JP6805473B2 - Absorption chiller - Google Patents

Description

The present invention relates to an absorption chiller, and particularly to an absorption chiller having a simple structure while introducing and operating a heat source fluid having a relatively low temperature.

There is an absorption chiller that cools cold water by an absorption refrigeration cycle of an absorption liquid and a refrigerant. The absorption chiller includes a hot water-fired absorption chiller that operates using exhaust hot water such as cooling water of a generator as a heat source. In the hot water-fired absorption chiller, the higher the temperature of the hot water, which is the heat source, the greater the amount of heat recovered from the hot water, which contributes to energy saving. On the other hand, the temperature of the discharged hot water is affected by the characteristics of the discharge source and may be low to be put into the hot water-fired absorption chiller. In consideration of such circumstances, a second-class absorption heat pump and an absorption chiller for taking out a medium to be heated having a temperature higher than the heat source temperature are provided, and the exhaust hot water is used as a heat source and the absorber of the second-class absorption heat pump is used from the exhaust hot water. There is also one that produces hot water at a high temperature and uses this as a heat source for an absorption chiller (see, for example, Patent Document 1).

JP-A-59-89962

However, the apparatus described in Patent Document 1 is a device in which a Type 2 absorption heat pump and an absorption chiller are each connected by piping, and has become large.

In view of the above problems, it is an object of the present invention to provide an absorption chiller having a simple structure while introducing and operating a heat source fluid having a relatively low temperature.

In order to achieve the above object, the absorption refrigerating machine according to the first aspect of the present invention, for example, as shown in FIG. 1, obtains latent heat of evaporation required when the liquid Vf of the refrigerant evaporates to become the refrigerant vapor Ve1. A first evaporator E1 that cools the cooling target fluid W by depriving it from the cooling target fluid W; and a first that introduces the refrigerant vapor Ve1 generated in the first evaporator E1 and absorbs it into the first absorbing liquid Sa1. Absorber A1; A second absorber A1 provided with a first absorber flow path 15 for flowing the first absorber Sw1 whose concentration has decreased due to the absorption of the refrigerant vapor Ve1 in the first absorber A1. A second absorber A2 that heats the first absorbent Sw1 flowing through the first absorbent flow path 15 by the absorbed heat released when the second absorbent Sa2 absorbs the refrigerant vapor Ve2. The heat source fluid H that directly or indirectly heats the liquid Vf of the refrigerant for generating the steam Ve2 of the refrigerant supplied to the second absorber A2 is introduced, and the introduced heat source fluid H A second evaporator E2 that heats the liquid Vf of the refrigerant with the heat possessed to generate the steam Ve2 of the refrigerant; and is generated by heating the first absorbent Sw1 in the second absorber A2. A gas-liquid separation unit 90 that separates the refrigerant Vs separated from the first absorption liquid Sw1 and the first absorption liquid Sa1 in which the refrigerant Vs is separated and the concentration is increased; generated by the gas-liquid separation unit 90. It is provided with a first concentrated solution flow path 91 that guides the first absorbing liquid Sa1 having an increased concentration to the first absorber A1.

With this configuration, the first absorption liquid can be regenerated by heating with the absorbed heat generated by the second absorber, and a heat source fluid having a relatively low temperature is introduced and operated to form a simple configuration. be able to.

Further, the absorption chiller according to the second aspect of the present invention is, for example, as shown in FIG. 3, in the absorption chiller 1A according to the first aspect of the present invention, the steam of the refrigerant in the second absorber A2. By introducing the second absorption liquid Sw2 whose concentration has decreased due to the absorption of Ve2 and heating the introduced second absorption liquid Sw2 with the heat possessed by the heat source fluid H, the refrigerant is supplied from the second absorption liquid Sw2. The regenerator G2 that releases Vg to increase the concentration of the second absorption fluid Sw2; the steam Vg of the refrigerant separated from the second absorption fluid Sw2 in the regenerator G2, and the refrigerant generated by the gas-liquid separation unit 90. The vapor Vs of the above is introduced, and the common condenser Cs that condenses the introduced refrigerant vapor Vg and Vs to generate the refrigerant liquid Vf is provided.

With this configuration, the refrigerant separated from the first absorption liquid and the refrigerant separated from the second absorption liquid can be condensed together, and the configuration can be further simplified.

Further, the absorption chiller according to the third aspect of the present invention is, for example, as shown in FIG. 5, in the absorption chiller according to the first aspect or the second aspect of the present invention, the second absorber A2a. Has a plurality of heating tubes 15 constituting the first absorption liquid flow path; so that the first absorption liquid Sw1 flowing inside the heating pipe 15 flows in the opposite direction inside another heating pipe 15. The reversing liquid chamber 54 leading to another heating tube 15 is provided; the plurality of heating tubes 15 are composed of a plurality of paths by the reversing liquid chamber 54; each of the plurality of paths has the same flow path cross-sectional area. It is configured as follows.

With this configuration, when the proportion of the vapor of the refrigerant separated from the first absorption liquid increases toward the downstream side of the flow, the flow velocity of the first absorption liquid goes toward the downstream side of the flow. As a result, the flow rate of the first absorbing liquid flowing into each heating tube becomes close to uniform, and it is possible to suppress a decrease in heat transfer efficiency due to non-uniform flow in the heating tube. It is possible to prevent the crystallization of the first absorption liquid by suppressing the situation where the concentration and temperature of the first absorption liquid are locally increased.

Further, the absorption chiller according to the fourth aspect of the present invention is the absorption chiller according to the first aspect or the second aspect of the present invention, in which the second absorber is the first absorption liquid flow path. It has one or more heating pipes constituting the above; an inlet liquid chamber that communicates with one or more heating pipes and supplies the first absorption liquid to the connected heating pipes; one or more It is provided with an outlet liquid chamber that communicates with the heating pipe and collects all the first absorption liquids supplied from the inlet liquid chamber to the heating pipe after flowing through the heating pipe.

With this configuration, the first absorbing liquid in a liquid state is supplied from the inlet liquid chamber to the heating tube, and it is possible to suppress a decrease in heat transfer efficiency due to non-uniform flow in the heating tube and the like. It is possible to prevent the crystallization of the first absorption liquid by suppressing the situation where the concentration and temperature of the first absorption liquid are locally increased.

Further, the absorption chiller according to the fifth aspect of the present invention is, for example, as shown in FIG. 9, in the absorption chiller 1 according to any one of the first to fourth aspects of the present invention. The first absorption liquid pump 99 for pushing the first absorption liquid Sw1 introduced into the second absorber A2 into the first absorption liquid flow path 15 is provided.

With this configuration, the flow rate of the first absorption liquid in the first absorption liquid flow path can be increased, and the flow rate in the first absorption liquid flow path is locally uneven. It is possible to suppress the situation where the concentration and temperature of the first absorbing liquid become high, and it is possible to avoid the crystallization of the first absorbing liquid and improve the heat transfer efficiency.

Further, the absorption chiller according to the sixth aspect of the present invention is, for example, as shown in FIG. 4, in the absorption chiller 1B according to any one of the first to fifth aspects of the present invention. The gas-liquid separation unit 90 is integrally formed with the second absorber A2 by arranging the inlet of the first absorption liquid Sw1 adjacent to the outlet of the first absorption liquid flow path 15. ..

With such a configuration, it is possible to suppress an increase in the size of the device.

Further, the absorption chiller according to the seventh aspect of the present invention is, for example, as shown in FIG. 5 (and FIG. 6), in the absorption chiller according to the sixth aspect of the present invention, the second absorber A2a. A liquid phase portion 55q provided along the can body 57 of (A2b) and temporarily storing the first absorption liquid Sa1 flowing through the first absorption liquid flow path 15, and a refrigerant separated from the first absorption liquid Sw1. The outlet liquid chamber 55 (55B) has an outlet liquid chamber 55 (55B) having a vapor phase portion 55 g through which vapor Vs pass; the outlet liquid chamber 55 (55B) is provided with an eliminator 96 (96B) in the gas phase portion 55 g to separate gas and liquid. It is configured to function as a unit.

With this configuration, the gas and liquid of the first absorption liquid can be separated in the outlet liquid chamber.

Further, the absorption chiller according to the eighth aspect of the present invention is, for example, as shown in FIG. 7, in the absorption chiller according to the sixth aspect of the present invention, in the can body 57 of the second absorber A2c. A liquid phase portion 55q that is provided along the line and temporarily stores the first absorption liquid Sa1 that has flowed through the first absorption liquid flow path 15, and a gas phase portion through which the refrigerant vapor Vs separated from the first absorption liquid Sw1 passes. An outlet liquid chamber 55C having 55 g and the like; the outlet liquid chamber 55C is configured so that the gas phase portion 55 g extends horizontally, and the refrigerant vapor Vs flowing through the gas phase portion 55 g flows to the left and right. A plurality of flow path limiting members 98 that limit the path are provided in the space of the gas phase portion 55 g, and are configured to function as a gas-liquid separation portion.

With this configuration, the outlet liquid chamber can function as a gas-liquid separation unit with a simple configuration.

Further, the absorption chiller according to the ninth aspect of the present invention is, for example, as shown in FIG. 8, in the absorption chiller 1C according to any one of the first to eighth aspects of the present invention. , The second high temperature evaporator E2H that generates the vapor of the refrigerant V supplied to the second absorber A2H; and the second absorption liquid S2 directly or indirectly introduced from the second absorber A2H is the refrigerant V. It is provided with a second low temperature absorber A2L that heats the refrigerant Vf of the second high temperature evaporator E2H by the absorption heat released when the steam is absorbed.

With this configuration, a lower temperature fluid can be used as the heat source fluid to be introduced into the second evaporator.

According to the present invention, the first absorbing liquid can be heated and regenerated by the absorbed heat generated by the second absorber, and a heat source fluid having a relatively low temperature is introduced and operated to have a simple configuration. be able to.

It is a schematic system diagram of the absorption chiller which concerns on embodiment of this invention. It is a Dühring diagram in the absorption chiller which concerns on embodiment of this invention. It is a schematic system diagram of the absorption chiller which concerns on the 1st modification of the Embodiment of this invention. It is a schematic system diagram of the absorption chiller which concerns on the 2nd modification of the Embodiment of this invention. It is sectional drawing of the 1st modification of the 2nd absorber provided in the absorption chiller which concerns on the 2nd modification of the Embodiment of this invention. It is sectional drawing of the 2nd modification of the 2nd absorber provided in the absorption chiller which concerns on the 2nd modification of the Embodiment of this invention. It is sectional drawing of the 3rd modification of the 2nd absorber provided in the absorption chiller which concerns on the 2nd modification of the Embodiment of this invention. It is a schematic system diagram of the absorption chiller which concerns on the 3rd modification of the Embodiment of this invention. It is a partial system diagram which shows the structure when the circulation pump is provided in the absorption chiller which concerns on embodiment of this invention.

Hereinafter, embodiments of the present invention will be described with reference to the drawings. In each figure, members that are the same as or correspond to each other are designated by the same or similar reference numerals, and duplicate description will be omitted.

First, the absorption chiller 1 according to the embodiment of the present invention will be described with reference to FIG. FIG. 1 is a schematic system diagram of the absorption chiller 1. The absorption chiller 1 has, as main equipment, a first absorber A1, a first evaporator E1, a first condenser C1, a second absorber A2, a second evaporator E2, and a second regenerator G2. A second condenser C2 and a gas-liquid separator 90 are provided. The absorption chiller 1 does not have a first regenerator as an independent configuration. The absorption chiller 1 is a device that causes heat transfer by circulating the refrigerant while undergoing a phase change with respect to the absorption liquid, and lowers the temperature of the cold water W, which is the fluid to be cooled. In the following description, the absorption liquid is referred to as "first rare solution Sw1", "second concentrated solution Sa2", etc. according to the properties and the position on the absorption cycle in order to facilitate the distinction on the absorption cycle. However, when the properties are unquestioned, they are collectively referred to as "absorbent solution S". Further, in order to facilitate the distinction of the refrigerant on the absorption cycle, "first evaporator refrigerant vapor Ve1", "regenerator refrigerant vapor Vg", and "refrigerant liquid Vf" are used according to the properties and the position on the absorption cycle. However, when the properties are unquestioned, they are collectively referred to as "refrigerant V". In this embodiment, the absorbing liquid S and LiBr solution is used as (a mixture of absorbent and refrigerant) is water (H 2 _O) is used as the refrigerant V, other refrigerants not limited thereto , May be used in combination with an absorbent (absorbent).

The first absorber A1 is a device that absorbs the first evaporator refrigerant vapor Ve1 generated by the first evaporator E1 with the first concentrated solution Sa1 and corresponds to the first absorber. The first absorber A1 has a cooling pipe 11 through which the cooling water Y flows, and a first concentrated solution spraying nozzle 12 for spraying the first concentrated solution Sa1 toward the outer surface of the cooling pipe 11. It has inside. The first concentrated solution spraying nozzle 12 is arranged above the cooling pipe 11 so that the sprayed first concentrated solution Sa1 falls on the cooling pipe 11. The first absorber A1 stores the first rare solution Sw1 whose concentration has decreased due to the sprayed first concentrated solution Sa1 absorbing the first evaporator refrigerant vapor Ve1 in the lower part of the first absorber can body 17. At the same time, the cooling water Y is configured to take away the endothermic heat generated when the first concentrated solution Sa1 absorbs the first evaporator refrigerant vapor Ve1. One end of the first dilute solution tube 18 that guides the first dilute solution Sw1 to the second absorber A2 is connected to the lower portion (typically the bottom portion) of the first absorber can body 17. The first dilute solution tube 18 is provided with a first dilute solution pump 19 for pumping the first dilute solution Sw1.

The first evaporator E1 is a device that cools the cold water W by evaporating the refrigerant liquid Vf with the heat of the cold water W to generate the first evaporator refrigerant vapor Ve1, and corresponds to the first evaporator. The first evaporator E1 has an evaporation pipe 21 through which cold water W flows and a refrigerant liquid spray nozzle 22 for spraying the refrigerant liquid Vf toward the outer surface of the evaporation pipe 21 inside the first evaporator can body 27. ing. The refrigerant liquid spray nozzle 22 is arranged above the evaporation pipe 21 so that the sprayed refrigerant liquid Vf falls on the evaporation pipe 21. The first evaporator E1 uses a refrigerant liquid pipe 28 that guides the refrigerant liquid Vf stored in the lower part of the first evaporator can body 27 to the refrigerant liquid spray nozzle 22 and a refrigerant liquid Vf in the refrigerant liquid pipe 28. It has a first refrigerant pump 29 that feeds to the spray nozzle 22. The first evaporator E1 takes away the heat of vaporization for the refrigerant liquid Vf sprayed on the outer surface of the evaporation pipe 21 to become the first evaporator refrigerant vapor Ve1 from the cold water W flowing in the evaporation pipe 21. The cold water W is cooled, and the non-evaporated refrigerant liquid Vf of the sprayed refrigerant liquid Vf is stored in the lower part of the evaporator can body 27.

In the present embodiment, the first absorber A1 and the first evaporator E1 are arranged adjacent to each other, and the upper part of the first absorber can body 17 and the upper part of the first evaporator can body 27 communicate with each other. ing. With such a configuration, the first evaporator refrigerant vapor Ve1 generated inside the first evaporator can body 27 can be guided to the inside of the first absorber can body 17.

The first condenser C1 is a device that introduces the separated refrigerant vapor Vs from the gas-liquid separator 90, cools and condenses the refrigerant liquid Vs, and generates the refrigerant liquid Vf to be sent to the first evaporator E1. The first condenser C1 has a condenser pipe 41 forming a flow path for the cooling water Y inside the first condenser can body 47. The condensing pipe 41 is preferably arranged so that the separated refrigerant vapor Vs is not immersed in the condensed refrigerant liquid Vf so that the separated refrigerant vapor Vs can be directly cooled. The other end of the cooling water connecting pipe 34, one end of which is connected to the cooling pipe 11, is connected to one end of the condensing pipe 41. The other end of the condensing pipe 41 and the other end of the cooling pipe 11 are connected to a pipe connected to a cooling tower (not shown) outside the absorption chiller 1. With such a configuration, the cooling water Y flowing out of the condensing pipe 41 is cooled by a cooling tower (not shown) and supplied to the cooling pipe 11. A refrigerant liquid pipe 48 that guides the condensed refrigerant liquid Vf to the first evaporator E1 is connected to the first condenser C1. One end of the refrigerant liquid pipe 48 is connected to a portion (typically the bottom portion) of the lower part of the first condenser can body 47 where the refrigerant liquid Vf is stored, and the other end is connected to the first evaporator can body 27. ing.

The second absorber A2 is a device that absorbs the second evaporator refrigerant vapor Ve2 generated by the second evaporator E2 with the second concentrated solution Sa2, and corresponds to the second absorber. The second absorber A2 has a heating tube 15 and a second concentrated solution spraying nozzle 52 for spraying the second concentrated solution Sa2 toward the outer surface of the heating tube 15 inside the second absorber can body 57. There is. The heating tube 15 is a tube that constitutes a flow path through which the first dilute solution Sw1 generated by the first absorber A1 flows, and corresponds to the first absorption liquid flow path. The second concentrated solution spraying nozzle 52 is arranged above the heating tube 15 so that the sprayed second concentrated solution Sa2 falls on the heating tube 15. The second absorber A2 stores the second rare solution Sw2 whose concentration has decreased due to the sprayed second concentrated solution Sa2 absorbing the second evaporator refrigerant vapor Ve2 in the lower part of the second absorber can body 57. At the same time, the first rare solution Sw1 flowing inside the heating tube 15 is heated by the endothermic heat generated when the second concentrated solution Sa2 absorbs the second evaporator refrigerant vapor Ve2. One end of the second rare solution tube 58 that guides the second rare solution Sw2 to the second regenerator G2 is connected to the lower part (typically the bottom) of the second absorber can body 57.

The second evaporator E2 is a device that generates the second evaporator refrigerant vapor Ve2 supplied to the second absorber A2, and corresponds to the second evaporator. The second evaporator E2 has a heat source pipe 61 forming a flow path of the heat source fluid H inside the second evaporator can body 67. The second evaporator E2 does not have a nozzle for spraying the refrigerant liquid Vf inside the second evaporator can body 67. Therefore, the heat source pipe 61 is arranged so as to be immersed in the refrigerant liquid Vf stored in the second evaporator can body 67 (full-liquid evaporator). The second evaporator E2 is configured so that the refrigerant liquid Vf around the heat source pipe 22 evaporates with the heat of the heat source fluid H flowing in the heat source pipe 22 to generate the second evaporator refrigerant vapor Ve2. A refrigerant liquid pipe 88 that supplies the refrigerant liquid Vf into the second evaporator can body 67 is connected to the second evaporator can body 67.

In the present embodiment, the second absorber A2 and the second evaporator E2 are arranged adjacent to each other, and the upper part of the second absorber can body 57 and the upper part of the second evaporator can body 67 communicate with each other. ing. With such a configuration, the second evaporator refrigerant vapor Ve2 generated inside the second evaporator can body 67 can be guided to the inside of the second absorber can body 57.

The second regenerator G2 is a device that heats and concentrates the second dilute solution Sw2 produced by the second absorber A2 to regenerate it into the second concentrated solution Sa2, and corresponds to the regenerator. The second regenerator G2 has a heat source tube 71 forming a flow path of the heat source fluid H and a second rare solution spray nozzle 72 for spraying the second rare solution Sw2 inside the second regenerator can body 77. doing. The other end of the second dilute solution tube 58 is connected to the second dilute solution spray nozzle 72. In the present embodiment, the heat source fluid H flowing through the heat source pipe 71 of the second regenerator G2 is the same as the heat source fluid H flowing through the heat source pipe 61 of the second evaporator E2, and after flowing through the heat source pipe 61. It is connected by a heat source fluid connecting pipe 37 so as to flow through the heat source pipe 71. Different heat source media may flow through the heat source tubes 61 and 71. The second rare solution spray nozzle 72 is arranged above the heat source pipe 71 so that the sprayed second rare solution Sw2 falls on the heat source pipe 71. In the second regenerator G2, the sprayed second rare solution Sw2 is heated by the heat source fluid H to generate a second concentrated solution Sa2 in which the refrigerant V evaporates from the second rare solution Sw2 and the concentration increases. To. The second regenerator G2 is configured so that the generated second concentrated solution Sa2 is stored in the lower part. A second concentrated solution tube 78 that guides the generated second concentrated solution Sa2 to the second absorber A2 is connected to the second regenerator G2. One end of the second concentrated solution tube 78 is connected to a portion (typically the bottom) where the second concentrated solution Sa2 is stored in the lower part of the second regenerator can body 77, and the other end is the second concentrated solution. It is connected to the spray nozzle 52. A second concentrated solution pump 79 for pumping the second concentrated solution Sa2 is provided in the second concentrated solution tube 78.

The second condenser C2 has a cooling water pipe 81 forming a flow path for the cooling water Y inside the second condenser can body 87. The second condenser C2 is configured to introduce the regenerator refrigerant vapor Vg, which is the vapor of the refrigerant V generated in the second regenerator G2, cool it with the cooling water Y, and condense it. The cooling water pipe 81 is preferably arranged so that the regenerator refrigerant vapor Vg is not immersed in the condensed refrigerant liquid Vf so that the regenerator refrigerant vapor Vg can be directly cooled. In the present embodiment, the cooling water Y flowing through the cooling water pipe 81 of the second condenser C2 is the same as the cooling water Y flowing through the cooling pipe 11 of the first absorber A1 and the condenser pipe 41 of the first condenser C1. It is configured to flow in parallel with the cooling pipe 11 and the condensing pipe 41. A refrigerant liquid pipe 88 that guides the condensed refrigerant liquid Vf to the second evaporator E2 is connected to the second condenser C2. One end of the refrigerant liquid pipe 88 is connected to a portion (typically the bottom portion) where the refrigerant liquid Vf is stored in the lower part of the second condenser can body 87, and the other end is connected to the second evaporator can body 67. Has been done. A condensed refrigerant pump 89 for pressure-feeding the refrigerant liquid Vf is provided in the refrigerant liquid pipe 88.

The second regenerator G2 and the second condenser C2 communicate with each other. By communicating the second regenerator G2 and the second condenser C2, the regenerator refrigerant vapor Vg generated in the second regenerator G2 can be supplied to the second condenser C2. The second regenerator G2 and the second condenser C2 communicate with each other at the upper gas phase portion. Further, since the second regenerator G2 and the second condenser C2 communicate with each other, the internal pressure is substantially the same. Further, in the present embodiment, the second regenerator G2 and the second condenser C2 are at the same height as the first condenser C1, below the second absorber A2 and the second evaporator E2, and first. It is provided above the absorber A1 and the first evaporator E1.

The gas-liquid separator 90 includes a mixed fluid Sm (the first concentrated solution Sa1 and the separated refrigerant steam Vs) generated by boiling the first rare solution Sw1 heated by passing through the heating tube 15 of the second absorber A2. It is a device that introduces a fluid mixed with) and separates the first concentrated solution Sa1 and the separated refrigerant vapor Vs, and corresponds to a gas-liquid separation part. The separated refrigerant vapor Vs is the vapor of the refrigerant V separated from the first rare solution Sw1. The first concentrated solution Sa1 is an absorbing solution S whose concentration has increased from the first rare solution Sw1 due to the separation of the separated refrigerant vapor Vs. The gas-liquid separator 90 includes a first concentrated solution pipe 91 that guides the first concentrated solution Sa1 to the first absorber A1, a separated refrigerant steam pipe 94 that guides the separated refrigerant steam Vs to the first condenser C1, and a first. The return pipe 95 that guides the concentrated solution Sa1 to the first rare solution pipe 18 in the vicinity of the second absorber A2 and the first absorption liquid pipe 16 after heating that introduces the mixed fluid Sm from the second absorber A2 are connected. There is. The first concentrated solution tube 91 constitutes a first concentrated solution flow path, and one end of the first concentrated solution tube 91 is connected to a portion (typically the bottom portion) in which the first concentrated solution Sa1 is stored in the lower part of the gas-liquid separator 90. The other end is connected to the first concentrated solution spraying nozzle 12. One end of the separated refrigerant vapor pipe 94 is connected to the gas phase portion (typically the top) of the upper part of the gas-liquid separator 90, and the other end is connected to the upper part of the first condenser can body 47. One end of the return pipe 95 is connected to a portion (typically the bottom portion) in the lower part of the gas-liquid separator 90 where the first concentrated solution Sa1 is stored, and the other end is the first rare in the vicinity of the second absorber A2. It is connected to the solution tube 18. After heating, one end of the first absorption liquid pipe 16 is connected to the heating pipe 15 of the second absorber A2, and the other end is connected to the gas phase portion on the side of the gas-liquid separator 90.

The absorption chiller 1 further includes a first heat exchanger 31 and a second heat exchanger 32. The first heat exchanger 31 is a device that exchanges heat between the first rare solution Sw1 flowing through the first rare solution tube 18 and the first concentrated solution Sa1 flowing through the first concentrated solution tube 91. The second heat exchanger 32 is a device that exchanges heat between the second rare solution Sw2 flowing through the second rare solution tube 58 and the second concentrated solution Sa2 flowing through the second concentrated solution tube 78.

The operation of the absorption chiller 1 will be described with reference to FIG. 2 in combination with FIG. FIG. 2 is a Dühring diagram of the absorption chiller 1. In the During 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 absorption liquid (LiBr aqueous solution in the present embodiment). The upward-sloping line represents the isobaric line of the absorbent liquid, and the concentration becomes higher toward the right and lower toward the left. Since the dew point temperature indicated by the vertical axis corresponds to the saturation pressure, in the absorption cycle of the present embodiment in which the vapor of the refrigerant is saturated vapor, the vertical axis represents the main components (absorber, evaporator, regenerator). , Condenser) can also be seen as representing the internal pressure.

The second condenser C2 receives the regenerator refrigerant vapor Vg evaporated by the second regenerator G2, cools it with the cooling water Y flowing through the cooling water pipe 81, and condenses it to obtain the refrigerant liquid Vf. The condensed refrigerant liquid Vf is sent into the second evaporator can body 67 of the second evaporator E2 by the condensed refrigerant pump 89. The refrigerant liquid Vf sent into the second evaporator can body 67 is heated by the heat source fluid H flowing in the heat source pipe 61 under the dew point temperature T2H and evaporates to become the second evaporator refrigerant vapor Ve2. The second evaporator refrigerant vapor Ve2 generated in the second evaporator E2 moves to the second absorber A2 which communicates with the second evaporator E2. As described above, in the absorption chiller 1, the refrigerant liquid Vf to be the second evaporator refrigerant vapor Ve2 supplied to the second absorber A2 is directly heated by the heat of the heat source fluid H.

In the second absorber A2, the second concentrated solution Sa2 is sprayed from the second concentrated solution spray nozzle 52, and the sprayed second concentrated solution Sa2 is moved from the second evaporator E2 to the second evaporator refrigerant vapor Ve2. To absorb. The concentration of the second concentrated solution Sa2 that has absorbed the second evaporator refrigerant vapor Ve2 decreases to become the second rare solution Sw2 (A2a to A2b). In the second absorber A2, endothermic heat is generated when the second concentrated solution Sa2 absorbs the second evaporator refrigerant vapor Ve2. The absorbed heat heats the first rare solution Sw1 flowing through the heating tube 15. The second rare solution Sw2 whose concentration has decreased from the second concentrated solution Sa2 by absorbing the second evaporator refrigerant vapor Ve2 is stored in the lower part of the second absorber can body 57. The stored second rare solution Sw2 flows through the second rare solution tube 58 toward the second regenerator G2 due to gravity and the difference in internal pressure between the second absorber A2 and the second regenerator G2, and exchanges the second heat. The vessel 32 exchanges heat with the second concentrated solution Sa2 to lower the temperature, leading to the second regenerator G2.

The second rare solution Sw2 sent to the second regenerator G2 is sprayed from the second rare solution spray nozzle 72, heated by the heat source fluid H flowing through the heat source tube 71 under the dew point temperature T2L, and sprayed. The refrigerant in the dilute solution Sw2 evaporates to become the second concentrated solution Sa2 (G2a to G2b), which is stored in the lower part of the second regenerator can body 77. On the other hand, the refrigerant V evaporated from the second rare solution Sw2 moves to the second condenser C2 as the regenerator refrigerant vapor Vg. The second concentrated solution Sa2 stored in the lower part of the second regenerator can body 77 is discharged by the second concentrated solution pump 79 via the second concentrated solution pipe 78 to the second concentrated solution spray nozzle 52 of the second absorber A2. Is pumped to. The second concentrated solution Sa2 flowing through the second concentrated solution tube 78 exchanges heat with the second rare solution Sw2 in the second heat exchanger 32, and after the temperature rises, flows into the second absorber A2 and flows into the second concentrated solution A2. It is sprayed from the solution spraying nozzle 52. The second concentrated solution Sa2 returned to the second absorber A2 absorbs the second evaporator refrigerant vapor Ve2, and the same cycle is repeated thereafter.

In parallel with the absorption cycle in the second absorber A2, the second evaporator E2, the second regenerator G2, and the second condenser C2 described above, the following absorption cycle is performed in the first absorber A1 and the like. Is done. The separated refrigerant vapor Vs introduced from the gas-liquid separator 90 to the first condenser C1 via the separated refrigerant vapor pipe 94 is cooled by the cooling water Y flowing through the condenser pipe 41 under the dew point temperature T1H and condensed. It becomes the refrigerant liquid Vf and is stored in the lower part of the first condenser can body 47. The refrigerant liquid Vf in the first condenser can body 47 is introduced into the first evaporator can body 27 via the refrigerant liquid pipe 48.

The refrigerant liquid Vf introduced from the first condenser can body 47 to the first evaporator can body 27 is stored in the lower part of the first evaporator can body 27. The refrigerant liquid Vf in the first evaporator can body 27 flows through the refrigerant liquid pipe 28 by the first refrigerant pump 29 and reaches the refrigerant liquid spray nozzle 22. The refrigerant liquid Vf that has reached the refrigerant liquid spray nozzle 22 is sprayed toward the evaporation pipe 21, obtains the heat of the cold water W flowing through the evaporation pipe 21, and partially evaporates under the dew point temperature T1L, and the first evaporator. It becomes the refrigerant steam Ve1 and is introduced into the first absorber can body 17. The cold water W whose heat has been taken away by the sprayed refrigerant liquid Vf drops in temperature and flows out from the evaporation pipe 21 and is supplied to a place where the cold water W is used, such as an air conditioner. The refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 22 and not evaporated is mixed with the refrigerant liquid Vf introduced from the first condenser can body 47 and stored in the lower part of the first evaporator can body 27.

The first evaporator refrigerant vapor Ve1 generated by the refrigerant liquid Vf taking heat from the cold water W flows into the first absorber can body 17 as described above. In the first absorber A1, the first concentrated solution Sa1 sprayed from the first concentrated solution spraying nozzle 12 toward the cooling pipe 11 absorbs the first evaporator refrigerant vapor Ve1 that has moved from the first evaporator E1. The concentration decreases to become the first dilute solution Sw1 (A1a to A1b). Endothermic heat is generated when the first concentrated solution Sa1 absorbs the first evaporator refrigerant vapor Ve1 in the first absorber can body 17. The generated absorbed heat is removed by the cooling water Y flowing through the cooling pipe 11. The cooling water Y flowing through the cooling pipe 11 takes away the absorbed heat, rises in temperature, flows out to the cooling water connecting pipe 34, and is supplied to the condenser pipe 41 of the first condenser C1. The first rare solution Sw1 generated in the first absorber can body 17 is stored in the first absorber can body 17.

The first dilute solution Sw1 in the first absorber can body 17 flows through the first dilute solution tube 18 by being pumped to the first dilute solution pump 19, and the first concentrated solution Sa1 in the first heat exchanger 31. The temperature rises by exchanging heat with. After that, in the first dilute solution Sw1, the remaining amount of the first concentrated solution Sa1 stored in the lower part of the gas-liquid separator 90 excluding the predetermined amount flowing out to the first concentrated solution tube 91 is returned to the return tube 95. The first dilute solution Sw1 merges with the inflowing first concentrated solution Sa1. The first rare solution Sw1 that has merged with the first concentrated solution Sa1 is introduced into the heating tube 15 in the second absorber A2. As described above, the first rare solution Sw1 introduced into the heating tube 15 in the second absorber A2 is heated by the endothermic heat generated when the second concentrated solution Sa2 absorbs the second evaporator refrigerant vapor Ve2. Will be done. In this way, the first dilute solution Sw1 is directly heated by the absorbed heat generated in the second absorber A2 when flowing through the heating tube 15 without passing through another medium, and thus is directly heated through another medium. It has better thermal efficiency than the conventional case of heating. Further, since the heating for the regeneration of the first rare solution Sw1 is performed in the heating tube 15 provided in the second absorber A2, a regenerator for the regeneration of the first rare solution Sw1 is not separately provided. It is possible to simplify the device configuration and suppress the increase in size of the device.

The first dilute solution Sw1 heated by flowing through the heating tube 15 becomes the first concentrated solution Sa1 in which the refrigerant V is separated and the concentration is increased (15a to 15b). The absorption liquid flowing out of the heating pipe 15 is a mixed fluid Sm of the separated refrigerant vapor Vs, which is the refrigerant V separated from the first rare solution Sw1, and the first concentrated solution Sa1, and is heated and then passed through the first absorption liquid pipe 16. It flows into the gas-liquid separator 90. In the gas-liquid separator 90, the separated refrigerant vapor Vs and the first concentrated solution Sa1 are separated, the separated refrigerant vapor Vs gathers in the upper gas phase portion, and the first concentrated solution Sa1 is stored in the lower part. The separated refrigerant vapor Vs separated by the gas-liquid separator 90 flows into the first condenser C1 via the separated refrigerant vapor pipe 94. On the other hand, in the first concentrated solution Sa1 stored in the lower part of the gas-liquid separator 90, a predetermined amount appropriate for the heat output in the first absorber A1 of the stored first concentrated solution Sa1 is the first concentrated solution tube. It flows through 91 and exchanges heat with the first rare solution Sw1 in the first heat exchanger 31 to lower the temperature before reaching the first concentrated solution spraying nozzle 12. Of the first concentrated solution Sa1 stored in the lower part of the gas-liquid separator 90, the remaining amount excluding the predetermined amount flowing out to the first concentrated solution pipe 91 is the return pipe 95 and a part of the first rare solution pipe. After merging with the first dilute solution Sw1 pumped by the first dilute solution pump 19 via 18, it flows into the heating pipe 15, is heated by the above-mentioned absorption heat, and after heating, the first absorption liquid pipe 16 is It returns to the gas-liquid separator 90 through. That is, the remaining amount of the first concentrated solution Sa1 stored in the lower part of the gas-liquid separator 90 excluding the predetermined amount flowing out to the first concentrated solution tube 91 is the heating tube 15 and the gas-liquid separator 90. Cycle between and. At this time, in the present embodiment, the first concentrated solution Sa1 circulating between the heating tube 15 and the gas-liquid separator 90 has a position head and a density difference between the gas-liquid separator 90 and the gas-liquid separator 90. It circulates naturally by the bubble pump action based on it. In this way, when the first concentrated solution Sa1 is naturally circulated between the gas-liquid separator 90 and the heating tube 15 by the bubble pumping action, the gas-liquid separator 90 is arranged at the uppermost part of the heating tube 15. If installed at a higher position, the bubble pump effect may be strong. After that, the same cycle is repeated.

As described above, according to the absorption chiller 1 according to the present embodiment, the second concentrated solution Sa2 in the second absorber A2, which is higher than the temperature of the introduced heat source fluid H, is the second evaporator. Since the first rare solution Sw1 flowing through the heating tube 15 is heated by the absorbed heat generated when the refrigerant steam Ve2 is absorbed, the cold water W can be produced even at a relatively low temperature of the introduced heat source fluid H. Further, since the first rare solution Sw1 flowing through the heating tube 15 is directly heated by the absorbed heat generated in the second absorber A2, the thermal efficiency is excellent. Further, since the heating for the regeneration of the first rare solution Sw1 is performed in the heating tube 15 provided in the second absorber A2, a regenerator for the regeneration of the first rare solution Sw1 is not separately provided. It is possible to simplify the device configuration and suppress the increase in size of the device.

Next, the absorption chiller 1A according to the first modification of the embodiment of the present invention will be described with reference to FIG. FIG. 3 is a schematic system diagram of the absorption chiller 1A. The absorption chiller 1A differs from the absorption chiller 1 (see FIG. 1) in the following points. The absorption chiller 1A is provided with a common condenser Cs in place of the first condenser C1 and the second condenser C2 in the absorption chiller 1 (see FIG. 1). The common condenser Cs introduces the regenerator refrigerant vapor Vg from the second regenerator G2 and introduces the separated refrigerant vapor Vs from the gas-liquid separator 90, and condenses the introduced refrigerant vapor Vg and Vs to produce the refrigerant liquid Vf. It is a device to generate. The common condenser Cs has a common cooling water pipe 481 forming a flow path of the cooling water Y inside the common condenser can body 487. The other end of the cooling water connecting pipe 34, one end of which is connected to the cooling pipe 11, is connected to one end of the common cooling water pipe 481. The common condenser Cs communicates with the second regenerator G2 at the upper gas phase portion so that the regenerator refrigerant vapor Vg can be introduced from the second regenerator G2. One end of the separated refrigerant vapor pipe 94 is connected to the gas phase portion (typically the top portion) of the upper portion of the common condenser can body 487. One end of the common refrigerant liquid pipe 488 for flowing out the refrigerant liquid Vf is connected to the liquid phase portion (typically the bottom portion) of the lower portion of the common condenser can body 487. At the other end of the common refrigerant liquid pipe 488, a refrigerant liquid pipe 48 that guides the refrigerant liquid Vf to the first evaporator E1 and a refrigerant liquid pipe 88 that guides the refrigerant liquid Vf to the second evaporator can body 67 are connected. There is. A condensed refrigerant pump 89 for pressure-feeding the refrigerant liquid Vf is provided in the refrigerant liquid pipe 88. The configuration of the absorption chiller 1A other than the above is the same as that of the absorption chiller 1 (see FIG. 1). According to the absorption chiller 1A configured as described above, the regenerator refrigerant vapor Vg and the separated refrigerant vapor Vs can be condensed together in the common condenser Cs, and the apparatus configuration can be further simplified. it can.

Next, the absorption chiller 1B according to the second modification of the embodiment of the present invention will be described with reference to FIG. FIG. 4 is a schematic system diagram of the absorption chiller 1B. The absorption chiller 1B is different from the absorption chiller 1 (see FIG. 1) in that the gas-liquid separator 90 is integrally configured with the second absorber A2. In the absorption chiller 1B, the outlet of the heating pipe 15 arranged inside the second absorber can body 57 is directly connected to the gas-liquid separator 90, so that the gas-liquid separator 90 absorbs the second. It is provided in contact with the side wall of the vessel body 57. Therefore, the absorption chiller 1B is not provided with the first absorption liquid pipe 16 (see FIG. 1) after heating, which was provided in the absorption chiller 1 (see FIG. 1). That is, in the absorption chiller 1B, the inlet of the mixed fluid Sm in the gas-liquid separator 90 is arranged adjacent to the outlet of the heating pipe 15, so that the gas-liquid separator 90 and the second absorber can body 57 are arranged. Are integrally configured. In the absorption chiller 1B, the gas-liquid separator 90 can be regarded as having the outlet liquid chamber of the second absorber A2 having a gas-liquid separation function. The configuration of the absorption chiller 1B other than the above is the same as that of the absorption chiller 1 (see FIG. 1). According to the absorption chiller 1B configured as described above, it is not necessary to make the gas-liquid separator 90 a can body independent of the second absorber A2, and it is possible to suppress the increase in size of the apparatus. The internal pressure of the gas-liquid separator 90 is as low as less than the atmospheric pressure like the internal pressure of the second condenser C2 into which the separated refrigerant vapor Vs flows, and the specific volume of the separated refrigerant vapor Vs is relatively large, so that the gas-liquid separator 90 Is likely to become large, but in order to suppress the increase in size, it is advisable to configure as follows.

FIG. 5 is a cross-sectional view of the second absorber A2a according to the modified example. In the second absorber A2a, the heating tube 15 and the second concentrated solution spraying nozzle 52 are housed in the second absorber can body 57, and the liquid chamber forming member 59 is provided outside the second absorber can body 57. It is composed of. The liquid chamber forming member 59 is a general term for a liquid chamber forming member 59A provided at one end of the second absorber can body 57 and a liquid chamber forming member 59B provided at the other end. The liquid chamber forming member 59 is a member that internally forms a liquid chamber for supplying the first dilute solution Sw1 to each heating tube 15 or collecting the first dilute solution Sw1 or the mixed fluid Sm from each heating tube 15. In this modification, the liquid chamber is distinguished by being referred to as an inlet liquid chamber 53, an outlet liquid chamber 55, and a reversing liquid chamber 54 which is a liquid chamber other than these, respectively, according to the function or application for convenience. The second absorber can body 57 is typically formed to be horizontally elongated when installed.

In this modification, a plurality of heating tubes 15 formed in a straight line are provided in the second absorber can body 57. Each heating tube 15 is joined to one end of the horizontally long second absorber can body 57 and the other end on the opposite side thereof. The surface of the second absorber can body 57 to which the heating tube 15 is joined is formed as a tube plate (heating tube plate) having holes through which the heating tube 15 can be inserted. The inside of the heating tube 15 joined to the tube plates at both ends of the second absorber can body 57 does not communicate with the inside of the second absorber can body 57. In other words, the first rare solution Sw1 or the mixed fluid Sm flowing in the heating tube 15 and the fluid flowing in and out of the second absorber can body 57 and existing outside the heating tube 15 (second concentrated solution Sa2 and It is configured so that it does not mix with the second evaporator fluid vapor Ve2).

In this modification, each heating tube 15 is arranged so that its axis is horizontal from the viewpoint of bringing the sprayed second concentrated solution Sa2 into contact with the outer surface of the heating tube 15 as a thin liquid film as much as possible. However, each heating tube 15 is arranged so that the axis line is slanted with an upward gradient within a range in which the second concentrated solution Sa2 wets and spreads on the outer surface to the extent that desired endothermic heat can be obtained. May be good. Of the heating pipes 15 provided in the second absorber can body 57, the heating pipe 15 arranged at the lowermost part in the vertical direction is arranged at a position where a space for storing the second rare solution Sw2 is secured below the heating pipe 15. Has been done. On the other hand, the heating tube 15 arranged at the uppermost portion of the second absorber can body 57 is arranged at a position where a space where the second concentrated solution spraying nozzle 52 can be installed is secured.

The liquid chamber forming member 59 is attached to both sides (tube plate) of the second absorber can body 57 to which the ends of the heating tubes 15 are joined. The liquid chamber forming member 59 is a rectangular parallelepiped member having an open surface, and the opened surface covers one end of a plurality of heating tubes 15 attached to the tube plate of the second absorber can body 57. , It is attached to the tube plate of the second absorber can body 57. By attaching the liquid chamber forming member 59 to the tube plate of the second absorber can body 57, the space surrounded by the liquid chamber forming member 59 and the tube plate of the second absorber can body 57 becomes a liquid chamber. By providing the partition plate 59s inside the liquid chamber forming member 59, the inside of one liquid chamber forming member 59A is divided into an inlet liquid chamber 53, a reversing liquid chamber 54, and an outlet liquid chamber 55, and the other liquid chamber is formed. The inside of the member 59B is divided into a plurality of reversing liquid chambers 54. The liquid chambers 53, 54, and 55 communicate with the inside of each heating tube 15. That is, the first rare solution Sw1 or the mixed fluid Sm flows in and out of the liquid chambers 53, 54, and 55. In each of the liquid chambers 53, 54, 55, one end of a heating pipe 15 through which the first rare solution Sw1 or the mixed fluid Sm flowing into the liquid chambers 53, 54, 55 flows, and / or the liquid chambers 53, 54, One end of the heating tube 15 through which the first rare solution Sw1 or the mixed fluid Sm flowing out from 55 flows is communicated.

In the partition plate 59s, one or two or more heating tubes 15 that allow the first rare solution Sw1 or the mixed fluid Sm to flow in and out of one liquid chamber communicate with different liquid chambers in the opposite liquid chamber. is set up. As a result, the first rare solution Sw1 or the mixed fluid Sm flowing through each heating tube 15 and the liquid chamber flows from the inlet liquid chamber 53 located at the uppermost stream through the heating tube 15 communicating with the inlet liquid chamber 53 in one direction, and flows on the opposite side. In the reversing liquid chamber 54, the direction of the flow is changed and another heating tube 15 communicating with the heating tube 15 flows in the direction opposite to one direction, so that the flow becomes one flow that proceeds while changing the direction as a whole. It is configured to pass through the absorber can body 57. Further, in the partition plate 59s, the first rare solution Sw1 or the mixed fluid Sm flowing as one flow through the heating pipes 15 and the liquid chambers 53, 54, 55 as a whole is downward as a whole in the second absorber can body 57. It is installed to partition the liquid chambers 53, 54, 55 so as to flow upward from the liquid chamber. In the example shown in FIG. 5, the heating tube 15 is configured in 4 passes. Here, the "pass" is a unit of a flow path in which a fluid flowing in a certain heating pipe 15 flows without merging with a fluid in another heating pipe 15.

In this modification, the flow path cross-sectional areas of each of the four paths are configured to be about the same. When the flow path cross-sectional area of each path is about the same, typically, each heating tube 15 has a uniform flow path cross-sectional area over the entire length, and all the heating tubes 15 have the same diameter. The number of heating tubes 15 constituting each path is the same, assuming that the fluids flowing in each heating tube 15 do not split or merge with the fluids in the other heating tubes 15. Although it indicates the degree, even if the diameter and / or the number of the heating tubes 15 differs depending on the path, the flow path cross-sectional area of each path may be the same. With this configuration, the amount of separated refrigerant vapor Vs separated from the first rare solution Sw1 in the mixed fluid Sm increases toward the downstream, and the volumetric flow rate of the mixed fluid Sm increases. Since the flow path cross-sectional areas of the paths are configured to be about the same, the flow velocity of the mixed fluid Sm flowing in the heating pipe 15 becomes faster toward the downstream, and the flow rate of the mixed fluid Sm flowing into each heating pipe 15 becomes uniform. Get closer. As a result, it is possible to suppress a decrease in heat transfer efficiency due to non-uniform flow in each heating tube 15, and also suppress a situation in which the concentration and temperature of the absorbing liquid S locally increase in each pass. It becomes possible to avoid crystallization of the absorption liquid S. It should be noted that the fact that the flow path cross-sectional areas of each pass are about the same includes the case where the area is equal and the ratio of the flow path cross-sectional areas of each pass is within a predetermined range. The ratio of the flow path cross-sectional areas of each path is within a predetermined range when the appearance of the heating pipe 15 in which the first rare solution Sw1 or the mixed fluid Sm does not flow in or the flow rate of the first rare solution Sw1 or the mixed fluid Sm inflowing. It is within the range of the flow path cross-sectional area ratio that can give the first dilute solution Sw1 or the mixed fluid Sm a flow velocity that can avoid the appearance of the heating tube 15 that has a small amount and deteriorates the evaporation performance. As an example of a predetermined range, depending on the conditions, the ratio of the cross-sectional area in the path having the maximum flow path cross-sectional area (maximum cross-sectional area / minimum cross-sectional area) to the cross-sectional area in the path having the minimum flow path cross-sectional area is 1. It may be 5 or less. There is no restriction on the order in which the paths in the flow path cross-sectional area within this ratio range are arranged from upstream to downstream, and there is no relation between the order in which the paths are arranged and the flow path cross-sectional area.

The heating tube 15 may be configured in, for example, 8 passes, 3 passes, or 2 passes other than 4 passes, or may be configured in 1 pass. When it is composed of a plurality of paths, it is preferable that the flow path cross-sectional area of each path is configured to be the same. In the case of one pass, the reversing liquid chamber 54 is omitted and the inlet liquid chamber 53 and the outlet liquid chamber 55 are provided. That is, in one pass, one end of one or two or more heating tubes 15 is connected to the inlet liquid chamber 53 for supplying the first dilute solution Sw1, and the other end is connected to the outlet liquid chamber 55 for collecting the mixed fluid Sm. In other words, the first dilute solution Sw1 that has flowed into the heating tube 15 flows into the outlet liquid chamber 55 after flowing through the heating tube 15, and is inside each of one or more heating tubes 15. It is configured so that the fluid flowing through the water does not split or merge between the inlet liquid chamber 53 and the outlet liquid chamber 55. With such a configuration, the first rare solution Sw1 in a liquid state is supplied from the inlet liquid chamber 53 to each heating tube 15, and the heat transfer efficiency is lowered due to non-uniform flow in the heating tube 15. It is possible to suppress the situation where the concentration and temperature of the absorbing liquid S are locally increased, and to avoid the crystallization of the absorbing liquid S.

The first dilute solution pipe 18 is connected to the inlet liquid chamber 53. The inlet liquid chamber 53 is configured to receive the first rare solution Sw1 from the first dilute solution tube 18 and guide the received first dilute solution Sw1 to the heating tube 15 communicating with the inlet liquid chamber 53. .. The return pipe 95 (see FIG. 4) may be connected to the inlet liquid chamber 53 instead of the first rare solution pipe 18. The reversing liquid chamber 54 is different from the heating pipe 15 introduced by reversing the first rare solution Sw1 or the mixed fluid Sm introduced from the inlet liquid chamber 53 or the reversing liquid chamber 54 on the upstream side via the heating pipe 15. The first dilute solution Sw1 or the mixed fluid Sm is configured to flow out to the heating pipe 15 (the heating pipe 15 communicating with the reversing liquid chamber 54 or the outlet liquid chamber 55 on the downstream side at the other end). The outlet liquid chamber 55 is configured to introduce the mixed fluid Sm from the reversing liquid chamber 54 via the heating pipe 15. In the second absorber A2a, the outlet liquid chamber 55 is configured to function as a gas-liquid separation unit.

The outlet liquid chamber 55 extends upward from the heating pipe 15 at the highest vertical position. In the second absorber A2a, the tube plate of the second absorber can body 57 at the portion forming the outlet liquid chamber 55 extends upward from the top plate of the second absorber can body 57. The upper part of the outlet liquid chamber 55 is a gas phase portion 55g mainly filled with gas, and the lower part is a liquid phase portion 55q filled with liquid. An eliminator 96 is arranged in the gas phase portion 55 g. The eliminator 96 is an elongated member having a shape formed by bending an elongated thin plate at a substantially right angle so that the elongated member extends horizontally in the longitudinal direction (so that a substantially right-angled polygonal line appears in the vertical cross section) and is orthogonal to the longitudinal direction. It is configured by arranging a plurality of them at predetermined intervals in the horizontal direction. The predetermined interval is an interval at which the droplet can be separated by passing the fluid through the eliminator 96 while bending along a substantially right angle. The eliminator 96 is attached so as to cover the entire cross-sectional area of the fluid flow path in the gas phase portion 55 g. A first concentrated solution pipe 91 for flowing out the first concentrated solution Sa1 separated from the mixed fluid Sm is connected to the liquid phase portion 55q of the outlet liquid chamber 55. The return pipe 95 is connected to the liquid phase portion 55q or the first concentrated solution pipe 91. A separated refrigerant vapor pipe 94 for flowing out the separated separated refrigerant vapor Vs is connected to the gas phase portion 55 g on the opposite side of the eliminator 96 from the liquid phase portion 55q. The second absorber A2a having the outlet liquid chamber 55 configured in this way can compactly configure the gas-liquid separation portion that tends to be large. In addition, in order to improve the gas-liquid separation effect in the outlet liquid chamber 55, a plurality of eliminators 96 may be provided in the flow direction of the separated refrigerant vapor Vs.

Next, the second absorber A2b according to another modification will be described with reference to FIG. FIG. 6 is a cross-sectional view of the second absorber A2b. The second absorber A2b is configured such that the outlet liquid chamber 55B extends vertically upward from the partition plate 59s and then extends horizontally so as to cover a part of the top plate of the second absorber can body 57. In that respect, it differs from the second absorber A2a (see FIG. 5). In the example shown in FIG. 6, the horizontally extending portion of the outlet liquid chamber 55B covers approximately 1/3 of the length of the top plate of the second absorber can body 57. In the outlet liquid chamber 55B, at least a portion higher than the top plate of the second absorber can body 57 is a gas phase portion 55 g, and a portion below the gas phase portion 55 g is a liquid phase portion 55q. An eliminator 96B is disposed in the gas phase portion 55g of the upper portion of the top plate of the second absorber can body 57. The eliminator 96B crosses the flow path by extending an elongated member having a shape formed by bending an elongated thin plate at a substantially right angle so that the longitudinal direction extends vertically (so that a substantially right-angled polygonal line appears in a horizontal cross section). It is configured by arranging a plurality of them at predetermined intervals in the horizontal direction. The eliminator 96B is attached so as to cover the entire cross-sectional area of the fluid flow path in the gas phase portion 55 g. The configuration of the second absorber A2b other than the above is the same as that of the second absorber A2a (see FIG. 5). The second absorber A2b having the outlet liquid chamber 55B configured in this way can freely change the cross-sectional area of the eliminator 96B in the height direction without affecting the sizes of the inlet liquid chamber 53 and the reversing liquid chamber 54. Therefore, a large-capacity separation refrigerant vapor Vs can be gas-liquid separated. In the second absorber A2b as well, in order to improve the gas-liquid separation effect, a plurality of eliminators 96B may be provided in the flow direction of the separated refrigerant vapor Vs, and the horizontally extending portion of the outlet liquid chamber 55B may be provided. 2 The length of the top plate of the absorber can body 57 may be changed as appropriate.

Next, with reference to FIG. 7, the second absorber A2c according to still another modification will be described. FIG. 7 is a cross-sectional view of the second absorber A2c. The second absorber A2c differs from the second absorber A2b (see FIG. 6) in the following points. In the outlet liquid chamber 55C of the second absorber A2c, the portion of the gas phase portion 55 g extending in the horizontal direction is not a part of the top plate of the second absorber can body 57, but the top of the second absorber can body 57. It is configured to cover the entire board. A plurality of gas phase partition plates 98 are provided in the gas phase portion 55 g of the outlet liquid chamber 55C. The gas phase partition plate 98 is a flat plate-shaped member that restricts the flow path so that the separated refrigerant vapor Vs flowing inside meanders to the left and right, and corresponds to the flow path limiting member. The upper and lower parts of the gas phase partition plate 98 are in contact with the liquid chamber forming member 59 and the second absorber can body 57, respectively, and one of the left and right is in contact with the liquid chamber forming member 59 and the other is in contact with the liquid chamber forming member 59. It is attached so that a space serving as a flow path is formed between them. The space formed on one of the left and right sides of the gas phase partition plate 98 is provided with the gas phase partition plate 98 so that every other of the plurality of arranged gas phase partition plates 98 is formed alternately on the left and right. ing. The configuration of the second absorber A2c other than the above is the same as that of the second absorber A2b (see FIG. 6). The second absorber A2c having the outlet liquid chamber 55C configured in this way can make the outlet liquid chamber 55C function as a gas-liquid separation unit with a simple configuration. In the second absorber A2c shown in FIG. 7, it was assumed that the horizontally extending portion of the gas phase portion 55 g was configured to cover the entire top plate of the second absorber can body 57, but it was separated. It may be shorter than the total length of the top plate of the second absorber can body 57 as long as the gas-liquid separation of the refrigerant vapor Vs can be appropriately performed. Further, a portion of the gas phase portion 55g extending in the horizontal direction may be provided along the upper side wall instead of the top plate of the second absorber can body 57. Further, the portion of the gas phase portion 55g extending in the horizontal direction may have an upslope. Further, in the second absorber A2c shown in FIG. 7, the eliminator is not provided in the gas phase portion 55 g, but the eliminator 96B (see FIG. 6) may be combined.

Next, the absorption chiller 1C according to the third modification of the embodiment of the present invention will be described with reference to FIG. FIG. 8 is a schematic system diagram of the absorption chiller 1C. The absorption chiller 1C is different in that the second absorber A2 and the second evaporator E2, which were single-stage in the absorption chiller 1 (see FIG. 1), are of the two-stage temperature rise type. That is, in the absorption chiller 1C, the second absorber A2 and the second evaporator E2 in the absorption chiller 1 shown in FIG. 1 are the second high temperature absorber A2H and the second high temperature evaporator E2H on the high temperature side. It is divided into a second low temperature absorber A2L and a second low temperature evaporator E2L on the low temperature side. At this time, the second high temperature absorber A2H corresponds to the second absorber, the second high temperature evaporator E2H corresponds to the second high temperature evaporator, and the second low temperature absorber A2L becomes the second low temperature absorber. The second low temperature evaporator E2L corresponds to the second evaporator. The second high temperature absorber A2H has a higher internal pressure than the second low temperature absorber A2L, and the second high temperature evaporator E2H has a higher internal pressure than the second low temperature evaporator E2L. The second high-temperature absorber A2H and the second high-temperature evaporator E2H communicate with each other at the upper part so that the vapor of the refrigerant V of the second high-temperature evaporator E2H can be moved to the second high-temperature absorber A2H. The second low temperature absorber A2L and the second low temperature evaporator E2L communicate with each other at the upper part so that the vapor of the refrigerant V of the second low temperature evaporator E2L can be moved to the second low temperature absorber A2L. Further, in the absorption chiller 1C, the refrigerant liquid pipe 88 in which the condensed refrigerant pump 89 in the absorption chiller 1 (see FIG. 1) is arranged is arranged with the high temperature condensed refrigerant pump 89H that leads to the system of the second high temperature evaporator E2H. It is divided into a high-temperature refrigerant liquid pipe 88H provided and a low-temperature refrigerant liquid pipe 88L in which a low-temperature condensing refrigerant pump 89L leading to the system of the second low-temperature evaporator E2L is arranged. The first dilute solution Sw1 introduced from the first absorber A1 is heated by the second high temperature absorber A2H. The heat source fluid H is introduced into the second low temperature evaporator E2L. The second low temperature absorber A2L is the heat absorbed when the second absorption liquid S2 introduced from the second high temperature absorber A2H absorbs the vapor of the refrigerant V that has moved from the second low temperature evaporator E2L, and is the second high temperature. The refrigerant solution Vf in the evaporator E2H is heated to generate vapor of the refrigerant V in the second high temperature evaporator E2H, and the generated vapor of the refrigerant V in the second high temperature evaporator E2H is the second high temperature absorber A2H. The first rare solution Sw1 is heated by the heat of absorption when it moves to and is absorbed by the second concentrated solution Sa2 in the second high temperature absorber A2H. That is, when the second absorber A2 and the second evaporator E2 are in multiple stages, the heat of the heat source fluid H generates a refrigerant liquid that becomes the refrigerant vapor supplied to the second high temperature absorber A2H (second absorber). The generated refrigerant vapor is absorbed by the absorbing liquid and is indirectly heated by the heat of the heat source fluid H through the absorbed heat generated. In the absorption chiller 1C, the configurations around the second absorbers A2a, A2b, and A2c shown in FIGS. 5 to 7 are typically applied to the second high temperature absorber A2H. Even when the second absorber A2 and the second evaporator E2 have three or more stages, the configuration around the second absorbers A2a, A2b, and A2c shown in FIGS. 5 to 7 typically has an internal temperature. And it is applied to the second absorber with the highest internal pressure. However, in the absorption chiller 1C, in addition to the first rare solution Sw1, the refrigerant V flowing in the heat transfer tube (heating tube) in the second low temperature absorber A2L also corresponds to the fluid to be heated.

In the above description, it is assumed that the second evaporator E2 and the second low temperature evaporator E2L are full-liquid type, but they may be spray type. When the second evaporator E2 and / or the second low temperature evaporator E2L is a spray type, the refrigerant liquid Vf is sprayed on the upper part of the second evaporator can body 67 and / or the second low temperature evaporator E2L. Refrigerant liquid pipe 88 and / or refrigerant liquid pipe which was provided with a refrigerant liquid spray nozzle and was connected to the lower part of the can body of the second evaporator can body 67 and / or the second low temperature evaporator E2L in the case of the full liquid type. The end of 88L may be connected to the refrigerant liquid spraying nozzle. Further, a pipe and a pump may be provided to supply the refrigerant liquid Vf at the lower part of the can body of the second evaporator can body 67 and / or the second low temperature evaporator E2L to the refrigerant liquid spray nozzle.

In the above description, a predetermined amount of the first concentrated solution Sa1 stored in the lower part of the gas-liquid separator 90 flows out to the first concentrated solution pipe 91, and the remaining amount is the return pipe 95, a part of the first concentration. It was decided to spontaneously circulate between the heating tube 15 and the gas-liquid separator 90 via the 1 rare solution tube 18 and the first absorbing solution tube 16 after heating by the bubble pumping action, but the partial system diagram of FIG. 9 shows. As shown, a circulation pump 99 may be provided in the first rare solution pipe 18 on the downstream side of the confluence with the return pipe 95 to forcibly circulate the solution. The circulation pump 99 is a pump that pushes the first rare solution Sw1 (first absorption liquid S1) that has merged with the first concentrated solution Sa1 into the heating pipe 15, and corresponds to the first absorption liquid pump. When the first absorption liquid S1 is pushed into the heating pipe 15 by the circulation pump 99, the flow rate of the first absorption liquid S1 in the heating pipe 15 can be increased and stabilized, and the flow in the heating pipe 15 can be increased. It is possible to suppress a decrease in heat transfer efficiency due to non-uniformity and the like, and it is possible to suppress a situation in which the concentration and temperature of the first absorption liquid S1 are locally increased, so that the crystals of the first absorption liquid S1 can be suppressed. It is possible to improve the heat transfer efficiency of the absorbed heat to the first absorbing liquid S1 by avoiding the formation. Further, when a throttle portion such as an orifice or a valve is provided at the inlet of the first absorption liquid S1 of the gas-liquid separator 90 in addition to the circulation pump 99, the pressure of the first absorption liquid S1 in the heating pipe 15 is increased. Since the boiling of the first absorbing liquid S1 in the heating pipe 15 can be suppressed and the evaporation of the refrigerant V in the heating pipe 15 can be suppressed, the change in the concentration of the first absorbing liquid S1 in the heating pipe 15 can be changed. Without it, the first absorption liquid S1 can be heated as it is, and the heat transfer action can be stabilized. The pressurized first absorption liquid S1 is heated by the absorption heat to a high temperature, is depressurized in the gas-liquid separator 90, generates separated refrigerant vapor Vs, and becomes the first concentrated solution Sa1.

1, 1A, 1B, 1C Absorption Refrigerator 15 Heating tube 55 Outlet liquid chamber 55g Gas phase part 55q Liquid phase part 57 Second absorber can body 90 Gas-liquid separator 91 First concentrated solution tube 96, 96B Eliminator 98 Gas phase Partition plate 99 Circulation pump A1 1st absorber A2, A2a, A2b, A2c 2nd absorber A2L 2nd low temperature absorber Cs Common condenser E1 1st evaporator E2 2nd evaporator E2H 2nd high temperature evaporator G2 2nd 2 Regenerator H Heat source fluid Sa1 1st concentrated solution Sa2 2nd concentrated solution Sw1 1st rare solution Sw2 2nd rare solution Vf refrigerant liquid Ve1 1st evaporator refrigerant steam Ve2 2nd evaporator refrigerant steam Vg regenerator refrigerant steam Vs separation Solution steam W cold water

Claims (9)

With the first evaporator that cools the cooling target fluid by removing the latent evaporation heat required when the refrigerant liquid evaporates to become refrigerant vapor from the cooling target fluid;
With the first absorber that introduces the refrigerant vapor generated in the first evaporator and absorbs it in the first absorbing liquid;
A second absorber provided with a first absorption liquid flow path for flowing the first absorption liquid whose concentration has decreased due to absorption of the refrigerant vapor in the first absorber. With the second absorber that heats the first absorption liquid flowing through the first absorption liquid flow path by the absorption heat released when the absorption liquid of 2 absorbs the vapor of the refrigerant;
A heat source fluid that directly or indirectly heats the liquid of the refrigerant for generating the vapor of the refrigerant supplied to the second absorber is introduced, and the liquid of the refrigerant is the heat possessed by the introduced heat source fluid. With a second evaporator that heats to produce refrigerant vapor;
The refrigerant separated from the first absorption liquid produced by heating the first absorption liquid in the second absorber and the first absorption in which the refrigerant is separated and the concentration is increased. A gas-liquid separator that separates the liquid and the liquid;
It is provided with a first concentrated solution flow path that guides the first absorbent liquid having an increased concentration generated in the gas-liquid separation unit to the first absorber;
Absorption chiller. By introducing the second absorption liquid whose concentration has decreased due to the absorption of the vapor of the refrigerant in the second absorber, and heating the introduced second absorption liquid with the heat possessed by the heat source fluid. With a regenerator that separates the refrigerant from the second absorption fluid to increase the concentration of the second absorption fluid;
In the regenerator, the vapor of the refrigerant separated from the second absorption liquid and the vapor of the refrigerant generated in the gas-liquid separation unit are introduced, and the vapor of the introduced refrigerant is condensed to produce the refrigerant liquid. Equipped with a common condenser to produce;
The absorption chiller according to claim 1. The second absorber has a plurality of heating tubes constituting the first absorption liquid flow path;
It is provided with a reversing liquid chamber that guides the first absorbing liquid that has flowed inside the heating tube to the other heating tube so as to flow in the opposite direction inside the other heating tube;
The plurality of heating tubes are composed of a plurality of paths by the reversing liquid chamber;
Each of the plurality of paths was configured to have a similar channel cross-sectional area;
The absorption chiller according to claim 1 or 2. The second absorber has one or more heating tubes constituting the first absorbent flow path;
An inlet liquid chamber that communicates with one or a plurality of the heating pipes and supplies the first absorbing liquid to the communicating heating pipes;
It is provided with an outlet liquid chamber that communicates with one or a plurality of the heating pipes and collects all the first absorbing liquids supplied from the inlet liquid chamber to the heating pipe after flowing through the heating pipe. ;
The absorption chiller according to claim 1 or 2. A first absorbent pump for pushing the first absorbent introduced into the second absorber into the first absorbent flow path;
The absorption chiller according to any one of claims 1 to 4. The gas-liquid separation unit is integrally configured with the second absorber by arranging the inlet of the first absorbing liquid adjacent to the outlet of the first absorbing liquid flow path;
The absorption chiller according to any one of claims 1 to 5. A liquid phase portion provided along the can body of the second absorber and temporarily storing the first absorbent liquid that has flowed through the first absorbent liquid flow path, and a liquid phase portion that is separated from the first absorbent liquid. It is provided with an outlet liquid chamber having a gas phase portion through which the refrigerant vapor passes;
The outlet liquid chamber is provided with an eliminator in the gas phase portion and is configured to function as the gas-liquid separation portion;
The absorption chiller according to claim 6. A liquid phase portion provided along the can body of the second absorber and temporarily storing the first absorbent liquid that has flowed through the first absorbent liquid flow path, and a liquid phase portion that is separated from the first absorbent liquid. It is provided with an outlet liquid chamber having a gas phase portion through which the refrigerant vapor passes;
The outlet liquid chamber is configured such that the gas phase portion extends horizontally, and the flow path limiting member that limits the flow path so as to meander the refrigerant vapor flowing through the gas phase portion to the left and right is the gas phase. A plurality of parts are provided in the space of the part, and are configured to function as the gas-liquid separation part;
The absorption chiller according to claim 6. With a second high temperature evaporator that produces the vapor of the refrigerant supplied to the second absorber;
A second low temperature that heats the refrigerant of the second high temperature evaporator by the absorbed heat released when the second absorbing liquid introduced directly or indirectly from the second absorber absorbs the vapor of the refrigerant. Equipped with an absorber;
The absorption chiller according to any one of claims 1 to 8.

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