CN109269150B

CN109269150B - Absorption heat pump

Info

Publication number: CN109269150B
Application number: CN201810687486.9A
Authority: CN
Inventors: 竹村与四郎; 青山淳; 平田甲介; 刘卫党; 撒卫华
Original assignee: Ebara Refrigeration Equipment and Systems China Co Ltd; Ebara Refrigeration Equipment and Systems Co Ltd
Current assignee: Ebara Refrigeration Equipment and Systems China Co Ltd; Ebara Refrigeration Equipment and Systems Co Ltd
Priority date: 2017-07-17
Filing date: 2018-06-28
Publication date: 2021-09-28
Anticipated expiration: 2038-06-28
Also published as: JP2019020111A; CN109269150A

Abstract

The invention provides an absorption heat pump, which increases output and restrains height. The absorption heat pump is provided with: a first regeneration condensation tank that houses a first regenerator that generates a first concentrated solution and a first condenser that cools and condenses refrigerant vapor from the first regenerator so as to communicate with each other; a second regeneration condensation tank that houses a second regenerator that generates a second concentrated solution and a second condenser that cools and condenses refrigerant vapor from the second regenerator in communication with each other, the second regeneration condensation tank having a gas phase portion that is independent of the first regeneration condensation tank; a cooling water connection flow path that leads cooling water from the first condenser to the second condenser; a first dilute solution introduction flow path that directly guides the absorption liquid flowing out from the absorber to the first regenerator; and a second dilute solution introduction flow path that directly guides the absorption liquid flowing out from the absorber to the second regenerator.

Description

Absorption heat pump

Technical Field

The present invention relates to an absorption heat pump, and more particularly to an absorption heat pump that extracts a heating target fluid having a temperature higher than that of a heat source fluid.

Background

A heat pump is known as a device that draws heat from a low-temperature heat source to become a high-temperature heat source. As one of the heat pumps, an absorption heat pump is known in which a heat medium is heated by absorption heat generated when an absorption liquid absorbs refrigerant vapor. As the absorption heat pump, there is a second type absorption heat pump which is a heating type heat pump for extracting a heated medium having a temperature higher than a temperature of a driving heat source. As an absorption heat pump that can extract the vapor of the medium to be heated while expanding the concentration range of the circulation of the absorption liquid even when the driving heat source temperature is relatively low, there is an absorption heat pump that: in a form in which two sets of tanks including an absorber and an evaporator and two sets of tanks including a regenerator and a condenser are stacked longitudinally in a vertical direction, cooling water is caused to flow in series between the two condensers, a heat source fluid is caused to flow in series between the two evaporators, an absorption liquid flowing out of one regenerator is caused to flow in series to the other regenerator by a difference in head and pressure between the two regenerators, and an absorption liquid flowing out of one absorber is caused to flow in series to the other absorber by a difference in head and pressure between the two absorbers (for example, see patent document 1).

Patent document 1: japanese patent laid-open publication No. 2006 and 177570

However, since the absorption heat pump described in patent document 1 has a small pressure difference between the two regenerators, it is necessary to ensure an appropriate difference in pressure between the two regenerators corresponding to the pressure difference of the absorption liquid distribution capable of distributing the absorption liquid in the subsequent regenerator in order to flow the absorption liquid from one regenerator to the other regenerator without providing a pump, and this is also the case with the absorber. If the difference in height between the two devices corresponding to the pressure difference in the absorption liquid distribution is secured, the height of the entire absorption heat pump increases, and the installation location of the absorption heat pump is restricted. This is significant in absorption heat pumps with large capacities.

Disclosure of Invention

The present invention has been made in view of the above problems, and an object thereof is to provide an absorption heat pump that increases output and suppresses height.

In order to achieve the above object, an absorption heat pump according to a first aspect of the present invention includes, for example, as shown in fig. 1: a first regenerative condensation tank 30 that houses a first regenerator G1 and a first condenser C1 such that a first regenerator G1 communicates with the first condenser C1, the first regenerator G1 heating an absorbent Sw having absorbed a refrigerant with a heat source fluid H to separate a refrigerant Vg1 from the absorbent Sw and generate a first concentrated solution Sa1 having an increased concentration of the absorbent, the first condenser C1 cooling and condensing a vapor Vg1 of the refrigerant separated from the first regenerator G1 with cooling water Y to become a first refrigerant liquid Vf 1; a second regeneration condensation tank 40 that houses a second regenerator G2 and a second condenser C2 such that a second regenerator G2 and the second condenser C2 communicate with each other, the second regenerator G2 heating an absorption liquid Sw after absorbing the refrigerant with a heat source fluid H and separating a refrigerant Vg2 from the absorption liquid Sw to generate a second concentrated solution Sa2 in which the concentration of the absorption liquid increases, the second condenser C2 cooling and condensing a vapor Vg2 of the refrigerant separated from the second regenerator G2 with cooling water Y to become a second refrigerant liquid Vf2, and a gas phase portion of the second regeneration condensation tank 40 being independent of the first regeneration condensation tank 30; a cooling water connection flow path 74 that guides the cooling water Y, which has cooled the refrigerant vapor Vg1 in the first condenser C1, to the second condenser C2; a first dilute solution introduction flow path 33 for directly introducing the absorption liquid Sw flowing out from the absorbers a1, a2 to the first regenerator G1; the second dilute solution introduction flow path 37 directly guides the absorption liquid Sw flowing out from the absorbers a1, a2 to the second regenerator G2.

In the above configuration, the first regeneration condensation tank and the second regeneration condensation tank are not communicated with each other at the gas phase portion, and the first dilute solution introduction flow path and the second dilute solution introduction flow path are provided, so that the absorption liquid is not communicated between the first regenerator and the second regenerator through the gas phase portion, the difference in height is not provided between the first regeneration condensation tank and the second regeneration condensation tank, and the cooling water is caused to flow in series from the first condenser to the second condenser.

As shown in fig. 1, for example, an absorption heat pump according to a second aspect of the present invention is an absorption heat pump 1 according to the first aspect of the present invention, comprising: a first absorption/evaporation tank 10 that houses a first absorber a1 and a first evaporator E1 such that the first absorber a1 and the first evaporator E1 communicate with each other, the first absorber a1 heating the fluid W to be heated by absorption heat generated when the refrigerant vapor Ve1 is absorbed by the absorption liquid Sa to become a first dilute solution Sw1 having a reduced concentration, and the first evaporator E1 heating the refrigerant liquid Vf by the heat source fluid H to generate the refrigerant vapor Ve1 that is absorbed by the absorption liquid Sa in the first absorber a 1; and a second absorption/evaporation tank 20 that houses the second absorber a2 and the second evaporator E2 so as to communicate the second absorber a2 with the second evaporator E2, wherein the second absorber a2 heats the fluid W to be heated by absorption heat generated when the refrigerant vapor Ve2 is absorbed by the absorption liquid Sa to become a second dilute solution Sw2 having a reduced concentration, the second evaporator E2 heats the refrigerant liquid Vf by the heat source fluid H to generate the refrigerant vapor Ve2 that is absorbed by the absorption liquid Sa in the second absorber a2, and a gas phase portion of the second absorption/evaporation tank 20 is independent of the first absorption/evaporation tank 10.

With this configuration, the first absorption/evaporation tank and the second absorption/evaporation tank do not communicate with each other at the gas phase portion, and therefore, the absorption liquid does not flow between the first absorber and the second absorber through the gas phase portion, and the difference in height between the first absorption/evaporation tank and the second absorption/evaporation tank does not have to be provided.

In addition to the absorption heat pump 1 according to the second aspect of the present invention described above, the absorption heat pump according to the third aspect of the present invention is configured such that, for example, as shown in fig. 1, the flow path of the heat source fluid H is configured as follows: the heat source fluid H is first caused to flow into the first evaporator E1 or the second regenerator G2, and flows in series in the first evaporator E1, the second evaporator E2, the first regenerator G1, and the second regenerator G2 in an appropriate order, and the flow path of the heating target fluid W is configured as follows: when the heat source fluid H flows through the first evaporator E1 and then flows through the second evaporator E2, the subject fluid H flows through the second absorber a2 and then flows through the first absorber a1, and when the heat source fluid H flows through the second evaporator E2 and then flows through the first evaporator E1, the subject fluid H flows through the first absorber a1 and then flows through the second absorber a2.

With this configuration, 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 heated flowing out can be increased. In addition, when the heat source fluid first flows into the first evaporator, the increase in the concentration of the absorbent in the first regenerator and the second regenerator can be effectively suppressed, and the absorbent can be prevented from being excessively concentrated and crystallized. In addition, when the heat source fluid connection flow path 72 (see fig. 1, for example) that guides the heat source fluid after the refrigerant liquid is heated in the first evaporator to the second evaporator is provided, the heat source fluid is caused to flow in series from the first evaporator to the second evaporator, and therefore the internal pressure of the first absorber communicating with the first evaporator can be made higher than the internal pressure of the second absorber communicating with the second evaporator, and the concentration of the first dilute solution can be reduced, so the output of the absorption heat pump can be increased.

As shown in fig. 6, for example, an absorption heat pump according to a fourth aspect of the present invention is an absorption heat pump 1C according to the second aspect of the present invention, including: a confluent rich solution pump 53p that pressure-feeds a confluent rich solution Sa obtained by confluent rich solution Sa1 of the first regenerator G1 and second rich solution Sa2 of the second regenerator G2 toward the first absorber a1 and the second absorber a 2; and a dilute solution merging flow path 51 for guiding the merged dilute solution Sw obtained by merging the first dilute solution Aw1 of the first absorber a1 with the second dilute solution Sw2 of the second absorber a2 to the first dilute solution introduction flow path 33 and the second dilute solution introduction flow path 37.

An absorption heat pump according to a fifth aspect of the present invention is the absorption heat pump 1C according to the third aspect of the present invention, further including: a confluent rich solution pump 53p that pressure-feeds a confluent rich solution Sa obtained by confluent rich solution Sa1 of the first regenerator G1 and second rich solution Sa2 of the second regenerator G2 toward the first absorber a1 and the second absorber a 2; and a dilute solution merging flow path 51 for guiding the merged dilute solution Sw obtained by merging the first dilute solution Aw1 of the first absorber a1 with the second dilute solution Sw2 of the second absorber a2 to the first dilute solution introduction flow path 33 and the second dilute solution introduction flow path 37. With this configuration, the flow paths through which the absorption liquid circulates between the two sets of absorbers and the regenerator can be optimized, and the output of the absorption heat pump can be increased.

An absorption heat pump according to a sixth aspect of the present invention is an absorption heat pump 1 according to the second aspect of the present invention, as shown in fig. 1, for example, and includes: a first concentrated solution pump 34p that pressurizes and conveys the first concentrated solution Sa1 from the first regenerator G1 to either one of the first absorber a1 and the second absorber a 2; a second rich solution pump 38p that pumps the second rich solution Sa2 in the second regenerator G2 to one of the first absorber a1 and the second absorber a2 to which the first rich solution pump 34p is not pressure-fed; a first dilute solution connecting passage 14 for guiding the first dilute solution Sw1 of the first absorber a1 to either one of the first dilute solution introduction passage 33 and the second dilute solution introduction passage 37; the second dilute solution connecting passage 18 leads the second dilute solution Sw2 of the second absorber a2 to one of the first dilute solution introduction passage 33 and the second dilute solution introduction passage 37 to which the first dilute solution Sw1 is not led.

An absorption heat pump according to a seventh aspect of the present invention is the absorption heat pump 1 according to the third aspect of the present invention, further including: a first concentrated solution pump 34p that pressurizes and conveys the first concentrated solution Sa1 from the first regenerator G1 to either one of the first absorber a1 and the second absorber a 2; a second rich solution pump 38p that pumps the second rich solution Sa2 in the second regenerator G2 to one of the first absorber a1 and the second absorber a2 to which the first rich solution pump 34p is not pressure-fed; a first dilute solution connecting passage 14 for guiding the first dilute solution Sw1 of the first absorber a1 to either one of the first dilute solution introduction passage 33 and the second dilute solution introduction passage 37; the second dilute solution connecting passage 18 leads the second dilute solution Sw2 of the second absorber a2 to one of the first dilute solution introduction passage 33 and the second dilute solution introduction passage 37 to which the first dilute solution Sw1 is not led.

With this configuration, the number of circulation flow paths of the absorbent can be reduced, and the structure can be simplified.

An absorption heat pump according to an eighth aspect of the present invention is, for example, an absorption heat pump 1A according to any one of the second to seventh aspects of the present invention described above, as shown in fig. 3, wherein the first absorber a1 has a first absorber heat transfer pipe 11 through which the fluid to be heated W flows, the second absorber a2 has a second absorber heat transfer pipe 15 through which the fluid to be heated W flows, and the first absorption-evaporation tank 10A and the second absorption-evaporation tank 20A are arranged such that: the difference in height between the uppermost portions of the first absorber heat transfer tubes 11 and the uppermost portions of the second absorber heat transfer tubes 15 is made smaller than the smaller of the difference in height between the uppermost portions and the lowermost portions of the first absorber heat transfer tubes 11 and the difference in height between the uppermost portions and the lowermost portions of the second absorber heat transfer tubes 15.

With this configuration, the first absorber and the second absorber are arranged in the horizontal direction, the height of the entire absorption heat pump can be suppressed, the difference in pressure at which the absorption liquid is supplied to each absorber can be reduced, the difference in the supply flow rate of the absorption liquid can be reduced, and a decrease in the heat output of one of the first absorber and the second absorber can be avoided.

For example, as shown in fig. 3, an absorption heat pump according to a ninth aspect of the present invention is the absorption heat pump 1A according to any one of the second to seventh aspects of the present invention, wherein the first evaporator E1 has a first evaporator heat transfer pipe 21 through which the heat source fluid H flows, the second evaporator E2 has a second evaporator heat transfer pipe 25 through which the heat source fluid H flows, and the first absorption evaporation tank 10A and the second absorption evaporation tank 20A are arranged such that: the height difference between the uppermost portion of the first evaporator heat transfer tubes 21 and the uppermost portion of the second evaporator heat transfer tubes 25 is made smaller than the smaller of the height difference between the uppermost portion and the lowermost portion of the first evaporator heat transfer tubes 21 and the height difference between the uppermost portion and the lowermost portion of the second evaporator heat transfer tubes 25.

With this configuration, the pressure required to press the heat source fluid into the first evaporator heat transfer tubes and the second evaporator heat transfer tubes can be suppressed.

An absorption heat pump according to a tenth aspect of the present invention is, for example, an absorption heat pump 1A according to any one of the first to seventh aspects of the present invention described above, as shown in fig. 3, wherein the first regenerator G1 has a first regenerator heat transfer pipe 31 through which the heat source fluid H flows, the second regenerator G2 has a second regenerator heat transfer pipe 35 through which the heat source fluid H flows, and the first regenerative condensation tank 30A and the second regenerative condensation tank 40A are arranged such that: the difference in height between the uppermost portion of the first regenerator heat transfer pipe 31 and the uppermost portion of the second regenerator heat transfer pipe 35 is made smaller than the smaller of the difference in height between the uppermost portion and the lowermost portion of the first regenerator heat transfer pipe 31 and the difference in height between the uppermost portion and the lowermost portion of the second regenerator heat transfer pipe 35.

With this configuration, the first regenerator and the second regenerator are arranged in the horizontal direction, so that the height of the entire absorption heat pump can be suppressed, the difference in pressure for supplying the absorption liquid to each regenerator can be reduced, the difference in supply flow rate of the absorption liquid can be reduced, and a decrease in heat output of one of the first regenerator and the second regenerator can be avoided.

An absorption heat pump according to an eleventh aspect of the present invention is, for example, an absorption heat pump 1A according to any one of the first to seventh aspects of the present invention described above, as shown in fig. 3, wherein the first condenser C1 has first condenser heat transfer pipes 41 through which cooling water Y flows, the second condenser C2 has second condenser heat transfer pipes 45 through which cooling water Y flows, and the first regenerative condensation tank 30A and the second regenerative condensation tank 40A are arranged such that: the height difference between the uppermost portion of the first condenser heat transfer pipe 41 and the uppermost portion of the second condenser heat transfer pipe 45 is made smaller than the smaller of the height difference between the uppermost portion and the lowermost portion of the first condenser heat transfer pipe 41 and the height difference between the uppermost portion and the lowermost portion of the second condenser heat transfer pipe 45.

With this configuration, the pressure required to press the cooling water into the first condenser heat transfer pipe and the second condenser heat transfer pipe can be suppressed.

As shown in fig. 8 (fig. 9), for example, an absorption heat pump according to a twelfth aspect of the present invention is an absorption heat pump 1D (1E) according to any one of the second to seventh aspects of the present invention, including: a gas-liquid separator 80 that introduces the heating target fluid W heated by the first absorber a1 and the heating target fluid W heated by the second absorber a2, and separates the heating target fluid W into a vapor Wv and a liquid Wq of the heating target fluid W; and a heating fluid liquid passage 81 for guiding the liquid Wq of the heating fluid in the gas-liquid separator 80 to at least one of the first absorber a1 and the second absorber a2.

With this configuration, the vapor of the fluid to be heated having a high utility value can be taken out.

As shown in fig. 10 (fig. 11), for example, an absorption heat pump according to a thirteenth aspect of the present invention is the absorption heat pump according to the twelfth aspect of the present invention described above (1F (1G)) further including a high-temperature absorber AH that introduces the vapor Wv of the refrigerant and absorbs the vapor Wv of the refrigerant by the absorption liquid Sa, and heats the medium to be heated Xq by absorption heat generated when the vapor Wv of the refrigerant is absorbed by the absorption liquid Sa, wherein the fluid to be heated W is composed of the refrigerant, and the absorption heat pump further includes a refrigerant vapor flow path 89 that guides the vapor Wv of the fluid to be heated by the gas-liquid separator 80 to the high-temperature absorber AH.

With this configuration, the medium to be heated having a temperature higher than that of the fluid to be heated can be taken out.

According to the present invention, since the first regeneration condensation tank and the second regeneration condensation tank are not communicated with each other at their gas phase portions and the first dilute solution introduction flow path and the second dilute solution introduction flow path are provided, the absorption liquid is not allowed to flow between the first regenerator and the second regenerator through the gas phase portion, and the cooling water can be made to flow in series from the first condenser to the second condenser without providing a difference in height between the first regeneration condensation tank and the second regeneration condensation tank, so that the internal pressure of the first regenerator communicated with the first condenser can be made lower than the internal pressure of the second regenerator communicated with the second condenser, the concentration of the first concentrated solution can be increased, and the output of the absorption heat pump can be increased.

Drawings

Fig. 1 is a schematic system diagram of an absorption heat pump according to an embodiment of the present invention.

Fig. 2 is a diagram of a dunline diagram of an absorption heat pump according to an embodiment of the present invention.

Fig. 3 is a schematic system diagram of an absorption heat pump according to a first modification of the embodiment of the present invention.

Fig. 4(a) and 4(B) are schematic diagrams showing a modification around the tank in the absorption heat pump according to the first modification of the embodiment of the present invention.

Fig. 5 is a schematic system diagram of an absorption heat pump according to a second modification of the embodiment of the present invention.

Fig. 6 is a schematic system diagram of an absorption heat pump according to a third modification of the embodiment of the present invention.

Fig. 7 is a diagram of a dunline diagram of an absorption heat pump according to a third modification of the embodiment of the present invention.

Fig. 8 is a schematic system diagram of an absorption heat pump according to a fourth modification of the embodiment of the present invention.

Fig. 9 is a schematic system diagram of an absorption heat pump according to a fifth modification of the embodiment of the present invention.

Fig. 10 is a schematic system diagram of an absorption heat pump according to a sixth modification of the embodiment of the present invention.

Fig. 11 is a schematic system diagram of an absorption heat pump according to a seventh modification of the embodiment of the present invention.

Description of reference numerals: an absorption heat pump; a first absorption-evaporation tank; a first absorption heat transfer tube; a second absorption heat transfer tube; a second absorption-evaporation tank; a first evaporation heat transfer tube; a second evaporation heat transfer tube; a first regenerative condensation tank; a first regeneration heat transfer tube; a first dilute solution inlet pipe; a second regenerative heat transfer tube; a second dilute solution inlet pipe; a second regenerative condensation tank; a first condensate heat transfer tube; 45.. a second condensate heat transfer tube; a dilute solution flow junction tube; a combined concentrated solution pump; a heat source evaporation connecting tube; a cooling water connection pipe; 80.. gas-liquid separator; 89.. heating the subject fluid vapor tube; a first absorber; a second absorber; AH.. a high temperature absorber; c1.. a first condenser; c2.. a second condenser; g1.. a first regenerator; g2.. a second regenerator; a first evaporator; a second evaporator; a heat source fluid; sa.. concentrated solution; a first concentrated solution; a second concentrated solution; sw.. dilute solution; a first dilute solution; (iii) a second dilute solution; a first evaporator refrigerant vapor; a second evaporator refrigerant vapor; a first regenerator refrigerant vapor; a second regenerator refrigerant vapor; vf.. refrigerant liquid; a first refrigerant liquid; vf2.. a second refrigerant liquid; heating a subject fluid; cooling water.

Detailed Description

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

First, an absorption heat pump 1 according to an embodiment of the present invention will be described with reference to fig. 1. Fig. 1 is a schematic system diagram of an absorption heat pump 1. The absorption heat pump 1 includes, as main devices: 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, and a second condenser C2. The absorption heat pump 1 is an apparatus that circulates a refrigerant while changing its phase, and thereby increases the temperature of the fluid W to be heated by transferring heat to the absorption liquid. In the following description, the absorption liquids are referred to as "first dilute solution Sw 1" and "second concentrated solution Sa 2" depending on the properties and the positions on the absorption cycle in order to facilitate the distinction of the absorption cycle, but are collectively referred to as "absorption liquid S" when the properties and the like are not taken into consideration. The refrigerant is referred to as "first evaporator refrigerant vapor Ve 1", "second regenerator refrigerant vapor Vg 2", and "refrigerant liquid Vf" depending on the properties and the position on the absorption cycle in order to facilitate the distinction in the absorption cycle, but the properties are not consideredAnd so on, collectively referred to as "refrigerant V". In the present embodiment, an aqueous LiBr solution is used as the absorbent S (mixture of the absorbent and the refrigerant), and water (H) is used₂O) is used as the refrigerant V, but the present invention is not limited thereto, and other refrigerants and absorption liquids (absorbents) may be used in combination.

The first absorber a1 is a device that absorbs the first evaporator refrigerant vapor Ve1 generated in the first evaporator E1 with the rich solution Sa, and corresponds to a first absorber. The first absorber a1 has: the absorber heat transfer tubes 11 through which the heating target fluid W flows (hereinafter referred to as "first absorber heat transfer tubes 11"), and the first rich solution scattering nozzles 12 that scatter the rich solution Sa toward the outer surfaces of the first absorber heat transfer tubes 11. The first concentrated solution scattering nozzles 12 are arranged above the first absorption heat transfer tubes 11 so as to drop the scattered concentrated solution Sa to the first absorption heat transfer tubes 11. The first absorber a1 is configured to: the first lean solution Sw1 (hereinafter referred to as "first lean solution Sw 1") whose concentration is reduced by the absorption of the first evaporator refrigerant vapor Ve1 by the spreading rich solution Sa is stored in the lower portion, and the heating target fluid W is heated by the absorption heat generated when the first evaporator refrigerant vapor Ve1 is absorbed by the rich solution Sa.

The first evaporator E1 is a device that generates a first evaporator refrigerant vapor Ve1 by evaporating the refrigerant liquid Vf using the heat of the heat source fluid H, and corresponds to a first evaporator. The first evaporator E1 has: a first evaporator heat transfer pipe 21 (hereinafter referred to as "first evaporation heat transfer pipe 21") through which the heat source fluid H flows, and a first refrigerant liquid scattering nozzle 22 that scatters the refrigerant liquid Vf toward the outer surface of the first evaporation heat transfer pipe 21. The first refrigerant liquid distribution nozzle 22 is disposed above the first evaporation heat transfer tube 21 so that the distributed refrigerant liquid Vf falls down to the first evaporation heat transfer tube 21.

The first absorber a1 and the first evaporator E1 are housed in a first absorption/evaporation tank (hereinafter referred to as "first absorption/evaporation tank 10") so as to be adjacent to each other in the horizontal direction. A first absorption/evaporation wall 19 is provided inside the first absorption/evaporation tank 10, and the first absorption/evaporation wall 19 substantially divides the internal space into two parts. The first absorber a1 is disposed on one side and the first evaporator E1 is disposed on the other side in the first absorption/evaporation tank 10 with the first absorption/evaporation wall 19 interposed therebetween. The first absorption-evaporation wall 19 is disposed so as not to contact the top surface of the first absorption-evaporation tank 10, so that the first absorber a1 communicates with the first evaporator E1 at the upper portion. That is, the first absorption/evaporation wall 19 is in contact with the first absorption/evaporation tank 10 at both side walls and the bottom portion except for the upper portion of the first absorption/evaporation tank 10. With this configuration, in the first absorption/evaporation tank 10, the first evaporator refrigerant vapor Ve1 can move from the first evaporator E1 to the first absorber a1.

The second absorber a2 is a device for absorbing the second evaporator refrigerant vapor Ve2 generated at the second evaporator E2 with the rich solution Sa, and corresponds to a second absorber. The second absorber a2 has: a second absorber heat transfer pipe 15 (hereinafter referred to as "second absorption heat transfer pipe 15") through which the heating target fluid W flows, and a second rich solution scattering nozzle 16 that scatters the rich solution Sa toward the outer surface of the second absorption heat transfer pipe 15. The second absorber a2 is configured similarly to the first absorber a1, and the second absorption heat transfer pipe 15 and the second concentrated solution scattering nozzle 16 correspond to the first absorption heat transfer pipe 11 and the first concentrated solution scattering nozzle 12, respectively. The second absorber a2 is configured to store the second lean solution Sw2 (hereinafter referred to as "second lean solution Sw 2") whose concentration is reduced by the absorption of the second evaporator refrigerant vapor Ve2 by the dispersed rich solution Sa in the lower portion, and to heat the fluid W to be heated by the absorption heat generated when the rich solution Sa absorbs the second evaporator refrigerant vapor Ve2. The second absorber heat transfer pipe 15 is connected to the first absorber heat transfer pipe 11 and the connection pipe 71 to be heated, and the connection pipe 71 to be heated guides the fluid W to be heated flowing through the second absorber heat transfer pipe 15 to the first absorber heat transfer pipe 11.

The second evaporator E2 is a device that generates a second evaporator refrigerant vapor Ve2 by evaporating the refrigerant liquid Vf using the heat of the heat source fluid H, and corresponds to a second evaporator. The second evaporator E2 has: a second evaporator heat transfer pipe 25 (hereinafter referred to as "second evaporation heat transfer pipe 25") through which the heat source fluid H flows, and a second refrigerant liquid scattering nozzle 26 that scatters the refrigerant liquid Vf toward the outer surface of the second evaporation heat transfer pipe 25. The second evaporator E2 is configured similarly to the first evaporator E1, and the second evaporation heat transfer tube 25 and the second refrigerant liquid distribution nozzle 26 correspond to the first evaporation heat transfer tube 21 and the first refrigerant liquid distribution nozzle 22, respectively. The first evaporation heat transfer pipe 21 and the second evaporation heat transfer pipe 25 are connected by a heat source evaporation connection pipe 72 serving as a heat source fluid connection flow path, and the heat source evaporation connection pipe 72 guides the heat source fluid H flowing through the first evaporation heat transfer pipe 21 to the second evaporation heat transfer pipe 25.

The second absorber a2 and the second evaporator E2 are housed in a second absorption-evaporation tank (hereinafter referred to as "second absorption-evaporation tank 20") so as to be adjacent to each other in the horizontal direction. A second absorption/evaporation wall 29 is provided inside the second absorption/evaporation tank 20, and the second absorption/evaporation wall 29 substantially divides the internal space into two parts. The second absorber a2 is provided on one side and the second evaporator E2 is provided on the other side in the second absorption/evaporation tank 20 with the second absorption/evaporation wall 29 interposed therebetween. The second absorption-evaporation wall 29 is disposed so as not to contact the top surface of the second absorption-evaporation tank 20, so that the second absorber a2 and the second evaporator E2 communicate at the upper portion. That is, the second absorption-evaporation wall 29 is in contact with the second absorption-evaporation tank 20 at both side walls and the bottom portion except for the upper portion of the second absorption-evaporation tank 20. With this configuration, the second evaporator refrigerant vapor Ve2 can move from the second evaporator E2 to the second absorber a2 in the second absorption/evaporation tank 20.

The first regenerator G1 is a device for heating and concentrating a merged dilute solution Sw (hereinafter, simply referred to as "dilute solution Sw") obtained by merging the first dilute solution Sw1 generated in the first absorber a1 and the second dilute solution Sw2 generated in the second absorber a2, and regenerating the merged dilute solution Sw in concentration, and corresponds to the first regenerator. The first regenerator G1 has: a first regenerator heat transfer pipe 31 (hereinafter referred to as "first regenerator heat transfer pipe 31") constituting a flow path of the heat source fluid H, and a first dilute solution dispersing nozzle 32 dispersing the dilute solution Sw. The first dilute solution dispersing nozzle 32 is disposed above the first regeneration heat transfer pipe 31 so as to allow the dispersed dilute solution Sw to fall down to the first regeneration heat transfer pipe 31. The first regenerator G1 is configured to: the refrigerant V is heated by the heat source fluid H due to the scattered lean solution Sw, thereby generating the first rich solution Sa1 (hereinafter referred to as "first rich solution Sa 1") whose concentration is increased by evaporation from the lean solution Sw. The first regenerator G1 is configured to store the generated first concentrated solution Sa1 in the lower part. In the first regenerator G1, the vapor of the refrigerant V desorbed from the lean solution Sw, i.e., the first regenerator refrigerant vapor Vg1, moves to the first condenser C1.

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 cooling water Y into the first refrigerant liquid Vf1 (hereinafter referred to as "first refrigerant liquid Vf 1"), and corresponds to the first condenser. The first condenser C1 is configured to store the generated first refrigerant liquid Vf1 in the lower portion. The first condenser C1 has a first condenser heat-transfer pipe 41 (hereinafter referred to as "first condenser heat-transfer pipe 41") that constitutes a flow path of the cooling water Y. The first condensation heat transfer pipe 41 is preferably arranged so as not to be immersed in the first refrigerant liquid Vf1 generated by condensation of the first regenerator refrigerant vapor Vg1, so as to be able to directly cool the first regenerator refrigerant vapor Vg1.

The first regenerator G1 and the first condenser C1 are accommodated in a first regenerative condensate tank (hereinafter referred to as "first regenerative condensate tank 30") so as to be adjacent to each other in the horizontal direction. A first regenerative condensation wall 39 is provided inside the first regenerative condensation tank 30, and the first regenerative condensation wall 39 substantially divides the internal space into two parts. The first regenerative condensation tank 30 is provided with a first regenerator G1 on one side and a first condenser C1 on the other side with a first regenerative condensation wall 39 therebetween. The first regenerative condensation wall 39 is disposed not to contact the top surface of the first regenerative condensation tank 30 so that the first regenerator G1 communicates with the first condenser C1 at the upper portion. That is, the first regenerative condensation wall 39 is in contact with the first regenerative condensation tank 30 at both side walls and the bottom portion except for the upper portion of the first regenerative condensation tank 30. With such a configuration, in the first regenerative condensation tank 30, the first regenerator refrigerant vapor Vg1 can move from the first regenerator G1 to the first condenser C1.

The second regenerator G2 is a device for heating and concentrating the dilute solution Sw to regenerate the dilute solution in concentration, and corresponds to a second regenerator. The second regenerator G2 has: a second regenerator heat transfer pipe 35 (hereinafter referred to as "second regeneration heat transfer pipe 35") constituting a flow path of the heat source fluid H, and a second dilute solution distribution nozzle 36 for distributing the dilute solution Sw. The second dilute solution dispersing nozzle 36 is disposed above the second regeneration heat transfer pipe 35 so as to drop the dispersed dilute solution Sw to the second regeneration heat transfer pipe 35. The second regenerator G2 is configured such that the refrigerant V evaporates from the dilute solution Sw due to the distributed dilute solution Sw being heated by the heat source fluid H, and generates a second rich solution Sa2 (hereinafter referred to as "second rich solution Sa 2") whose concentration increases. The second regenerator G2 is configured to store the generated second concentrated solution Sa2 in the lower part. The vapor of the refrigerant V desorbed from the lean solution Sw in the second regenerator G2, i.e., the second regenerator refrigerant vapor Vg2, moves to the second condenser C2. The first and second regeneration

heat transfer tubes

31 and 35 are connected by a heat source regeneration connection pipe 73, and the heat source regeneration connection pipe 73 guides the heat source fluid H flowing through the second regeneration heat transfer tube 35 to the first regeneration heat transfer tube 31. The second regeneration heat transfer pipe 35 and the second evaporation heat transfer pipe 25 are connected by a heat source evaporation connection pipe 75, and the heat source evaporation connection pipe 75 guides the heat source fluid H flowing through the second evaporation heat transfer pipe 25 to the second regeneration heat transfer pipe 35.

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 cooling water Y into the second refrigerant liquid Vf2 (hereinafter referred to as "second refrigerant liquid Vf 2"), and corresponds to a second condenser. The second condenser C2 is configured to store the generated second refrigerant liquid Vf2 in the lower portion. The second condenser C2 has a second condenser heat transfer pipe 45 (hereinafter referred to as "second condenser heat transfer pipe 45") that constitutes a flow path of the cooling water Y. The second condensation heat transfer pipe 45 is preferably disposed so as not to be immersed in the second refrigerant liquid Vf2 generated by condensation of the second regenerator refrigerant vapor Vg2, so that the second regenerator refrigerant vapor Vg2 can be directly cooled. The first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45 are connected by a cooling water connection pipe 74 as a cooling water connection flow path, and the cooling water connection pipe 74 guides the cooling water Y flowing through the first condensation heat transfer pipe 41 to the second condensation heat transfer pipe 45.

The second regenerator G2 and the second condenser C2 are accommodated in a second regeneration condensation tank (hereinafter referred to as "second regeneration condensation tank 40") so as to be adjacent to each other in the horizontal direction. A second regeneration condensation wall 49 is provided inside the second regeneration condensation tank 40, and the second regeneration condensation wall 49 approximately divides the inner space into two parts. The second regeneration condensation tank 40 is provided with a second regenerator G2 on one side and a second condenser C2 on the other side, with a second regeneration condensation wall 49 therebetween. The second regeneration condensation wall 49 is disposed not to contact with the top surface of the second regeneration condensation tank 40 so that the second regenerator G2 is in upper communication with the second condenser C2. That is, the second regeneration condensation wall 49 is in contact with the second regeneration condensation tank 40 at both side walls and the bottom portion except for the upper portion of the second regeneration condensation tank 40. With such a configuration, the second regenerator refrigerant vapor Vg2 can move from the second regenerator G2 to the second condenser C2 in the second regeneration condensation tank 40.

The first absorption-evaporation tank 10, the second absorption-evaporation tank 20, the first regeneration-condensation tank 30, and the second regeneration-condensation tank 40 are vertically stacked in a horizontal state in a vertical up-down line. In the present embodiment, the second regeneration condensation tank 40, the first regeneration condensation tank 30, the first absorption evaporation tank 10, and the second absorption evaporation tank 20 are arranged in this order from the bottom to the top. A space for installing the piping described below may be secured between the tanks.

One end of a first dilute solution outflow pipe 14 serving as a first dilute solution outflow path is connected to a lower portion (typically, the bottom portion) of the first absorber a1, and the first dilute solution outflow pipe 14 is through which the stored first dilute solution Sw1 flows out. One end of a second dilute solution outflow pipe 18 as a second dilute solution outflow path is connected to a lower portion (typically, a bottom portion) of the second absorber a2, and the second dilute solution outflow pipe 18 is through which the stored second dilute solution Sw2 flows out. 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 a dilute solution joining pipe 51 through which the dilute solution Sw flows after the first dilute solution Sw1 and the second dilute solution Sw2 join together. The dilute solution confluence pipe 51 corresponds to a dilute solution confluence flow path. One end of the first dilute solution introduction pipe 33 and one end of the second dilute solution introduction pipe 37 are connected to the other end of the dilute solution confluence pipe 51.

The other end of the first dilute solution introduction pipe 33 is connected to the first dilute solution spreading nozzle 32. The first dilute solution introduction pipe 33 is a pipe for directly introducing the dilute solution Sw flowing out from the first absorber a1 and the second absorber a2 to the first regenerator G1, and corresponds to a first dilute solution introduction flow path. Here, directing the dilute solution Sw flowing out of the absorber directly to the first regenerator G1 means: the dilute solution Sw flowing out from the absorber flows into the first regenerator G1 without passing through other main apparatuses (absorber, evaporator, regenerator, condenser). The other end of the second dilute solution introduction pipe 37 is connected to the second dilute solution spreading nozzle 36. The second dilute solution introduction pipe 37 is a pipe for directly introducing the dilute solution Sw flowing out from the first absorber a1 and the second absorber a2 to the second regenerator G2, and corresponds to a second dilute solution introduction flow path. Here, the fact that the dilute solution Sw flowing out from the absorber is directly led to the second regenerator G2 means that: the dilute solution Sw flowing out from the absorber flows into the second regenerator G2 without passing through other main equipment.

The first absorber a1 and the second absorber a2 are connected via the first dilute solution outlet pipe 14 and the second dilute solution outlet pipe 18, but when the absorption heat pump 1 is operated, the connected portions (the first dilute solution outlet pipe 14 and the second dilute solution outlet pipe 18) are liquid-sealed with the absorbent S, so that the gas phases thereof are not communicated, and the internal pressures thereof can take different values. Further, the gas phase portions of the first absorption/evaporation tank 10 and the second absorption/evaporation tank 20 are not communicated with each other (independent), and the internal pressures of the two tanks can be made different from each other.

One end of a first concentrated solution outflow pipe 34 through which the stored first concentrated solution Sa1 flows out is connected to a lower portion (typically, the bottom portion) of the first regenerator G1. One end of a second concentrated solution outflow pipe 38 through which the stored second concentrated solution Sa2 flows out is connected to a lower portion (typically, the bottom portion) of the second regenerator G2. 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 a concentrated solution confluence pipe 53 through which a confluence concentrated solution Sa (hereinafter, simply referred to as "concentrated solution Sa") where the first concentrated solution Sa1 and the second concentrated solution Sa2 are confluent flows. A confluence concentrated solution pump 53p for pressure-feeding the concentrated solution Sa is provided in the concentrated solution confluence pipe 53. Further, a solution heat exchanger 52 is disposed in the rich solution flow joining pipe 53 and the lean solution flow joining pipe 51. The solution heat exchanger 52 is an apparatus that performs heat exchange between the rich solution Sa flowing through the rich solution flow joint 53 and the lean solution Sw flowing through the lean solution flow joint 51. One end of the first concentrated solution introduction pipe 13 and one end of the second concentrated solution introduction pipe 17 are connected to the other end of the concentrated solution confluence pipe 53.

The other end of the first concentrated solution introduction pipe 13 is connected to the first concentrated solution scattering nozzle 12. In the present embodiment, the first concentrated solution introduction pipe 13 is a pipe that directly guides the concentrated solution Sa flowing out from the first regenerator G1 and the second regenerator G2 to the first absorber a1. Here, the direct introduction of the concentrated solution Sa flowing out of the regenerator to the first absorber a1 means that: the rich solution Sa flowing out of the regenerator flows into the first absorber a1 without passing through other equipment (main equipment, gas-liquid separator, etc.). The other end of the second concentrated solution introduction pipe 17 is connected to the second concentrated solution scattering nozzle 16. In the present embodiment, the second rich solution introduction pipe 17 is a pipe that directly guides the rich solution Sa flowing out from the first regenerator G1 and the second regenerator G2 to the second absorber a2. Here, the direct introduction of the rich solution Sa flowing out of the regenerator to the second absorber a2 means that: the rich solution Sa flowing out of the regenerator flows into the second absorber a2 without passing through other equipment (main equipment, gas-liquid separator, etc.). In this way, the absorption heat pump 1 includes: a first concentrated solution introduction pipe 13 corresponding to a first concentrated solution introduction flow path for directly introducing the absorption liquid flowing out of the regenerator to the first absorber a 1; and a second rich solution introduction pipe 17 corresponding to a second rich solution introduction flow path for directly introducing the absorption liquid flowing out from the regenerator to the second absorber a2.

One end of a first refrigerant liquid outflow pipe 44 from which the stored first refrigerant liquid Vf1 flows out is connected to a lower portion (typically, a bottom portion) of the first condenser C1. One end of a second refrigerant liquid outflow pipe 48 from which the stored second refrigerant liquid Vf2 flows out is connected to a lower portion (typically, a bottom portion) of the second condenser C2. The other end of the first refrigerant flow outlet pipe 44 and the other end of the second refrigerant flow outlet pipe 48 are connected to one end of a refrigerant liquid flow junction pipe 54 through which a refrigerant liquid Vf obtained by merging the first refrigerant liquid Vf1 and the second refrigerant liquid Vf2 flows. A merged refrigerant pump 54p that pressure-feeds the refrigerant liquid Vf is disposed in the refrigerant liquid merging pipe 54. One end of the first refrigerant liquid introduction pipe 23 and one end of the second refrigerant liquid introduction pipe 27 are connected to the other end of the refrigerant liquid junction pipe 54. The other end of the first refrigerant liquid introduction pipe 23 is connected to the first refrigerant liquid distribution nozzle 22. The other end of the second refrigerant liquid introduction pipe 27 is connected to the second refrigerant liquid distribution nozzle 26.

The first regenerator G1 and the second regenerator G2 are connected via the first rich solution outlet pipe 34 and the second rich solution outlet pipe 38, but when the absorption heat pump 1 is operated, the connected portions (the first rich solution outlet pipe 34 and the second rich solution outlet pipe 38) are sealed with the absorption liquid S, so that the gas phase portions of the two are not communicated, and the internal pressures of the two can have different values. The first condenser C1 and the second condenser C2 are connected via the first refrigerant flow-out pipe 44 and the second refrigerant flow-out pipe 48, but when the absorption heat pump 1 is operated, the connected portions (the first refrigerant flow-out pipe 44 and the second refrigerant flow-out pipe 48) are sealed by the refrigerant liquid Vf, so that the gas phase portions of the two are not communicated, and the internal pressures of the two can take different values. As is clear from the above description, the gas phase portions of the first regeneration condensation tank 30 and the second regeneration condensation tank 40 are not communicated with each other (independent), and the internal pressures of the two can be made different.

Next, the operation of the absorption heat pump 1 will be described with reference to fig. 2 together with fig. 1. Fig. 2 is a diagram of a dunline of the absorption heat pump 1. In the durin diagram of fig. 2, the vertical axis represents the dew point temperature of the refrigerant (water in the present embodiment), and the horizontal axis represents the temperature of the absorbing liquid (LiBr aqueous solution in the present embodiment). The line inclined upward to the right represents an isoconcentration line of the absorbent, and the higher the concentration to the right, the lower the concentration to the left. Since the dew point temperature and the saturation pressure shown on the ordinate correspond to each other, the ordinate can be regarded as indicating the internal pressure of the main equipment (absorber, evaporator, regenerator, condenser) in the absorption cycle of the present embodiment in which the vapor of the refrigerant is saturated vapor.

The first condenser C1 receives the first regenerator refrigerant vapor Vg1 evaporated in the first regenerator G1, and is cooled and condensed by the cooling water Y flowing through the first condensation heat transfer pipe 41 to become the first refrigerant liquid Vf1. The second condenser C2 receives the second regenerator refrigerant vapor Vg2 evaporated in the second regenerator G2, and cools and condenses it by the cooling water Y flowing through the second condensation heat transfer pipe 45 to become the second refrigerant liquid Vf2. Since the cooling water Y flows through the cooling water connection pipe 74 and then flows through the first condensation heat transfer pipe 41 and the second condensation heat transfer pipe 45, the temperature of the cooling water Y flowing through the first condensation heat transfer pipe 41 is lower than the temperature of the cooling water Y flowing through the second condensation heat transfer pipe 45, and the internal pressure (TC1) of the first condenser C1 is lower than the internal pressure (TC2) of the second condenser C2. The liquid level of the first refrigerant liquid Vf1 in the first condenser C1 is higher than the liquid level of the second refrigerant liquid Vf2 in the second condenser C2 by an amount that the internal pressure thereof is lower than the internal pressure of the second condenser C2. However, in the present embodiment, since the first regenerative condensation tank 30 having a low internal pressure is disposed above the second regenerative condensation tank 40, the liquid level of the first refrigerant liquid Vf1 in the first condenser C1 and the liquid level of the second refrigerant liquid Vf2 in the second condenser C2 can be maintained appropriately. Therefore, the first condensate heat transfer tubes 41 and the second condensate heat transfer tubes 45 can be suppressed from sinking into the first refrigerant liquid Vf1 and the second refrigerant liquid Vf2.

In the case where the difference between the internal pressure of the first regenerative condensation tank 30 and the internal pressure of the second regenerative condensation tank 40 is large (the difference between the inlet temperature and the outlet temperature of the cooling water Y is large), if a pressure adjustment device such as an orifice or a valve is provided in the second refrigerant flow-out pipe 48 through which the second refrigerant liquid Vf2 flows out from the second condenser C2 having a high internal pressure and the second concentrated solution flow-out pipe 38 through which the second concentrated solution Sa2 flows out from the second regenerator G2, and the difference between the liquid level of the second refrigerant liquid Vf2 in the second condenser C2 and the liquid level of the first refrigerant liquid Vf1 in the first condenser C1 and the liquid level of the second concentrated solution Sa2 in the second regenerator G2 and the liquid level of the first concentrated solution Sa1 in the first regenerator G1 is reduced, the difference between the installation heights of the first regenerative condensation tank 30 and the second regenerative condensation tank 40 can be reduced.

The first refrigerant liquid Vf1 produced in the first condenser C1 flows out to the first refrigerant liquid outlet pipe 44, and the second refrigerant liquid Vf2 produced in the second condenser C2 flows out to the second refrigerant liquid outlet pipe 48. The first refrigerant liquid Vf1 flowing through the first refrigerant flow-out tube 44 and the second refrigerant liquid Vf2 flowing through the second refrigerant flow-out tube 48 flow into the refrigerant liquid junction tube 54 and are mixed together to become the refrigerant liquid Vf. The refrigerant liquid Vf in the refrigerant-liquid junction tube 54 is sent under pressure by the junction refrigerant pump 54p, and is branched to the first refrigerant-liquid introduction tube 23 and the second refrigerant-liquid introduction tube 27. The refrigerant liquid flowing through the first refrigerant liquid introduction pipe 23 is distributed from the first refrigerant liquid distribution nozzle 22 into the first evaporator E1. On the other hand, the refrigerant liquid flowing through the second refrigerant liquid introduction pipe 27 is distributed into the second evaporator E2 from the second refrigerant liquid distribution nozzle 26.

In the first evaporator E1, the refrigerant liquid Vf distributed from the first refrigerant liquid distribution nozzle 22 is heated and evaporated by the heat source fluid H flowing through the first evaporation heat transfer tubes 21, and becomes first evaporator refrigerant vapor Ve1. The first evaporator refrigerant vapor Ve1 generated in the first evaporator E1 moves toward the first absorber a1 communicating with the first evaporator E1. On the other hand, in the second evaporator E2, the refrigerant liquid Vf distributed from the second refrigerant liquid distribution nozzle 26 is heated and evaporated by the heat source fluid H flowing through the second evaporation heat transfer tubes 25, and becomes second evaporator refrigerant vapor Ve2. The second evaporator refrigerant vapor Ve2 generated in the second evaporator E2 moves toward the second absorber a2 communicating with the second evaporator E2. Since the heat source fluid H flows through the heat source evaporation connection pipe 72 and then flows through the second evaporation heat transfer pipes 25 after flowing through the first evaporation heat transfer pipes 21, the temperature when flowing through the first evaporation heat transfer pipes 21 is higher than the temperature when flowing through the second evaporation heat transfer pipes 25, and the internal pressure of the first evaporator E1 (TE1) is higher than the internal pressure of the second evaporator E2 (TE 2).

In the first absorber a1, the first rich solution Sa1 is dispersed from the first rich solution dispersing nozzle 12, and the dispersed first rich solution Sa1 absorbs the first evaporator refrigerant vapor Ve1 moving from the first evaporator E1. The first rich solution Sa1 that absorbed the first evaporator refrigerant vapor Ve1 decreased in concentration to become a first lean solution Sw1(A1a to A1 b). In the first absorber a1, absorption heat is generated when the first rich solution Sa1 absorbs the first evaporator refrigerant vapor Ve1. The fluid to be heated W flowing through the first absorption heat transfer tubes 11 is heated by the absorption heat. The first lean solution Sw1, which absorbs the first evaporator refrigerant vapor Ve1 to be reduced in concentration from the first rich solution Sa1, is stored in the lower portion of the first absorber a1. In the second absorber a2, the second rich solution Sa2 is distributed from the second rich solution distribution nozzle 16, and the distributed second rich solution Sa2 absorbs the second evaporator refrigerant vapor Ve2 moved from the second evaporator E2. The second rich solution Sa2 that absorbed the second evaporator refrigerant vapor Ve2 decreased in concentration to become a second dilute solution Sw2(A2a to A2 b). In the second absorber a2, absorption heat is generated when the second rich solution Sa2 absorbs the second evaporator refrigerant vapor Ve2. The fluid to be heated W flowing through the second absorber heat exchanger tube 15 is heated by the absorption heat. The second lean solution Sw2, which absorbs the second evaporator refrigerant vapor Ve2 to decrease in concentration from the second rich solution Sa2, is stored in the lower portion of the second absorber a2.

At this time, the internal pressure (TE1) of the first absorber a1 communicating with the first evaporator E1 is higher than the internal pressure (TE2) of the second absorber a2 communicating with the second evaporator E2. Since the subject fluid W flows through the first absorbing heat transfer tubes 11 after flowing through the second absorbing heat transfer tubes 15, the temperature of the subject fluid W flowing through the first absorber A1 is higher than the temperature of the subject fluid W flowing through the second absorber A2, and the temperature (A1b) of the first dilute solution Sw1 is higher than the temperature (A2b) of the second dilute solution Sw2. Here, in comparison with the case where there is one absorption-evaporation tank, when there is one absorption-evaporation tank, the internal pressure of the absorber is close to the internal pressure of the second absorber a2 (TE2) having a low internal pressure in the absorption heat pump 1 of the present embodiment, and the temperature of the dilute solution flowing out of the absorber is close to the temperature of the first dilute solution Sw1 having a high temperature in the absorption heat pump 1 of the present embodiment (A1 b). In the absorption heat pump 1 of the present embodiment, since the internal pressure (TE1) of the first absorber a1 is higher than the internal pressure (TE2) of the second absorber a2, the concentration of the first dilute solution Sw1 is lower than that of the absorption/evaporation tank by the amount of the internal pressure increase when the dilute solution flowing out from the absorber has a single concentration. In the absorption heat pump 1 according to the present embodiment, when the concentration of the second dilute solution Sw2 is lower than that of the absorption/evaporation tank, the dilute solution flowing out of the absorber has a lower concentration than the temperature of the absorption liquid. Therefore, in the absorption heat pump 1 of the present embodiment, when the concentration of the first dilute solution Sw1 and the concentration of the second dilute solution Sw2 are set to be lower than that of the absorption/evaporation tank, the concentration of the dilute solution flowing out of the absorber can be made lower, and the output can be increased. In this way, if the order of the tanks through which the heat supply source fluid H flows is from the first evaporator E1 to the second evaporator E2, and the order of the tanks through which the heating target fluid W flows is reversed, and the heating target fluid W flows in the order from the second absorber a2 to the first absorber a1, it is suitable to reduce the concentration of the first dilute solution Sw1 and the concentration of the second dilute solution Sw2.

The liquid level of the second dilute solution Sw2 inside the second absorber a2 is higher than the liquid level of the first dilute solution Sw1 inside the first absorber a1 by an amount that the internal pressure thereof is lower than the internal pressure of the first absorber a1. However, in the present embodiment, the second absorption-evaporation tank 20 having a low internal pressure is disposed above the first absorption-evaporation tank 10, and therefore the liquid level of the second dilute solution Sw2 in the second absorber a2 and the liquid level of the first dilute solution Sw1 in the first absorber a1 can be appropriately maintained. It is therefore possible to suppress the first absorbing heat transfer pipe 11 from sinking into the first dilute solution Sw1 and the second absorbing heat transfer pipe 15 from sinking into the second dilute solution Sw2.

In addition, when the difference between the internal pressure of the first absorption/evaporation tank 10 and the internal pressure of the second absorption/evaporation tank 20 is large (when the difference between the inlet temperature and the outlet temperature of the heat source fluid H is large), if a pressure adjusting device such as an orifice or a valve is provided in the first dilute solution outflow pipe 14 through which the first dilute solution Sw1 flows out from the first absorber a1 having a high internal pressure, and the difference between the liquid level of the first dilute solution Sw1 in the first absorber a1 and the liquid level of the second dilute solution Sw2 in the second absorber a2 is reduced, the difference between the installation heights of the first absorption/evaporation tank 10 and the second absorption/evaporation tank 20 can be reduced.

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. The first dilute solution Sw1 flowing through the first dilute solution outlet pipe 14 and the second dilute solution Sw2 flowing through the second dilute solution outlet pipe 18 respectively flow into the dilute solution flow joining pipe 51 and are mixed to become the dilute solution Sw (ab). The dilute solution Sw flowing through the dilute solution flow junction pipe 51 is branched to the first dilute solution introduction pipe 33 and the second dilute solution introduction pipe 37 after the temperature thereof is lowered by heat exchange with the concentrated solution Sa in the solution heat exchanger 52. The dilute solution Sw flowing through the first dilute solution introduction pipe 33 is distributed from the first dilute solution distribution nozzle 32 into the first regenerator G1. On the other hand, the dilute solution Sw flowing through the second dilute solution introduction pipe 37 is distributed from the second dilute solution distribution nozzle 36 into the second regenerator G2.

At this time, under normal operating conditions, since the difference between the evaporation saturation temperature TE1 and the condensation saturation temperature TC1 is 30 ℃ or more, the difference between the internal pressure of the first absorber a1 and the internal pressure of the first regenerator G1 becomes a sufficient pressure difference necessary for the dilute solution Sw to be dispersed in the first regenerator G1, and the dilute solution Sw can be stably dispersed in the first regenerator G1. In the absorption heat pump 1, since the absorption liquid S does not directly flow between the first regenerator G1 and the second regenerator G2, a step for obtaining the distribution pressure of the absorption liquid S is not required between the first regenerator G1 and the second regenerator G2, and the difference in height between the first regenerator G1 and the second regenerator G2 (the difference in height between the first regenerative condensation tank 30 and the second regenerative condensation tank 40) can be reduced.

In the first regenerator G1, the dilute solution Sw sprayed from the first dilute solution spraying nozzle 32 is heated by the heat source fluid H flowing through the first regeneration heat transfer tubes 31, and the refrigerant in the sprayed dilute solution Sw evaporates to become the first concentrated solution Sa1(G1a to G1b), and is stored in the lower portion of the first regenerator G1. The refrigerant evaporated from the lean solution Sw moves as first regenerator refrigerant vapor Vg1 toward the first condenser C1. On the other hand, in the second regenerator G2, the dilute solution Sw sprayed from the second dilute solution spraying nozzle 36 is heated by the heat source fluid H flowing through the second regeneration heat transfer pipe 35, and the refrigerant in the sprayed dilute solution Sw evaporates to become the second concentrated solution Sa2(G2a to G2b), and is stored in the lower portion of the second regenerator G2. The refrigerant evaporated from the lean solution Sw moves toward the second condenser C2 as second regenerator refrigerant vapor Vg2. As described above, the internal pressure (TC1) of the first regenerative condensation tank 30 is lower than the internal pressure (TC2) of the second regenerative condensation tank 40. Since the heat source fluid H flows through the second regeneration heat transfer tubes 35 and then flows through the first regeneration heat transfer tubes 31, the temperature of the heat source fluid H flowing through the second regenerator G2 is higher than the temperature of the heat source fluid H flowing through the first regenerator G1, and the temperature of the second concentrated solution Sa2(G2 b) is higher than the temperature of the first concentrated solution Sa1(G1 b). Here, in comparison with the case where there is one regeneration condensation tank, when there is one regeneration condensation tank, the internal pressure of the regenerator is close to the internal pressure of the second regenerator G2 having a high internal pressure in the absorption heat pump 1 of the present embodiment (TC2), and the temperature of the rich solution flowing out of the regenerator is close to the temperature of the first rich solution Sa1 having a low temperature in the absorption heat pump 1 of the present embodiment (G1 b). In the absorption heat pump 1 of the present embodiment, since the internal pressure (TC1) of the first regenerator G1 is lower than the internal pressure (TC2) of the second regenerator G2, the concentration of the first rich solution Sa1 is higher than that of the rich solution flowing out of the regenerator by an amount that is lower than the internal pressure when the concentration of the first rich solution Sa1 is higher than that of the regeneration condensation tank. In the absorption heat pump 1 according to the present embodiment, when the concentration of the second rich solution Sa2 is higher than that of the regeneration condensation tank, the concentration of the rich solution flowing out of the regenerator is higher than the temperature of the absorption liquid. Therefore, when the concentrations of the first concentrated solution Sa1 and the second concentrated solution Sa2 are higher than the concentration of the regeneration condensation tank, the concentration of the concentrated solution flowing out of the regenerator can be increased, and the output can be increased. In this way, if the order of the tanks through which the cooling water Y flows is changed from the first condenser C1 to the second condenser C2, and the order of the tanks through which the heat supply fluid H flows is reversed, and the heat supply fluid H flows in the order from the second regenerator G2 to the first regenerator G1, it is suitable to increase the concentration of the first concentrated solution Sa1 and the concentration of the second concentrated solution Sa2.

The first concentrated solution Sa1 generated by the first regenerator G1 flows out to the first concentrated solution outflow pipe 34, and the second concentrated solution Sa2 generated by the second regenerator G2 flows out to the second concentrated solution outflow pipe 38. The first rich solution Sa1 flowing through the first rich solution outflow pipe 34 and the second rich solution Sa2 flowing through the second rich solution outflow pipe 38 respectively flow into the rich solution flow-merging pipe 53 and are mixed to become a rich solution Sa (gb). The rich solution Sa in the rich solution flow line 53 is pressurized and sent by the rich solution merging pump 53p, flows toward the first absorber a1 and the second absorber a2, undergoes heat exchange with the lean solution Sw in the solution heat exchanger 52, increases in temperature, and then is branched to the first rich solution introduction line 13 and the second rich solution introduction line 17. The rich solution Sa flowing through the first rich solution introduction pipe 13 is dispersed from the first rich solution dispersing nozzle 12 into the first absorber a1, and thereafter the above-described cycle is repeated. On the other hand, the rich solution Sa flowing through the second rich solution introduction pipe 17 is dispersed from the second rich solution dispersion nozzle 16 into the second absorber a2, and thereafter the above-described cycle is repeated. In the absorption heat pump 1, since the absorption liquid S does not directly flow between the first absorber a1 and the second absorber a2, a head difference for obtaining the distribution pressure of the absorption liquid S is not required between the first absorber a1 and the second absorber a2, and the difference in height between the first absorber a1 and the second absorber a2 (the difference in height between the first absorption/evaporation tank 10 and the second absorption/evaporation tank 20) can be reduced.

As described above, according to the absorption heat pump 1 of the present embodiment, it is not necessary to provide a step for obtaining the distribution pressure of the absorption liquid S between the first regenerator G1 and the second regenerator G2 and between the first absorber a1 and the second absorber a2, and the height can be suppressed. Further, by flowing the cooling water Y through the first condensation heat transfer tubes 41 and then through the second condensation heat transfer tubes 45, the internal pressure of the first regenerator G1 can be made lower than the internal pressure of the second regenerator G2, and by flowing the heat source fluid H through the second regeneration heat transfer tubes 35 in the order reverse to the tank through which the cooling water Y flows, and then through the first regeneration heat transfer tubes 31, the temperature of the second concentrated solution Sa2 flowing out of the second regenerator G2 can be made higher than the temperature of the first concentrated solution Sa1 flowing out of the first regenerator G1, and the concentration of the first concentrated solution Sa1 and the concentration of the second concentrated solution Sa2 can be made one in the regeneration condensation tank, the concentration of the concentrated solution flowing out of the regenerator can be made higher, and by flowing the heat source fluid H through the first evaporation heat transfer tubes 21 and then through the second evaporation heat transfer tubes 25, the internal pressure of the first absorption device a1 can be made higher than the internal pressure of the second absorption device a2, when the target fluid W to be heated flows through the second absorption heat transfer tubes 15 and then through the first absorption heat transfer tubes 11 in the reverse order to the order of the tanks through which the heat source fluid H flows, the temperature of the second dilute solution Sw2 flowing out of the second absorber a2 can be made lower than the temperature of the first dilute solution Sa1 flowing out of the first absorber a1, and the concentration of the first dilute solution Sw1 and the concentration of the second dilute solution Sw2 can be made lower than the concentration of the absorption evaporation tanks, and the output of the absorption heat pump 1 can be increased.

Next, an absorption heat pump 1A according to a first modification of the embodiment of the present invention will be described with reference to fig. 3. Fig. 3 is a schematic system diagram of the absorption heat pump 1A. The absorption heat pump 1A is different from the absorption heat pump 1 (see fig. 1) in the following points. In the absorption heat pump 1A, the first absorber a1 and the first evaporator E1 housed in the first absorption/evaporation tank 10A are vertically arranged. In the present modification, the first evaporator E1 is disposed above the first absorber a1. The first evaporation heat transfer tubes 21 and the first refrigerant liquid distribution nozzles 22 constituting the first evaporator E1 are housed in the first evaporation container 19A whose upper portion is open. The first evaporator E1 is disposed above the first absorber a1, and therefore, the absorption liquid S in the first absorber a1 can be prevented from leaking into the first evaporator E1 and contaminating the refrigerant liquid Vf in the first evaporator E1. In the second absorption/evaporation tank 20A, the second evaporator E2 housed therein is disposed vertically above the second absorber a2, as in the first absorption/evaporation tank 10A. The second evaporation heat transfer tubes 25 and the second refrigerant liquid distribution nozzle 26 constituting the second evaporator E2 are housed in the second evaporation container 29A whose upper portion is open.

The first absorption-vaporization tank 10A and the second absorption-vaporization tank 20A are disposed adjacent to each other in the horizontal direction. In this case, if the difference in height between the uppermost portions of the first heat exchanger tube 11 and the second heat exchanger tube 15 is made smaller than the smaller one of the differences in height between the uppermost portions and the lowermost portions of the first heat exchanger tube 11 and the second heat exchanger tube 15, the first rich solution dispersing nozzle 12 and the second rich solution dispersing nozzle 16 are arranged at a predetermined height above the uppermost portions of the first heat exchanger tube 11 and the second heat exchanger tube 15, respectively, so that the concentrated solution Sa dispersing pressures in the first absorber a1 and the second absorber a2 are substantially equal to each other, the concentrated solution Sa dispersing amounts are substantially equal to each other, and a decrease in heat output in one of the first absorber a1 and the second absorber a2 can be avoided, which is preferable. In the present modification, the uppermost portions of the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 are configured to have the same height, and the first concentrated solution scattering nozzle 12 and the second concentrated solution scattering nozzle 16 are configured to be disposed at the same height. The same height as referred to herein includes substantially equal heights (ranges in which the dispersion pressure of the rich solution Sa differs to the extent that the respective heat outputs of the first absorber a1 and the second absorber a2 differ within an allowable range). Further, if the difference in height between the uppermost portions of the first and second evaporation

heat transfer pipes

21, 25 is made smaller than the smaller of the differences in height between the uppermost portions and the lowermost portions of the first and second evaporation

heat transfer pipes

21, 25, the pressure at which the heat source fluid H is pushed in can be made smaller than in the absorption heat pump 1 (see fig. 1) in which the difference exists between the uppermost portions and the lowermost portions. In the present modification, the uppermost portions of the first evaporation heat transfer tube 21 and the second evaporation heat transfer tube 25 are configured to have the same height, and the first refrigerant liquid distribution nozzle 22 and the second refrigerant liquid distribution nozzle 26 are configured to be disposed at the same height. The same height as referred to herein includes substantially equal heights. This can suppress the height of the first absorption-vaporization tank 10A and the second absorption-vaporization tank 20A when they are arranged.

In the absorption heat pump 1A, the first regenerator G1 and the first condenser C1 housed in the first regeneration and condensation tank 30A are vertically arranged. 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 housed in the first condensation container 39A whose upper portion is open. The first condenser C1 is disposed above the first regenerator G1, and thereby the absorption liquid S in the first regenerator G1 can be prevented from leaking into the first condenser C1 and contaminating the refrigerant liquid Vf in the first condenser C1. Similarly to the first regenerative condensation tank 30A, the second regenerative condensation tank 40A is disposed vertically above the second regenerator G2, and the second condenser C2 is housed therein. The second condensation heat transfer pipe 45 constituting the second condenser C2 is housed in the second condensation container 49A whose upper portion is open.

The first regeneration condensation tank 30A and the second regeneration condensation tank 40A are disposed adjacent to each other in the horizontal direction. At this time, if the difference in height between the uppermost portions of the first and second regeneration

heat transfer tubes

31, 35 is made smaller than the smaller one of the differences in height between the uppermost portions and the lowermost portions of the first and second regeneration

heat transfer tubes

31, 35, the first and second dilute

solution distribution nozzles

32, 36 are respectively arranged at positions higher than the uppermost portions of the first and second regeneration

heat transfer tubes

31, 35 by a predetermined height, so that the dilute solution Sw distribution pressures in the first and second regenerators G1, G2 are substantially equal to each other, the dilute solution Sw distribution amounts are substantially equal to each other, and a decrease in heat output in one of the first and second regenerators G1, G2 can be avoided, which is preferable. In the present modification, the uppermost portions of the first and second regeneration

heat transfer tubes

31 and 35 are configured to have the same height, and the first and second dilute

solution distribution nozzles

32 and 36 are configured to be disposed at the same height. The same height as referred to herein includes substantially equal heights (ranges in which the dispersion pressure of the dilute solution Sw is different to the extent that the heat output of each of the first regenerator G1 and the second regenerator G2 is different within the allowable range). Further, if the difference in height between the uppermost portions of the first and second condensation

heat transfer pipes

41, 45 is made smaller than the smaller of the differences in height between the uppermost portions and the lowermost portions of the first and second condensation

heat transfer pipes

41, 45, the pressure for pressing the cooling water Y can be made smaller than in the absorption heat pump 1 (see fig. 1) in which the difference exists between the uppermost portions and the lowermost portions, which is preferable. In the present modification, the uppermost portions of the first and second condensate

heat transfer tubes

41 and 45 are arranged at the same height. The same height as referred to herein includes substantially equal heights. This can suppress the height of the first regeneration condensation tank 30A and the second regeneration condensation tank 40A when they are arranged. The first regeneration condensation tank 30A and the second regeneration condensation tank 40A, which are arranged adjacent to each other in the horizontal direction, are arranged below the first absorption/evaporation tank 10A and the second absorption/evaporation tank 20A, which are arranged adjacent to each other in the horizontal direction. The configuration of the absorption heat pump 1A other than the above is the same as that of the absorption heat pump 1 (see fig. 1).

The absorption heat pump 1A configured as described above basically functions in the same manner as the absorption heat pump 1 (see fig. 1). Since the cooling water Y flows through the second condensation heat transfer tubes 45 after flowing through the first condensation heat transfer tubes 41, the temperature of the cooling water Y flowing through the first condensation heat transfer tubes 41 is lower than the temperature of the cooling water Y flowing through the second condensation heat transfer tubes 45, the internal pressure of the first regeneration condensation tank 30A including the first condenser C1 is lower than the internal pressure of the second regeneration condensation tank 40A including the second condenser C2, and the concentration of the first concentrated solution Sa1 flowing out of the first regenerator G1 and the concentration of the second concentrated solution Sa2 flowing out of the second regenerator G2 can be made higher than those of the case where one regeneration condensation tank is provided, and the output can be increased. Since the first condenser C1 and the second condenser C2 are disposed at the same height, the level of the first refrigerant liquid Vf1 in the first condenser C1 is higher than the level of the second refrigerant liquid Vf2 in the second condenser C2 by the amount that the internal pressure of the first regenerative condensation tank 30A is lower than the internal pressure of the second regenerative condensation tank 40A, but when the difference between the internal pressure of the first regenerative condensation tank 30A and the internal pressure of the second regenerative condensation tank 40A is large, a pressure adjusting device such as an orifice or a valve is disposed to reduce the difference between the level of the first refrigerant liquid Vf1 in the first condenser C1 and the level of the second refrigerant liquid Vf 37 in the second condenser C2, and the level of the second refrigerant liquid Vf 34 in the second regenerative condensation tank 30A and the pressure in the second regenerative condensation tank 40A by the pressure adjusting device such as the second refrigerant liquid Vf2 flowing out of the second condenser C2 having a high internal pressure and the pressure adjusting device such as the second concentrated solution Sa2 flowing out of the second regenerator G2, and the pressure adjusting device such as a valve is disposed to reduce the difference between the level of the first refrigerant liquid Vf1 in the first condenser C8234 and the regenerative solution in the second condenser C1 The difference in liquid level of Sa2.

Further, since the heat source fluid H flows through the second evaporation heat transfer tubes 25 after flowing through the first evaporation heat transfer tubes 21, the temperature of the heat source fluid H flowing through the first evaporation heat transfer tubes 21 is higher than the temperature of the heat source fluid H flowing through the second evaporation heat transfer tubes 25, the internal pressure of the first absorption/evaporation tank 10A including the first evaporator E1 is higher than the internal pressure of the second absorption/evaporation tank 20A including the second evaporator E2, and the concentration of the first dilute solution Sw1 flowing out of the first absorber a1 and the concentration of the second dilute solution Sw2 flowing out of the second absorber a2 can be made lower than in the case where one absorption/evaporation tank is used, and the output can be increased. Further, since the first absorber a1 and the second absorber a2 are provided at the same height, the liquid level of the second dilute solution Sw2 in the second absorber a2 is higher than the liquid level of the first dilute solution Sw1 in the first absorber a1 by the amount that the internal pressure of the second absorption/evaporation tank 20A is lower than the internal pressure of the first absorption/evaporation tank 10A, but when the difference between the internal pressure of the first absorption/evaporation tank 10A and the internal pressure of the second absorption/evaporation tank 20A is large, a pressure adjustment device such as an orifice or a valve may be provided in the first dilute solution outflow pipe 14 through which the first dilute solution Sw1 flows out from the first absorber a1 having a high internal pressure, so as to reduce the difference between the liquid level of the first dilute solution Sw1 in the first absorber a1 and the liquid level of the second dilute solution Sw2 in the second absorber a2. In the absorption heat pump 1A, the space between the tank bodies adjacent in the height direction is one position between the first absorption/evaporation tank body 10A and the first regeneration/condensation tank body 30A (or between the second absorption/evaporation tank body 20A and the second regeneration/condensation tank body 40A), and therefore the height of the absorption heat pump 1A can be suppressed.

As shown in fig. 4(a), the configuration may be such that: the first absorption-vaporization tank 10A and the second absorption-vaporization tank 20A are arranged in the lateral direction and in contact with each other, and a communication port 129h is formed in the lower portion, and the first dilute solution Sw1 and the second dilute solution Sw2 are mixed in the tanks. The communication port 129h is formed so as to be lower than the liquid level of the first dilute solution Sw1 in the first absorber a1 and lower than the liquid level of the second dilute solution Sw2 in the second absorber a2 at the upper end thereof. With such a configuration, since the communication port 129h is sealed with the dilute solution Sw, the gas phase of the first absorption/evaporation tank 10A and the gas phase of the second absorption/evaporation tank 20A do not communicate with each other, and the internal pressures of the first absorption/evaporation tank 10A and the second absorption/evaporation tank 20A are maintained independently (in a state where the allowable internal pressures are different from each other). In this case, the first dilute solution outlet pipe 14 (see fig. 3) and the second dilute solution outlet pipe 18 (see fig. 3) can be omitted, and the dilute solution junction pipe 51 can be connected to the lower portion of the tank (typically, the bottom portion directly below the communication port 129 h). In this case, the dilute solution confluence pipe 51 serves as both the first dilute solution outflow passage and the second dilute solution outflow passage. Although not shown, the wall that divides the first absorption/evaporation tank body 10A and the second absorption/evaporation tank body 20A may be extended to the bottom of the first absorption/evaporation tank body 10A and the second absorption/evaporation tank body 20A without providing the communication port 129h, and the solution storage chamber that opens in both the first absorption/evaporation tank body 10A and the second absorption/evaporation tank body 20A may be attached to the bottom lower surface of the first absorption/evaporation tank body 10A and the second absorption/evaporation tank body 20A, and the dilute solution flow combining pipe 51 may be connected to the lower portion of the solution storage chamber. Similarly to the embodiment shown in fig. 4(a), as shown in fig. 4(B), after the first regeneration condensation tank 30A and the second regeneration condensation tank 40A are arranged in the lateral direction and brought into contact with each other, a communication port 349h may be formed in the lower portion, and the first concentrated solution Sa1 and the second concentrated solution Sa2 may be mixed in the tanks. The communication port 349h is formed such that the upper end thereof is below the liquid level of the first rich solution Sa1 in the first regenerator G1 and below the liquid level of the second rich solution Sa2 in the second regenerator G2. With this configuration, since the communication port 349h is sealed with the concentrated solution Sa, the gas phase of the first regeneration condensation tank 30A and the gas phase of the second regeneration condensation tank 40A are not communicated with each other, and the internal pressures of the first regeneration condensation tank 30A and the second regeneration condensation tank 40A are maintained independently (in a state where the allowable internal pressures are different from each other). In this case, the first rich solution outlet pipe 34 (see fig. 3) and the second rich solution outlet pipe 38 (see fig. 3) can be omitted, and the rich solution flow-in pipe 53 can be connected to the lower portion of the tank (typically, the bottom portion directly below the communication port 349 h). In this case, the rich solution flow-merging pipe 53 doubles as a first rich solution outflow passage and a second rich solution outflow passage. Although not shown, the wall defining the first regeneration condensation tank 30A and the second regeneration condensation tank 40A may be extended to the bottom of the first regeneration condensation tank 30A and the second regeneration condensation tank 40A without providing the communication port 349h, and the solution storage chambers opened in both the first regeneration condensation tank 30A and the second regeneration condensation tank 40A may be attached to the bottom lower surfaces of the first regeneration condensation tank 30A and the second regeneration condensation tank 40A, and the concentrated solution flow pipe 53 may be connected to the lower portion of the solution storage chamber.

Next, an absorption heat pump 1B according to a second modification of the embodiment of the present invention will be described with reference to fig. 5. Fig. 5 is a schematic system diagram of the absorption heat pump 1B. The absorption heat pump 1B is different from the absorption heat pump 1A (see fig. 3) in the following points. In the absorption heat pump 1B, the first absorber a1 and the first evaporator E1 housed in the first absorption/evaporation tank 10B are vertically arranged, but the first absorber a1 is disposed above the first evaporator E1. The first absorption heat transfer pipe 11 and the first concentrated solution scattering nozzle 12 constituting the first absorber a1 are housed in the first absorption container 19B whose upper portion is open. The first evaporation vessel 19A is not provided (see fig. 3). The first evaporator E1 is disposed below the first absorber a1, and therefore the pushing pressure of the heat source fluid H supplied to the first evaporation heat transfer pipe 21 can be reduced, and the power of a pump (not shown) that pressurizes and conveys the heat source fluid H can be reduced. Similarly to the first absorption/evaporation tank 10B, the second absorber a2 housed in the second absorption/evaporation tank 20B is disposed vertically above the second evaporator E2. The second absorption heat transfer pipe 15 and the second concentrated solution scattering nozzle 16 constituting the second absorber a2 are housed in the second absorption vessel 29B whose upper portion is open. The second evaporation vessel 29A is not provided (see fig. 3). In a state where the first absorber a1 is disposed vertically above the first evaporator E1 and the second absorber a2 is disposed vertically above the second evaporator E2, the first concentrated solution distribution nozzle 12 and the second concentrated solution distribution nozzle 16 are disposed at the same height (including substantially the same height), and the first refrigerant liquid distribution nozzle 22 and the second refrigerant liquid distribution nozzle 26 are disposed at the same height (including substantially the same height).

In the absorption heat pump 1B, the first regenerator G1 and the first condenser C1 housed in the first regenerative/condensation tank 30B are vertically arranged, but the first regenerator G1 is disposed above the first condenser C1. The first regeneration heat transfer pipe 31 and the first dilute solution distribution nozzle 32 constituting the first regenerator G1 are housed in the first regeneration tank 39B whose upper portion is open. The first condensation container 39A (see fig. 3) is not provided. The first condenser C1 is disposed below the first regenerator G1, and therefore, the pressing pressure for raising the cooling water Y supplied to the first condensation heat transfer pipe 41 can be reduced, and the power of a pump (not shown) for pressurizing and conveying the cooling water Y can be reduced. Similarly to the first regenerative condensation tank 30B, the second regenerative condensation tank 40B has a second regenerator G2 accommodated therein and disposed vertically above the second condenser C2. The second regeneration heat transfer pipe 35 and the second dilute solution distribution nozzle 36 constituting the second regenerator G2 are housed in a second regeneration vessel 49B whose upper portion is open. The second condensation container 49A is not provided (see fig. 3). In a state where the first regenerator G1 is disposed vertically above the first condenser C1 and the second regenerator G2 is disposed vertically above the second condenser C2, the first dilute solution scattering nozzle 32 and the second dilute solution scattering nozzle 36 are disposed at the same height (including substantially the same height), and the uppermost portions of the first condensate heat transfer pipe 41 and the second condensate heat transfer pipe 45 are disposed at the same height (including substantially the same height). The configuration of the absorption heat pump 1B other than the above is the same as that of the absorption heat pump 1A (see fig. 3).

The absorption heat pump 1B configured as described above basically functions in the same manner as the absorption heat pump 1A (see fig. 3). The absorption heat pump 1B can reduce the power of a pump (not shown) that pumps the heat source fluid H and a pump (not shown) that pumps the cooling water Y.

Next, an absorption heat pump 1C according to a third modification of the embodiment of the present invention will be described with reference to fig. 6. Fig. 6 is a schematic system diagram of the absorption heat pump 1C. The absorption heat pump 1C is different from the absorption heat pump 1A (see fig. 3) in the following points. In the absorption heat pump 1C, the first absorption/evaporation tank 10A, the second absorption/evaporation tank 20A, the first regeneration/condensation tank 30A, and the second regeneration/evaporation tank 40A have the same configuration and arrangement as the absorption heat pump 1A (see fig. 3), but the pipes connecting the tanks are configured as follows in which the first dilute solution Sw1 and the second dilute solution Sw2 do not merge, the first concentrated solution Sa1 and the second concentrated solution Sa2 do not merge, and the first refrigerant liquid Vf1 and the second refrigerant liquid Vf2 do not merge. In the absorption heat pump 1C, the first dilute solution outlet pipe 14 is directly connected to the first dilute solution inlet pipe 33 without passing through the dilute solution junction pipe 51 (see fig. 3), and corresponds to a first dilute solution connection flow path. The second dilute solution outlet pipe 18 is directly connected to the second dilute solution inlet pipe 37 without passing through the dilute solution junction pipe 51 (see fig. 3), and corresponds to a second dilute solution connection flow path. The first rich solution outflow pipe 34 is directly connected to the first rich solution introduction pipe 13 without passing through the rich solution confluence pipe 53 (see fig. 3). A first rich solution pump 34p for pressure-feeding the first rich solution Sa1 is provided in the first rich solution outflow pipe 34. Further, the second concentrated solution outflow pipe 38 is connected to the second concentrated solution introduction pipe 17. A second rich solution pump 38p that pressure-feeds the second rich solution Sa2 is provided in the second rich solution outflow pipe 38. A first solution heat exchanger 52A is disposed in the first dilute solution outflow pipe 14 and the first concentrated solution outflow pipe 34, and the first solution heat exchanger 52A exchanges heat with the first concentrated solution Sa1 by the first dilute solution Sw1. A second solution heat exchanger 52B is disposed in the second dilute solution outflow pipe 18 and the second concentrated solution outflow pipe 38, and the second solution heat exchanger 52B exchanges heat with the second concentrated solution Sa2 by the second dilute solution Sw2. The first refrigerant liquid outlet pipe 44 is connected to the first refrigerant liquid inlet pipe 23. A first refrigerant liquid pump 44p that pressurizes and conveys the first refrigerant liquid Vf1 is disposed in the first refrigerant liquid flow tube 44. The second refrigerant liquid outlet pipe 48 is connected to the second refrigerant liquid inlet pipe 27. A second refrigerant liquid pump 48p that pressurizes and conveys the second refrigerant liquid Vf2 is disposed in the second refrigerant liquid flow pipe 48. The absorption heat pump 1C is not provided with: the solution heat exchanger 52 in the absorption heat pump 1A (see fig. 3) is replaced with a first solution heat exchanger 52A and a second solution heat exchanger 52B by a weak solution flow junction pipe 51, a rich solution flow junction pipe 53 provided with a converging rich solution pump 53p, and a refrigerant liquid flow junction pipe 54 provided with a converging refrigerant liquid pump 54 p. The configuration of the absorption heat pump 1C other than the above is the same as that of the absorption heat pump 1A (see fig. 3).

Fig. 7 shows a durin diagram of the absorption heat pump 1C shown in fig. 6. In the absorption heat pump 1C, the circulation circuits of the absorption liquid S are two circuits, i.e., a first circuit D1 circulating as the first dilute solution Sw1 and the first concentrated solution Sa1, and a second circuit D2 circulating as the second dilute solution Sw2 and the second concentrated solution Sa2, and the respective circuits D1 and D2 can be optimized to improve the output performance. Further, since the first absorber a1 and the second absorber a2 are independent of the first regenerator G1 and the second regenerator G2, the internal pressures do not affect each other, and the difference in the internal pressures does not appear as a difference in liquid level, and liquid level control can be performed easily. Further, by operating the first rich solution pump 34p and the second rich solution pump 38p independently from each other, the liquid level control of each of the first absorber a1 and the second absorber a2 can be appropriately performed.

Next, an absorption heat pump 1D according to a fourth modification of the embodiment of the present invention will be described with reference to fig. 8. Fig. 8 is a schematic system diagram of the absorption heat pump 1D. The absorption heat pump 1D is different from the absorption heat pump 1 (see fig. 1) in that a gas-liquid separator 80 is provided. The gas-liquid separator 80 is a device that separates the heating target fluid W heated by the first absorber a1 and the second absorber a2 into the heating target fluid vapor Wv and the heating target fluid liquid Wq. The fluid to be heated Wq flowing out of the gas-liquid separator 80 is supplied in parallel to one end of each of the first absorption heat transfer tubes 11 of the first absorber a1 and the second absorption heat transfer tubes 15 of the second absorber a2 via the fluid to be heated liquid supply tube 81. The heating fluid liquid supply pipe 81 is typically connected to the bottom of the gas-liquid separator 80. The fluid to be boiled and heated Wb which flows out from the other end of each of the first absorption heat transfer tube 11 and the second absorption heat transfer tube 15 and is heated and boiled merges via the fluid pipe to be boiled and heated 83, and flows into the gas-liquid separator 80. The boiling heating target fluid pipe 83 is connected to a gas phase portion of the gas-liquid separator 80 (typically, an upper side portion of the gas-liquid separator 80). A heating target fluid vapor pipe 89 is connected to an upper portion (typically, a top portion) of the gas-liquid separator 80, and the heating target fluid vapor pipe 89 guides the separated heating target fluid vapor Wv to the outside of the absorption heat pump 1D toward a demand target. A supply pipe 85 is also provided for introducing a supply fluid Ws for supplying the heating target fluid W mainly as vapor to the outside of the absorption heat pump 1D from the outside of the absorption heat pump 1D. In the present modification, the supply pipe 85 is connected to the side surface of the gas-liquid separator 80, but may be connected to the heating target fluid-liquid supply pipe 81. The configuration of the absorption heat pump 1D other than the above is the same as that of the absorption heat pump 1 (see fig. 1).

In the absorption heat pump 1D configured as described above, the fluid to be heated Wq flowing out of the gas-liquid separator 80 is supplied to the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 by the bubble pump action based on the difference in specific gravity between the fluid to be heated W in the fluid pipe to be heated 81 and the fluid pipe to be boiled 83 between the gas-liquid separator 80 and the first absorber a1 and the second absorber a2. The bubble pump effect of the absorption heat pump 1D differs depending on the installation heights of the first absorber a1 and the second absorber a2, and the flow rates of the heating target fluid liquid Wq supplied to the absorbers a1 and a2 differ. That is, the flow rate of the fluid liquid to be heated Wq supplied to the first absorber a1 disposed below is larger than the flow rate of the fluid liquid to be heated Wq supplied to the second absorber a2 disposed above. In such a situation, in order to optimize the flow rate of the fluid liquid to be heated Wq supplied to the second absorption heat transfer tube 15 of the second absorber a2 disposed above and the flow rate of the fluid liquid to be heated Wq supplied to the first absorption heat transfer tube 11 of the first absorber a1 disposed below, respectively, from the viewpoint of avoiding heat transfer inhibition due to an excessively small flow rate of the fluid liquid to be heated Wq and inhibition of the gas-liquid separation effect due to an excessively large flow rate of the fluid liquid to be heated Wq, a flow rate adjustment device such as an orifice or a valve may be provided in the fluid liquid to be heated supply tube 81 that supplies the fluid liquid to be heated Wq to the first absorption heat transfer tube 11 of the first absorber a1 disposed below.

Next, an absorption heat pump 1E according to a fifth modification of the embodiment of the present invention will be described with reference to fig. 9. Fig. 9 is a schematic system diagram of the absorption heat pump 1E. The absorption heat pump 1E is an absorption heat pump in which the absorption heat pump 1A shown in fig. 3 is combined with the configuration around the gas-liquid separator 80 of the absorption heat pump 1D shown in fig. 8. According to the absorption heat pump 1E, the height can be suppressed as compared with the absorption heat pump 1D (see fig. 8). In the absorption heat pump 1E, the difference in height between the gas-liquid separator 80 and the first absorber a1 is preferably the same as the difference in height between the gas-liquid separator 80 and the second absorber a2, and the flow rate of the fluid to be heated Wq supplied to the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 can be preferably the same when the fluid to be heated Wq flowing out from the gas-liquid separator 80 is supplied to the first absorption heat transfer pipe 11 and the second absorption heat transfer pipe 15 by the bubble pump action.

Next, an absorption heat pump 1F according to a sixth modification of the embodiment of the present invention will be described with reference to fig. 10. Fig. 10 is a schematic system diagram of the absorption heat pump 1F. The absorption heat pump 1F differs from the absorption heat pump 1D (see fig. 8) in the following points. The absorption heat pump 1F includes: a high-temperature absorber AH having a higher operating pressure and temperature than the operating pressure and temperature of the first absorber a1 and the second absorber a 2; and a high-temperature gas-liquid separator 90 for separating the heating medium X heated by the high-temperature absorber AH into a heating medium vapor Xv and a heating medium liquid Xq. In the absorption heat pump 1F, the fluid W to be heated serves as a refrigerant constituting an absorption cycle. Therefore, although the heating target fluid W is different from the refrigerant V in terms of convenience, the heating target fluid W and the refrigerant V are the same fluid. The high-temperature absorber AH is a device that absorbs the heating target fluid vapor Wv separated by the gas-liquid separator 80 with the rich solution Sa. The high-temperature absorber AH has: a high-temperature absorbing heat transfer pipe 111 through which the medium X to be heated flows, and a high-temperature concentrated solution scattering nozzle 112 that scatters the concentrated solution Sa toward the outer surface of the high-temperature absorbing heat transfer pipe 111. The high-temperature concentrated solution distribution nozzle 112 is connected to a concentrated solution flow pipe 53, and the concentrated solution flow pipe 53 is configured to introduce the concentrated solution Sa into the high-temperature absorber AH. The high-temperature absorber AH is connected to a heating target fluid steam pipe 89, and is configured to be able to introduce the heating target fluid steam Wv from the gas-liquid separator 80. The high temperature absorber AH is configured to store the medium concentration solution Sm, the concentration of which has decreased as the concentrated solution Sa absorbs the fluid vapor to be heated Wv, in the lower portion, and to heat the medium to be heated X by absorption heat generated when the concentrated solution Sa absorbs the fluid vapor to be heated Wv.

The heating medium liquid Xq flowing out of the high-temperature gas-liquid separator 90 is supplied to one end of the high-temperature absorption heat transfer pipe 111 of the high-temperature absorber AH via the heating medium liquid supply pipe 91. The heating medium liquid supply pipe 91 is typically connected to the bottom of the high-temperature gas-liquid separator 90. The boiling heating medium Xb that flows out from the other end of the high-temperature absorption heat transfer pipe 111 and is heated and boiled flows into the high-temperature gas-liquid separator 90 through the boiling heating medium pipe 93. The boiling heating medium pipe 93 is connected to a gas phase portion of the high-temperature gas-liquid separator 90 (typically, an upper side portion of the high-temperature gas-liquid separator 90). A heating medium vapor pipe 99 is connected to an upper portion (typically, a top portion) of the high-temperature gas-liquid separator 90, and the heating medium vapor pipe 99 guides the separated heating medium vapor Xv to the outside of the absorption heat pump 1F toward a demand target. A supply pipe 95 is provided for introducing a supply fluid Xs for supplying the medium X to be heated, which is supplied to the outside of the absorption heat pump 1F mainly as vapor, from the outside of the absorption heat pump 1F. In the present modification, the supply pipe 95 is connected to the heating medium liquid supply pipe 91, but may be connected to a side surface of the high-temperature gas-liquid separator 90.

In the absorption heat pump 1F, one end of the medium concentration solution outflow pipe 151 through which the medium concentration solution Sm flowing out of the high temperature absorber AH flows is connected to a lower portion (typically, a bottom portion) of the high temperature absorber AH. The other end of the medium concentration solution outflow pipe 151 is separated into a first medium concentration solution introduction pipe 113 and a second medium concentration solution introduction pipe 117. The other end of the first medium-concentration solution introduction pipe 113 is connected to the first concentrated solution distribution nozzle 12 of the first absorber a1. The first medium concentration solution introduction pipe 113 corresponds to a first dilute solution introduction flow path. The other end of the second medium-concentration solution introduction pipe 117 is connected to the second concentrated solution distribution nozzle 16 of the second absorber a2. The second medium-concentration solution introduction pipe 117 corresponds to a second dilute solution introduction flow path. In this way, the absorption heat pump 1F is configured to introduce the medium concentration solution Sm into the first and second rich

solution distribution nozzles

12 and 16 and distribute the medium concentration solution Sm inside the first and second absorbers a1 and a2. A high-temperature-solution heat exchanger 152 is disposed in the medium-concentration-solution outflow pipe 151 and the rich-solution flow-merging pipe 53, and the high-temperature-solution heat exchanger 152 exchanges heat with the rich solution Sa using the medium concentration solution Sm. The solution heat exchanger 52 is disposed in the dilute solution flow junction pipe 51 and the concentrated solution flow junction pipe 53 on the upstream side of the high temperature solution heat exchanger 152. One end of an internal makeup pipe 185 is connected to the gas-liquid separator 80, and the internal makeup pipe 185 introduces the refrigerant liquid Vf inside the absorption heat pump 1F but not outside as a makeup fluid Ws. The other end of the internal replenishment pipe 185 is connected to the refrigerant liquid junction pipe 54, the first refrigerant liquid introduction pipe 23, or the second refrigerant liquid introduction pipe 27. The configuration of the absorption heat pump 1F other than the above is the same as that of the absorption heat pump 1D (see fig. 8).

The absorption heat pump 1F configured as described above functions as a two-stage heating type second-type absorption heat pump and can extract the medium vapor to be heated Xv having a higher temperature than the fluid vapor to be heated Wv. Further, the present invention is not limited to the two-stage heating type, and can be applied to a second-type absorption heat pump of a multi-stage heating type including a three-stage heating type. The multistage temperature-raising type second-type absorption heat pump can take out the medium X to be heated while maintaining a liquid (warm water) state, in addition to taking out the medium vapor Xv to be heated as in the present modification, and can save the high-temperature gas-liquid separator 90 when taking out the medium X to be heated while maintaining a liquid state.

Next, an absorption heat pump 1G according to a seventh modification of the embodiment of the present invention will be described with reference to fig. 11. Fig. 11 is a schematic system diagram of the absorption heat pump 1G. The absorption heat pump 1G is a combination of the absorption heat pump 1E shown in fig. 9 and the absorption heat pump 1F shown in fig. 10 configured around the high-temperature absorber AH and around the high-temperature gas-liquid separator 90. The absorption heat pump 1G can be kept at a lower height than the absorption heat pump 1F (see fig. 10). In the case of the two-stage heating type, the heat capacity of the regenerator is about 2 times that of the evaporator, and therefore, it is preferable to dispose the regenerator having a large heat transfer area below the condenser, like the absorption heat pump 1G of the present modification.

In the above description, the heat source fluid H flowing through the first regenerator heat transfer tubes 31 of the first regenerator G1 and the second regenerator heat transfer tubes 35 of the second regenerator G2 is the same as the heat source fluid H flowing through the first evaporation heat transfer tubes 21 of the first evaporator E1 and the second evaporation heat transfer tubes 25 of the second evaporator E2, and flows through the second regeneration heat transfer tubes 35 and the first regeneration heat transfer tubes 31 after flowing through the first evaporation heat transfer tubes 21 and the second evaporation heat transfer tubes 25, but the heat source fluid H flowing through the first evaporation heat transfer tubes 21 and the second evaporation heat transfer tubes 25 and the heat source fluid H flowing through the second regeneration heat transfer tubes 35 and the first regeneration heat transfer tubes 31 may be different types of fluid, and when the same type of heat source fluid H flows through the second regeneration heat transfer tubes 35 and the first regeneration heat transfer tubes 31, the heat source fluid H may flow through the first evaporation heat transfer tubes 21 and the second evaporation heat transfer tubes 25 after flowing through the second regeneration heat transfer tubes 35 and the first regeneration heat transfer tubes 31, the order of the flows in the second regeneration heat transfer pipe 35 and the first regeneration heat transfer pipe 31 may be replaced. Alternatively, the heat exchanger may flow through the second regenerator heat transfer tubes 35 after the first evaporator heat transfer tubes 21 flow and the first regenerator heat transfer tubes 31 after the second evaporator heat transfer tubes 25 flow, or may flow through the first evaporator heat transfer tubes 21 after the second regenerator heat transfer tubes 35 flow and the second evaporator heat transfer tubes 25 after the first regenerator heat transfer tubes 31 flow. Further, after flowing through the first evaporation heat transfer pipes 21, the refrigerant may flow from the second regeneration heat transfer pipes 35 to the first regeneration heat transfer pipes 31 or from the first regeneration heat transfer pipes 31 to the second regeneration heat transfer pipes 35, and then flow through the second evaporation heat transfer pipes 25. In this way, after flowing through the first evaporator heat transfer pipes 21, the heat flows through the second regenerator heat transfer pipes 35 and/or the first regenerator heat transfer pipes 31, and then flows through the second evaporator heat transfer pipes 25. Further, after flowing through the second regenerated heat transfer pipe 35, the first and second evaporator

heat transfer pipes

21 and 25 may flow through the first regenerated heat transfer pipe 31, or the order of the flows through the second regenerated heat transfer pipe 35 and the first regenerated heat transfer pipe 31 may be replaced. As the heat source fluid H, warm water can be typically used, but in addition to warm water, steam, chemical liquids such as petroleum, and condensable chemical vapors such as ethanol may be used. Similarly, the fluid W to be heated may be a chemical liquid such as petroleum or a chemical liquid accompanied by boiling such as ethanol, in addition to hot water or steam.

In the above description, the heat source fluid H flows from the second regenerator G2 to the first regenerator G1 in the reverse order of the tank in which the cooling water Y flows, but the heat source fluid H may flow from the first regenerator G1 to the second regenerator G2 and the order of the tank in which the cooling water Y flows may be the same as the order of the tank in which the cooling water Y flows, depending on the heat source fluid H, after flowing through the first condensation heat transfer tubes 41 of the first condenser C1, flowing through the second condensation heat transfer tubes 45 of the second condenser C2, flowing through the first regeneration heat transfer tubes 31 of the first regenerator G1 and then flowing through the second regeneration heat transfer tubes 35 of the second regenerator G2. Alternatively, the heat source fluid H may flow in parallel through the first regeneration heat transfer pipe 31 of the first regenerator G1 and the second regeneration heat transfer pipe 35 of the second regenerator G2. In this way, the internal pressure of the first regenerator G1 can be made lower than the internal pressure of the regenerator in the case of one regeneration condensation tank, and the concentration of the first concentrated solution Sa1 flowing out of the first regenerator G1 and/or the concentration of the second concentrated solution Sa2 flowing out of the second regenerator G2 can be made higher, thereby increasing the output.

In the above description, the heat source fluid H flows through the first evaporation heat transfer tubes 21 of the first evaporator E1 and then through the second evaporation heat transfer tubes 25 of the second evaporator E2, but the heat source fluid H may flow through the second evaporation heat transfer tubes 25 of the second evaporator E2 and then through the first evaporation heat transfer tubes 21 of the first evaporator E1 depending on the heat source fluid H, after the cooling water Y flows through the first condensation heat transfer tubes 41 of the first condenser C1 and then through the second condensation heat transfer tubes 45 of the second condenser C2, or the heat source fluid H may flow in parallel through the first evaporation heat transfer tubes 21 of the first evaporator E1 and the second evaporation heat transfer tubes 25 of the second evaporator E2. The heat source fluid H may flow in parallel through 4 of the first evaporator heat transfer pipe 21 of the first evaporator E1, the second evaporator heat transfer pipe 25 of the second evaporator E2, the first regenerator heat transfer pipe 31 of the first regenerator G1, and the second regenerator heat transfer pipe 35 of the second regenerator G2. The heat source fluid H may be divided into two streams, one of which flows from the first evaporator heat transfer tubes 21 of the first evaporator E1 to the second evaporator heat transfer tubes 25 of the second evaporator E2, the other of which flows from the second evaporator heat transfer tubes 25 of the second evaporator E2 to the first evaporator heat transfer tubes 21 of the first evaporator E1, the other of which flows from the first regenerator heat transfer tubes 31 of the first regenerator G1 to the second regenerator heat transfer tubes 35 of the second regenerator G2, or the other of which flows from the second regenerator heat transfer tubes 35 of the second regenerator G2 to the first regenerator heat transfer tubes 31 of the first regenerator G1. Similarly, the heat source fluid H may be divided into two streams, one of which flows from the second regeneration heat transfer tubes 35 of the second regenerator G2 to the first evaporation heat transfer tubes 21 of the first evaporator E1, the other of which flows from the first evaporation heat transfer tubes 21 of the first evaporator E1 to the second regeneration heat transfer tubes 35 of the second regenerator G2, the other of which flows from the first regeneration heat transfer tubes 31 of the first regenerator G1 to the second evaporation heat transfer tubes 25 of the second evaporator E2, or the other of which flows from the second evaporation heat transfer tubes 25 of the second evaporator E2 to the first regeneration heat transfer tubes 31 of the first regenerator G1. Similarly, the heat source fluid H may be divided into two streams, one of which flows from the first evaporator heat transfer tubes 21 of the first evaporator E1 to the first evaporator heat transfer tubes 31 of the first regenerator G1, the other of which flows from the first regenerator heat transfer tubes 31 of the first regenerator G1 to the first evaporator heat transfer tubes 21 of the first evaporator E1, the other of which flows from the second evaporator heat transfer tubes 25 of the second evaporator E2 to the second regenerator heat transfer tubes 35 of the second regenerator G2, or the other of which flows from the second regenerator heat transfer tubes 35 of the second regenerator G2 to the second evaporator heat transfer tubes 25 of the second evaporator E2.

In the above description, in the

absorption heat pumps

1, 1A, 1B, and 1C, the fluid W to be heated is made to flow through the second absorption heat transfer tubes 15 of the second absorber a2 and then through the first absorption heat transfer tubes 11 of the first absorber a1, but the fluid W to be heated may be made to flow through the first absorption heat transfer tubes 11 of the first absorber a1 and then through the second absorption heat transfer tubes 15 of the second absorber a2 so that the fluid W to be heated flows from the first absorber a1 to the second absorber a2, and the sequence of the tank body through which the heat source fluid H flows is the same as the sequence of the tank body through which the heat source fluid H flows. As shown in fig. 8 and the like, the fluid W to be heated, which does not involve boiling, may be caused to flow in parallel through the first absorption heat transfer tubes 11 of the first absorber a1 and the second absorption heat transfer tubes 15 of the second absorber a2. This also enables an increase in output.

In the description so far, the flow order of the heat source fluid H is in the illustrated embodiments in which the first evaporator E1, the second evaporator E2, the second regenerator G2, and the first regenerator G1 flow in series in this order, and the modifications not shown in the drawings may be the same as described above, but the order described so far may be, for example, the following order. The heat source fluid H may be constituted by: when the first regenerator G1, the second regenerator G2, the first evaporator E1, and the second evaporator E2 are configured to flow in series, they first flow into the first evaporator E1 or the second regenerator G2. Here, when the heat source fluid H first flows into the first evaporator E1, the flow patterns of the heat source fluid H flowing out of the first evaporator E1 and thereafter are represented by reference numerals in the order of flow for convenience of description, and are (1) E2, G1, G2, (2) E2, G2, G1, (3) G1, E2, G2, (4) G2, E2, G1, (5) G1, G2, E2, (6) G2, G1, and E2. On the other hand, when the heat source fluid H first flows into the second regenerator G2, the flow pattern of the heat source fluid H flowing out of the second regenerator G2 is represented by the reference numerals only in the flow order of (7) G1, E1, E2, (8) G1, E2, E1, (9) E1, G1, E2, (10) E1, E2, G1, (11) E2, G1, E1, (12) E2, E1, and G1. When the heat source fluid H flows in series in any of the above-described manners, the flow order of the fluid to be heated W may be independent of the order of the first regenerator G1 and the second regenerator G2, and when the heat source fluid H flows in the order of the first evaporator E1 and the second evaporator E2, the fluid to be heated W may flow in the order of the second absorber a2 and the first absorber a1 when the heat source fluid H flows in the order of the first evaporator E1 and the second evaporator E2, and the fluid to be heated W may flow in the order of the first absorber a1 and the second absorber a2 when the heat source fluid H flows in the order of the second evaporator E2 and the first evaporator E1. With any of the above-described configurations, the concentration difference of the circulating absorption liquid S can be increased, the amount of heat transferred from the heat source fluid H to the fluid to be heated W can be increased, and the temperature of the fluid to be heated W flowing out can be increased. In addition, when the heat source fluid H first flows into the first evaporator E1, the increase in the concentration of the absorbent S in the first regenerator G1 and the second regenerator G2 can be effectively suppressed, and the absorbent S can be prevented from being excessively concentrated and crystallized. In any of the embodiments, the cooling water Y flows in the order of the first condenser C1 and the second condenser C2, but under typical operating conditions, the flow order of the heat source fluid H is not dependent on the order of the first evaporator E1 and the second evaporator E2, and when only the order of the first regenerator G1 and the second regenerator G2 is focused, the output can be further increased by flowing in the order of the second regenerator G2 and the first regenerator G1, which is preferable.

In the above description, the first evaporator E1 and the second evaporator E2 are of the dispersion type, but the first evaporator E1 and/or the second evaporator E2 may be of the flooded type. When the first evaporator E1 and the second evaporator E2 are flooded, the first refrigerant liquid distribution nozzle 22 and the second refrigerant liquid distribution nozzle 26 can be omitted. Similarly, the first regenerator G1 and the second regenerator G2 are of the dispersion type, but the first regenerator G1 and/or the second regenerator G2 may be of the flooded type. When the first and second regenerators G1 and G2 are flooded, the first and second dilute

solution distribution nozzles

32 and 36 can be omitted.

In the above description, in the

absorption heat pumps

1A, 1B, 1C, 1E, and 1G, the first regeneration condensation tank 30A (30B) and the second regeneration condensation tank 40A (40B) which are disposed adjacent to each other in the horizontal direction are disposed below the first absorption evaporation tank 10A (10B) and the second absorption evaporation tank 20A (20B) which are disposed adjacent to each other in the horizontal direction, but the first absorption evaporation tank 10A (10B) and the second absorption evaporation tank 20A (20B) may be disposed adjacent to the first regeneration condensation tank 30A (30B) and the second regeneration condensation tank 40A (40B) in the horizontal direction. That is, four tanks, i.e., the first absorption-evaporation tank 10A (10B), the second absorption-evaporation tank 20A (20B), the first regeneration-condensation tank 30A (30B), and the second regeneration-condensation tank 40A (40B), may be arranged in a horizontal direction. In this configuration, although the installation area is increased, the height can be suppressed, and this is preferable when the installation area is set in a machine room such as a basement with a low ceiling.

Alternatively, in one absorption heat pump, the first absorption/evaporation tank 10 and the second absorption/evaporation tank 20 in which the absorber and the evaporator are arranged adjacent to each other in the horizontal direction, and the first regeneration/condensation tank 30A (30B) and the second regeneration/condensation tank 40A (40B) in which the regenerator and the condenser are arranged vertically may be combined, or alternatively, the first absorption/evaporation tank 10A (10B) and the second absorption/evaporation tank 20A (20B) in which the absorber and the evaporator are arranged vertically, and the first regeneration/condensation tank 30 and the second regeneration/condensation tank 40 in which the regenerator and the condenser are arranged adjacent to each other in the horizontal direction may be combined.

In the above description, two absorbers, that is, the first absorber a1 and the second absorber a2, and the first evaporator E1 and the second evaporator E2 are provided for each of the absorbers and the evaporators, but one absorber and one evaporator may be provided for each of the absorbers and the evaporators. That is, any one of the first absorption/evaporation tank 10(10A, 10B) and the second absorption/evaporation tank 20(20A, 20B) may be omitted. In the above description, the absorption-evaporation tank bodies (10(10A, 10B), 20(20A, 20B)) and the regeneration-condensation tank bodies (30(30A, 30B), 40(40A, 40B)) are provided in two sets, respectively, but one or both of the absorption-evaporation tank bodies and the regeneration-condensation tank bodies may be provided in 3 or more sets.

In the above description, in the

absorption heat pumps

1D, 1E, 1F, and 1G, the heating target fluid W is supplied from the gas-liquid separator 80 to the first absorber a1 and the second absorber a2 by the bubble pump action, but a pump for pressurizing and conveying the heating target fluid Wq may be provided. If a pump for pressurizing and transporting the heating target fluid W is provided, the gas-liquid separator 80 can be set at a low position, and an absorption heat pump with a further suppressed height can be formed.

Claims

1. An absorption heat pump is characterized by comprising:

a first regenerative condensation tank that houses a first regenerator and a first condenser so as to communicate the first regenerator with the first condenser, the first regenerator heating an absorption liquid that has absorbed a refrigerant with a heat source fluid to separate the refrigerant from the absorption liquid and generate a first concentrated solution in which the concentration of the absorption liquid increases, the first condenser cooling and condensing vapor of the refrigerant separated by the first regenerator with cooling water to form a first refrigerant liquid;

a second regenerative condensation tank that houses a second regenerator and a second condenser so as to communicate the second regenerator with the second condenser, the second regenerator heating an absorption liquid having absorbed a refrigerant with a heat source fluid to separate the refrigerant from the absorption liquid and generate a second concentrated solution having an increased concentration of the absorption liquid, the second condenser cooling and condensing a vapor of the refrigerant separated by the second regenerator with the cooling water to become a second refrigerant liquid, and a gas phase portion of the second regenerative condensation tank being independent of the first regenerative condensation tank;

a cooling water connection flow path that guides the cooling water, which has cooled the vapor of the refrigerant in the first condenser, to the second condenser;

a first dilute solution introduction flow path that directly guides the absorption liquid flowing out from the absorber to the first regenerator; and

a second dilute solution introduction flow path that directly guides the absorption liquid flowing out from the absorber to the second regenerator,

a first absorption/evaporation tank that accommodates a first absorber that heats a fluid to be heated by absorption heat generated when an absorption liquid absorbs refrigerant vapor and turns into a first dilute solution having a reduced concentration, and a first evaporator that heats refrigerant liquid by a heat source fluid and generates the refrigerant vapor absorbed by the absorption liquid in the first absorber, so as to communicate the first absorber and the first evaporator; and

a second absorption/evaporation tank that accommodates a second absorber that heats a fluid to be heated by absorption heat generated when an absorption liquid absorbs refrigerant vapor and becomes a second dilute solution having a decreased concentration, and a second evaporator that heats refrigerant liquid by a heat source fluid and generates the refrigerant vapor to be absorbed by the absorption liquid in the second absorber, the second absorption/evaporation tank being configured such that a second absorber and the second evaporator are communicated with each other, the second absorber and the second evaporator being independent of each other in a gas phase portion thereof,

the flow path of the heat source fluid is configured to: flowing the heat source fluid first into the first evaporator or the second regenerator and in series in the first evaporator, the second evaporator, the first regenerator, and the second regenerator in a suitable order,

the flow path of the fluid to be heated is configured to: when the heat source fluid flows through the second evaporator after flowing through the first evaporator, the subject fluid to be heated is caused to flow through the first absorber after flowing through the second absorber, and when the heat source fluid flows through the first evaporator after flowing through the second evaporator, the subject fluid to be heated is caused to flow through the second absorber after flowing through the first absorber.

2. An absorption heat pump according to claim 1, comprising:

a confluent rich solution pump that pressure-feeds a confluent rich solution in which the first rich solution of the first regenerator and the second rich solution of the second regenerator are confluent toward the first absorber and the second absorber;

and a dilute solution merging flow path that guides a merged dilute solution obtained by merging the first dilute solution of the first absorber and the second dilute solution of the second absorber to the first dilute solution introduction flow path and the second dilute solution introduction flow path.

3. An absorption heat pump according to claim 1, comprising:

a first concentrated solution pump that pressurizes and conveys the first concentrated solution in the first regenerator to either one of the first absorber and the second absorber;

a second concentrated solution pump that pumps the second concentrated solution from the second regenerator to one of the first absorber and the second absorber to which the first concentrated solution pump is not pumped;

a first dilute solution connection channel for guiding the first dilute solution of the first absorber to either one of the first dilute solution introduction channel and the second dilute solution introduction channel; and

and a second dilute solution connection passage that leads the second dilute solution of the second absorber to one of the first dilute solution introduction passage and the second dilute solution introduction passage to which the first dilute solution is not led.

4. An absorption heat pump according to any one of claims 1 to 3,

the first absorber has first absorber heat transfer tubes through which the subject heating fluid flows,

the second absorber has a second absorber heat transfer pipe through which the heating target fluid flows,

the first absorption-evaporation tank and the second absorption-evaporation tank are configured to: the difference in height between the uppermost portion of the first absorber heat transfer tubes and the uppermost portion of the second absorber heat transfer tubes is made smaller than the smaller of the difference in height between the uppermost portion and the lowermost portion of the first absorber heat transfer tubes and the difference in height between the uppermost portion and the lowermost portion of the second absorber heat transfer tubes.

5. An absorption heat pump according to any one of claims 1 to 3,

the first evaporator has a first evaporator heat transfer tube for the flow of the heat source fluid,

the second evaporator has a second evaporator heat transfer tube for the flow of the heat source fluid,

the first absorption-evaporation tank and the second absorption-evaporation tank are configured to: the height difference between the uppermost portion of the first evaporator heat transfer tubes and the uppermost portion of the second evaporator heat transfer tubes is made smaller than the smaller of the height difference between the uppermost portion and the lowermost portion of the first evaporator heat transfer tubes and the height difference between the uppermost portion and the lowermost portion of the second evaporator heat transfer tubes.

6. An absorption heat pump according to any one of claims 1 to 3,

the first regenerator has first regenerator heat transfer tubes for the flow of the heat source fluid,

the second regenerator has a second regenerator heat transfer tube for flowing the heat source fluid,

the first and second regeneration condensate tanks are configured to: the height difference between the uppermost portion of the first regenerator heat transfer pipe and the uppermost portion of the second regenerator heat transfer pipe is made smaller than the smaller of the height difference between the uppermost portion and the lowermost portion of the first regenerator heat transfer pipe and the height difference between the uppermost portion and the lowermost portion of the second regenerator heat transfer pipe.

7. An absorption heat pump according to any one of claims 1 to 3,

the first condenser is provided with a first condenser heat transfer pipe for flowing the cooling water,

the second condenser is provided with a second condenser heat transfer pipe for flowing the cooling water,

the first and second regeneration condensate tanks are configured to: the height difference between the uppermost portion of the first condenser heat transfer pipe and the uppermost portion of the second condenser heat transfer pipe is made smaller than the smaller of the height difference between the uppermost portion and the lowermost portion of the first condenser heat transfer pipe and the height difference between the uppermost portion and the lowermost portion of the second condenser heat transfer pipe.

8. An absorption heat pump according to any one of claims 1 to 3, comprising:

a gas-liquid separator that introduces the fluid to be heated by the first absorber and the fluid to be heated by the second absorber, and separates the fluid to be heated into vapor and liquid of the fluid to be heated; and

and a heating target fluid liquid passage that guides the liquid of the heating target fluid in the gas-liquid separator to at least one of the first absorber and the second absorber.

9. An absorption heat pump according to claim 8,

a high-temperature absorber for introducing the vapor of the refrigerant and absorbing the vapor with an absorbing liquid, and heating a medium to be heated by absorption heat generated when the absorbing liquid absorbs the vapor of the refrigerant,

the heating target fluid is constituted by the refrigerant,

the absorption heat pump further includes a refrigerant vapor flow path that guides vapor of the heating target fluid in the gas-liquid separator to the high-temperature absorber.