JP6521793B2 - Absorption heat pump - Google Patents

Description

  BACKGROUND OF THE INVENTION Field of the Invention The present invention relates to an absorption heat pump, and more particularly to an absorption heat pump that performs heat exchange of internal fluid efficiently.

  There is an absorption heat pump as a heat source machine which takes out the medium to be heated having a temperature higher than the driving heat source temperature. The absorption heat pump mainly includes an evaporator for evaporating the refrigerant liquid, an absorber for absorbing the refrigerant vapor by the absorption liquid, a regenerator for separating the refrigerant from the absorption liquid, and a condenser for condensing the refrigerant vapor. In the absorption heat pump, one of the purposes is to improve the COP (coefficient of performance), by replenishing the medium to be heated which has flowed out of the system, and preheating the refrigerant liquid sent from the condenser to the evaporator. Is done. In order to preheat the replenishment fluid and the refrigerant liquid, there is one in which a heat exchanger is installed in each of the flow path of the replenishment fluid and the flow path of the refrigerant liquid (see, for example, Patent Document 1).

JP, 2006-162113, A (Drawing 5 grade etc.)

  However, the replenishment fluid and the refrigerant liquid often have a flow rate smaller than that of the heating side fluid, and it is difficult to achieve heat balance between the replenishment fluid or the refrigerant liquid and the heating side fluid, and the pressure loss of the heat exchanger is avoided. Therefore, the heat exchanger becomes large by selecting it according to the large flow rate. In addition, in the case of supplying the refrigerant liquid to a plurality of places as in the multistage temperature rising type, the number of heat exchangers is increased by increasing the number of refrigerant liquid flow paths.

  An object of the present invention is to provide an absorption heat pump which reduces the number of heat exchangers while maintaining heat balance between the replenishing fluid and the refrigerant liquid and the heating side fluid.

  In order to achieve the above object, an absorption heat pump according to a first aspect of the present invention has a heat transfer pipe 11 for flowing a medium to be heated W inside, as shown in FIG. 1, for example, The high temperature absorber 10 which heats the medium to be heated W with the absorption heat generated when absorbing the vapor Va into the absorbing solution Sa; and the regenerator heat source fluid pipe 71 for flowing the regenerator heat source fluid hg inside, high temperature In the absorber 10, the absorbent Sb which absorbed the refrigerant vapor Va is directly or indirectly introduced, and the introduced absorbent Sw is heated by the regenerator heat source fluid hg to generate the refrigerant vapor Vg from the absorbent Sw to be absorbed. A regenerator 70 for increasing the concentration of the liquid Sw; a condenser 80 for introducing the refrigerant vapor Vg generated in the regenerator 70; cooling and condensing the introduced refrigerant vapor Vg; and producing the refrigerant liquid Vf; Steaming the fluid he inside A low temperature evaporator 60 for introducing a refrigerant liquid Vf from the condenser 80 and heating the introduced refrigerant liquid Vf with the evaporator heat source fluid he to generate refrigerant vapor Vc; A resupply fluid supply unit 97 for supplying a resupply fluid Ws for resupplying the medium to be heated W introduced into the fluid; an absorbent Sw introduced into the regenerator 70; a regenerator heat source fluid hg introduced into the regenerator heat source fluid pipe 71 The regenerator heat source fluid hg flowing out from the regenerator heat source fluid pipe 71, the evaporator heat source fluid he introduced into the evaporator heat source fluid pipe 61, or the evaporator heat source fluid he flowing out from the evaporator heat source fluid pipe 61 A heating side flow passage 155 for flowing the heating side fluid Sw selected from the above, a replenishment fluid flow passage 195 for flowing the replenishment fluid Ws, and a refrigerant liquid passage 188 for flowing the refrigerant liquid Vf which has flowed out of the condenser 80, Heating side channel 155 Heat fluid Sw's to be, and a heat exchanger 100 to be transmitted to the refrigerant liquid Vf flowing up fluid Ws and the coolant flow path 188 through the supply fluid passage 195.

  With this configuration, heat exchange between the relatively small flow rate of the replenishment fluid and the refrigerant liquid is performed simultaneously with the relatively large flow rate of the heating side fluid, so that the heat balance between the replenishment fluid and the refrigerant liquid and the heating side fluid is facilitated. At the same time, the number of heat exchangers can be reduced because it is not necessary to separately provide heat exchangers for the replenishment fluid and heat exchangers for the refrigerant liquid.

  The absorption heat pump according to the second aspect of the present invention is, for example, as shown in FIG. 1, FIG. 3 (B) and FIG. 3 (C), the absorption heat pump according to the first aspect of the present invention Directly or indirectly before introducing into the regenerator 70 the absorbing liquid Sb which has the first refrigerant heating pipe 51 for flowing the refrigerant liquid Vf flowing out from the vessel 80 inside and which has absorbed the refrigerant vapor Va in the high temperature absorber 10 Inside the first refrigerant heating pipe 51 by absorption heat generated when the refrigerant vapor Vc generated by the low temperature evaporator 60 is introduced and the introduced refrigerant vapor Vc is absorbed by the absorbing liquid Sc. Heat exchangers 100B and 100C, the refrigerant liquid flow path is a low temperature refrigerant liquid flow path 186 for flowing the refrigerant liquid Vf introduced to the low temperature evaporator 60 and the heat exchangers 100B and 100C , Leading to the first refrigerant heating pipe 51 It is configured to include a medium temperature refrigerant liquid flow paths 183 and 184 to flow a refrigerant liquid Vf being.

  According to this structure, the refrigerant fluid flowing through the low temperature refrigerant fluid channel and the refrigerant fluid flowing through the medium temperature refrigerant fluid channel in addition to the replenishment fluid are subjected to heat exchange simultaneously with the heating side fluid. Heat balance with the heating side fluid can be more easily achieved.

  The absorption heat pump according to the third aspect of the present invention is, for example, as shown in FIG. 1 and FIG. 3C, in the absorption heat pump according to the second aspect of the present invention, the first refrigerant heating pipe 51 Medium-heated gas-liquid separator 41 for introducing the refrigerant heated at step S2 and separating the refrigerant vapor Vb from the introduced refrigerant; and the second refrigerant heating pipe 31 for flowing the refrigerant liquid Vf discharged from the condenser 80 inside; Before introducing the absorbing solution Sb which has absorbed the refrigerant vapor Va in the high temperature absorber 10 into the low temperature absorber 50 directly or indirectly, and introducing the refrigerant vapor Vb separated in the medium-temperature air-liquid separator 41 The medium temperature absorber 30 for heating the refrigerant liquid Vf flowing inside the second refrigerant heating pipe 31 by the absorption heat generated when the introduced refrigerant vapor Vb is absorbed by the absorbing liquid Sb; heat exchanger 100C The refrigerant liquid flow path is the second It is configured to include a high-temperature refrigerant liquid flow path 182 for flowing the high-temperature refrigerant liquid Vf to be introduced into the refrigerant heating pipe 31.

  According to this configuration, the refrigerant fluid flowing through the high temperature refrigerant liquid flow passage is heated in addition to the replenishment fluid, the refrigerant liquid flowing through the low temperature refrigerant liquid flow passage, and the refrigerant fluid flowing through the medium temperature refrigerant liquid flow passage. At the same time, the heat exchange is performed, which further facilitates the heat balance between the replenishing fluid and the refrigerant liquid and the heating side fluid.

  The absorption heat pump according to the fourth aspect of the present invention is, for example, as shown in FIG. 1, in the absorption heat pump 1 according to any one of the first to third aspects of the present invention. The heating side flow path 155 is an absorption liquid flow path in which the absorption liquid Sw introduced into the regenerator 70 flows.

  According to this structure, the temperature of the absorbing liquid flowing into the regenerator can be lowered, and the absorbing liquid flowing into the regenerator can be inhibited from self-evaporation, thereby suppressing a decrease in the amount of heat drawn from the outside. be able to. Further, by suppressing the self-evaporation of the absorbent flowing into the regenerator, it is possible to suppress the increase in volumetric flow rate and pressure loss accompanying the self-vaporization of the absorbent, and the desired flow rate of the absorbent can be obtained. It can be secured.

  According to the present invention, heat exchange between the relatively small flow rate of the replenishing fluid and the refrigerant liquid is simultaneously performed with the relatively large flow rate of the heating side fluid, so that the heat balance between the replenishing fluid and the refrigerant liquid and the heating side fluid is facilitated. At the same time, the number of heat exchangers can be reduced because it is not necessary to separately provide heat exchangers for the replenishment fluid and heat exchangers for the refrigerant liquid.

It is a typical systematic diagram of an absorption heat pump concerning an embodiment of the invention. It is sectional drawing which shows an example of a structure of the preheat heat exchanger of the absorption heat pump which concerns on embodiment of this invention. (A) is a schematic diagram around a preheating heat exchanger of an absorption heat pump according to an embodiment of the present invention, (B) is a three-stage temperature rising absorption heat pump according to a first modification of the embodiment of the present invention FIG. 7C is a schematic diagram of the periphery of the preheating heat exchanger of the three-stage temperature rising absorption heat pump according to a second modification of the embodiment of the present invention. (A) is a schematic system diagram around a preheating heat exchanger of a two-stage temperature rising absorption heat pump according to a third modification of the embodiment of the present invention, (B) is a fourth schematic view of the embodiment of the present invention It is a schematic diagram of a preheating heat exchanger circumference of a two-stage temperature rising absorption heat pump concerning a modification. It is a schematic diagram of a preheating heat exchanger circumference of a single stage temperature rising absorption heat pump concerning the 5th modification of an embodiment of the 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 pump 1 according to an embodiment of the present invention will be described with reference to FIG. FIG. 1 is a schematic diagram of the absorption heat pump 1. The absorption heat pump 1 is a three-stage temperature rising absorption heat pump. In the present embodiment, the absorption heat pump 1 introduces, as a heat source medium, low temperature (for example, about 80 ° C. to 90 ° C.) low temperature (eg, about 80 ° C. to 90 ° C.) drainage hot water he that has low utility value as a heat source medium. For example, it is a second-type absorption heat pump capable of taking out a pressure exceeding about 0.2 MPa (gauge pressure), desirably about 0.8 MPa (gauge pressure). The absorption heat pump 1 includes, as main components, a high temperature absorber 10, a high temperature evaporator 20, a medium temperature absorber 30, a medium temperature evaporator 40, a low temperature absorber 50, a low temperature evaporator 60, and a regenerator 70. , And a condenser 80. Moreover, the absorption heat pump 1 is provided with the gas-liquid separator 90 which takes out the to-be-heated-medium vapor | steam Wv, and the preheat heat exchanger 100. As shown in FIG.

In the following description, “high concentration solution Sa” according to the property and the position on the heat pump cycle, in order to facilitate the distinction on the heat pump cycle, regarding the absorbent (sometimes referred to as “solution”). It is called “medium concentration solution Sb”, “low concentration solution Sc”, “diluted solution Sw”, etc., but when the property etc. are unquestioned, it is collectively referred to as “absorption solution S”. Similarly, regarding the refrigerant, in order to facilitate distinction on the heat pump cycle, “high temperature refrigerant vapor Va”, “medium temperature refrigerant vapor Vb”, “low temperature refrigerant vapor Vc”, “high temperature refrigerant vapor Va” according to the property or the position on the heat pump cycle. It is called "regenerator refrigerant vapor Vg", "refrigerant liquid Vf", etc., but when the property etc. are unquestioned, it is collectively referred to as "refriger 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. Further, the medium to be heated W is a medium to be heated W, which is a medium to be heated of liquid W, a medium to be heated vapor Wv which is a medium to be heated of W, and a medium to be heated Wq mixed with a medium to be heated Wv. It is a generic term for mixed heated medium Wm and make-up water Ws. In the present embodiment, water (H ₂ O) is used as the medium to be heated W.

  The high temperature absorber 10 internally includes a heat transfer tube 11 constituting a flow path of the medium to be heated W and a high concentration solution dispersion nozzle 12 for dispersing the high concentration solution Sa. The high concentration solution dispersion nozzle 12 is disposed above the heat transfer tube 11 so that the dispersed high concentration solution Sa falls on the heat transfer tube 11. The high temperature absorber 10 disperses the high concentration solution Sa from the high concentration solution dispersion nozzle 12 and generates absorption heat when the high concentration solution Sa absorbs the high temperature refrigerant vapor Va. The absorbed heat is received by the medium to be heated W flowing through the heat transfer tube 11, and the medium to be heated W is heated. In the lower part of the high temperature absorber 10, a storage portion 13 in which the medium concentration solution Sb is stored is formed. The medium concentration solution Sb is an absorbing solution S in which the high concentration solution Sa dispersed from the high concentration solution dispersion nozzle 12 absorbs the high temperature refrigerant vapor Va and the concentration decreases from the high concentration solution Sa. The heat transfer tube 11 is disposed above the storage portion 13 so as not to be immersed in the medium concentration solution Sb. In this way, the generated absorption heat is rapidly transmitted to the medium to be heated W flowing in the heat transfer tube 11, and the recovery of the absorption capacity can be accelerated.

  The high temperature evaporator 20 is a component for supplying the high temperature refrigerant vapor Va to the high temperature absorber 10. The high temperature evaporator 20 has a refrigerant gas-liquid separation cylinder 21 accommodating the refrigerant liquid Vf and the high temperature refrigerant vapor Va, a high temperature refrigerant liquid supply pipe 22, and a high temperature refrigerant vapor reception pipe 24. The high temperature refrigerant liquid supply pipe 22 is a pipe which constitutes a flow path for leading the refrigerant liquid Vf to the heating pipe 31 of the medium temperature absorber 30. The high temperature refrigerant vapor receiving pipe 24 is a refrigerant gas-liquid phase of the high temperature refrigerant vapor Va or the high temperature refrigerant vapor Va and the refrigerant liquid Vf generated by heating the refrigerant liquid Vf in the heating pipe 31 of the medium temperature absorber 30 It is a pipe that constitutes a flow path for guiding to the separation cylinder 21. In the refrigerant gas-liquid separation cylinder 21, a baffle plate (not shown) for colliding and separating droplets of the refrigerant V contained in the high-temperature refrigerant vapor Va is provided. In the present embodiment, the inner surface of the heating tube 31 of the medium temperature absorber 30 is used as the heat transfer surface of the high temperature evaporator 20. Further, a refrigerant liquid pipe 82 for introducing the refrigerant liquid Vf is connected to the high temperature evaporator 20. A flow control valve 83 is disposed in the refrigerant liquid pipe 82 connected to the high temperature evaporator 20. One end of the high temperature refrigerant liquid supply pipe 22 is connected to the portion of the refrigerant gas-liquid separation cylinder 21 where the refrigerant liquid Vf is stored, and the other end is connected to one end of the heating pipe 31. One end of the high temperature refrigerant vapor receiving pipe 24 is connected to the refrigerant gas-liquid separation cylinder 21, and the other end is connected to the other end of the heating pipe 31. In the high-temperature evaporator 20, the refrigerant liquid Vf changes to steam inside the heating pipe 31, and the density is greatly reduced. Therefore, the refrigerant in the refrigerant gas-liquid separation cylinder 21 is operated as the heating pipe 31 functions as a bubble pump. The pump for sending the liquid Vf to the heating pipe 31 is omitted. A pump (not shown) for sending the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 21 to the heating pipe 31 may be disposed in the high temperature refrigerant liquid supply pipe 22.

  The high temperature evaporator 20 and the high temperature absorber 10 are connected by a high temperature refrigerant vapor pipe 29 as a high temperature refrigerant vapor flow path. One end of the high temperature refrigerant vapor pipe 29 is connected to the upper portion (typically the top) of the refrigerant gas-liquid separation cylinder 21, and the other end is high temperature absorption above the high concentration solution dispersion nozzle 12 Connected to the vessel 10. With such a configuration, the high temperature refrigerant vapor Va generated by the high temperature evaporator 20 can be supplied to the high temperature absorber 10 through the high temperature refrigerant vapor pipe 29.

  The medium temperature absorber 30 internally includes a heating pipe 31 as a second refrigerant heating pipe that constitutes a flow path of the refrigerant liquid Vf and the high-temperature refrigerant vapor Va, and a medium concentration solution dispersion nozzle 32. As described above, the heating pipe 31 is connected at one end to the high temperature refrigerant liquid supply pipe 22 and at the other end to the high temperature refrigerant vapor receiving pipe 24. The medium concentration solution dispersion nozzle 32 disperses the medium concentration solution Sb in the present embodiment. The medium concentration solution dispersion nozzle 32 is disposed above the heating tube 31 so that the dispersed medium concentration solution Sb falls on the heating tube 31. One end of a medium concentration solution pipe 15 through which the medium concentration solution Sb flows is connected to the medium concentration solution dispersion nozzle 32. The medium temperature absorber 30 heats the refrigerant liquid Vf flowing through the heating pipe 31 by the absorption heat generated when the medium concentration solution Sb is dispersed from the medium concentration solution dispersion nozzle 32 and the medium concentration solution Sb absorbs the medium temperature refrigerant vapor Vb. Thus, the high temperature refrigerant vapor Va can be generated. The medium temperature absorber 30 is configured to operate at a lower pressure (dew point temperature) than the high temperature absorber 10, and has a lower operating temperature than the high temperature absorber 10. In the lower part of the medium-temperature absorber 30, a storage portion 33 in which the low concentration solution Sc is stored is formed. The low concentration solution Sc is an absorbing solution S in which the medium concentration solution Sb dispersed from the medium concentration solution dispersion nozzle 32 absorbs the medium temperature refrigerant vapor Vb to reduce the concentration. The heating pipe 31 is disposed above the storage section 33.

  The medium temperature evaporator 40 is a component that supplies the medium temperature refrigerant vapor Vb to the medium temperature absorber 30. The medium-temperature evaporator 40 has a refrigerant gas-liquid separation cylinder 41 as a medium-temperature gas-liquid separator containing the refrigerant liquid Vf and the medium-temperature refrigerant vapor Vb, an medium-temperature refrigerant liquid supply pipe 42, and an medium-temperature refrigerant vapor reception pipe 44. ing. The medium temperature refrigerant liquid supply pipe 42 is a pipe that constitutes a flow path for leading the refrigerant liquid Vf to the heating pipe 51 of the low temperature absorber 50. The medium temperature refrigerant vapor receiving pipe 44 is a refrigerant gas / liquid phase of the medium temperature refrigerant vapor Vb generated by heating the refrigerant liquid Vf in the heating pipe 51 of the low temperature absorber 50 or the medium temperature refrigerant vapor Vb and the refrigerant liquid Vf. It is a pipe that constitutes a flow path for guiding to the separation cylinder 41. The refrigerant gas-liquid separation cylinder 41 is configured in the same manner as the refrigerant gas-liquid separation cylinder 21 of the high temperature evaporator 20. In the present embodiment, the inner surface of the heating tube 51 of the low temperature absorber 50 is used as the heat transfer surface of the medium temperature evaporator 40. Further, a refrigerant liquid pipe 84 for introducing the refrigerant liquid Vf is connected to the medium temperature evaporator 40. The refrigerant liquid pipe 84 is branched from the refrigerant liquid pipe 82. A flow control valve 85 is disposed in the refrigerant liquid pipe 84 connected to the medium temperature evaporator 40. The medium temperature refrigerant liquid supply pipe 42 has one end connected to the portion of the refrigerant gas-liquid separation cylinder 41 where the refrigerant liquid Vf is stored, and the other end connected to one end of the heating pipe 51. The medium temperature refrigerant vapor receiving pipe 44 has one end connected to the refrigerant gas-liquid separation cylinder 41 and the other end connected to the other end of the heating pipe 51. Since the medium temperature evaporator 40 changes the refrigerant liquid Vf to steam inside the heating pipe 51 and the density is greatly reduced, the refrigerant in the refrigerant gas-liquid separation cylinder 41 is made to function as the heating pipe 51 as a bubble pump. The pump for sending the liquid Vf to the heating pipe 51 is omitted. A pump (not shown) for feeding the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 41 to the heating pipe 51 may be disposed in the medium temperature refrigerant liquid supply pipe 42.

  The medium temperature evaporator 40 and the medium temperature absorber 30 are connected by a medium temperature refrigerant vapor pipe 49 as an medium temperature refrigerant vapor flow path. One end of the medium temperature refrigerant vapor pipe 49 is connected to the upper portion (typically the top) of the refrigerant gas-liquid separation cylinder 41, and the other end is medium temperature absorption above the medium concentration solution dispersion nozzle 32. It is connected to the vessel 30. With such a configuration, the medium temperature refrigerant vapor Vb generated by the medium temperature evaporator 40 can be supplied to the medium temperature absorber 30 through the medium temperature refrigerant vapor pipe 49.

  The low temperature absorber 50 internally includes a heating pipe 51 as a first refrigerant heating pipe that constitutes a flow path of the refrigerant liquid Vf and the medium temperature refrigerant vapor Vb, and a low concentration solution dispersion nozzle 52. As described above, the heating pipe 51 is connected at one end to the medium temperature refrigerant liquid supply pipe 42 and at the other end to the medium temperature refrigerant vapor receiving pipe 44. The low concentration solution distribution nozzle 52 distributes the low concentration solution Sc in the present embodiment. The low concentration solution dispersion nozzle 52 is disposed above the heating tube 51 so that the dispersed low concentration solution Sc falls on the heating tube 51. One end of a low concentration solution pipe 35 through which the low concentration solution Sc flows is connected to the low concentration solution dispersion nozzle 52. In the low temperature absorber 50, the low concentration solution Sc is dispersed from the low concentration solution dispersion nozzle 52, and the refrigerant heat flowing through the heating pipe 51 is heated by the absorption heat generated when the low concentration solution Sc absorbs the low temperature refrigerant vapor Vc. The intermediate temperature refrigerant vapor Vb can be generated. The low temperature absorber 50 is configured to operate at a pressure (dew point temperature) lower than that of the medium temperature absorber 30, and the operating temperature is lower than that of the medium temperature absorber 30. In the lower part of the low temperature absorber 50, a storage part 53 in which the dilute solution Sw is stored is formed. The dilute solution Sw is an absorbing solution S in which the absorbing solution S (in the present embodiment, the low concentration solution Sc) dispersed from the low concentration solution dispersion nozzle 52 absorbs the low temperature refrigerant vapor Vc to reduce the concentration. The dilute solution Sw contains a large amount of the refrigerant V as compared with the high concentration solution Sa and the medium concentration solution Sb. The heating pipe 51 is disposed above the storage section 53.

  The low temperature evaporator 60 includes a heat source pipe 61 as an evaporator heat source fluid pipe that constitutes a flow path of the evaporator heat source hot water as an evaporator heat source fluid, and a refrigerant liquid dispersion nozzle 62 for dispersing the refrigerant liquid Vf. Have. The refrigerant liquid dispersion nozzle 62 is disposed above the heat source pipe 61 so that the dispersed refrigerant liquid Vf falls on the heat source pipe 61. The low temperature evaporator 60 is connected to one end of a refrigerant liquid pipe 86 through which the refrigerant liquid Vf flows. The refrigerant liquid pipe 86 is provided with a flow control valve 87 for adjusting the flow of the refrigerant liquid Vf introduced into the low temperature evaporator 60. One end of a low temperature refrigerant liquid pipe 65 for leading the refrigerant liquid Vf stored in the lower part of the low temperature evaporator 60 to the refrigerant liquid distribution nozzle 62 is connected to the lower portion (typically the bottom) of the low temperature evaporator 60. The other end of the low temperature refrigerant liquid pipe 65 is connected to the refrigerant liquid dispersion nozzle 62. The low temperature refrigerant liquid pipe 65 is provided with a low temperature refrigerant liquid pump 66 for pressure-feeding the refrigerant liquid Vf flowing therein. In the low temperature evaporator 60, the refrigerant liquid Vf is dispersed from the refrigerant liquid distribution nozzle 62, and the dispersed refrigerant liquid Vf is evaporated by the heat of the evaporator heat source warm water he flowing in the heat source pipe 61 to generate the low temperature refrigerant vapor Vc. Is configured as. The low temperature evaporator 60 is configured to operate at a pressure (dew point temperature) lower than that of the medium temperature evaporator 40, and the operating temperature is lower than that of the medium temperature evaporator 40.

  The low temperature absorber 50 and the low temperature evaporator 60 are in communication with each other. The low temperature absorber 50 and the low temperature evaporator 60 communicate with each other so that the low temperature refrigerant vapor Vc generated in the low temperature evaporator 60 can be supplied to the low temperature absorber 50. The low temperature absorber 50 and the low temperature evaporator 60 are typically communicated with each other above the low concentration solution distribution nozzle 52 and above the refrigerant liquid distribution nozzle 62.

  The regenerator 70 has a heat source pipe 71 as a regenerator heat source fluid pipe that constitutes a flow path of the regenerator heat source warm water hg as a regenerator heat source fluid, and a dilute solution dispersion nozzle 72 that disperses the dilute solution Sw. There is. The regenerator heat source warm water hg flowing through the heat source pipe 71 of the regenerator 70 may be the same hot water as the evaporator heat source warm water he flowing through the heat source pipe 61 of the low temperature evaporator 60. It is good to be connected by piping (not shown) so that it may flow through heat source pipe 71 later. Different heat source media may flow in the heat source tubes 61 and 71, respectively. The dilute solution spray nozzle 72 is disposed above the heat source pipe 71 so that the sprayed dilute solution Sw falls on the heat source pipe 71. In the regenerator 70, the dispersed dilute solution Sw is heated by the regenerator heat source warm water hg, whereby the refrigerant V evaporates from the dilute solution Sw to generate a high concentration solution Sa having an increased concentration. The regenerator 70 is configured such that the generated high concentration solution Sa is stored at the bottom.

  The condenser 80 has a cooling water pipe 81 which forms a cooling medium channel. Cooling water c as a cooling medium flows through the cooling water pipe 81. The condenser 80 is configured to introduce a regenerator refrigerant vapor Vg, which is the vapor of the refrigerant V generated by the regenerator 70, and cool and condense it with the cooling water c. The cooling water pipe 81 is disposed so as not to be immersed in the refrigerant liquid Vf in which the regenerator refrigerant vapor Vg is condensed so that the regenerator refrigerant vapor Vg can be directly cooled. Connected to the condenser 80 is one end of a refrigerant liquid pipe 88 that sends the condensed refrigerant liquid Vf toward the high temperature evaporator 20, the medium temperature evaporator 40, and the low temperature evaporator 60. The other end of the refrigerant liquid pipe 88 is connected to the refrigerant liquid pipe 82 connected to the high temperature evaporator 20 and the refrigerant liquid pipe 86 connected to the low temperature evaporator 60, and the refrigerant liquid Vf in the condenser 80 is heated to a high temperature It is configured to be able to be distributed to the evaporator 20, the medium temperature evaporator 40 and the low temperature evaporator 60. The refrigerant liquid pipe 88 is provided with a condensing refrigerant pump 89 for pressure-feeding the refrigerant liquid Vf.

  The regenerator 70 and the condenser 80 are in communication with each other. The regenerator 70 and the condenser 80 communicate with each other, so that the regenerator refrigerant vapor Vg generated in the regenerator 70 can be supplied to the condenser 80. The regenerator 70 and the condenser 80 communicate with each other in the upper gas phase portion. In the present embodiment, the regenerator 70 and the condenser 80 are provided below the high temperature absorber 10, the high temperature evaporator 20, the medium temperature absorber 30, the medium temperature evaporator 40, the low temperature absorber 50, and the low temperature evaporator 60. It is done.

  A portion of the regenerator 70 where the high concentration solution Sa is stored, and the high concentration solution dispersion nozzle 12 of the high temperature absorber 10 are connected by a high concentration solution pipe 75. In the high concentration solution pipe 75, a high concentration solution pump 76 that pumps the high concentration solution Sa in the regenerator 70 to the high concentration solution dispersion nozzle 12 is disposed. The storage portion 13 of the high temperature absorber 10 and the medium concentration solution dispersion nozzle 32 of the medium temperature absorber 30 are connected by a medium concentration solution pipe 15. A medium concentration solution pump 16 for pressure-feeding the medium concentration solution Sb in the high temperature absorber 10 to the medium temperature absorber 30 is disposed in the medium concentration solution pipe 15. The storage portion 33 of the medium temperature absorber 30 and the low concentration solution dispersion nozzle 52 of the low temperature absorber 50 are connected by a low concentration solution pipe 35. In the low concentration solution pipe 35, a low concentration solution pump 36 for pumping the low concentration solution Sc in the medium temperature absorber 30 to the low temperature absorber 50 is disposed. The reservoir 53 of the low temperature absorber 50 and the dilute solution dispersion nozzle 72 of the regenerator 70 are connected by a dilute solution pipe 55.

  A high temperature heat exchanger 18 is disposed in the medium concentration solution pipe 15 and the high concentration solution pipe 75. The high temperature heat exchanger 18 is a device for performing heat exchange between the medium concentration solution Sb flowing through the medium concentration solution pipe 15 and the high concentration solution Sa flowing through the high concentration solution pipe 75. A medium temperature heat exchanger 38 is disposed in the low concentration solution pipe 35 and the high concentration solution pipe 75. The medium-temperature heat exchanger 38 is a device that performs heat exchange between the low concentration solution Sc flowing through the low concentration solution pipe 35 and the high concentration solution Sa flowing through the high concentration solution pipe 75. A low temperature heat exchanger 58 is disposed in the dilute solution pipe 55 and the high concentration solution pipe 75. The low temperature heat exchanger 58 is a device for performing heat exchange between the dilute solution Sw flowing in the dilute solution pipe 55 and the high concentration solution Sa flowing in the high concentration solution pipe 75.

  The gas-liquid separator 90 is a device that flows through the heat transfer tube 11 of the high-temperature absorber 10 to introduce the heated heating medium W and separates the heating medium vapor Wv and the heating medium liquid Wq. The lower portion of the gas-liquid separator 90 and one end of the heat transfer pipe 11 of the high temperature absorber 10 are connected by a heated medium liquid pipe 92 which guides the heated medium liquid Wq to the heat transfer pipe 11. The side surface of the gas-liquid separator 90 whose inside is a gas phase portion and the other end of the heat transfer tube 11 are connected by a heated heated medium pipe 94 for guiding the heated heated medium W to the gas-liquid separator 90 There is. Connected to the heated medium liquid pipe 92 is a replenishing water pipe 95 for introducing replenishing water Ws from the outside of the system as a replenishing fluid for replenishing the heated medium W supplied to the outside of the system as steam. A makeup water pump 96 for pumping the makeup water Ws toward the gas-liquid separator 90 is disposed in the makeup water pipe 95. In the present embodiment, the makeup water supply unit 97 is configured by the makeup water pipe 95 and the makeup water pump 96. Further, in the gas-liquid separator 90, a heated medium vapor supply pipe 99 for supplying the heated medium vapor Wv out of the system is connected to the top (typically at the top). The gas-liquid separator 90 may introduce a mixed heated medium Wm in which the heated medium liquid Wq and the heated medium vapor Wv are mixed by evaporating a part of the heated medium liquid Wq in the heat transfer pipe 11 The liquid to be heated Wq may be introduced into the gas-liquid separator 90 as it is, decompressed, and partially vaporized to make the mixed medium to be heated Wm gas-liquid separated.

  In the present embodiment, the preheating heat exchanger 100 supplies the dilute solution Sw flowing through the dilute solution pipe 55 downstream of the low temperature heat exchanger 58, the refrigerant liquid Vf flowing through the refrigerant liquid pipe 88, and the replenishment flowing through the makeup water pipe 95. It is a heat exchanger which performs heat exchange with water Ws. In the present embodiment, a shell and tube type heat exchanger (multi-tubular type heat exchanger) is used as the preheating heat exchanger 100. During operation of the absorption heat pump 1, for example, the refrigerant liquid Vf of approximately 5 to 10 liters per minute is supplied to each of the high temperature evaporator 20, the medium temperature evaporator 40, and the low temperature evaporator 60. Therefore, the refrigerant liquid Vf flows about 15 to 30 liters per minute through the refrigerant liquid pipe 88. In addition, makeup water Ws of approximately 5 to 10 liters per minute flows through the makeup water pipe 95. On the other hand, the dilute solution Sw flowing through the dilute solution pipe 55 is about 100 to 150 liters per minute.

  An example of a structure of the preheat heat exchanger 100 is shown in FIG. In the present embodiment, in the preheating heat exchanger 100, the dilute solution Sw flows on the shell side, and the refrigerant liquid Vf and the makeup water Ws flow in the tube. In the preheating heat exchanger 100, a refrigerant liquid tube 188 as a refrigerant liquid flow path for flowing the refrigerant liquid Vf and a replenishment water tube 195 as a replenishment fluid flow path for flowing the replenishment water Ws are provided inside the shell 101. There is. The inside of the shell 101 outside the refrigerant liquid tube 188 and the makeup water tube 195 is a dilute solution flow path 155 through which the dilute solution Sw flows. The dilute solution flow channel 155 corresponds to an absorption liquid flow channel, and the absorption liquid flow channel is a form of the heating side flow channel. Inside the shell 101, a plate 102 for meandering the dilute solution Sw in the dilute solution flow path 155 is provided in order to increase the contact area between the dilute solution Sw and the refrigerant liquid tube 188 and the makeup water tube 195. ing. The refrigerant liquid tube 188 is connected to the refrigerant liquid pipe 88. The makeup water tube 195 is connected to the makeup water pipe 95. The dilute solution flow channel 155 is connected to the dilute solution pipe 55.

  Continuing to refer to FIG. 1, the operation of the absorption heat pump 1 will be described. First, the refrigerant side cycle will be described. In the condenser 80, the regenerator refrigerant vapor Vg generated in the regenerator 70 is received, and the regenerator refrigerant vapor Vg is cooled and condensed by the cooling water c flowing through the cooling water pipe 81 to be the refrigerant liquid Vf. The condensed refrigerant liquid Vf is pressure-fed by the condensing refrigerant pump 89 toward the high temperature evaporator 20, the medium temperature evaporator 40, and the low temperature evaporator 60. The refrigerant liquid Vf pressure-fed by the condensing refrigerant pump 89 flows through the refrigerant liquid pipe 88, and the temperature thereof is increased by the preheating heat exchanger 100 in the middle, and then is divided into the refrigerant liquid pipe 82 and the refrigerant liquid pipe 86. The refrigerant liquid Vf is preheated by the preheating heat exchanger 100, whereby the start-up of the absorption heat pump 1 is quickened, and the operation can be stabilized early. A part of the refrigerant liquid Vf flowing through the refrigerant liquid pipe 82 flows into the refrigerant liquid pipe 84 along the way, and the remainder flows through the refrigerant liquid pipe 82 and is introduced into the high temperature refrigerant liquid supply pipe 22. The refrigerant liquid Vf flowing through the refrigerant liquid pipe 84 is introduced into the medium temperature refrigerant liquid supply pipe 42. The refrigerant liquid Vf flowing through the refrigerant liquid pipe 86 is introduced into the low temperature evaporator 60.

  The refrigerant liquid Vf introduced into the low temperature evaporator 60 is pressure-fed to the refrigerant liquid distribution nozzle 62 by the low temperature refrigerant liquid pump 66 and dispersed from the refrigerant liquid distribution nozzle 62 toward the heat source pipe 61. The refrigerant liquid Vf distributed from the refrigerant liquid distribution nozzle 62 is heated by the evaporator heat source warm water he flowing in the heat source pipe 61 and evaporated to become the low temperature refrigerant vapor Vc. The low temperature refrigerant vapor Vc generated in the low temperature evaporator 60 moves to the low temperature absorber 50 in communication with the low temperature evaporator 60. On the other hand, the refrigerant liquid Vf introduced into the medium temperature refrigerant liquid supply pipe 42 flows into the heating pipe 51 of the low temperature absorber 50 by the action of the bubble pump. The refrigerant liquid Vf having flowed into the heating pipe 51 is heated in the low temperature absorber 50 by the absorption heat generated when the low temperature refrigerant vapor Vc moved from the low temperature evaporator 60 is absorbed by the low concentration solution Sc, It evaporates by this and becomes medium temperature refrigerant vapor Vb. The medium temperature refrigerant vapor Vb generated in the heating pipe 51 flows through the medium temperature refrigerant vapor receiving pipe 44 and reaches the refrigerant gas-liquid separation cylinder 41. The medium temperature refrigerant vapor Vb that has flowed into the refrigerant gas-liquid separation cylinder 41 moves to the medium temperature absorber 30 communicating with the medium temperature evaporator 40 via the medium temperature refrigerant vapor pipe 49. Further, the refrigerant liquid Vf introduced into the high temperature refrigerant liquid supply pipe 22 flows into the heating pipe 31 of the medium temperature absorber 30 by the action of the bubble pump. The refrigerant liquid Vf flowing into the heating pipe 31 is heated by the absorption heat generated when the medium temperature refrigerant vapor Vb transferred from the medium temperature evaporator 40 is absorbed by the medium concentration solution Sb in the medium temperature absorber 30, and this heating is performed It evaporates by this and becomes high temperature refrigerant vapor Va. The high temperature refrigerant vapor Va generated in the heating pipe 31 flows through the high temperature refrigerant vapor receiving pipe 24 and reaches the refrigerant gas-liquid separation cylinder 21. The high temperature refrigerant vapor Va flowing into the refrigerant gas-liquid separation cylinder 21 moves to the high temperature absorber 10 in communication with the high temperature evaporator 20 through the high temperature refrigerant vapor pipe 29.

  Next, the cycle on the absorbent side of the absorption heat pump 1 will be described. In the high temperature absorber 10, the high concentration solution Sa is dispersed from the high concentration solution dispersion nozzle 12, and the dispersed high concentration solution Sa absorbs the high temperature refrigerant vapor Va transferred from the high temperature evaporator 20. The high concentration solution Sa that has absorbed the high temperature refrigerant vapor Va is reduced in concentration to become a medium concentration solution Sb. In the high temperature absorber 10, absorption heat is generated when the high concentration solution Sa absorbs the high temperature refrigerant vapor Va. The absorbed heat causes the heated medium liquid Wq flowing through the heat transfer tube 11 to be heated. Here, the operation around the gas-liquid separator 90 for taking out the heating medium vapor Wv will be described.

  The makeup water Ws is introduced into the gas-liquid separator 90 from outside the system via the makeup water pipe 95. The makeup water Ws is pressure-fed through the makeup water pipe 95 by the makeup water pump 96 and is introduced into the heated medium liquid pipe 92 after the temperature thereof is increased by the preheating heat exchanger 100 in the middle. By making the makeup water Ws preheated by the preheating heat exchanger 100, the COP of the absorption heat pump 1 becomes high, and the flow rate of the heating medium vapor Wv to be generated can be increased. The make-up water Ws introduced into the medium fluid pipe 92 to be heated merges with the medium fluid Wq to be heated which has flowed from the lower part of the gas-liquid separator 90 as the medium fluid Wq to be heated. Flows into the heat transfer tube 11 of the vessel 10. The to-be-heated medium liquid Wq which has flowed into the heat transfer tube 11 is heated by the above-mentioned absorption heat in the high temperature absorber 10. The liquid-to-be-heated liquid Wq heated by the heat transfer tube 11 is separated as a mixed liquid-to-be-heated medium Wm in which a part is evaporated to become the liquid-to-be-heated medium vapor Wv After heating to the vessel 90, it flows through the heated medium tube 94. When the heated medium liquid Wq whose temperature has risen flows through the heated medium pipe 94 after heating, the heated medium liquid Wq is decompressed when introduced into the gas-liquid separator 90, and a part of it is evaporated to be heated. It is introduced into the gas-liquid separator 90 as the mixed heated medium Wm that has become the heating medium vapor Wv. The mixed heated medium Wm introduced into the gas-liquid separator 90 separates the heated medium liquid Wq and the heated medium vapor Wv. The separated medium fluid Wq to be heated is stored in the lower part of the gas-liquid separator 90 and is again sent to the heat transfer tube 11 of the high temperature absorber 10. On the other hand, the separated heated medium vapor Wv flows out to the heated medium vapor supply pipe 99 and is supplied to the steam utilization site. In the present embodiment, the heating medium vapor Wv of about 0.8 MPa (gauge pressure) is supplied.

  It returns to description of the cycle by the side of absorption liquid of absorption heat pump 1 again. The high concentration solution Sa that has absorbed the high temperature refrigerant vapor Va by the high temperature absorber 10 is reduced in concentration to become a medium concentration solution Sb, and is stored in the storage section 13. The medium concentration solution Sb in the reservoir 13 flows through the medium concentration solution pipe 15 toward the medium temperature absorber 30 by the operation of the medium concentration solution pump 16 and exchanges heat with the high concentration solution Sa in the high temperature heat exchanger 18 Reaches a medium concentration solution spray nozzle 32. As described above, in the present embodiment, the absorbent S in the high temperature absorber 10 is directly introduced into the medium temperature absorber 30 (without passing through another absorber). The internal pressure of the high temperature absorber 10 becomes higher than the internal pressure of the medium temperature absorber 30, and even if the medium concentration solution pump 16 is not operating, the medium concentration solution in the high temperature absorber 10 is determined If Sb can be delivered to the medium temperature absorber 30, the medium concentration solution pump 16 may be stopped.

  In the medium temperature absorber 30, the medium concentration solution Sb is dispersed from the medium concentration solution dispersion nozzle 32, and the dispersed medium concentration solution Sb absorbs the medium temperature refrigerant vapor Vb transferred from the medium temperature evaporator 40. The medium concentration solution Sb having absorbed the medium temperature refrigerant vapor Vb is reduced in concentration to be a low concentration solution Sc, and is stored in the storage section 33. In the medium temperature absorber 30, absorption heat is generated when the medium concentration solution Sb absorbs the medium temperature refrigerant vapor Vb. As described above, the refrigerant liquid Vf flowing through the heating pipe 31 is heated by the absorbed heat. The low concentration solution Sc in the reservoir 33 flows through the low concentration solution pipe 35 toward the low temperature absorber 50 by the operation of the low concentration solution pump 36 and exchanges heat with the high concentration solution Sa in the medium temperature heat exchanger 38 Reaches a low concentration solution spray nozzle 52. As described above, in the present embodiment, the absorbent S in the high temperature absorber 10 is indirectly introduced to the low temperature absorber 50 via the medium temperature absorber 30. The internal pressure of the medium temperature absorber 30 becomes higher than the internal pressure of the low temperature absorber 50, and even if the low concentration solution pump 36 is not operating, the low concentration solution Sc in the intermediate temperature absorber 30 is determined The low concentration solution pump 36 may be stopped if it can be transported to the low temperature absorber 50.

  In the low temperature absorber 50, the low concentration solution Sc flowing into the low concentration solution dispersion nozzle 52 is dispersed toward the heating pipe 51. The sprayed low concentration solution Sc absorbs the low temperature refrigerant vapor Vc transferred from the low temperature evaporator 60. The low concentration solution Sc that has absorbed the low temperature refrigerant vapor Vc has a reduced concentration and becomes a dilute solution Sw. In the low temperature absorber 50, absorption heat is generated when the low concentration solution Sc absorbs the low temperature refrigerant vapor Vc. As described above, the refrigerant liquid Vf flowing through the heating pipe 51 is heated by the absorbed heat, and the medium temperature refrigerant vapor Vb is generated. The dilute solution Sw in the low temperature absorber 50 flows in the dilute solution pipe 55 toward the regenerator 70 by gravity. At this time, the dilute solution Sw exchanges heat with the high concentration solution Sa in the low temperature heat exchanger 58 to lower the temperature, and further exchanges heat with the refrigerant liquid Vf and the makeup water Ws in the preheating heat exchanger 100 to reduce the temperature After that, it is introduced into the regenerator 70. As described above, in the present embodiment, the absorbent S in the high temperature absorber 10 is indirectly introduced into the regenerator 70 via the medium temperature absorber 30 and the low temperature absorber 50.

  In the preheating heat exchanger 100, the refrigerant liquid Vf and the makeup water Ws having relatively small flow rates are simultaneously subjected to heat exchange simultaneously with respect to the dilute solution Sw having a relatively large flow rate. Therefore, the dilute solution Sw, the refrigerant liquid Vf, and the replenishment are supplied. Easy to balance heat with water Ws. Further, in the preheating heat exchanger 100, by lowering the temperature of the dilute solution Sw before flowing into the regenerator 70, it is possible to suppress the self-evaporation of the diluted solution Sw flowing into the regenerator 70. At 70, the heat of the regenerator heat source warm water hg can be used more and it becomes particularly useful when the regenerator heat source warm water hg is waste water. In addition, if the dilute solution Sw is self-evaporated inside and outside the dilute solution pipe 55, volumetric flow rate may increase, pressure loss may increase, and the flow rate of the dilute solution Sw may run short. By reducing the temperature of the dilute solution Sw at this time, it is possible to suppress the self evaporation of the dilute solution Sw inside and outside the dilute solution tube 55, and it is possible to secure the desired flow rate of the dilute solution Sw.

  The dilute solution Sw sent to the regenerator 70 is sprayed from a dilute solution spray nozzle 72. The dilute solution Sw sprayed from the dilute solution spray nozzle 72 is heated by the regenerator heat source warm water hg (about 80 ° C. in this embodiment) flowing through the heat source pipe 71, and the refrigerant in the sprayed dilute solution Sw evaporates As a result, the high concentration solution Sa is stored in the lower part of the regenerator 70. On the other hand, the refrigerant V evaporated from the dilute solution Sw moves to the condenser 80 as a regenerator refrigerant vapor Vg. The high concentration solution Sa stored in the lower part of the regenerator 70 is pumped by the high concentration solution pump 76 to the high concentration solution dispersion nozzle 12 of the high temperature absorber 10 through the high concentration solution pipe 75. The high concentration solution Sa flowing through the high concentration solution pipe 75 exchanges heat with the dilute solution Sw in the low temperature heat exchanger 58 and rises in temperature, and exchanges heat with the low concentration solution Sc in the medium temperature heat exchanger 38 to further increase the temperature The temperature rises and then exchanges heat with the medium concentration solution Sb in the high temperature heat exchanger 18 to further increase the temperature, and then flows into the high temperature absorber 10 and is dispersed from the high concentration solution dispersion nozzle 12. The same cycle is repeated thereafter.

  As described above, in the preheating heat exchanger 100, the absorption heat pump 1 according to the present embodiment uses the refrigerant liquid Vf and the makeup water Ws, which have a relatively small flow rate, with respect to the dilute solution Sw, which has a relatively large flow rate. Since heat exchange is performed simultaneously and collectively, it is easy to maintain heat balance between the dilute solution Sw and the refrigerant liquid Vf and the makeup water Ws. Further, in the preheating heat exchanger 100, by lowering the temperature of the dilute solution Sw before flowing into the regenerator 70, it becomes possible to use more heat of the regenerator heat source hot water hg, and the desired dilute solution The flow rate of Sw can be secured.

  In the above description, although the absorption heat pump 1 is a three-stage temperature rising type, it may be a two-stage temperature rising type or a single-stage temperature rising type. In the case of the two-stage heating type, the configuration around the medium-temperature absorber 30 and the middle-temperature evaporator 40 is omitted from the configuration of the three-stage heating absorption heat pump 1, and the high-temperature refrigerant liquid supply pipe 22 and the high temperature of the high-temperature evaporator 20 are omitted. The refrigerant vapor receiving pipe 24 is connected to the heating pipe 51 of the low temperature absorber 50, and the medium concentration solution pipe 15 is connected to the low concentration solution dispersion nozzle 52 so that the medium concentration solution Sb in the high temperature absorber 10 is directly To the low temperature absorber 50). In the case of the single-stage heating type, the high-temperature evaporator 20 and the low-temperature absorber 50 are further omitted from the configuration of the above-described two-stage heating type absorption heat pump, and the low-temperature refrigerant vapor Vc generated in the low-temperature evaporator 60 absorbs high temperatures The medium concentration solution tube 15 is connected to the dilute solution dispersion nozzle 72 in the regenerator 70 to directly introduce the medium concentration solution Sb in the high temperature absorber 10 (other absorbers are It may be configured to be introduced into the regenerator 70). Further, in each of the three-stage heating type, the two-stage heating type, and the single-stage heating type absorption heat pump, the configuration around the preheating heat exchanger can be variously modified, and is exemplified below.

  FIG. 3A is a schematic system diagram around the preheating heat exchanger 100 of the absorption heat pump 1 described above. As described above, the preheating heat exchanger 100 has the dilute solution flow path 155 as the heating side flow path, the replenishment water tube 195 as the replenishment fluid flow path, and the refrigerant liquid tube 188 as the refrigerant liquid flow path. doing. In the following description of the modified examples, differences in configuration from the periphery of the preheating heat exchanger 100 according to the present embodiment will be mainly described. FIG. 3B is a schematic system diagram around a preheating heat exchanger 100B of a three-stage temperature rising absorption heat pump according to a first modified example of the embodiment of the present invention. The preheating heat exchanger 100B includes a low temperature refrigerant liquid tube 186 as a low temperature refrigerant liquid flow passage for flowing the refrigerant liquid Vf introduced into the low temperature evaporator 60, and a medium high temperature refrigerant liquid tube 183. It is. The medium-high temperature refrigerant liquid tube 183 flows the refrigerant liquid Vf introduced into the inside of the heating tube 51 of the low temperature absorber 50 via the medium temperature evaporator 40 and the inside of the heating tube 31 of the medium temperature absorber 30 via the high temperature evaporator 20. And the high temperature coolant liquid flow path. In the first modification, the refrigerant liquid pipe 88 (see FIG. 3A) is omitted, and the refrigerant liquid pipe 86 provided with the condensing refrigerant pump 89L and the refrigerant liquid provided with the condensing refrigerant pump 89MH. Two lines of tubes 82 are directly connected to the condenser 80. A low temperature refrigerant liquid tube 186 is connected to the refrigerant liquid pipe 86, and a medium high temperature refrigerant liquid pipe 183 is connected to the refrigerant liquid pipe 82. In the preheating heat exchanger 100B, the heat exchangers conventionally divided into three are integrated into one.

  FIG. 3C is a schematic system diagram around a preheating heat exchanger 100C of a three-stage temperature rising absorption heat pump according to a second modification of the embodiment of the present invention. The preheating heat exchanger 100C absorbs the low temperature through the medium temperature evaporator 40 and the low temperature refrigerant liquid tube 186 as a low temperature refrigerant liquid flow path for the refrigerant liquid flow path to flow the refrigerant liquid Vf introduced into the low temperature evaporator 60. The medium temperature refrigerant liquid tube 184 as a medium temperature refrigerant liquid flow path for flowing the refrigerant liquid Vf introduced into the heating pipe 51 inside the heating unit 50 and the inside of the heating pipe 31 of the medium temperature absorber 30 via the high temperature evaporator 20 And a high temperature refrigerant liquid tube 182 as a high temperature refrigerant liquid flow path for flowing the refrigerant liquid Vf. In the second modification, the refrigerant liquid pipe 88 (see FIG. 3A) is omitted, and the refrigerant liquid pipe 86 provided with the condensing refrigerant pump 89L and the refrigerant liquid pipe provided with the condensing refrigerant pump 89M. Each of three systems of the refrigerant liquid pipe 82 in which the condensing refrigerant pump 89H is disposed is directly connected to the condenser 80. A low temperature refrigerant liquid tube 186 is connected to the refrigerant liquid pipe 86, a medium temperature refrigerant liquid pipe 184 is connected to the refrigerant liquid pipe 84, and a high temperature refrigerant liquid pipe 182 is connected to the refrigerant liquid pipe 82. In the preheating heat exchanger 100C, the heat exchangers conventionally divided into four are integrated into one.

  FIG. 4A is a schematic system diagram around a preheating heat exchanger 100D of a two-stage temperature rising absorption heat pump according to a third modification of the embodiment of the present invention. In the preheating heat exchanger 100D, the refrigerant liquid flow path includes the refrigerant liquid Vf introduced into the low temperature evaporator 60 and the refrigerant liquid Vf introduced into the inside of the heating pipe 51 of the low temperature absorber 50 via the high temperature evaporator 20. It is a low temperature / high temperature refrigerant liquid tube 185 to flow. The low temperature / high temperature refrigerant liquid tube 185 serves both as the low temperature refrigerant liquid flow path and the medium temperature refrigerant liquid flow path. In the third modification, since the medium temperature absorber 30 (see FIG. 3A) and the medium temperature evaporator 40 (see FIG. 3A) are omitted, the refrigerant liquid pipe 84 (FIG. 3A) Although it is not provided, it is similar to the preheating heat exchanger 100 (see FIG. 3A) in that the refrigerant liquid pipe 86 and the refrigerant liquid pipe 82 are branched after passing through the preheating heat exchanger 100D. . A low temperature / high temperature refrigerant liquid tube 185 is connected to the refrigerant liquid pipe 88. In the preheating heat exchanger 100D, the heat exchangers conventionally divided into two are integrated into one.

  FIG. 4B is a schematic system diagram around a preheating heat exchanger 100E of a two-stage temperature rising absorption heat pump according to a fourth modification of the embodiment of the present invention. In the preheating heat exchanger 100E, low temperature absorption through the high temperature evaporator 20 and the low temperature refrigerant liquid tube 186 as the low temperature refrigerant liquid flow channel for the low temperature refrigerant liquid flow path in which the refrigerant liquid flow path flows the refrigerant liquid Vf introduced into the low temperature evaporator 60 And a high temperature refrigerant liquid tube 182 as a medium temperature refrigerant liquid flow path for flowing the refrigerant liquid Vf introduced into the heating pipe 51 of the vessel 50. In the fourth modification, the refrigerant liquid pipe 88 (see FIG. 3A) is omitted, and two systems of the refrigerant liquid pipe 86 and the refrigerant liquid pipe 82 are directly connected to the condenser 80. A low temperature refrigerant liquid tube 186 is connected to the refrigerant liquid pipe 86, and a high temperature refrigerant liquid pipe 182 is connected to the refrigerant liquid pipe 82. In the preheating heat exchanger 100E, the heat exchangers conventionally divided into three are integrated into one.

  FIG. 5 is a schematic system diagram around a preheating heat exchanger 100F of a single-stage temperature rising absorption heat pump according to a fifth modification of the embodiment of the present invention. In the preheating heat exchanger 100F, the refrigerant liquid flow path is a low temperature refrigerant liquid tube 186 as a low temperature refrigerant liquid flow path for flowing the refrigerant liquid Vf introduced into the low temperature evaporator 60. In the fifth modification, a refrigerant liquid pipe 86 is connected to the condenser 80, and a low temperature refrigerant liquid tube 186 is connected to the refrigerant liquid pipe 86. In the preheating heat exchanger 100F, the heat exchangers conventionally divided into two are integrated into one.

  In the above description, the fluid flowing through the heating side flow passage of the preheating heat exchanger 100 to 100F is the diluted solution Sw, but instead of the diluted solution Sw, the regenerator introduced into the heat source pipe 71 of the regenerator 70 Even heat source warm water hg, regenerator heat source warm water hg flowing out from heat source tube 71, evaporator heat source warm water he introduced into heat source tube 61 of low temperature evaporator 60, or evaporator heat source warm water he flowing out from heat source tube 61 Good.

DESCRIPTION OF SYMBOLS 1 absorption heat pump 10 high temperature absorber 11 heat transfer tube 30 medium temperature absorber 31 heating tube 41 refrigerant gas-liquid separation cylinder 50 low temperature absorber 51 heating tube 60 low temperature evaporator 61 heat source tube 70 regenerator 71 heat source tube 80 condenser 97 supply water supply Part 100 Preheating heat exchanger 155 Dilute solution flow path 182 High temperature refrigerant liquid tube 183 Medium temperature refrigerant liquid tube 184 Medium temperature refrigerant liquid tube 185 Low temperature refrigerant liquid tube 186 Low temperature refrigerant liquid tube 188 Refrigerant liquid tube 195 Refill water tube he Evaporator heat source Hot water hg Regenerator heat source Hot water Sa High concentration solution Sb Medium concentration solution Sc Low concentration solution Sw Dilute solution Va High temperature refrigerant vapor Vb Medium temperature refrigerant vapor Vc Low temperature refrigerant vapor Vg Regenerator refrigerant vapor Vf Refrigerant liquid W Heated medium Ws Refill water

Claims (4)

A high temperature absorber having a heat transfer pipe for flowing a medium to be heated inside, and heating the medium to be heated by absorption heat generated when absorbing refrigerant vapor which is refrigerant vapor into the absorbing liquid;
The regenerator heat source fluid pipe for flowing the regenerator heat source fluid inside, the absorption liquid which absorbed the refrigerant vapor in the high temperature absorber is directly or indirectly introduced, and the absorption liquid introduced is the regenerator heat source A regenerator, which is heated with a fluid to generate refrigerant vapor from the absorbing liquid to increase the concentration of the absorbing liquid;
A condenser which introduces refrigerant vapor generated in the regenerator, cools and condenses the introduced refrigerant vapor, and generates a refrigerant liquid;
An evaporator heat source fluid pipe for internally flowing an evaporator heat source fluid, the refrigerant liquid is introduced from the condenser, and the introduced refrigerant liquid is heated by the evaporator heat source fluid to generate refrigerant vapor. And
A replenishing fluid supply unit that supplies a replenishing fluid to replenish the heated medium introduced into the heat transfer tube;
The absorbing liquid introduced into the regenerator, the regenerator heat source fluid introduced into the regenerator heat source fluid pipe, the regenerator heat source fluid flowing out from the regenerator heat source fluid pipe, the evaporator heat source fluid pipe A heating side channel for flowing a heating side fluid selected from any of an evaporator heat source fluid and an evaporator heat source fluid flowing out from the evaporator heat source fluid pipe, a replenishment fluid flow path for flowing the replenishment fluid, and the condensation And a refrigerant liquid flow path for flowing the refrigerant liquid that has flowed out of the cooling unit, and heat held by the fluid flowing in the heating side flow path flows in the replenishment fluid flow path and the refrigerant liquid flow path flowing in the replenishment fluid flow path. A heat exchanger for transferring the refrigerant liquid;
Absorption heat pump. It has a first refrigerant heating pipe for flowing the refrigerant liquid discharged from the condenser into the inside, and the high temperature absorber directly or indirectly before introducing the absorption liquid which has absorbed the refrigerant vapor into the regenerator Inside the first refrigerant heating pipe by the absorption heat generated when the refrigerant vapor generated by the low temperature evaporator is introduced and the introduced refrigerant vapor is absorbed by the absorbing liquid. A low temperature absorber for heating the flowing refrigerant liquid;
In the heat exchanger, the refrigerant liquid flow path flows the refrigerant liquid flow path for low temperature flowing the refrigerant liquid introduced to the low temperature evaporator, and the refrigerant liquid introduced to the first refrigerant heating pipe Configured to include a medium temperature refrigerant liquid flow path;
The absorption heat pump according to claim 1. A medium-temperature gas-liquid separator for introducing a refrigerant heated by the first refrigerant heating pipe and separating refrigerant vapor from the introduced refrigerant;
It has a second refrigerant heating pipe for internally flowing the refrigerant liquid discharged from the condenser, and the high temperature absorber directly or before introducing the absorption liquid having absorbed the refrigerant vapor into the low temperature absorber The second refrigerant heating pipe is generated by the absorption heat generated when the refrigerant vapor separated by the medium temperature air-liquid separator is introduced while being introduced indirectly and the introduced refrigerant vapor is absorbed by the absorbing liquid. A medium temperature absorber for heating the refrigerant liquid flowing inside the chamber;
In the heat exchanger, the refrigerant liquid flow path includes a high temperature refrigerant liquid flow path for flowing the high temperature refrigerant liquid introduced into the second refrigerant heating pipe;
The absorption heat pump according to claim 2. The heating side flow path is an absorption liquid flow path for flowing the absorption liquid introduced into the regenerator;
The absorption heat pump of any one of Claim 1 thru | or 3.

Images