JP2019113260A - Absorption type heat exchange system - Google Patents

Abstract

To provide an absorption 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 A first absorption portion A1, a second absorption portion A2, a first condensation portion C1 and a second condensation portion C2 for increasing a temperature of a heated fluid FL, a first evaporation portion E1, a second evaporation portion E2, a first regeneration portion G1 and a second regeneration portion G2 for lowering a temperature of a heating source fluid FH, and a heat exchange portion 80 for exchanging heat between the heated fluid FL before flowing out from the condensation portions C1, C2 and flowing into the absorption portions A1, A2, and a part of the heating source fluid FHs branched from the heating source fluid FH before introduced to the evaporation portions E1, E2 and the regeneration portions G1, G2. 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 the heated fluid FL flowing out from the heat exchange portion 80, flows into the absorption portions A1, A2.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 exchange is performed between two fluids such that the outlet temperature of the cryogenic fluid is higher than the inlet temperature of the hot 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. Since waste heat is heat that is discarded without being used, the outlet temperature of the low temperature fluid that recovers the waste heat and raises the temperature should be higher than the inlet temperature of the high temperature fluid containing waste heat. If it is possible, the range of utilization will be expanded.

  SUMMARY OF THE INVENTION In view of the above problems, the present invention provides an absorption heat exchange system capable of making the outlet temperature of a heated fluid corresponding to a low temperature fluid higher than the inlet temperature of a heating source fluid corresponding to a high temperature fluid. The purpose is

  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 absorption part A1 for raising the temperature of the fluid to be heated FL; and a second absorption part A2 for raising the temperature of the fluid to be heated FL by the absorption heat released when the absorbent Sa absorbs the vapor Ve2 of the refrigerant. And the first condensation section C1 which raises the temperature of the fluid to be heated FL by condensation heat released when the refrigerant vapor Vg1 condenses and becomes the refrigerant liquid Vf1; and the refrigerant liquid Vf2 condenses the refrigerant vapor Vg2 And / or the second condenser C2 which raises the temperature of the fluid to be heated FL by the heat of condensation released from the liquid; and / or the refrigerant liquid directly or indirectly from at least one of the first condenser C1 and the second condenser C2. Introduced Vf, The temperature of the heat source fluid FH is lowered by depriving the heat source fluid FH of the latent heat of vaporization necessary when the introduced refrigerant liquid Vf evaporates and becomes the vapor Ve1 of the refrigerant supplied to the first absorption section A1 The refrigerant liquid Vf is directly or indirectly introduced from at least one of the evaporation part E1 of 1; the first condensation part C1 and the second condensation part C2, and the introduced refrigerant liquid Vf is evaporated and the second absorption part A second evaporation section E2 for reducing the temperature of the heat source fluid FH by depriving the heat source fluid FH of the evaporation latent heat necessary for becoming the vapor Ve2 of the refrigerant supplied to the A2; a first absorption section A1 and The absorbing solution Sw is introduced directly or indirectly from at least one of the second absorbing units A2 to heat the introduced absorbing solution Sw in order to generate the vapor Vg1 of the refrigerant supplied to the first condensing unit C1. Required to separate the refrigerant from the absorbent Sw. Heat from the heat source fluid FH to lower the temperature of the heat source fluid FH directly or indirectly from at least one of the first regeneration unit G1 and the first absorption unit A1 and the second absorption unit A2; In order to introduce the absorbing solution Sw and generate the refrigerant vapor Vg2 supplied to the second condenser C2, the heat necessary for heating the introduced absorbing solution Sw and separating the refrigerant from the absorbing solution Sw is used. A second regeneration unit G2 that lowers the temperature of the heating source fluid FH by depriving the heating source fluid FH; a first condensing unit C1 and a second condensing unit C2; The fluid to be heated FL before flowing into the two absorption units A2, and heating before being introduced into the first evaporation unit E1, the second evaporation unit E2, the first regeneration unit G1, and the second regeneration unit G2 Heat exchange is performed between a part of the heat source fluid FHs branched from the source fluid FH The first heat exchange section E1 has a higher internal pressure and temperature than the first condensation section C1, and the second heat evaporation section E2 is provided. Is configured such that the internal pressure and temperature are higher than that of the second condensation part C2; the heated fluid FL that has flowed out of the heat exchange part 80 flows into the first absorption part A1 and the second absorption part A2 Thus, the flow path of the heated fluid FL is configured.

  According to this structure, the temperature of the fluid to be heated which flows out from the first absorbing portion and the second absorbing portion can be calculated by using the first evaporating portion, the second evaporating portion, the first regenerating portion, and the second regenerating portion. It can be higher than the temperature of the heat source fluid before entering the

  The absorption heat exchange system according to the second aspect of the present invention is, for example, as shown in FIG. 1, an outflow from the heat exchange section 80 in the absorption heat exchange system 1 according to the first aspect of the present invention. The heated source fluid FHs is combined with the heated source fluid FH that has flowed out 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

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

  In order to achieve the above object, in the absorption heat exchange system according to the third aspect of the present invention, for example, as shown in FIG. 2, the absorption heat released when the absorption liquid Sa absorbs the refrigerant vapor Ve1 A first absorption part A1 for raising the temperature of the fluid to be heated FL; and a second absorption part A2 for raising the temperature of the fluid to be heated FL by the absorption heat released when the absorbent Sa absorbs the vapor Ve2 of the refrigerant. And the first condensation section C1 which raises the temperature of the fluid to be heated FL by the condensation heat released when the refrigerant vapor Vg1 condenses and becomes the refrigerant liquid Vf1; the refrigerant vapor Vg2 condenses and the refrigerant liquid Vf2 And / or the second condenser C2 which raises the temperature of the fluid to be heated FL by the heat of condensation released from the liquid; and / or the refrigerant liquid directly or indirectly from at least one of the first condenser C1 and the second condenser C2. Introduce Vf, The temperature of the heat source fluid FH is lowered by depriving the heat source fluid FH of the latent heat of vaporization necessary when the introduced refrigerant liquid Vf evaporates and becomes the vapor Ve1 of the refrigerant supplied to the first absorption section A1 The refrigerant liquid Vf is directly or indirectly introduced from at least one of the evaporation part E1 of 1; the first condensation part C1 and the second condensation part C2, and the introduced refrigerant liquid Vf is evaporated and the second absorption part A second evaporation section E2 for reducing the temperature of the heat source fluid FH by depriving the heat source fluid FH of the evaporation latent heat necessary for becoming the vapor Ve2 of the refrigerant supplied to the A2; a first absorption section A1 and The absorbing solution Sw is introduced directly or indirectly from at least one of the second absorbing units A2 to heat the introduced absorbing solution Sw in order to generate the vapor Vg1 of the refrigerant supplied to the first condensing unit C1. Required to separate the refrigerant from the absorbent Sw. Heat from the heat source fluid FH to lower the temperature of the heat source fluid FH directly or indirectly from at least one of the first regeneration unit G1 and the first absorption unit A1 and the second absorption unit A2; In order to introduce the absorbing solution Sw and generate the refrigerant vapor Vg2 supplied to the second condenser C2, the heat necessary for heating the introduced absorbing solution Sw and separating the refrigerant from the absorbing solution Sw is used. A second regeneration unit G2 that lowers the temperature of the heating source fluid FH by depriving the heating source fluid FH; a first condensing unit C1 and a second condensing unit C2; 2 to be heated before flowing into the absorption part A2, the heating source fluid FH which has flowed out from the first evaporation part E1, the second evaporation part E2, the first regeneration part G1, and the second regeneration part G2 And a heat exchange unit 80 for heat exchange between the absorption liquid and the refrigerant. The pressure and temperature inside the first evaporator E1 is higher than the pressure in the first condenser C1, and the pressure and temperature inside the second evaporator E2 is higher than the second condenser C2. The flow path of the to-be-heated fluid FL so that the to-be-heated fluid FL flowing out of the heat exchange unit 80 flows into the first absorbing unit A1 and the second absorbing unit A2 There is.

  According to this structure, the temperature of the fluid to be heated which flows out from the first absorbing portion and the second absorbing portion can be calculated by using the first evaporating portion, the second evaporating portion, the first regenerating portion, and the second regenerating portion. It can be higher than the temperature of the heat source fluid before entering the

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

  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 fifth aspect of the present invention is, for example, as shown in FIG. 3, an absorption heat according to any one of the first to third aspects of the present invention. In the exchange system 3, the absorbent flowing into the first regeneration unit G1 or the second regeneration unit G2 directly or indirectly from at least one of the first absorption unit A1 and the second absorption unit A2 is the first regeneration. Part G1 and the second regeneration part G2 flow in series, from at least one of the first regeneration part G1 and the second regeneration part G2 directly or indirectly to the first absorbing part A1 or the second absorbing part A2 A flow path of the absorbing liquid is configured such that the inflowing absorbing liquid flows through the first absorbing portion A1 and the second absorbing portion A2 in series.

  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 sixth aspect of the present invention is, for example, as shown in FIG. 4, an absorption heat according to any one of the first to third aspects of the present invention. In the exchange system 4, 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. As described above, the first absorbent circulation passage 14 and 34 for circulating the absorbent between the first absorbent part A1 and the first regeneration part G1; and the absorbent Sw2 having flowed out the second absorbent A2 The second absorbing portion A2 and the second regenerating portion G2 are configured such that the absorbent Sa2 flowing into the second regenerating portion G2 and flowing out of the second regenerating portion G2 flows into the second absorbing portion A2. And a second absorbent circulation passage 18, 38 for circulating between them.

  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 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 flow path of the fluid to be heated FL is configured such that the fluid to be heated FL flows in series through the first absorption portion A1 and the second absorption portion A2.

  With this configuration, the temperature of the fluid to be heated can be raised in two steps, and the fluid to be heated at a higher temperature can be taken out.

  The absorption heat exchange system according to the eighth aspect of the present invention is, for example, as shown in FIG. 5, an absorption heat according to any one of the first to seventh aspects of the present invention. In the exchange system 5, the heating source fluid FH 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 FH is configured to flow in series in an appropriate order in the G2 and the second evaporation part E2; the fluid to be heated FL includes the first condensation part C1 and the second condensation part C2 After flowing in series, it flows into the first absorption part A1 or the second absorption part A2, and when the heat source fluid FH flows in the first evaporation part E1 and then flows in the second evaporation part E2, the second Of the heat source fluid FH so as to flow through the first absorbing portion A1 after flowing through the absorbing portion A2 of In the case of flowing through the first evaporating unit E1 after flowing through the evaporating unit E2, the flow path of the fluid to be heated FL is configured to flow through the second absorbing unit A2 after flowing through the first absorbing unit A1. There is.

  According to this structure, when the heat source fluid first flows into the first regeneration unit, the amount of heat transferred from the heat source fluid to the fluid to be heated can be increased, and the temperature of the fluid to be discharged is increased. In the case where the heating source fluid first flows into the first evaporation section, in addition to the increase in the amount of heat transferred from the heating source fluid to the heating fluid and the increase in temperature of the flowing heating fluid, the first It is possible to suppress an increase in the concentration of the absorbing liquid in the regenerating part and the second regenerating part, and it is possible to avoid that the absorbing liquid is excessively concentrated and crystallized.

  Further, an absorption heat exchange system according to a ninth aspect of the present invention relates to any one of the first aspect to the sixth aspect of the present invention as shown in, for example, FIG. 6 and FIG. In the absorption type heat exchange systems 6, 7, the heat source fluid FH 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 FH is configured to be introduced (see, for example, FIG. 7), and the heated fluid FL is introduced in parallel to the first absorbing portion A1 and the second absorbing portion A2 The heating fluid FL (not shown) and / or the heating fluid FL is at least one of introduced into the first condenser C1 and the second condenser C2 in parallel (for example, see FIG. 6). And at least one of the forming of the flow path of the .

  With this configuration, the resistance of at least one of the heat source fluid and the fluid to be heated can be reduced.

  The absorption heat exchange system according to the tenth aspect of the present invention is, for example, as shown in FIG. 8, an absorption heat according to any one of the first to ninth 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 steam containing 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; The first regenerative condenser cylinder 30 and the second regenerative condenser cylinder 40 are disposed at different positions in the horizontal direction; the first absorption evaporator cylinder 10 and the second absorption evaporator can The first absorbing evaporator can 10 and the second absorbing evaporator can 20 are disposed above the first regenerative condenser can 30 and the second regenerative condensing can 40, respectively. 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 eleventh aspect of the present invention is, for example, as shown in FIG. 10, an absorption heat according to any one of the first to tenth aspects of the present invention. In the exchange system 9, the third absorbing portion A3 which raises the temperature of the fluid to be heated FL 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 and the refrigerant liquid At least one of a third condenser C3 for raising the temperature of the fluid FL to be heated by the heat of condensation released when Vf3 is reached; a first condenser C1, a second condenser C2, and a third condenser C3; The latent heat of vaporization required when the refrigerant liquid Vf is introduced directly or indirectly from one source and the introduced refrigerant liquid Vf evaporates to become the vapor Ve3 of the refrigerant supplied to the third absorption part A3 Heat source fluid FH by taking away from The absorbing liquid Sw is introduced directly or indirectly from at least one of the third evaporation part E3 for reducing the temperature; the first absorption part A1, the second absorption part A2 and the third absorption part A3, In order to generate the vapor Vg3 of the refrigerant to be supplied to the condenser C3 of 3, the heat necessary for removing the refrigerant from the absorbing liquid Sw is removed from the heat source fluid FH by heating the introduced absorbing liquid Sw. And a third regeneration unit G3 for reducing the temperature of the heating source fluid FH; the pressure and temperature inside the third evaporation unit E3 are higher than those of the third condensation unit C3 by the absorption heat pump cycle of the absorbing liquid and the refrigerant The heat exchange unit 80 flows out of the first condenser C1, the second condenser C2 and the third condenser C3 to form a first absorption part A1 and a second absorption part A2. And the heated fluid FL before flowing into the third absorbing portion A3 Flow of the fluid to be heated FL so that the fluid to be heated FL that has flowed out of the heat exchange unit 80 flows into the first absorption unit A1, the second absorption unit A2, and the third absorption unit A3. The road is configured.

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

  According to the present invention, the temperature of the fluid to be heated which flows out from the first absorbing portion and the second absorbing portion is the temperature of the first evaporating portion, the second evaporating portion, the first regenerating portion, and the second regenerating portion. It can be higher than the temperature of the heat source fluid before entering the

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 typical systematic diagram of the absorption type heat exchange system concerning a 7th 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 the 8th Embodiment of this invention. It is a typical systematic diagram of the absorption type heat exchange system concerning a 9th embodiment of the present invention. It is a typical systematic diagram of the absorption type heat exchange system concerning a 10th 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. In the absorption heat exchange system 1, the low temperature fluid FL and the high temperature fluid FH are used so that the outlet temperature of the low temperature fluid FL is higher than the inlet temperature of the high temperature fluid FH using the absorption heat pump cycle of the absorption liquid and the refrigerant. Heat exchange system. Here, the low temperature fluid FL is a fluid whose temperature is to be raised in the absorption heat exchange system 1, and corresponds to a fluid to be heated. The high temperature fluid FH is a fluid whose temperature is reduced in the absorption heat exchange system 1 and corresponds to a heating source fluid. Examples of the low-temperature fluid FL include fluids used for heating and other heat sources of heat-source equipment such as other absorption refrigerators and absorption heat pumps. Examples of the high temperature fluid FH include fluids discharged from a steel mill, a power plant, a factory manufacturing process, and the like. 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. A heat regenerator 80 is further provided, including a 1 regenerator G1, a second regenerator G2, a first condenser C1, and a second condenser C2.

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 path of the low temperature fluid FL, 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. Have to. 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 low temperature fluid FL flowing through the first absorption heat transfer tube 11 so that the low temperature fluid FL 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 high temperature fluid FH to generate a first evaporator refrigerant vapor Ve1, and corresponds to a first evaporation unit. The first evaporator E1 has a first evaporating heat source pipe 21 constituting a flow path of the high temperature fluid FH 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). The first evaporator E1 is configured such that the refrigerant liquid Vf around the first evaporation heat source pipe 21 is evaporated by the heat of the high temperature fluid FH flowing in the first evaporation heat source pipe 21 to generate a first evaporator refrigerant vapor Ve1. It is done. 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 is internally provided with a second absorption heat transfer tube 15 constituting a flow path of the low temperature fluid FL, and a second absorber solution supply device 16 for supplying the concentrated solution Sa to the surface of the second absorption heat transfer tube 15 Have to. 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 low temperature fluid FL flowing through the second absorption heat transfer tube 15, so that the low temperature fluid FL 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 an absorber low temperature fluid 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 high temperature fluid FH to generate a second evaporator refrigerant vapor Ve2, and corresponds to a second evaporation unit. The 2nd evaporator E2 has the 2nd evaporation heat source pipe 25 which comprises the flow path of the high temperature fluid FH inside the can barrel of the 2nd 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. The second evaporator E2 is configured such that the refrigerant liquid Vf around the second evaporation heat source pipe 25 evaporates with the heat of the high temperature fluid FH flowing in the second evaporation heat source pipe 25 to generate a second evaporator refrigerant vapor Ve2 It is done. One end of the first evaporation heat source pipe 21 and one end of the second evaporation heat source pipe 25 are connected by an evaporator high temperature fluid communication pipe 72. 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 is a first regeneration heat source pipe 31 for flowing the high temperature fluid FH for heating the dilute solution Sw inside, and a first regenerator solution supply device for supplying the dilution solution Sw to the surface of the first regeneration heat source pipe 31 And 32. In the first regenerator G 1, the dilute solution Sw supplied from the first regenerator solution supply device 32 is heated to the high temperature fluid FH flowing in the first regeneration heat source pipe 31 to evaporate the refrigerant V from the dilute solution Sw. Thus, the first concentrated solution Sa1 having an increased concentration is generated. 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 fluid FL to form the first refrigerant liquid Vf1, and corresponds to a first condensation section. . The first condenser C1 has a first condensation heat transfer pipe 41 through which the low temperature fluid FL 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 fluid FL flowing in the space 41 receives heat, so that the low temperature fluid FL is heated to increase its temperature. 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 is a second regenerating heat source pipe 35 for flowing the high temperature fluid FH for heating the dilute solution Sw inside, and a second regenerator solution supply device for supplying the dilute solution Sw to the surface of the second regenerating heat source pipe 35 And 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 high temperature fluid FH flowing in the second regeneration heat source pipe 35, whereby the refrigerant V is evaporated from the dilute solution Sw. Thus, the second concentrated solution Sa2 having an increased concentration is generated. 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 regenerative heat source pipe 35 and one end of the first regenerative heat source pipe 31 are connected by a regenerator high temperature fluid 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 a device that cools and condenses the second regenerator refrigerant vapor Vg2 generated in the second regenerator G2 with the low temperature fluid FL to form the second refrigerant liquid Vf2, and corresponds to a second condensation unit. . The second condenser C2 has a second condensation heat transfer pipe 45 through which the low temperature fluid FL 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 fluid FL flowing inside 45 receives heat, and the low temperature fluid FL 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 condenser low temperature fluid 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 low temperature 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 absorber low temperature fluid communication pipe 71 is connected. Is connected. The cryogenic fluid outflow pipe 53 is a pipe that constitutes a flow path through which the heated cryogenic fluid FL flows. Further, an end of the second absorption heat transfer pipe 15 of the second absorber A2 opposite to the end to which the end of the absorber low temperature fluid connection pipe 71 is connected, and a first condensation transfer of the first condenser C1. An absorption condensation cryogenic fluid communication pipe 81 is connected to an end of the heat pipe 41 opposite to the end to which the one end of the condenser cryogenic fluid communication pipe 74 is connected. 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 evaporator high temperature fluid communication pipe 72 is connected, and a second regenerated heat source of the second regenerator G2. An evaporation regenerative high temperature fluid communication pipe 75 is connected to the end of the pipe 35 opposite to the end to which the end of the regenerator high temperature fluid communication pipe 73 is connected. Further, a high temperature 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 evaporator high temperature fluid communication pipe 72 is connected. There is. The high temperature heat source outflow pipe 56 is a pipe that constitutes a flow path for flowing the high temperature fluid FH which is used as a heat source and whose temperature is lowered. In addition, as described above, the first condensation heat transfer pipe 41 of the first condenser C1 has an absorption condensation low temperature fluid at the end opposite to the end to which the one end of the condenser low temperature fluid connection pipe 74 is connected. One end of the communication pipe 81 is connected. Further, the end of the second condensation heat transfer pipe 45 of the second condenser C2 opposite to the end to which the end of the condenser low temperature fluid connection pipe 74 is connected is the low temperature fluid FL before it is heated. A low temperature fluid introduction pipe 57 that constitutes a flow path is connected.

  In addition, a high temperature heat source introduction pipe 52 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 one end of the regenerator high temperature fluid communication pipe 73 is connected. There is. The high temperature heat source introduction pipe 52 is a pipe that constitutes a flow path for leading the high temperature fluid FH before the temperature drops. The high temperature heat source introduction pipe 52 is provided with a high temperature heat source valve 52v for adjusting the flow rate of the high temperature fluid FH flowing therein. The other end of the high temperature heat source introduction pipe 52 is connected to the high temperature fluid inflow pipe 55 together with the other end of the heat exchange branch pipe 82. The high temperature fluid inflow tube 55 is a tube constituting a flow path through which the high temperature fluid FH flows before the partial high temperature fluid FHs branches. The partial high temperature fluid FHs is branched from the high temperature fluid FH, and the substance is the high temperature fluid FH, but in view of its use, it is another name for convenience of explanation in view of its use. The high temperature fluid FH flowing through the high temperature fluid inflow pipe 55 is configured such that a part of the high temperature fluid FH flows into the heat exchange branch pipe 82 and the rest flows into the high temperature heat source introduction pipe 52. The heat exchange branch pipe 82 is provided with a heat exchange branch valve 82v that adjusts the flow rate of the partial high temperature fluid FHs flowing inside. The other end of the heat exchange branch pipe 82 is connected to the high temperature fluid outflow pipe 59 together with the other end of the high temperature heat source outflow pipe 56. The high temperature fluid outflow pipe 59 is a pipe constituting a flow path through which the high temperature fluid FH flows after the partial high temperature fluid FHs flowing through the heat exchange branch pipe 82 merges with the high temperature fluid FH flowing through the high temperature heat source outflow pipe 56 is there.

  In the present embodiment, the heat exchange unit 80 is disposed in the absorption-condensing low-temperature fluid communication pipe 81 and the heat exchange branch pipe 82, and the heat-exchange branch with the low-temperature fluid FL flowing through the absorption-condensing low-temperature fluid communication pipe 81 Heat exchange is performed with the partial high temperature fluid FHs flowing through the pipe 82. The heat exchange unit 80 is typically configured of a shell and tube type heat exchanger, but may be a device that performs heat exchange between two fluids, such as a plate type heat exchanger.

  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.

  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 and condensed by the low temperature fluid FL flowing through the first condensing heat transfer pipe 41 As a result, the first refrigerant liquid Vf1 is obtained. At this time, the temperature of the low temperature fluid FL rises due to the heat of condensation released when the first regenerator refrigerant vapor Vg1 condenses. 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 second regenerator refrigerant vapor Vg2 is cooled and condensed by the low temperature fluid FL flowing through the second condensation heat transfer pipe 45 As a result, the second refrigerant liquid Vf2 is obtained. At this time, the temperature of the low temperature fluid FL rises due to the heat of condensation released when the second regenerator refrigerant vapor Vg2 condenses. In the present embodiment, since the low temperature fluid FL flows through the second condensation heat transfer pipe 45 and then flows through the first condensation heat transfer pipe 41 via the condenser low temperature fluid connection pipe 74, the low temperature fluid FL 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 that has flowed into the first evaporator E1 is heated by the high temperature fluid FH flowing through the first evaporation heat source pipe 21 and is evaporated to become the first evaporator refrigerant vapor Ve1. At this time, the high temperature fluid FH 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 high temperature fluid FH flowing through the second evaporation heat source pipe 25 and is evaporated to become the second evaporator refrigerant vapor Ve2. At this time, the high temperature fluid FH 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 high temperature fluid FH flows through the first evaporation heat source pipe 21 and then flows through the second evaporation heat source pipe 25 via the evaporator high temperature fluid communication pipe 72, the temperature of the high temperature fluid FH flowing through the first evaporation heat source pipe 21 is The temperature is higher than when flowing through the second evaporation heat source pipe 25, and the internal pressure of the first evaporator E1 is higher than the internal pressure of the second evaporator E2.

  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. The absorbed heat heats the low temperature fluid FL flowing through the first absorption heat transfer tube 11, and the temperature of the low temperature fluid FL 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. The absorbed heat heats the low temperature fluid FL flowing through the second absorption heat transfer tube 15, and the temperature of the low temperature fluid FL rises. Since the low temperature fluid FL flows through the second absorption heat transfer pipe 15 and then flows through the first absorption heat transfer pipe 11 via the absorber low temperature fluid connection pipe 71, the low temperature fluid outflow pipe 53 flows out of the first absorber A1. The temperature of the low temperature fluid FL is higher than the temperature of the low temperature fluid flowing through the absorber low temperature fluid communication pipe 71, and the temperature of the low temperature fluid FL can be further raised. 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 high temperature fluid FH flowing through the first regeneration heat source pipe 31, and the refrigerant in the supplied dilute solution Sw is evaporated. As a result, it becomes a first concentrated solution Sa1 and is stored in the lower part of the first regenerator G1. At this time, the high temperature fluid FH flowing in the first regeneration heat source pipe 31 is deprived of heat by the dilute solution Sw and the temperature drops. 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 high temperature fluid FH flowing through the second regeneration heat source pipe 35, and the refrigerant in the supplied dilute solution Sw is supplied. Is evaporated to form a second concentrated solution Sa2, which is stored in the lower part of the second regenerator G2. At this time, the high temperature fluid FH 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.

  Changes in the temperatures of the low temperature fluid FL and the high temperature fluid FH in the process of performing the absorption heat pump cycle as described above by the absorption liquid S and the refrigerant V will be described by way of specific examples. Assuming that the high temperature fluid FH flowing through the high temperature fluid inlet pipe 55 is 95 ° C., the divided high temperature fluid FH and the partial high temperature fluid FHs are also 95 ° C., respectively. When the 95 ° C. high temperature fluid FH flowing through the high temperature heat source inlet tube 52 flows through the first regeneration heat source tube 31 of the first regenerator G1, its temperature is reduced due to the heat taken away by the dilute solution Sw and thereafter the regenerator It flows into the second regenerator G2 via the high temperature fluid communication pipe 73, and when it flows through the second regeneration heat source pipe 35 of the second regenerator G2, heat is taken away by the dilute solution Sw, and the evaporation regeneration high temperature fluid communication pipe When it reaches 75, the temperature drops to 88 ° C. Thereafter, when flowing through the first evaporation heat source pipe 21 of the first evaporator E1, the high temperature fluid FH flowing through the evaporation / regeneration high temperature fluid communication pipe 75 loses heat by the refrigerant liquid Vf to lower its temperature, and then evaporates. Heat flows into the second evaporator E2 via the high temperature fluid communication pipe 72 and flows through the second evaporation heat source pipe 25 of the second evaporator E2, the heat is taken away by the refrigerant liquid Vf, and the high temperature heat source outflow pipe 56 The temperature drops to 81 ° C. The partial high temperature fluid FHs branched from the high temperature fluid inflow pipe 55 and flowing into the heat exchange branch pipe 82 flows toward the heat exchange unit 80 and flows into the heat exchange unit 80.

  On the other hand, when the low temperature fluid FL flowing through the low temperature fluid introduction pipe 57 is 32 ° C., the low temperature fluid FL flowing through the low temperature fluid introduction pipe 57 flows through the second condensation heat transfer pipe 45 of the second condenser C2. The second regenerator refrigerant vapor Vg2 is condensed to become the refrigerant liquid Vf to obtain the condensation heat released and the temperature rises, and then flows into the first condenser C1 via the condenser low temperature fluid communication pipe 74 The heat of condensation that is released when the first regenerator refrigerant vapor Vg1 condenses and becomes the refrigerant liquid Vf when flowing through the first condensation heat transfer pipe 41 of the first condenser C1 is obtained by absorption condensation low temperature fluid communication When the tube 81 is reached, the temperature rises to 53 ° C. The cryogenic fluid FL flowing through the absorption condensation cryogenic fluid communication pipe 81 flows into the heat exchange unit 80. In the heat exchange unit 80, heat exchange is performed between the low temperature fluid FL flowing through the absorbing and condensing low temperature fluid communication pipe 81 and the partial high temperature fluid FHs flowing through the heat exchange branch pipe 82, and the low temperature fluid FL of 53 ° C. is 92 ° C. The temperature rises and the 95 ° C. partial hot fluid FHs drops in temperature to 56 ° C. The partial high temperature fluid FHs whose temperature has dropped to 56 ° C. continues to flow through the heat exchange branch pipe 82 and merges with the 81 ° C. high temperature fluid FH flowing through the high temperature heat source outlet pipe 56 to become a high temperature fluid FH 75 ° C. It flows through the fluid outflow pipe 59 and is discharged from the absorption heat exchange system 1. On the other hand, when the low temperature fluid FL whose temperature has risen to 92 ° C. flows from the absorption condensation low temperature fluid connection pipe 81 into the second absorption heat transfer pipe 15 of the second absorber A 2 and flows through the second absorption heat transfer pipe 15, The concentrated solution Sa obtains the heat of absorption generated when absorbing the second evaporator refrigerant vapor Ve2, and the temperature rises, and then flows into the first absorber A1 through the absorber low temperature fluid communication pipe 71, 1) When flowing through the first absorption heat transfer pipe 11 of the absorber A1, the absorption heat generated when the concentrated solution Sa absorbs the first evaporator refrigerant vapor Ve1 is obtained, and reaches the low temperature fluid outflow pipe 53, 111 The temperature rises to ° C. At this time, the temperature of the high temperature fluid FH flowing through the first evaporator E1 is higher than the temperature of the high temperature fluid FH flowing through the second evaporator E2, so the internal pressure and temperature of the second evaporator E2 and the second absorber A2 are , Lower than the internal pressure and temperature of the first evaporator E1 and the first absorber A1, and when the low temperature fluid FL is introduced in order from the second absorber A2 to the first absorber A1, the heating and raising in the respective absorbers A2 and A1 The temperature of the warmed low-temperature fluid FL can be raised in order. The 111 ° C. cryogenic fluid FL flowing through the cryogenic fluid outflow pipe 53 is supplied to the use site.

  In the absorption type heat exchange system 1, the ratio of the flow rate of the high temperature fluid FH flowing through the high temperature heat source introduction pipe 52 to the flow rate of the partial high temperature fluid FHs flowing through the heat exchange branch pipe 82 in order to establish the above temperature relationship. And the ratio of the flow rate of the cryogenic fluid FL to the flow rate of the partial hot fluid FHs. In the present embodiment, the flow ratio of the high temperature fluid FH to the partial high temperature fluid FHs is approximately 4: 1. It should be noted that the temperature of the low temperature fluid FL flowing out of the heat exchange unit 80 rises relatively if the flow rate of the partial high temperature fluid FHs is increased, and the temperature decrease flowing out of the heat exchange unit 80 if the flow rate of the partial high temperature fluid FHs is decreased The temperature of the fluid FL is lowered. Further, in the present embodiment, the flow ratio of the low temperature fluid FL to the partial high temperature fluid FHs is about 1: 1. Here, the flow rate ratio of each of the high temperature fluid FH, the partial high temperature fluid FHs, and the low temperature fluid FL may be fixed by using piping or an orifice having a size adopted according to a predetermined value. It may be configured to be adjustable automatically or manually using a heat source valve 52v and a heat exchange branch valve 82v or an alternative three-way valve), etc., and is provided in a control device (not shown) in the case of automatic adjustment. It may be set in advance in the storage device (not shown), or may be set as needed by an input device (not shown) provided in the control device. In this manner, the temperature (111 ° C.) of the low temperature fluid FL flowing out of the absorption heat exchange system 1 can be higher than the temperature (95 ° C.) of the high temperature fluid FH flowing into the absorption heat exchange system 1 . Here, the absorption type heat exchange system 1 can be regarded as one heat exchanger which performs heat exchange between the high temperature fluid FH and the low temperature fluid FL. In the conventional heat exchanger, if the flow rate of the low temperature fluid is smaller than the flow rate of the high temperature fluid, the outlet temperature of the low temperature fluid can be made closer to the inlet temperature of the high temperature fluid. It could not be higher than the inlet temperature. In this point, in the absorption heat exchange system 1 according to the present embodiment, as described above, the temperature of the low temperature fluid FL flowing out of the absorption heat exchange system 1 is the high temperature fluid FH flowing into the absorption heat exchange system 1. And can be suitable for long distance transport of thermal fluid.

  As explained above, according to the absorption type heat exchange system 1 according to the present embodiment, the first absorber A1, the second absorber A2, and the first evaporator E1 that exhibit the function of the type 2 absorption heat pump , High temperature fluid indirectly through the absorption heat pump cycle of the absorbing liquid S and the refrigerant V in the second evaporator E2, the first regenerator G1, the second regenerator G2, the first condenser C1, and the second condenser C2 By performing heat exchange between FH and the low temperature fluid FL and directly performing heat exchange between the partial high temperature fluid FH (high temperature fluid FH) and the low temperature fluid FL in the heat exchange unit 80, the low temperature fluid FL is high temperature After removing the heat from the fluid FH, the temperature of the cryogenic fluid FL flowing out of the absorption heat exchange system 1 can be made higher than the temperature of the incoming hot fluid FH. Further, since the first absorber A1 and the second absorber A2 are provided, it is possible to increase the temperature of the low temperature fluid FL as compared with the case of one absorber. Further, in the absorption heat exchange system 1, the low temperature fluid FL passed through the first condenser C1 and the second condenser C2 is introduced into the first absorber A1 and the second absorber A2 to raise the temperature of the low temperature fluid FL Since the second type absorption heat pump does not require cooling water, incidental facilities (cooling water pump, cooling tower, etc.) are not required. Further, in the absorption type heat exchange system 1, there is no heat to be discarded in the cooling water as in the type 2 absorption heat pump, and the heat of condensation in the first condenser C1 and the second condenser C2 is used to heat the low temperature fluid FL. Because of this, the efficiency (COP) can be made higher (approximately twice as much) than a type 2 absorption heat pump and equal to a large heat exchanger.

  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 high temperature fluid FH flowing into the heat exchange section 80 is a first evaporator E1 and a second evaporator E2. The first regenerator G1 and the second regenerator G2 are not the partial high temperature fluid FHs (see FIG. 1) branched from the high temperature fluid FH before entering, but the high temperature fluid FH after leaving It 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 heat exchange branch pipe 82 provided with the heat exchange branch valve 82v provided in the absorption type heat exchange system 1 (see FIG. 1) is not provided. Also, the high temperature heat source valve 52v is not provided. Further, the heat exchange unit 80 is disposed in the high temperature fluid outflow pipe 59 instead of the heat exchange branch pipe 82, and the high temperature fluid flowing through the low temperature fluid FL flowing through the absorption condensation low temperature fluid communication pipe 81 and the high temperature fluid outflow pipe 59. It is comprised so that heat exchange may be performed with FH. 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). It should be noted that the high temperature fluid inflow pipe 55 and the high temperature heat source introduction pipe 52 are naturally integrated because there is no piping (the heat exchange branch pipe 82 (see FIG. 1)) branched to their connection point. Although it is good, for convenience of comparison with the absorption type heat exchange system 1 (refer to FIG. 1), it is supposed that the two names are kept. Similarly, although the high temperature heat source outflow pipe 56 and the high temperature fluid outflow pipe 59 may be integrally configured, they are assumed to have the same names.

  In the absorption type heat exchange system 2 configured as described above, the high temperature fluid FH flowing through the first regenerator G1, the second regenerator G2, the first evaporator E1, and the second evaporator E2 is absorbed heat exchange system 1 Compared to the case of (see FIG. 1), the flow rate is increased by the amount that the partial high temperature fluid FHs (see FIG. 1) does not branch, but flows through the high temperature heat source outflow pipe 56 and the high temperature fluid outflow pipe 59 When it flows in, it will be 82 degreeC of temperature lower than absorption type heat exchange system 1 (refer FIG. 1). On the other hand, the 32.degree. C. cryogenic fluid FL flowing through the cryogenic fluid inlet pipe 57 rises in temperature to 58.degree. C. in the second condenser C2 and the first condenser C1 and reaches the condensing cryogenic fluid communication pipe 81, and the heat exchange section 80 Flow into In the heat exchange unit 80, heat exchange is performed between the high temperature fluid FH flowing through the high temperature fluid outflow pipe 59 and the low temperature fluid FL flowing through the absorbing condensation low temperature fluid communication pipe 81, and the high temperature fluid FH at 82 ° C is heated to 77 ° C. The temperature of the low temperature fluid FL of 58.degree. C. rises to 79.degree. The flow ratio of the high temperature fluid FH and the low temperature fluid FL passing through the heat exchange unit 80 is about 4: 1. Thus, since the flow ratio of the high temperature fluid FH to the low temperature fluid FL in the heat exchange unit 80 is relatively large, the heat transfer performance of the heat exchange unit 80 is improved to reduce the heat transfer area per heat exchange amount. be able to. The high temperature fluid FH having a temperature lowered to 77 ° C. and flowing out of the heat exchange unit 80 continues to flow through the high temperature fluid outflow pipe 59 and is discharged from the absorption heat exchange system 1. The temperature of the low temperature fluid FL which has risen to 79 ° C. and flows out from the heat exchange unit 80 flows into the first absorber A1 in the same manner as the absorption heat exchange system 1 (see FIG. 1), and the first absorber A1 and the first absorber A1 are 2) After the temperature rises to 104 ° C. in the absorber A2, it flows through the cryogenic fluid outflow pipe 53 and is supplied to the use site. In the absorption type heat exchange system 2, since the temperature of the low temperature fluid FL heated by the heat exchange unit 80 is lowered, the temperature of the low temperature fluid FL flowing out to the low temperature fluid outflow pipe 53 is the absorption type heat exchange system 1 (FIG. 1) and the amount of heat given from the high temperature fluid FH to the low temperature fluid FL also decreases. Like the absorption heat exchange system 1 (see FIG. 1), the absorption heat exchange system 2 makes the temperature of the low temperature fluid FL flowing out of the absorption heat exchange system 2 higher than the temperature of the inflowing high temperature fluid FH It is possible to raise the temperature of the cryogenic fluid FL compared to the case of one absorber.

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. Absorption type heat exchange system 3
In comparison with the absorption heat exchange system 1 (see FIG. 1), the flow of the absorption liquid S and the refrigerant V and the flow sequence of the low temperature fluid FL and the evaporative regeneration high temperature fluid communication pipe 75 The order of flow of the high temperature fluid FH at the downstream side is different. 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 second dilute solution outflow pipe 18 for flowing the second dilute solution Sw2 flowing out of 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-type heat exchange system 3, 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 3, the other end of the second refrigerant liquid outflow pipe 48 for flowing the second refrigerant liquid Vf2 which has flowed 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 Further, in the absorption type heat exchange system 3, an evaporator refrigerant liquid introduction pipe 28 for supplying a part of the first refrigerant liquid Vf1 stored in the second evaporator E2 to the first 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 3, 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 3, the low temperature fluid 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. There is. One end of the absorption condensation cryogenic fluid communication pipe 81 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 condenser cold fluid communication pipe 74 is connected There is. The other end of the absorption condensation low temperature fluid communication pipe 81 is connected to one end of the first absorption heat transfer pipe 11 of the first absorber A1, not the second absorption heat transfer pipe 15 of the second absorber A2. One end of a low temperature fluid outflow pipe 53 is connected to an end of the second absorption heat transfer pipe 15 of the second absorber A2 opposite to the end to which the low temperature fluid communication pipe 71 is connected. With such a configuration, the cryogenic fluid FL flowing through the cryogenic fluid introduction pipe 57 flows in series in the order of the first condenser C1, the second condenser C2, the first absorber A1, and the second absorber A2, and the cryogenic fluid outflow The tube 53 is to be reached. Further, in the absorption type heat exchange system 3, the other end of the evaporation / regeneration high temperature fluid communication pipe 75 whose one end is connected to the second regeneration heat source pipe 35 is not the first evaporation heat source pipe 21 of the first evaporator E1, but It is connected to one end of the second evaporation heat source pipe 25 of the two-evaporator E2. One end of a high temperature 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 evaporator high temperature fluid connection pipe 72 is connected. With such a configuration, the high temperature fluid FH flowing through the evaporative regeneration high temperature fluid communication pipe 75 after flowing through the first regenerator G1 and the second regenerator G2 in series is in the order of the second evaporator E2 and the first evaporator E1. It flows in series to reach the high temperature heat source outlet pipe 56. 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 heat exchange system 3 configured in this manner causes the temperature of the cryogenic fluid FL flowing through the second condenser C2 to be higher than the temperature of the cryogenic fluid FL flowing through the first condenser C1, and thus the second regenerator G2 Since the internal pressure of the second condenser 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, It is suitable for flowing the absorbing solution 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 3, 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. 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 heat exchange system 4 is different from the absorption heat exchange system 2 (see FIG. 2) in the flow of the absorption liquid S and the refrigerant V and the flow order of the high temperature fluid FH when viewed from an overview. . 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 2 (see FIG. 2) mainly in the following points. In the absorption type heat exchange system 4, 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 4, 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 4, 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 4, the second dilute solution Sw2 and the second concentrated solution Sa2 are circulated 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 4, instead of the solution heat exchanger 62 (see FIG. 2), 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 4, the other end of the first refrigerant liquid outflow pipe 44 for flowing the first refrigerant liquid Vf1 which has 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 4, the refrigerant V changes phases with the first refrigerant liquid Vf 1, the first evaporator refrigerant vapor Ve 1, and the first regenerator refrigerant vapor Vg 1 as a first system, and the first condenser C 1 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 4, the end of the high temperature heat source introduction pipe 52 opposite to the end connected to the high temperature fluid inflow pipe 55 is the first regenerative heat source pipe 31 of the first regenerator G1. Instead, it is connected to one end of the first evaporation heat source pipe 21 of the first evaporator E1. 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. One end of the high temperature heat source outflow pipe 56 is connected to the other end of the second regenerative heat source pipe 35, and the other end of the high temperature heat source outflow pipe 56 is connected to the end of the high temperature fluid outflow pipe 59. With such a configuration, the high temperature fluid FH flowing through the high temperature 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, and the high temperature heat source outflow The tube 56 is to be reached. In the absorption heat exchange system 4, the evaporator high temperature fluid communication pipe 72, the regenerator high temperature fluid communication pipe 73, and the evaporative regeneration high temperature fluid communication pipe 75 provided in the absorption heat exchange system 2 (see FIG. 2) Not provided. The remaining configuration of the absorptive heat exchange system 4 is similar to that of the absorptive heat exchange system 2 (see FIG. 2). The absorption 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, and controls and manages the absorption heat pump cycle with a plurality. Can. In addition, since the temperature of the high temperature fluid FH is lower in the first regenerator G1 than in the first evaporator E1, the increase in the concentration of the absorbent S in the first regenerator G1 is suppressed, and the absorbent S becomes excessive. Concentration can be avoided.

  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 4 (see FIG. 4) in the order of the flow of the high temperature fluid FH and the state of the high temperature fluid FH flowing into the heat exchange section 80 ing. 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 4 (see FIG. 4) mainly in the following points. In the absorption heat exchange system 5, the heat exchange branch pipe 82 is disposed in the same manner as the absorption heat exchange system 1 (see FIG. 1), and in the heat exchange unit 80, the low temperature flowing through the absorption condensation low temperature fluid communication pipe 81 Heat exchange is performed between the fluid FL and the partial high temperature fluid FHs flowing through the heat exchange branch pipe 82. Further, the end of the high temperature heat source introduction pipe 52 opposite to the end connected to the high temperature fluid inflow pipe 55 and the heat exchange branch pipe 82 is the first evaporation heat source pipe 21 of the first evaporator E1. Instead, it 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 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 high temperature 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 ends of the heat exchange branch pipe 82 and the high temperature fluid outflow pipe 59. With such a configuration, the high temperature fluid FH flowing through the high temperature 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 to flow out the high temperature heat source The tube 56 is to be reached. The remaining configuration of the absorptive heat exchange system 5 is similar to that of the absorptive heat exchange system 4 (see FIG. 4). The absorption type heat exchange system 5 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 4. Multiple heat pump cycles can be controlled and managed. Further, in the absorption heat exchange system 5, the temperature of the high temperature fluid FH 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 higher than that of the absorption heat exchange system 4 (see FIG. 4). Since the temperature also becomes high, depending on the operating conditions, the temperature after raising the temperature of the low temperature fluid FL can be made higher than that of the absorption heat exchange system 4 (see FIG. 4) to increase the heat output.

  In the absorption type heat exchange systems 4 and 5 shown in FIG. 4 and FIG. 5, ascension occurs in a situation where there is an existing type 2 absorption heat pump provided with an absorber, an evaporator, a regenerator and a condenser. When it is desired to further increase the temperature of the fluid to be warmed, a second absorption heat pump equipped with an absorber, an evaporator, a regenerator, and a condenser is additionally provided and piping of the high temperature fluid FH and the low temperature fluid FL Can be connected as shown in the present embodiment to make a slight change to the control system.

  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-type heat exchange system 6 is different from the absorption-type heat exchange system 1 (see FIG. 1) in the flow direction of the low-temperature fluid FL upstream of the heat exchange unit 80 when viewed from an overview. Accordingly, the configuration of the absorption type heat exchange system 6 differs 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 6, the low temperature fluid introduction pipe 57 is branched into a first low temperature fluid introduction pipe 57A and a second low temperature fluid introduction pipe 57B on the way, and the first low temperature fluid introduction pipe 57A is a first condenser C1. The second low temperature fluid introduction pipe 57B is connected to one end of the second condensation heat transfer pipe 45 of the second condenser C2. The other end of the first condensation heat transfer pipe 41 is connected to one end of a first absorption condensation low temperature fluid communication pipe 81A, and the other end of the second condensation heat transfer pipe 45 is connected to one end of a second absorption condensation low temperature fluid communication pipe 81B. It is done. The other end of the first absorbent condensation cryogenic fluid communication pipe 81A and the other end of the second absorbent condensation cryogenic fluid communication pipe 81B are both connected to one end of the absorbent condensation cryogenic fluid communication pipe 81, and the absorbent condensation cryogenic fluid communication pipe The other end of 81 is connected to the end of the second absorption heat transfer tube 15 of the second absorber A2 after passing through the heat exchange unit 80. In the absorption heat exchange system 6, the condenser low temperature fluid communication pipe 74 provided in the absorption heat exchange system 1 (see FIG. 1) is not provided. With such a configuration, the low temperature fluid FL flowing through the low temperature fluid introduction pipe 57 is divided into the first low temperature fluid introduction pipe 57A and the second low temperature fluid introduction pipe 57B, and the low temperature fluid FL is supplied to the first condenser C1 and the second condenser C2. After flowing in parallel and respectively flowing out to the first absorbing / condensing cryogenic fluid communication pipe 81A and the second absorbing / condensing cryogenic fluid communication pipe 81B, they merge again and reach the absorbing / condensing cryogenic fluid communication pipe 81. The remaining configuration of the absorptive heat exchange system 6 is the same as that of the absorptive heat exchange system 1 (see FIG. 1). The absorption-type heat exchange system 6 configured in this way has a flow resistance at the time when the low temperature fluid FL is divided and flows through the first condenser C1 and the second condenser C2, as shown in FIG. (See Reference), which is preferable when the allowable pressure difference in flowing the low temperature fluid FL is small.

  Next, an absorption heat exchange system 7 according to a seventh embodiment of the present invention will be described with reference to FIG. FIG. 7 is a schematic system diagram of the absorption type heat exchange system 7. The absorption heat exchange system 7 is different from the absorption heat exchange system 4 (see FIG. 4) in terms of the flow of the high temperature fluid FH in overview. Accordingly, the configuration of the absorption heat exchange system 7 differs from the configuration of the absorption heat exchange system 4 (see FIG. 4) mainly in the following points. In the absorption type heat exchange system 7, the high temperature heat source introduction pipe 52 (see FIG. 4) is not provided, and one end of the first high temperature heat source introduction pipe 52A and one end of the second high temperature heat source introduction pipe 52B are high temperature fluid inflow pipes Connected to 55. The other end of the first high temperature heat source introduction pipe 52A is connected to one end of the first evaporation heat source pipe 21 of the first evaporator E1, and the other end of the second high temperature heat source introduction pipe 52B is a second evaporation heat source of the second evaporator E2. It is connected to one end of the tube 25. One end of a first high-temperature heat source outflow pipe 56A is connected to an end of the first regenerative heat source pipe 31 of the first regenerator G1 opposite to the end to which the heat source first connection pipe 76 is connected. . One end of a second high temperature heat source outflow pipe 56B is connected to an 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. . The other end of the first high temperature heat source outflow pipe 56A and the other end of the second high temperature heat source outflow pipe 56B are connected to the high temperature fluid outflow pipe 59. In the absorption type heat exchange system 7, the high temperature heat source outflow pipe 56 and the heat source intermediate communication pipe 77 provided in the absorption type heat exchange system 4 (see FIG. 4) are not provided. With such a configuration, the high temperature fluid FH flowing through the high temperature fluid inflow pipe 55 is divided into the first high temperature heat source introduction pipe 52A and the second high temperature heat source introduction pipe 52B, and the first evaporator E1 and the first regenerator G1 , Flows in parallel to the second evaporator E2 and the second regenerator G2 and flows out to the first high temperature heat source outflow pipe 56A and the second high temperature heat source outflow pipe 56B respectively, and then merges into the high temperature fluid outflow pipe 59. Finally, it flows toward the heat exchange unit 80. The remaining configuration of the absorptive heat exchange system 7 is the same as that of the absorptive heat exchange system 4 (see FIG. 4). The absorption-type heat exchange system 7 configured in this manner causes the high temperature fluid FH to branch and flow 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 made smaller than that of the absorption heat exchange system 4 (see FIG. 4), which is suitable when the pressure difference allowed in flowing the high temperature fluid FH is small. In the example shown in FIG. 7, of the two high temperature fluids FH divided from the high temperature fluid inflow pipe 55, one flows from the first evaporator E1 to the first regenerator G1, and the other flows from the second evaporator E2 to the second Although it is assumed that the two regenerators G2 flow, 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 high temperature fluid FH flowing through the high temperature fluid inflow pipe 55 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 hot fluid FH flows through each regenerator and each evaporator can be minimized.

  Next, with reference to FIG. 8, an absorption heat exchange system 1A according to a 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 1A. In the absorption heat exchange system 1A, the flow of fluid (absorption liquid S, refrigerant V, low temperature fluid FL, high temperature fluid FH) is the same as that of the absorption heat exchange system 1 (see FIG. 1). More specifically, the arrangement of 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 respective top portions of the first absorption heat transfer tube 11 and the second absorption heat transfer tube 15 are the same, it is possible to suppress the pressure applied for pumping the low temperature fluid FL. 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, the pressure applied to pump the high temperature fluid FH can be suppressed. 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. Assuming that 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 are close to each other, taking into consideration only the mounting height of the pipe 18 The height can be reduced to make the device configuration compact.

  Next, with reference to FIG. 9, an absorption heat exchange system 8 according to an eighth embodiment of the present invention will be described. FIG. 9 is a schematic block diagram of the absorption type heat exchange system 8. The absorption-type heat exchange system 8 is different from the absorption-type heat exchange system 1A (see FIG. 8) in the flow of the high-temperature fluid FH when viewed from an overview. Along with this, the configuration of the absorption type heat exchange system 8 is different from the configuration of the absorption type heat exchange system 1A (see FIG. 8) mainly in the following points. In the absorption type heat exchange system 8, as in the absorption type heat exchange system 2 (see FIG. 2), the heat exchange branch pipe 82 (see FIG. 8) in which the heat exchange branch valve 82v (see FIG. 8) is disposed. Is not provided, along with which the high temperature heat source valve 52v (see FIG. 8) is not provided, and the heat exchange unit 80 is replaced with the heat exchange branch pipe 82 (see FIG. 8) to provide a high temperature fluid. It is arranged in the outflow pipe 59. Moreover, in the absorption type heat exchange system 8, the end on the opposite side to the end connected to the high temperature fluid inflow pipe 55 of the high temperature heat source introduction pipe 52 is the first regenerative heat source pipe 31 of the first regenerator G1. Instead, it is connected to one end of the first evaporation heat source pipe 21 of the first evaporator E1. At the end of the second evaporation heat source pipe 25 opposite to the end connected to the evaporator high temperature fluid communication pipe 72, one end of the evaporation regenerative high temperature fluid communication pipe 75, not the high temperature heat source outflow pipe 56 It is connected. The other end of the evaporation / regeneration high temperature fluid communication pipe 75 is connected not to the second reproduction heat source pipe 35 but to one end of the first reproduction heat source pipe 31. One end of the high temperature heat source outflow pipe 56 is connected to the end of the second regenerative heat source pipe 35 opposite to the end connected to the regenerator high temperature fluid communication pipe 73. With such a configuration, the high temperature fluid FH flowing through the high temperature 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 flow out the high temperature heat source The tube 56 is to be reached. The remaining configuration of the absorption-type heat exchange system 8 is similar to that of the absorption-type heat exchange system 1A (see FIG. 8). The absorption-type heat exchange system 8 configured as described above has the temperature of the high-temperature fluid FH introduced into the second regenerator G2 and the first regenerator G1 compared to the absorption-type heat exchange system 1A (see FIG. 8). As the heat is reduced by the amount of heat consumed by the first evaporator E1 and the second evaporator E2, an increase in the concentration of the absorbent S in the second regenerator G2 and the first regenerator G1 can be suppressed. It is possible to avoid excessive concentration and crystallization of S.

  Although the flow sequences of the high temperature fluid FH and the low temperature fluid FL have been illustrated in the description of the various embodiments so far, the flow sequences of these fluids are not limited to those illustrated, for example, shown below You can change it as appropriate. When the high temperature fluid FH is configured to flow in series to the devices 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 1 evaporator E1. Here, when the high temperature fluid FH flows into the first regenerator G1 first, the flow of the high temperature fluid FH which has flowed out of the first regenerator G1 will be shown in the order of flow only by the code for the convenience of explanation. , (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 high temperature fluid FH first flows into the first evaporator E1, the flow of the high temperature fluid FH which has flowed out of the first evaporator E1 will be (7) E2, G1 in the order of flow only with reference numerals. , G2, (8) E2, G2, G1, (9) G1, E2, G2, (10) G2, E2, G1, (11) G1, G2, E2, (12) G2, G1, E2, It will be. When the high temperature fluid FH flows in series in any of the above-described manners, the order of flow of the low temperature fluid FL is the first evaporator E1 and the second evaporation regardless of the order of the first regenerator G1 and the second regenerator G2. Focusing only on the order of the vessel E2, when the high temperature fluid FH flows in the order of the first evaporator E1 and the second evaporator E2, the low temperature fluid FL flows in the order of the second absorber A2 and the first absorber A1, and the high temperature fluid When FH flows in the order of the second evaporator E2 and the first evaporator E1, the low temperature fluid FL may flow in the order of the first absorber A1 and the second absorber A2. Further, the low temperature fluid FL on the upstream side of the heat exchange unit 80 may flow in series regardless of which of the first condenser C1 and the second condenser C2 comes first, but the first evaporator E1 and the second evaporation Focusing only on the order of the first regenerator G1 and the second regenerator G2 regardless of the order of the vessel E2, if the high temperature fluid FH flows in the order of the first regenerator G1 and the second regenerator G2, the low temperature fluid FL If the high temperature fluid FH flows in the order of the second regenerator G2 and the first regenerator G1, the low temperature fluid FL flows in the order of the first condenser C1 and the second condenser C2. It is preferable to configure to flow in order. When configured in any of the above-described modes, when the high temperature fluid FH first flows into the first regenerator G1, the amount of heat transferred from the high temperature fluid FH to the low temperature fluid FL can be increased and the low temperature fluid FL flows out. Temperature can be raised. On the other hand, when the high temperature fluid FH first flows into the first evaporator E1, the first regenerator G1 is added to the increase in heat transferred from the high temperature fluid FH to the low temperature fluid FL and the increase in temperature of the low temperature fluid FL which flows out. The increase in the concentration of the absorbing solution S in 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. 10, an absorption-type heat exchange system 9 according to a ninth embodiment of the present invention will be described. FIG. 10 is a schematic system diagram of the absorptive heat exchange system 9. The absorption heat exchange system 9 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 cryogenic fluid FL. In the absorption type heat exchange system 9, 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 absorber low temperature fluid connection 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 absorber low temperature fluid connection pipe 71A and the second absorption heat transfer pipe 15 and the third absorption heat transfer pipe 311 Are connected by a second absorber cryogenic fluid communication pipe 71B. Further, the third condenser C3 is disposed between the first condenser C1 and the second condenser C2 when viewed from the flow of the cryogenic fluid FL. In the absorption heat exchange system 9, the first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45 are connected by the condenser low temperature fluid communication pipe 74 (see FIG. 1) in the absorption heat exchange system 1 (see FIG. 1) Instead of the above, the first condensation heat transfer pipe 41 and the third condensation heat transfer pipe 341 are connected by the first condenser low temperature fluid connection pipe 74A, and the second condensation heat transfer pipe 45 and the third condensation heat transfer pipe 341 Are connected by a second condenser cryogenic fluid communication pipe 74B. With such a configuration, the low temperature fluid FL flowing through the low temperature fluid inlet pipe 57 is subjected to the second condenser C2, the third condenser C3, the first condenser C1, the heat exchange unit 80, the second absorber A2, the third absorption It flows in series in the order of the vessel A3 and the first absorber A1 to reach the cryogenic fluid outlet pipe 53. The third evaporator E3 is disposed between the first evaporator E1 and the second evaporator E2 when viewed from the flow of the high temperature fluid FH. In the absorption type heat exchange system 9, the first evaporation heat source pipe 21 and the second evaporation heat source pipe 25 are connected by the evaporator high temperature fluid communication pipe 72 (see FIG. 1) in the absorption type heat exchange system 1 (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 evaporator high temperature fluid connection pipe 72A and the second evaporation heat source pipe 25 and the third evaporation heat source pipe 321 Are connected by a second evaporator high temperature fluid communication pipe 72B. The third regenerator G3 is disposed between the first regenerator G1 and the second regenerator G2 as viewed from the flow of the high temperature fluid FH. In the absorption type heat exchange system 9, the first regeneration heat source pipe 31 and the second regeneration heat source pipe 35 are connected by the regenerator high temperature fluid communication pipe 73 (see FIG. 1) in the absorption type heat exchange system 1 (see FIG. 1). Instead of the above, the first regenerative heat source pipe 31 and the third regenerative heat source pipe 331 are connected by the first regenerator high temperature fluid communication pipe 73A and the second regenerative heat source pipe 35 and the third regenerative heat source pipe 331 Are connected by a second regenerator high temperature fluid communication pipe 73B. With such a configuration, the high temperature fluid FH flowing through the high temperature heat source introduction pipe 52 is subjected to the first regenerator G1, the third regenerator G3, the second regenerator G2, the first evaporator E1, the third evaporator E3, the second It flows in series in order of the evaporator E2 to reach the high temperature heat source outlet pipe 56. The remaining configuration of the absorptive heat exchange system 9 is the same as that of the absorptive heat exchange system 1 (see FIG. 1).

  In the absorption type heat exchange system 9 configured as described above, the low temperature fluid FL flows to the second condenser C2, the third condenser C3 and the first condenser C1 and is heated three times, and the heat exchange unit 80 After being heated, the temperature of the low temperature fluid FL flowing through the low temperature fluid outflow pipe 53 is absorbed by the heat exchange type heat exchanger, since it flows three times with the second absorber A2, the third absorber A3 and the first absorber A1. It can be higher than system 1 (see FIG. 1). Also, the temperature of the high temperature fluid FH flowing through the first evaporator E1 is higher than the temperature of the high temperature fluid FH flowing through the third evaporator E3, and the temperature of the high temperature fluid FH flowing through the third evaporator E3 is the second evaporator E2 Because 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, the internal pressure and temperature of each evaporator and each absorber are then the third evaporator E3. And the internal pressure and temperature of the first absorber A3 and the internal pressure and temperature of the first evaporator E1 and the first absorber A1, and when the low temperature fluid FL is introduced in this order, the low temperature is heated by each absorber The temperature of the fluid FL can be raised one after another. 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 cryogenic fluid FL can be heated four times to increase the temperature after heating.

  Next, with reference to FIG. 11, an absorption heat exchange system 10 according to a tenth embodiment of the present invention will be described. FIG. 11 is a schematic system diagram of the absorptive heat exchange system 10. The absorption heat exchange system 10 has a third absorber A3, a third evaporator in addition to the configuration of the absorption heat exchange system 4 (see FIG. 4) as compared to the absorption heat exchange system 4 (see FIG. 4) 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 9 (see FIG. 10), 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. 10) and not the third concentrated solution outflow pipe 334, which is connected to the third evaporator E3 is the third refrigerant liquid outflow pipe 344 instead of the third refrigerant liquid introduction pipe 323 (see FIG. 10) 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 9 (see FIG. 10), 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. 10) but not the third dilute solution outflow pipe 314. In the absorption type heat exchange system 10, the dilute solution joining pipe 61 (see FIG. 10) and the concentrated solution joining pipe 63 (see FIG. 10) provided in the absorption type heat exchange system 9 (see FIG. 10) are not provided. . In the absorption type heat exchange system 10, 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. In the absorption heat exchange system 10, a 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 cryogenic fluid FL. In the absorption heat exchange system 10, in the absorption heat exchange system 4 (see FIG. 4), the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 are connected by the absorber low temperature fluid communication pipe 71 (see FIG. 4) Instead of the above, the first absorption heat transfer pipe 11 and the third absorption heat transfer pipe 311 are connected by the first absorber low temperature fluid connection pipe 71A and the second absorption heat transfer pipe 15 and the third absorption heat transfer pipe 311 Are connected by a second absorber cryogenic fluid communication pipe 71B. Further, the third condenser C3 is disposed between the first condenser C1 and the second condenser C2 when viewed from the flow of the cryogenic fluid FL. In the absorption heat exchange system 10, the first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45 are connected by the condenser low temperature fluid communication pipe 74 (see FIG. 4) in the absorption heat exchange system 4 (see FIG. 4) Instead of the above, the first condensation heat transfer pipe 41 and the third condensation heat transfer pipe 341 are connected by the first condenser low temperature fluid connection pipe 74A, and the second condensation heat transfer pipe 45 and the third condensation heat transfer pipe 341 Are connected by a second condenser cryogenic fluid communication pipe 74B. With such a configuration, the low temperature fluid FL flowing through the low temperature fluid inlet pipe 57 is subjected to the second condenser C2, the third condenser C3, the first condenser C1, the heat exchange unit 80, the second absorber A2, the third absorption It flows in series in the order of the vessel A3 and the first absorber A1 to reach the cryogenic fluid outlet pipe 53. The third evaporator E3 and the third regenerator G3 are disposed 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 high temperature fluid FH. It is done. In the absorption type heat exchange system 10, 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 4 (see FIG. 4), 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 high temperature fluid FH flowing through the high temperature heat source introduction pipe 52 is subjected 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 the order of the regenerator G2 to reach the high temperature heat source outlet pipe 56. The remaining configuration of the absorptive heat exchange system 10 is the same as that of the absorptive heat exchange system 4 (see FIG. 4).

  In the absorption-type heat exchange system 10 configured in this manner, a plurality of independent paths (three) of absorption heat pump cycles of the absorption liquid S and the refrigerant V are provided similarly to the absorption-type heat exchange system 4 (see FIG. 4). In addition to being able to control and manage a plurality of absorption heat pump cycles, the low temperature fluid FL flows into the second condenser C2, the third condenser C3 and the first condenser C1 and heated three times. And the second absorber A2, the third absorber A3, and the first absorber A1 to be heated three times so that the cryogenic fluid FL flowing through the cryogenic fluid outflow pipe 53 is heated. Can be higher than the absorption heat exchange system 4 (see FIG. 4). Also, the temperature of the high temperature fluid FH flowing through the first evaporator E1 is higher than the temperature of the high temperature fluid FH flowing through the third evaporator E3, and the temperature of the high temperature fluid FH flowing through the third evaporator E3 is the second evaporator E2 Because 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, the internal pressure and temperature of each evaporator and each absorber are then the third evaporator E3. And the internal pressure and temperature of the first absorber A3 and the internal pressure and temperature of the first evaporator E1 and the first absorber A1, and when the low temperature fluid FL is introduced in this order, the low temperature is heated by each absorber The temperature of the fluid FL can be raised one after another. 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, and in this configuration, the low temperature fluid FL can be heated four times to increase the temperature after heating.

  In the above description, although the low temperature fluid FL 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. Alternatively, or instead, the cryogenic fluid FL flows mainly in series in the first condenser C1 and the second condenser C2 and the third condenser C3 if present, but in parallel It may be Assuming that the low temperature fluid FL flows in parallel through the respective absorbers A1, A2, A3 and / or the respective condensers C1, C2, C3, the respective absorbers A1, A2, A3 and / or the respective condensers C1, C2, C3 The flow resistance when flowing through is smaller than that when flowing in series, which is preferable when the pressure difference allowed when flowing the low temperature fluid FL is small.

  In the above description, the absorption type heat exchange system 1, 2, 3, 4, 5, 6, 7, 9, 10, the first evaporator E1 and the second evaporator E2 and the third evaporator E3 if present Although it has been described that it is full liquid type, it may be falling liquid 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, 8 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 system 1A, 8 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 type heat exchange system 1, 1A, 3, 5, 6, 9, the partial high temperature fluid FHs that has flowed out from the heat exchange unit 80 is the first regenerator G1, the second regenerator G2, the first It is decided to join the high temperature fluid FH which has flowed out of the evaporator E1 and the second evaporator E2, but the outflow from the first regenerator G1, the second regenerator G2, the first evaporator E1 and the second evaporator E2 Instead of joining the high temperature fluid FH, the high temperature fluid FH may flow into a system other than the one flowing out. Furthermore, although the partial high temperature fluid FHs flowing into the heat exchange unit 80 is branched from the high temperature fluid FH in the above description, it may be introduced from a system different from the high temperature fluid FH. In this way, a wide variety of heat can be used.

  In the above description, in the absorption heat exchange systems 1A and 8, 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 evaporation heat exchanger system 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 9 and 10, the low temperature fluid FL is made to flow in series in the order of the second condenser C2, the third condenser C3 and the first condenser C1. Conversely, the first condenser C1, the third condenser C3, and the second condenser C2 may be flowed in series in this order. In the absorption heat exchange system 9, the low temperature fluid FL is made to flow in series in the order of the first absorber A1, the third absorber A3 and the second absorber A2, but conversely, the second absorption The flow may be performed in series in the order of the vessel A2, the third absorber A3, and the first absorber A1. In the absorption type heat exchange system 10, the low temperature fluid FL is made to flow in series in the order of the second absorber A2, the third absorber A3 and the first absorber A1, but, conversely, the first absorption It is good also as flowing in series in order of vessel A1, 3rd absorber A3, and 2nd absorber A2.

1, 1A, 2, 3, 4, 5, 6, 7, 8, 9, 10 Absorbent heat exchange system 10 first absorption evaporator can barrel 14 first dilute solution outflow pipe 18 second dilute solution outflow pipe 20 second Absorbing evaporation can barrel 30 1st regeneration condensation can barrel 34 1st concentrated solution outflow pipe 38 2nd concentration solution outflow pipe 40 2nd regeneration condensation can barrel A1 1st absorber A2 2nd absorber A3 3rd absorber C1 1st 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 FH High temperature fluid FL Low temperature fluid Sa Concentration 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 evaporator refrigerant vapor Ve3 second 3Evaporator 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 (11)

A first absorption unit that raises the temperature of the 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 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 fluid to be heated by the heat of condensation released when the refrigerant vapor condenses to form a refrigerant liquid;
A second condensation unit that raises the temperature of the fluid to be heated by the heat of condensation released when the refrigerant vapor condenses to form 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;
The to-be-heated fluid before flowing out of the first condensation part and the second condensation part and flowing into the first absorption part and the second absorption part, the first evaporation part, the first evaporation part, Heat for causing heat exchange between the second evaporation part, the first regeneration part, and a part of the heating source fluid branched from the heating source fluid before being introduced into the second regeneration part With exchange unit;
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 flow path of the fluid to be heated is configured such that the fluid to be heated flowing out of the heat exchange portion flows into the first absorption portion and the second absorption portion;
Absorption heat exchange system. The heat source fluid that has flowed out of the heat exchange unit is joined to the heat source fluid that has flowed out of the first evaporation unit, the second evaporation unit, the first regeneration unit, and the second regeneration unit. And the flow path of the heat source fluid is configured;
The absorption heat exchange system according to claim 1. A first absorption unit that raises the temperature of the 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 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 fluid to be heated by the heat of condensation released when the refrigerant vapor condenses to form a refrigerant liquid;
A second condensation unit that raises the temperature of the fluid to be heated by the heat of condensation released when the refrigerant vapor condenses to form 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;
The to-be-heated fluid before flowing out of the first condensation part and the second condensation part and flowing into the first absorption part and the second absorption part, the first evaporation part, the first evaporation part, A heat exchange unit for exchanging heat between the evaporation unit 2 and the heat source fluid flowing out of the first regeneration unit and the second regeneration unit;
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 flow path of the fluid to be heated is configured such that the fluid to be heated flowing out of the heat exchange portion flows into the first absorption portion and the second absorption portion;
Absorption heat exchange system. 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-type heat exchange system according to any one of claims 1 to 3. 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-type heat exchange system according to any one of claims 1 to 3. 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-type heat exchange system according to any one of claims 1 to 3. The flow path of the fluid to be heated is configured such that the 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 6. 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
The to-be-heated fluid flows into the first absorption unit or the second absorption unit after flowing through the first condensation unit and the second condensation unit in series, and the heat source fluid is transferred to the first heat absorption fluid In the case of flowing through the second evaporating unit after having flowed through the evaporating unit of 1, the heat source fluid is allowed to flow through the first absorbing unit after flowing through the second absorbing unit, the second evaporating unit And the flow path of the fluid to be heated is configured to flow in the second absorbing portion after flowing in the first absorbing portion when flowing in the first evaporating portion after flowing
The absorption heat exchange system according to any one of claims 1 to 7. 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 is configured, the heated fluid is introduced in parallel to the first absorbing portion and the second absorbing portion, and the heated fluid is supplied to the first condensing portion and the first condensing portion. The flow path of the fluid to be heated is configured to be at least one of being introduced in parallel to the two condensers; and at least one of the flow paths is configured to be performed;
The absorption-type heat exchange system according to any one of claims 1 to 6. 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 9. A third absorbing unit that raises the temperature of the fluid to be heated by the absorption heat released when the absorbing liquid absorbs the vapor of the refrigerant;
A third condensing unit that raises the temperature of the fluid to be heated by the heat of condensation released when the refrigerant vapor condenses to form 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 heat exchange unit flows out of the first condensation unit, the second condensation unit, and the third condensation unit, and flows to the first absorption unit, the second absorption unit, and the third absorption unit. The heated fluid prior to flowing in is configured to flow in;
The flow path of the fluid to be heated is configured such that the fluid to be heated that has flowed out of the heat exchange portion flows into the first absorption portion, the second absorption portion, and the third absorption portion;
The absorption-type heat exchange system according to any one of claims 1 to 10.

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