with the absorption heat exchange system 3 (see FIG. 3).

  Next, an absorption heat exchange system 5 according to a fifth embodiment of the present invention will be described with reference to FIG. FIG. 5 is a schematic system diagram of the absorption type heat exchange system 5. The absorption-type heat exchange system 5 is different from the absorption-type heat exchange system 1 (see FIG. 1) in terms of the flow of the low-temperature heat source fluid GP when viewed from the overview. Along with this, the configuration of the absorption type heat exchange system 5 is different from the configuration of the absorption type heat exchange system 1 (see FIG. 1) mainly in the following points. In the absorption type heat exchange system 5, the low temperature heat source introduction pipe 57 is branched into a first low temperature heat source introduction pipe 57A and a second low temperature heat source introduction pipe 57B on the way, and the first low temperature heat source introduction pipe 57A is a first condenser C1. The second low-temperature heat source introduction pipe 57B is connected to one end of the first condensation heat-transfer pipe 45 of the second condenser C2. One end of a first low temperature heat source outflow pipe 58A is connected to the other end of the first condensation heat transfer pipe 41, and one end of a second low temperature heat source outflow pipe 58B is connected to the other end of the second condensation heat transfer pipe 45. The other end of the first low temperature heat source outflow pipe 58A and the other end of the second low temperature heat source outflow pipe 58B are both connected to one end of the low temperature heat source outflow pipe 58, and the other end of the low temperature heat source outflow pipe 58 It is connected to the end of the pipe 56 and the heat source fluid outflow pipe 59. In the absorption type heat exchange system 5, the low temperature heat source communication pipe 74 provided in the absorption type heat exchange system 1 (see FIG. 1) is not provided. With such a configuration, the low temperature heat source fluid GP flowing through the low temperature heat source introduction pipe 57 is divided into the first low temperature heat source introduction pipe 57A and the second low temperature heat source introduction pipe 57B, and the first condenser C1 and the second condenser C2 are divided. Flow to the first low-temperature heat source outflow pipe 58A and the second low-temperature heat source outflow pipe 58B, respectively, and then rejoin to reach the low-temperature heat source outflow pipe 58. The remaining configuration of the absorptive heat exchange system 5 is similar to that of the absorptive heat exchange system 1 (see FIG. 1). The absorption-type heat exchange system 5 configured as described above has a flow resistance at the time when the low-temperature heat source fluid GP is branched and flows through the first condenser C1 and the second condenser C2 as shown in FIG. 1), which is suitable when the pressure difference allowed when flowing the low temperature heat source fluid GP is small.

  Next, an absorption heat exchange system 6 according to a sixth embodiment of the present invention will be described with reference to FIG. FIG. 6 is a schematic system diagram of the absorption type heat exchange system 6. The absorption heat exchange system 6 is different from the absorption heat exchange system 3 (see FIG. 3) in terms of the flow of the driving heat source fluid RS when viewed from the overview. Accordingly, the configuration of the absorption type heat exchange system 6 is different from the configuration of the absorption type heat exchange system 3 (see FIG. 3) mainly in the following points. In the absorption type heat exchange system 6, the driving heat source introduction pipe 52 is branched into a first driving heat source introduction pipe 52A and a second driving heat source introduction pipe 52B in the middle, and the first driving heat source introduction pipe 52A is a first evaporator E1. The second drive heat source introduction pipe 52B is connected to one end of the first evaporation heat source pipe 21 and the one end of the second evaporation heat source pipe 25 of the second evaporator E2. One end of a first drive heat source outflow pipe 56A is connected to an end of the first regenerative heat source pipe 31 of the first regenerator G1 on the opposite side to the end to which the heat source first communication pipe 76 is connected. . The other end of the low temperature heat source outflow pipe 58 is connected to the first drive heat source outflow pipe 56A, and the low temperature heat source fluid GP which has flowed out of the first condenser C1 is a drive heat source fluid RS which has flowed out of the first regenerator G1. And merge to become a partially merged heat source fluid Ra. One end of a second drive heat source outflow pipe 56B is connected to the end of the second regenerative heat source pipe 35 of the second regenerator G2 on the opposite side to the end to which the heat source second communication pipe 78 is connected. . One end of the heat source fluid outflow pipe 59 is not the other end of the drive heat source outflow pipe 56 (see FIG. 3) and the other end of the low temperature heat source outflow pipe 58, but the other end of the first drive heat source outflow pipe 56A and the second drive heat source The other end of the outflow pipe 56B is connected. In the absorption type heat exchange system 6, the heat source intermediate communication pipe 77 provided in the absorption type heat exchange system 3 (see FIG. 3) is not provided. With such a configuration, the driving heat source fluid RS flowing through the driving heat source introduction pipe 52 is divided into the first driving heat source introduction pipe 52A and the second driving heat source introduction pipe 52B, and the first evaporator E1 and the first regenerator G1. , And flows in parallel to the second evaporator E2 and the second regenerator G2 and flows out to the first drive heat source outflow pipe 56A and the second drive heat source outflow pipe 56B, respectively, and flows through the first drive heat source outflow pipe 56A After the low-temperature heat source fluid GP merges with the drive heat source fluid RS to become a partial merge heat source fluid Ra, the drive heat source fluid RS flowing through the second drive heat source outflow pipe 56B merges and reaches the heat source fluid outflow pipe 59 The fluid RA flows toward the heat source equipment HSF as the fluid RA. The remaining configuration of the absorptive heat exchange system 6 is the same as that of the absorptive heat exchange system 3 (see FIG. 3). In the absorption type heat exchange system 6 configured as described above, the driving heat source fluid RS is divided and flows through the first evaporator E1 and the first regenerator G1, and the second evaporator E2 and the second regenerator G2. The flow resistance can be smaller than that of the absorption heat exchange system 3 (see FIG. 3), which is suitable when the pressure difference allowed when flowing the driving heat source fluid RS is small. In the example shown in FIG. 6, of the two drive heat source fluids RS divided from the drive heat source inlet pipe 52, one flows from the first evaporator E1 to the first regenerator G1, and the other from the second evaporator E2. Although the flow to the second regenerator G2 is made, one may flow from the first regenerator G1 to the first evaporator E1, and the other may flow from the second regenerator G2 to the second evaporator E2. Alternatively, the driving heat source fluid RS flowing through the driving heat source introduction pipe 52 is divided into four and supplied in parallel to four points of the first regenerator G1, the first evaporator E1, the second regenerator G2, and the second evaporator E2. In this case, the flow resistance when the drive heat source fluid RS flows in each regenerator and each evaporator can be minimized.

  Next, an absorption heat exchange system 1A according to a modification of the first embodiment of the present invention will be described with reference to FIG. FIG. 7 is a schematic configuration diagram of the absorption type heat exchange system 1A. In the absorption heat exchange system 1A, the flow of fluids (absorption liquid S, refrigerant V, temperature increase target fluid RP, drive heat source fluid RS, low temperature heat source fluid GP) with respect to the absorption type heat exchange system 1 (see FIG. 1) Is the same, but more specifically shows the arrangement of each device. In this modification, the first absorber A1 and the first evaporator E1 are partitioned in the first absorber cylinder 10 in place of the first absorber wall 19 (see FIG. 1), the first evaporator 19A. It has become. In the first absorption evaporator cylinder 10, a first absorber A1 and a first evaporator E1 accommodated inside are vertically arrayed. In the present variation, the first evaporator E1 is disposed above the first absorber A1. The first evaporation heat source pipe 21 constituting the first evaporator E1 is accommodated in a first evaporation container 19A whose upper portion is open. In the first evaporation container 19A, the first refrigerant liquid supply device 22 is provided above the first evaporation heat source pipe 21 so that the refrigerant liquid Vf is dispersed from above to the entire first evaporation heat source pipe 21. It is also good. The first refrigerant liquid supply pipe 22 is connected to the first refrigerant liquid supply device 22. Since the first evaporator E1 is disposed above the first absorber A1, the absorbent S in the first absorber A1 leaks into the first evaporator E1 and the refrigerant in the first evaporator E1 Contamination of the liquid Vf can be prevented. Further, in the absorption type heat exchange system 1A, the second absorption evaporation wall 29 (see FIG. 1) is used to divide the second absorber A2 and the second evaporator E2 in the second absorption evaporator cylinder 20. , And the second evaporation container 29A. Similar to the first absorption evaporator cylinder 10, in the second absorption evaporator cylinder 20, a second evaporator E2 housed inside is disposed vertically above the second absorber A2. The second evaporation heat source pipe 25 constituting the second evaporator E2 is accommodated in a second evaporation container 29A whose upper portion is open. Also in the second evaporation container 29A, the second refrigerant liquid supply device 26 corresponding to the first refrigerant liquid supply device 22 may be provided. The first absorber cylinder 10 and the second absorber cylinder 20 are arranged at different positions in the horizontal direction. The position different in the horizontal direction means that the position in plan view is different, and in the present modification, they are arranged adjacently or closely in the horizontal direction. In this modification, the heights of the top portions of the first absorption heat transfer tube 11 and the second absorption heat transfer tube 15 are configured to be the same, and the first absorber solution supply device 12 and the second absorber are configured. The solution supply device 16 is disposed at the same height. Here, the same height includes substantially the same height (a range in which the supply pressure of the concentrated solution Sa differs to such an extent that the heat output of each of the first absorber A1 and the second absorber A2 differs within an acceptable range). Be Similarly, the heights of the uppermost portions of the first evaporation heat source pipe 21 and the second evaporation heat source pipe 25 are configured to be the same, and the first refrigerant liquid supply device 22 and the second refrigerant liquid supply device 26 and the same height.

  In the absorption heat exchange system 1A, the first regeneration condenser G1 and the first condenser C1 are partitioned in the first regeneration condenser can 30 instead of the first regeneration condensation wall 39 (see FIG. 1). , And the first condensation container 39A. In the first regenerative condenser can barrel 30, a first regenerator G1 and a first condenser C1 accommodated therein are vertically vertically arrayed. In the present modification, the first condenser C1 is disposed above the first regenerator G1. The first condensation heat transfer pipe 41 constituting the first condenser C1 is accommodated in a first condensation container 39A whose upper portion is open. Since the first condenser C1 is disposed above the first regenerator G1, the absorbent S in the first regenerator G1 leaks into the first condenser C1 and the refrigerant in the first condenser C1 Contamination of the liquid Vf can be prevented. Further, in the absorption type heat exchange system 1A, the second regeneration condenser wall 49 (see FIG. 1) is used to partition the second regenerator G2 and the second condenser C2 in the second regeneration condenser can 40. , The second condensation container 49A. Similar to the first regenerative condenser can 30, the second condenser C2 accommodated in the second regenerative condenser can 40 is disposed vertically above the second regenerator G2. The second condensation heat transfer pipe 45 constituting the second condenser C2 is accommodated in a second condensation container 49A whose upper portion is open. The first regenerated condensing can barrel 30 and the second regenerated condensing can barrel 40 are disposed at different positions in the horizontal direction, and are arranged adjacent to or in close contact in the horizontal direction in this modification. In this modification, the tops of the first regeneration heat source pipe 31 and the second regeneration heat source pipe 35 are configured to have the same height, and the first regenerator solution supply device 32 and the second regenerator are configured. The solution supply device 36 is disposed at the same height. Here, the same height includes substantially the same height (a range in which the supply pressure of the dilute solution Sw is different to such an extent that the heat output of each of the first regenerator G1 and the second regenerator G2 is different within the allowable range). Be Similarly, the tops of the first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45 are configured to have the same height. In addition, the first absorption evaporator can barrel 10 is disposed horizontally adjacent to or in close contact with the first regenerating condensing can barrel 30 and the second regenerating condensing can barrel 40 that are disposed adjacently or closely to each other in the horizontal direction. And a second absorber cylinder 20 is arranged. Further, in the absorption type heat exchange system 1A, the first concentration solution pump 34p and the second concentration solution outflow disposed in the first concentration solution outflow pipe 34 provided in the absorption type heat exchange system 1 (see FIG. 1) Instead of the second concentrated solution pump 38p disposed in the pipe 38, a concentrated solution pump 63p disposed in the concentrated solution merging pipe 63 is provided. In addition, the first refrigerant liquid pump 44p disposed in the first refrigerant liquid outflow pipe 44 provided in the absorption type heat exchange system 1 (see FIG. 1) and the second refrigerant liquid outflow pipe 48 The refrigerant liquid pump 64p disposed in the refrigerant liquid junction pipe 64 is provided instead of the two refrigerant liquid pump 48p. The configuration of the absorption-type heat exchange system 1A other than the above is the same as that of the absorption-type heat exchange system 1 (see FIG. 1). In the absorption type heat exchange system 1A configured as described above, since the first absorber solution supply device 12 and the second absorber solution supply device 16 are disposed at the same height, the first absorber solution supply device is provided. The pressure applied to the concentrated solution Sa to be pumped to the apparatus 12 and the second absorber solution supply apparatus 16 can be made close to each other, and the discharge pressure of the concentrated solution pump 63p can be suppressed. Similarly, the discharge pressure of the refrigerant liquid pump 64p that pumps the refrigerant liquid Vf to the first refrigerant liquid supply device 22 and the second refrigerant liquid supply device 26 can be suppressed. In addition, since the heights of the top portions of the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 are the same, it is possible to suppress the pressure applied to pump the temperature raising target fluid RP. Similarly, since the heights of the tops of the first evaporating heat source pipe 21 and the second evaporating heat source pipe 25 are the same, it is possible to suppress the pressure applied to pump the driving heat source fluid RS. In addition, the first dilute solution outflow pipe 14 and the second dilute solution outflow between the first absorption evaporator cylinder 10 and the second absorption evaporator cylinder 20 and the first regeneration condenser cylinder 30 and the second regeneration condenser cylinder 40. If the first absorbing and evaporating can barrel 10 and the second absorbing and evaporating can barrel 20, and the first and second regenerative condensing can bodies 30 and 40 are arranged close to each other in consideration of the mounting height of the pipe 18, The height can be reduced to make the device configuration compact.

  Next, with reference to FIG. 8, an absorption-type heat exchange system 1B according to another modification of the first embodiment of the present invention will be described. FIG. 8 is a schematic configuration diagram of the absorption-type heat exchange system 1B. The absorption-type heat exchange system 1B is different from the absorption-type heat exchange system 1A (see FIG. 7) in the order of the flow of the driving heat source fluid RS when viewed in outline. Along with this, the configuration of the absorption type heat exchange system 1B is different from the configuration of the absorption type heat exchange system 1A (see FIG. 7) mainly in the following points. In the absorption type heat exchange system 1B, the end of the drive heat source introduction pipe 52 opposite to the end connected to the heat source fluid inflow pipe 55 and the temperature raising fluid introduction pipe 51 is the first regenerator G1. It is connected to one end of the first evaporation heat source pipe 21 of the first evaporator E1 instead of the first regeneration heat source pipe 31. One end of the heat source evaporation reproduction communication pipe 75 is connected to the other end of the second evaporation heat source pipe 25 instead of the other end of the first evaporation heat source pipe 21. The other end of the heat source evaporation regeneration communication pipe 75 is connected to one end of the first regeneration heat source pipe 31 instead of one end of the second regeneration heat source pipe 35. One end of the drive heat source outflow pipe 56 is connected to the end of the second regeneration heat source pipe 35 opposite to the end connected to the heat source regeneration communication pipe 73, and the other of the drive heat source outflow pipe 56 The end is connected to the low temperature heat source outflow pipe 58 and the end of the heat source fluid outflow pipe 59. With such a configuration, the drive heat source fluid RS flowing through the drive heat source introduction pipe 52 flows in series in the order of the first evaporator E1, the second evaporator E2, the first regenerator G1, and the second regenerator G2 to drive the heat source. It comes to the outflow pipe 56. The remaining configuration of the absorption-type heat exchange system 1B is similar to that of the absorption-type heat exchange system 1A (see FIG. 7). The absorption-type heat exchange system 1B configured in this manner has the temperature of the driving heat source fluid RS introduced to the first regenerator G1 and the second regenerator G2 compared to the absorption-type heat exchange system 1A (see FIG. 7). Is reduced by the amount of heat consumed by the first evaporator E1 and the second evaporator E2, so that the increase in the concentration of the absorbent S in the first regenerator G1 and the second regenerator G2 can be suppressed. It is possible to avoid that the solution S is excessively concentrated and crystallized.

  In the description of the various embodiments so far, the order of various flows of the driving heat source fluid RS, the temperature raising target fluid RP, and the low temperature heat source fluid GP is exemplified, but the order of flow of these fluids is exemplified For example, as shown below, it can also change suitably. When the driving heat source fluid RS is configured to flow in series to each device of the first regenerator G1, the second regenerator G2, the first evaporator E1, and the second evaporator E2, the first regenerator G1 or It is good to constitute so that it may flow into the 1st evaporator E1. Here, when the driving heat source fluid RS flows into the first regenerator G1 first, the flow of the driving heat source fluid RS that has flowed out of the first regenerator G1 is in the order of flow only by the code for the convenience of description. (1) G2, E1, E2, (2) G2, E2, E1, (3) E1, G2, E2, (4) E1, E2, G2, (5) E2, G2, E1, (6) ) E2, E1 or G2 On the other hand, when the driving heat source fluid RS flows into the first evaporator E1 first, the flow of the driving heat source fluid RS that has flowed out of the first evaporator E1 will be (7) E2 , G1, G2, (8) E2, G2, G1, (9) G1, E2, G2, (10) G2, E2, G1, (11) G1, G2, E2, (12) G2, G1, E2, It will be either. When the driving heat source fluid RS flows in series in any of the modes described above, the flow of the temperature raising target fluid RP is in the same order as the first evaporator E1 and the second evaporator G1 regardless of the order of the first regenerator G1 and the second regenerator G2. Focusing only on the order of the second evaporator E2, when the driving heat source fluid RS flows in the order of the first evaporator E1 and the second evaporator E2, the temperature raising target fluid RP is the second absorber A2, the first absorber A1 In the case where the driving heat source fluid RS flows in the order of the second evaporator E2 and the first evaporator E1, the heating target fluid RP may be configured to flow in the order of the first absorber A1 and the second absorber A2 . In addition, although the low temperature heat source fluid GP preferably flows the first condenser C1 and the second condenser C2 in series regardless of which one goes first, regardless of the order of the first evaporator E1 and the second evaporator E2, Focusing only on the order of the one regenerator G1 and the second regenerator G2, when the driving heat source fluid RS flows in the order of the first regenerator G1 and the second regenerator G2, the low temperature heat source fluid GP is the second condenser C2, the second When the heat source fluid RS flows in the order of the first condenser C1 and the drive heat source fluid RS flows in the order of the second regenerator G2 and the first regenerator G1, the low temperature heat source fluid GP flows in the order of the first condenser C1 and the second condenser C2. It is preferable to construct. When the drive heat source fluid RS first flows into the first regenerator G1 when configured in any of the modes described above, the amount of heat transferred from the drive heat source fluid RS to the temperature raising target fluid RP can be increased and the outflow The temperature of the temperature raising target fluid RP can be raised. On the other hand, when the driving heat source fluid RS first flows into the first evaporator E1, in addition to the increase in the amount of heat transferred from the driving heat source fluid RS to the temperature raising target fluid RP and the increase in temperature of the temperature raising target fluid RP flowing out. An increase in the concentration of the absorbing solution S in the first regenerator G1 and the second regenerator G2 can be suppressed, and the absorbing solution S can be prevented from being excessively concentrated and crystallized.

  Next, with reference to FIG. 9, an absorption heat exchange system 7 according to a seventh embodiment of the present invention will be described. FIG. 9 is a schematic system diagram of the absorptive heat exchange system 7. The absorption heat exchange system 7 has a third absorber A3, a third evaporator in addition to the configuration of the absorption heat exchange system 1 (see FIG. 1) as compared to the absorption heat exchange system 1 (see FIG. 1) The main difference is that E3, a third regenerator G3, and a third condenser C3 are provided. This main difference will be described below, including different configurations. The third absorber A3 corresponds to a third absorber, and includes a third absorption heat transfer pipe 311 and a third absorber solution supply device 312, and the third concentrated solution introduction pipe 313 and the third dilute solution The outflow pipe 314 is connected. The configuration of the third absorber A3 and the periphery thereof is the same as that of the first absorber A1, and the third absorption heat transfer tube 311, the third absorber solution supply device 312, the third concentrated solution introduction tube 313, the third absorption heat transfer tube The third dilute solution outlet tube 314 corresponds to the first absorption heat transfer tube 11, the first absorber solution supply device 12, the first concentrated solution inlet tube 13, and the first dilute solution outlet tube 14 in the first absorber A1, respectively. . The third evaporator E3 corresponds to a third evaporation unit, includes a third evaporation heat source pipe 321, and is connected to a third refrigerant liquid introduction pipe 323. The configuration of the third evaporator E3 and the periphery thereof is the same as that of the first evaporator E1, and the third evaporation heat source pipe 321 and the third refrigerant liquid introduction pipe 323 are respectively connected to the first evaporator E1 in the first evaporator E1. 1 corresponds to the evaporation heat source pipe 21 and the first refrigerant liquid introduction pipe 23. The third absorber A3 and the third evaporator E3 are accommodated in the third absorption evaporator cylinder 310, and both are divided by the third absorption evaporation wall 319 following the first absorption evaporator cylinder 10 . The third regenerator G3 corresponds to a third regeneration unit, and includes a third regeneration heat source pipe 331 and a third regenerator solution supply device 332, and a third dilute solution introduction tube 333 and a third concentrated solution A third concentrated solution outflow pipe 334 provided with a pump 334p is connected. The configuration of the third regenerator G3 and the periphery thereof is the same as that of the first regenerator G1, and the third regeneration heat source pipe 331, the third regenerator solution supply device 332, the third dilute solution introduction tube 333, the third The third concentrated solution outflow pipe 334 and the third concentrated solution pump 334p are respectively the first regeneration heat source pipe 31, the first regenerator solution supply device 32, the first dilute solution introduction pipe 33, and the first concentration in the first regenerator G1. The solution outflow pipe 34 corresponds to a first concentrated solution pump 34p. The third condenser C3 corresponds to a third condenser and includes a third condensing heat transfer pipe 341, and is connected to a third refrigerant liquid outflow pipe 344 provided with a third refrigerant liquid pump 344p. . The configuration of the third condenser C3 and the periphery thereof is the same as that of the first condenser C1, and the third condensing heat transfer pipe 341, the third refrigerant liquid outflow pipe 344, and the third refrigerant liquid pump 344p are respectively configured It corresponds to the first condensation heat transfer pipe 41, the first refrigerant liquid outflow pipe 44, and the first refrigerant liquid pump 44p in the first condenser C1. The third regenerator G3 and the third condenser C3 are accommodated in the third regenerating condensing can body 330, and both are divided by the third regenerating condensing wall 339 following the first regenerating condensing can body 30. .

  In the present embodiment, the other end of the third dilute solution outflow pipe 314, one end of which is connected to the third absorber A3, is connected to the second dilute solution outflow pipe 18 and flows out of the third absorber A3. The third dilute solution Sw3 is joined to the second dilute solution Sw2. Further, the other end of the third concentrated solution introduction pipe 313, one end of which is connected to the third absorber solution supply device 312, is connected to the second concentrated solution introduction pipe 17, and flows through the second concentrated solution introduction pipe 17. A portion of the concentrated solution Sa is supplied to the third absorber A3. Further, the other end of the third refrigerant liquid introduction pipe 323 whose one end is connected to the third evaporator E3 is connected to the second refrigerant liquid introduction pipe 27, and the refrigerant liquid Vf flowing through the second refrigerant liquid introduction pipe 27 A part of is supplied to the third evaporator E3. The other end of the third concentrated solution outflow pipe 334, one end of which is connected to the third regenerator G3, is connected to the first concentrated solution outflow pipe 34, and the third concentrated solution which has flowed out of the third regenerator G3. Sa3 merges with the first concentrated solution Sa1. Further, the other end of the third dilute solution introduction pipe 333 whose one end is connected to the third regenerator solution supply device 332 is connected to the first dilute solution introduction pipe 33 and flows in the first dilute solution introduction pipe 33 A portion of the dilute solution Sw is supplied to the third regenerator G3. Further, the other end of the third refrigerant liquid outflow pipe 344 whose one end is connected to the third condenser C3 is connected to the first refrigerant liquid outflow pipe 44, and the third refrigerant liquid which has flowed out of the third condenser C3 Vf3 merges with the first refrigerant liquid Vf1.

  The third absorber A3 is disposed between the first absorber A1 and the second absorber A2 when viewed from the flow of the temperature raising target fluid RP. In the absorption type heat exchange system 7, in the absorption type heat exchange system 1 (see FIG. 1), the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 are connected by the temperature increase target communication pipe 71 (see FIG. 1). Instead of the above, the first absorption heat transfer pipe 11 and the third absorption heat transfer pipe 311 are connected by the first heating target communication pipe 71A, and the second absorption heat transfer pipe 15 and the third absorption heat transfer pipe 311 are (2) It is connected by the temperature increase target communication pipe 71B. With such a configuration, the temperature raising target fluid RP flowing through the temperature rising fluid introduction pipe 51 flows in series in the order of the second absorber A2, the third absorber A3 and the first absorber A1, and the temperature rising fluid outlet pipe 53 It has come to The third evaporator E3 is disposed between the first evaporator E1 and the second evaporator E2 when viewed from the flow of the drive heat source fluid RS. In the absorption type heat exchange system 7, in the absorption type heat exchange system 1 (see FIG. 1), the first evaporation source pipe 21 and the second evaporation source pipe 25 are connected by the heat source evaporation connection pipe 72 (see FIG. 1) Instead of the above, the first evaporation heat source pipe 21 and the third evaporation heat source pipe 321 are connected by the first heat source evaporation communication pipe 72A and the second evaporation heat source pipe 25 and the third evaporation heat source pipe 321 are the second heat source It is connected by the evaporation connection pipe 72B. The third regenerator G3 is disposed between the first regenerator G1 and the second regenerator G2 when viewed from the flow of the drive heat source fluid RS. In the absorption type heat exchange system 7, in the absorption type heat exchange system 1 (see FIG. 1), the first regeneration heat source pipe 31 and the second regeneration heat source pipe 35 are connected by the heat source regeneration communication pipe 73 (see FIG. 1) Instead of the above, the first regeneration heat source pipe 31 and the third regeneration heat source pipe 331 are connected by the first heat source regeneration communication pipe 73A, and the second regeneration heat source pipe 35 and the third regeneration heat source pipe 331 are the second heat source. It is connected by the regeneration communication pipe 73B. With such a configuration, the drive heat source fluid RS flowing through the drive heat source introduction pipe 52 is supplied to the first regenerator G1, the third regenerator G3, the second regenerator G2, the first evaporator E1, the third evaporator E3, the third regenerator G1. It flows in series in the order of the two evaporators E2 to reach the driving heat source outlet pipe 56. The third condenser C3 is disposed between the first condenser C1 and the second condenser C2 when viewed from the flow of the low-temperature heat source fluid GP. In the absorption heat exchange system 7, the first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45 are connected by the low temperature heat source communication pipe 74 (see FIG. 1) in the absorption heat exchange system 1 (see FIG. 1). Instead, the first condensing heat transfer pipe 41 and the third condensing heat transfer pipe 341 are connected by the first low temperature heat source communication pipe 74A and the second condensing heat transfer pipe 45 and the third condensing heat transfer pipe 341 have the second low temperature. The heat source communication pipe 74B is connected. With such a configuration, the low temperature heat source fluid GP flowing through the low temperature heat source introduction pipe 57 flows in series in the order of the second condenser C2, the third condenser C3 and the first condenser C1 to reach the low temperature heat source outflow pipe 58 It has become. The remaining configuration of the absorptive heat exchange system 7 is the same as that of the absorptive heat exchange system 1 (see FIG. 1).

  In the absorption-type heat exchange system 7 configured as described above, the temperature raising target fluid RP flows to the second absorber A2, the third absorber A3, and the first absorber A1, and is heated three times, so that heat is generated. The temperature of the temperature raising target fluid RP supplied to the utilization facility HCF can be made higher than that of the absorption type heat exchange system 1 (see FIG. 1). Further, the temperature of the drive heat source fluid RS flowing through the first evaporator E1 is higher than the temperature of the drive heat source fluid RS flowing through the third evaporator E3, and the temperature of the drive heat source fluid RS flowing through the third evaporator E3 is the second Since the internal pressure and temperature of each evaporator and each absorber are lower than the temperature of the second evaporator E2 and the second absorber A2 because the temperature of the heat source fluid RS flowing through the evaporator E2 is higher than that of the driving heat source fluid RS, (3) The internal pressure and temperature of the evaporator E3 and the third absorber A3 become higher in the order of the internal pressure and temperature of the first evaporator E1 and the first absorber A1, and when the fluid RP to be heated is introduced in this order, The temperature of the temperature raising target fluid RP to be heated can be successively raised. A fourth absorber, a fourth evaporator, and a fourth regenerator according to the configuration in which the third absorber A3, the third evaporator E3, the third regenerator G3, and the third condenser C3 are added. And a fourth condenser, and a fourth absorber and a fourth evaporator are provided between the first absorber A1 and the first evaporator E1 and the third absorber A3 and the third evaporator E3. A fourth regenerator and a fourth condenser may be provided between the first regenerator G1 and the first condenser C1 and the third regenerator G3 and the third condenser C3, and thus the configuration Then, the temperature raising target fluid RP is heated four times, and the temperature after heating can be increased.

  Next, with reference to FIG. 10, an absorption heat exchange system 8 according to an eighth embodiment of the present invention will be described. FIG. 10 is a schematic system diagram of the absorption type heat exchange system 8. The absorption heat exchange system 8 has a third absorber A3, a third evaporator in addition to the configuration of the absorption heat exchange system 3 (see FIG. 3) as compared to the absorption heat exchange system 3 (see FIG. 3) The main difference is that E3, a third regenerator G3, and a third condenser C3 are provided. A description will be given below including the different configurations accompanying this main difference. The third absorber A3 and the third evaporator E3 are generally configured in the same manner as the third absorber A3 and the third evaporator E3 in the absorption heat exchange system 7 (see FIG. 9), and the third absorption evaporation evaporation It is common that the third absorption evaporator cylinder 310 is divided by the wall 319, but the third absorber solution supply device 312 is connected to the third concentrated solution introduction pipe 313 (Fig. The third concentrated solution outflow pipe 334 instead of 9) and the third refrigerant liquid outflow pipe 344 instead of the third refrigerant liquid introduction pipe 323 (refer to FIG. 9) is connected to the third evaporator E3. The points are different. The third regenerator G3 and the third condenser C3 are generally configured in the same manner as the third regenerator G3 and the third condenser C3 in the absorption heat exchange system 7 (see FIG. 9), and the third regeneration condenser is used. It is common to the point that it is accommodated in the third regeneration condenser cylinder 330 divided by the wall 339, but the third dilute solution introduction pipe 333 (shown in FIG. 3) is connected to the third regenerator solution supply device 332. 9) but not the third dilute solution outflow pipe 314. In the absorption type heat exchange system 8, the dilute solution joining pipe 61 (see FIG. 9) and the concentrated solution joining pipe 63 (see FIG. 9) provided in the absorption type heat exchange system 7 (see FIG. 9) are not provided. . In the absorption type heat exchange system 8, the third dilute solution Sw3 and the third concentrated solution Sa3 circulate between the third absorber A3 and the third regenerator G3 while changing the concentration, and the third dilute solution outflow The pipe 314 and the third concentrated solution outflow pipe 334 cooperate with the third absorber A3 and the third regenerator G3 to constitute a third absorbent circulation channel. Further, in the absorption type heat exchange system 8, the third solution heat exchanger 62C is provided in the third dilute solution outflow pipe 314 and the third concentrated solution outflow pipe 334. In addition, the third condenser C3 and the third evaporator E3 change the phase of the refrigerant V with the third refrigerant liquid Vf3, the third evaporator refrigerant vapor Ve3 and the first regenerator refrigerant vapor Vg3 as a third system. , And the third absorber A3 and the third regenerator G3.

  The third absorber A3 is disposed between the first absorber A1 and the second absorber A2 when viewed from the flow of the temperature raising target fluid RP. In the absorption heat exchange system 8, the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 in the absorption heat exchange system 3 (see FIG. 3) are connected by the temperature-rising target communication pipe 71 (see FIG. 3) Instead of the above, the first absorption heat transfer pipe 11 and the third absorption heat transfer pipe 311 are connected by the first heating target communication pipe 71A, and the second absorption heat transfer pipe 15 and the third absorption heat transfer pipe 311 are (2) It is connected by the temperature increase target communication pipe 71B. With such a configuration, the temperature raising target fluid RP flowing through the temperature rising fluid introduction pipe 51 flows in series in the order of the second absorber A2, the third absorber A3 and the first absorber A1, and the temperature rising fluid outlet pipe 53 It has come to The third evaporator E3 and the third regenerator G3 are between the first evaporator E1 and the first regenerator G1 and the second evaporator E2 and the second regenerator G2 as viewed from the flow of the drive heat source fluid RS. It is arranged. In the absorption type heat exchange system 8, the first regeneration heat source pipe 31 and the second evaporation heat source pipe 25 are connected by the heat source intermediate communication pipe 77 in the absorption type heat exchange system 3 (see FIG. 3), The first regeneration heat source pipe 31 and the third evaporation heat source pipe 321 are connected by the first heat source intermediate connection pipe 77A, and the second evaporation heat source pipe 25 and the third regeneration heat source pipe 331 are the second heat source intermediate connection pipe 77B. It is connected. The third evaporation heat source pipe 321 and the third regeneration heat source pipe 331 are connected by a heat source third connection pipe 79. With such a configuration, the drive heat source fluid RS flowing through the drive heat source introduction pipe 52 is supplied to the first evaporator E1, the first regenerator G1, the third evaporator E3, the third regenerator G3, the second evaporator E2, the second It flows in series in order of 2 regenerators G2 to reach the drive heat source outflow pipe 56. The third condenser C3 is disposed between the first condenser C1 and the second condenser C2 when viewed from the flow of the low-temperature heat source fluid GP. In the absorption heat exchange system 8, the first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45 are connected by the low temperature heat source communication pipe 74 (see FIG. 3) in the absorption heat exchange system 3 (see FIG. 3) Instead, the first condensing heat transfer pipe 41 and the third condensing heat transfer pipe 341 are connected by the first low temperature heat source communication pipe 74A and the second condensing heat transfer pipe 45 and the third condensing heat transfer pipe 341 have the second low temperature. The heat source communication pipe 74B is connected. With such a configuration, the low temperature heat source fluid GP flowing through the low temperature heat source introduction pipe 57 flows in series in the order of the second condenser C2, the third condenser C3 and the first condenser C1 to reach the low temperature heat source outflow pipe 58 It has become. The remaining configuration of the absorptive heat exchange system 8 is the same as that of the absorptive heat exchange system 3 (see FIG. 3).

In addition to being able to manage multiple absorption heat pump cycles of the absorption liquid S and the refrigerant V similarly to the absorption type heat exchange system 3 (see FIG. 3), the absorption type heat exchange system 8 configured in this way can Since the temperature raising target fluid RP flows through the second absorber A2, the third absorber A3 and the first absorber A1 and is heated three times, the temperature of the temperature raising target fluid RP supplied to the heat utilization facility HCF is absorbed It can be higher than the heat exchange system 3 (see FIG. 3). Further, the temperature of the drive heat source fluid RS flowing through the first evaporator E1 is higher than the temperature of the drive heat source fluid RS flowing through the third evaporator E3, and the temperature of the drive heat source fluid RS flowing through the third evaporator E3 is the second Since the internal pressure and temperature of each evaporator and each absorber are lower than the temperature of the second evaporator E2 and the second absorber A2 because the temperature of the heat source fluid RS flowing through the evaporator E2 is higher than that of the driving heat source fluid RS, (3) The internal pressure and temperature of the evaporator E3 and the third absorber A3 become higher in the order of the internal pressure and temperature of the first evaporator E1 and the first absorber A1, and when the fluid RP to be heated is introduced in this order, The temperature of the temperature raising target fluid RP to be heated can be successively raised. A fourth absorber, a fourth evaporator, and a fourth regenerator according to the configuration in which the third absorber A3, the third evaporator E3, the third regenerator G3, and the third condenser C3 are added. , A fourth condenser, and a fourth absorber, a fourth evaporator, a fourth condenser between the second absorber A2 and the second evaporator E2 and the third regenerator G3 and the third condenser C3. The fourth regenerator and the fourth condenser may be provided. With this configuration, the temperature raising target fluid RP is heated four times, and the temperature after heating can be increased.

  In the above description, the low-temperature heat source fluid GP having flowed out of the first condenser C1 and the second condenser C2 flowed out of the first evaporator E1 and the second evaporator E2, and the first regenerator G1 and the second regenerator G2. The heat source fluid RS is to be merged, but the fluid flowing in the first condensation heat transfer pipe 41 of the first condenser C1 and the second condensation heat transfer pipe 45 of the second condenser C2 The low temperature heat source outlet pipe 58 is connected to the driving heat source outlet pipe 56 and the heat source fluid outlet pipe 59 while the low temperature heat source outlet pipe 58 is connected to the heat source fluid outlet pipe 59 while The fluid flowing out of the condenser C1 and the second condenser C2 may be joined to the driving heat source fluid RS. Further, the low temperature heat source fluid GP which has flowed out the first condenser C1 and the second condenser C2 without connecting the low temperature heat source outflow pipe 58 to the driving heat source outflow pipe 56 and the heat source fluid outflow pipe 59 is the first evaporator E1 and the first evaporator E1. The two evaporators E2 and the first regenerator G1 and the second regenerator G2 may not be merged with the flowed out drive heat source fluid RS, but may be introduced into an independent system separate from the system of the combined heat source fluid RA. Furthermore, the fluid flowing in the first condensation heat transfer pipe 41 of the first condenser C1 and the second condensation heat transfer pipe 45 of the second condenser C2 is introduced from a system independent of the fluid flowing out of the heat utilization facility HCF. In addition, the low temperature heat source outflow pipe 58 may not be connected to the driving heat source outflow pipe 56 and the heat source fluid outflow pipe 59, and may flow out to a system independent of the heat source equipment HSF (in this case, from the heat utilization equipment HCF The discharged fluid may be joined to the driving heat source fluid RS. In this way, a wide variety of heat can be used.

  In the above description, although the temperature raising target fluid RP flows in series through the first absorber A1 and the second absorber A2 and the third absorber A3 when they are present, they may flow in parallel. Assuming that the temperature raising target fluid RP flows in parallel in the respective absorbers A1, A2 and A3, the flow resistance when flowing in the respective absorbers A1, A2 and A3 can be made smaller than in the case of flowing in series. It is suitable when the pressure difference permitted when flowing the temperature raising target fluid RP is small.

  In the above description, the heating source fluid (the combined heat source fluid RA, the driving heat source fluid RS) and the fluid to be heated (the temperature raising target fluid RP, the low temperature heat source fluid GP) are the same type fluid because they are divided and merged. The fluid to be applied may be a heat medium liquid or a chemical liquid other than warm water. In particular, when a heat medium liquid or a chemical liquid having a boiling point higher than that of water is used, application to a high temperature range may be possible without exerting high pressure on the fluid in order to suppress boiling of the fluid.

  In the above description, in the absorption heat exchange systems 1, 2, 3, 4, 5, 6, 7, 8, the first evaporator E1 and the second evaporator E2 and the third evaporator E3, if present, are full Although it is a formula, it may be a falling film type. When the evaporator is a falling liquid film type, the refrigerant liquid Vf is supplied to the upper part in the evaporator like the first refrigerant liquid supply device 22 or the second refrigerant liquid supply device 26 in the absorption type heat exchange systems 1A and 1B. A refrigerant liquid supply device may be provided, and the end of the refrigerant liquid pipe, which is to be connected to the evaporator in the case of the liquid-filled type, may be connected to the refrigerant liquid supply device. Moreover, you may provide piping and a pump which supply the refrigerant liquid Vf of the lower part of an evaporator to a refrigerant liquid supply apparatus. On the contrary, in the absorption type heat exchange systems 1A and 1B in which the evaporator is a falling liquid film type, the evaporator may be a full liquid type such as the absorption type heat exchange system 1 or the like.

  In the above description, in the absorption heat exchange systems 1A and 1B, the first evaporator E1 is disposed above the first absorber A1 in the first absorption evaporator cylinder 10, and the second evaporator E2 is arranged in the second absorption evaporator cylinder 20. The evaporator E2 is disposed above the second absorber A2, the first condenser C1 is disposed above the first regenerator G1 in the first regenerative condenser can barrel 30, and the second condenser C1 is disposed in the second regenerative condenser cylinder 40. The condenser C2 is disposed above the second regenerator G2. However, in the first absorption evaporator can barrel 10, the first absorber A1 is disposed above the first evaporator E1, and the second absorption evaporator can barrel At 20, the second absorber A2 is disposed above the second evaporator E2, and at the first regeneration condenser can barrel 30, the first regenerator G1 is disposed above the first condenser C1, and the second regeneration condenser can At 40, the second regenerator G2 may be disposed above the second condenser C2.

  In the above description, in the absorption-type heat exchange systems 7 and 8, the temperature raising target fluid RP is made to flow in series in the order of the second absorber A2, the third absorber A3 and the first absorber A1. Conversely, the first absorber A1, the third absorber A3, and the second absorber A2 may be flowed in series in this order. Also, although the low temperature heat source fluid GP is made to flow in series in the order of the second condenser C2, the third condenser C3 and the first condenser C1, the first condenser C1 and the third condenser are conversely reversed. It is good also as flowing in series in order of C3 and the 2nd condenser C2.

1, 1A, 1B, 2, 3, 4, 5, 6, 7, 8 absorption heat exchange system 10 first absorption evaporation can barrel 14 first dilution solution outflow pipe 18 second dilution solution outflow pipe 20 second absorption evaporation Can barrel 30 first regenerated condensing can barrel 34 first concentrated solution outflow pipe 38 second concentrated solution outflow pipe 40 second regenerated condensing can barrel A1 first absorber A2 second absorber A3 third absorber C1 first condenser C2 Second Condenser C3 Third Condenser E1 First Evaporator E2 Second Evaporator E3 Third Evaporator G1 First Regenerator G2 Second Regenerator G3 Third Regenerator RS Drive Heat Source Fluid RP Heat-up Target Fluid GP Low temperature heat source fluid Sa concentrated solution Sa1 first concentrated solution Sa2 second concentrated solution Sa3 third concentrated solution Sw dilute solution Sw1 first dilute solution Sw2 second dilute solution Sw3 third dilute solution Ve1 first evaporator refrigerant vapor Ve2 second evaporation Refrigerant vapor Ve3 third evaporator refrigerant vapor Vf refrigerant liquid Vf1 First refrigerant liquid Vf2 Second refrigerant liquid Vf3 Third refrigerant liquid Vg1 First regenerator refrigerant vapor Vg2 Second regenerator refrigerant vapor Vg3 Third regenerator refrigerant vapor

Claims (10)

A first absorption unit that raises the temperature of the first fluid to be heated by the absorption heat released when the absorption liquid absorbs the vapor of the refrigerant;
A second absorption unit that raises the temperature of the first fluid to be heated by the absorption heat released when the absorption liquid absorbs the vapor of the refrigerant;
A first condensation section that raises the temperature of the second fluid to be heated by the heat of condensation released when the refrigerant vapor condenses into a refrigerant liquid;
A second condensation section that raises the temperature of the second fluid to be heated by the heat of condensation released when the refrigerant vapor condenses into a refrigerant liquid;
The refrigerant liquid is introduced directly or indirectly from at least one of the first condenser and the second condenser, and the introduced refrigerant is evaporated and supplied to the first absorber. A first evaporation section which lowers the temperature of the heat source fluid by depriving the heat source fluid of the latent heat of vaporization necessary for becoming the vapor of
The refrigerant liquid is introduced directly or indirectly from at least one of the first condenser and the second condenser, and the introduced refrigerant is evaporated and supplied to the second absorber. A second evaporation section which lowers the temperature of the heat source fluid by depriving the heat source fluid of the latent heat of vaporization necessary for becoming the vapor of
The absorption liquid is introduced directly or indirectly from at least one of the first absorption part and the second absorption part, and is introduced to generate the vapor of the refrigerant supplied to the first condensation part. A first regenerating unit that lowers the temperature of the heat source fluid by removing from the heat source fluid the heat necessary to heat the absorbent solution and release the refrigerant from the absorbent solution;
The absorption liquid is introduced directly or indirectly from at least one of the first absorption unit and the second absorption unit, and is introduced to generate the vapor of the refrigerant supplied to the second condensation unit. A second regenerating unit that lowers the temperature of the heat source fluid by removing from the heat source fluid the heat necessary to heat the absorbent solution and release the refrigerant from the absorbent solution;
Due to the absorption heat pump cycle of the absorbing liquid and the refrigerant, the internal pressure and temperature of the first evaporator become higher than that of the first condenser, and the second evaporator is the second condenser. Configured to have higher internal pressure and temperature than;
The part of the heat source fluid branched from the heat source fluid before being introduced to the first evaporation part, the second evaporation part, the first regeneration part and the second regeneration part Configured to be introduced into the first absorbing portion and the second absorbing portion as a first heated fluid;
Absorption heat exchange system. The second to-be-heated fluid that has flowed out from the first condenser and the second condenser is the first evaporator, the second evaporator, the first regenerator, and the second regenerator. The flow path of the second heated fluid is configured to join the heating source fluid that has flowed out of the regeneration unit;
The absorption heat exchange system according to claim 1. The absorbing liquid that has flowed out from at least one of the first absorbing portion and the second absorbing portion directly or indirectly flows in parallel into the first regeneration portion and the second regeneration portion. The absorbing liquid that has flowed out from at least one of the first regeneration unit and the second regeneration unit flows directly or indirectly into the first absorption unit and the second absorption unit in parallel. The flow path of the absorbing fluid
The absorption heat exchange system according to claim 1 or 2. The absorbing liquid that has flowed directly or indirectly from at least one of the first absorbing portion and the second absorbing portion into the first regenerating portion or the second regenerating portion is the first regenerating portion and the first regenerating portion The absorption that flows in series in the second regeneration unit and flows directly or indirectly from at least one of the first regeneration unit and the second regeneration unit into the first absorption unit or the second absorption unit A flow path of the absorbing liquid is configured such that the liquid flows in series through the first absorbing portion and the second absorbing portion;
The absorption heat exchange system according to claim 1 or 2. The absorbing liquid flowing out of the first absorbing portion flows into the first regenerating portion and the absorbing liquid flowing out of the first regenerating portion flows into the first absorbing portion. A first absorbent circulation passage that circulates between the first absorbent portion and the first regeneration portion;
The absorbing liquid flowing out of the second absorbing portion flows into the second regenerating portion and the absorbing liquid flowing out of the second regenerating portion flows into the second absorbing portion. And a second absorbent circulation passage that circulates between the second absorber and the second regeneration unit;
The absorption heat exchange system according to claim 1 or 2. A flow path of the first fluid to be heated is configured such that the first fluid to be heated flows in series through the first absorbing portion and the second absorbing portion;
The absorption-type heat exchange system according to any one of claims 1 to 5. The heating source fluid first flows into the first regeneration unit or the first evaporation unit, and the first regeneration unit, the first evaporation unit, the second regeneration unit, and the second The flow path of the heat source fluid is configured to flow in series in an appropriate order in the evaporation section of
In the case where the first heated fluid flows through the second evaporating unit after the heating source fluid flows through the first evaporating unit, the first heated fluid flows through the second absorbing unit, and then the first absorbing unit If the heat source fluid flows in the second evaporation section and then flows in the first evaporation section, the heat source fluid flows in the first absorption section and then flows in the second absorption section. A flow path of the first heated fluid;
The flow path of the second heated fluid is configured such that the second heated fluid flows in series through the first condensing portion and the second condensing portion;
The absorption-type heat exchange system according to any one of claims 1 to 6. The heating source fluid is introduced in parallel to at least two of the first evaporation unit, the second evaporation unit, the first regeneration unit, and the second regeneration unit. The flow path of the first heated fluid is configured such that the flow path is configured, and the first heated fluid is introduced in parallel to the first absorbing portion and the second absorbing portion. And a flow path of the second heated fluid is configured such that the second heated fluid is introduced in parallel to the first condensing portion and the second condensing portion. And at least one of which is configured to be performed;
The absorption-type heat exchange system according to any one of claims 1 to 5. A first regenerated condensing can barrel that accommodates the first regeneration unit and the first condensation unit such that the first regeneration unit and the first condensation unit communicate with each other;
A first absorption evaporation can body that accommodates the first absorption portion and the first evaporation portion such that the first absorption portion and the first evaporation portion communicate with each other;
A second regenerated condensing can barrel that accommodates the second regeneration unit and the second condensation unit such that the second regeneration unit and the second condensation unit communicate with each other;
And a second absorption evaporator can that accommodates the second absorption portion and the second evaporation portion such that the second absorption portion and the second evaporation portion communicate with each other;
Said first regenerative condensing can barrel and said second regenerative condensing can barrel are disposed at different positions in the horizontal direction;
The first absorption evaporator cylinder and the second absorption evaporator cylinder are disposed at horizontally different positions;
The first absorbing evaporator can and the second absorbing evaporator are disposed above the first regenerative condensing can and the second regenerative condensing can;
An absorption heat exchange system according to any one of claims 1 to 8. A third absorbing section which raises the temperature of the first fluid to be heated by the absorption heat released when the absorbing liquid absorbs the vapor of the refrigerant;
A third condensation section that raises the temperature of the second fluid to be heated by the heat of condensation released when the refrigerant vapor condenses into a refrigerant liquid;
The refrigerant liquid is introduced directly or indirectly from at least one of the first condenser part, the second condenser part and the third condenser part, and the introduced refrigerant liquid is evaporated and the third A third evaporation unit that reduces the temperature of the heat-source fluid by depriving the heat-source fluid of the latent heat of vaporization necessary for becoming vapor of the refrigerant supplied to the absorber;
The absorbing liquid is introduced directly or indirectly from at least one of the first absorbing portion, the second absorbing portion, and the third absorbing portion, and the refrigerant supplied to the third condensing portion A third regeneration for reducing the temperature of the heat source fluid by heating the absorbent solution introduced to generate vapor and depriving the heat source fluid of heat necessary for separating the refrigerant from the absorbent solution. With the department;
The third evaporating section is configured to have a higher internal pressure and temperature than the third condensing section by an absorption heat pump cycle of the absorbing liquid and the refrigerant;
The heating before being introduced to the first evaporation unit, the second evaporation unit, the third evaporation unit, the first regeneration unit, the second regeneration unit, and the third regeneration unit It is configured to introduce a part of the heating source fluid branched from the source fluid as the first heated fluid to the first absorbing portion, the second absorbing portion and the third absorbing portion. ;
An absorption heat exchange system according to any one of claims 1 to 9.

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