JP7080001B2 - Absorption chiller - Google Patents

Description

The present invention relates to an absorption chiller including a plurality of sets of evaporators and absorbers, in which the absorber on the low pressure side is cooled by the evaporator on the high pressure side.

An absorption chiller equipped with two sets of evaporators and an absorber can utilize a low temperature heat source more than an absorption chiller equipped with one set of an evaporator and an absorber. On the other hand, since two sets of a combination of an evaporator and an absorber are required, the external dimensions of the absorption chiller become large, and the miniaturization of the apparatus becomes an issue. In the absorption chiller described in JP-A-2008-95976 (Patent Document 1), the low pressure on the low pressure side of the combination of two sets of evaporators and absorbers having different pressure levels in order to reduce the size of the apparatus. The absorber and the high-pressure evaporator on the high-pressure side are composed of vertical tubes (heat transfer tubes arranged vertically), the outer surface of the vertical tube is the low-pressure absorber, the inner surface of the tube is the high-pressure evaporator, and the low-pressure absorber and high-pressure evaporator are. It is a flow-down liquid film type heat exchanger. In the absorption chiller of Patent Document 1, the solution from the high-pressure regenerator passes through the high-temperature heat exchanger, merges with the solution from the low-pressure regenerator, and then circulates in the order of the high-pressure absorber and the low-pressure absorber. That is, the amount of solution sprayed into the high-pressure absorber and the low-pressure absorber is slightly larger in the low-pressure absorber because the solution after absorbing the refrigerant vapor from the high-pressure evaporator flows into the low-pressure absorber. , High pressure absorber and low pressure absorber are almost the same.

Further, in the absorption chiller described in JP-A-2001-317835 (Patent Document 2), the solution from the high-pressure regenerator passes through the high-temperature heat exchanger and then merges with the solution from the low-pressure regenerator, and the solution pump is used. After boosting the pressure and passing through the medium-temperature heat exchanger, it branches and circulates to the high-pressure absorber on one side and the low-pressure absorber on the other side.

Japanese Unexamined Patent Publication No. 2008-95976 Japanese Unexamined Patent Publication No. 2001-317835

In an absorption chiller consisting of a low-pressure absorber and a high-pressure evaporator, in order to obtain sufficient performance, it is effective to wet the heat transfer surface of the low-pressure absorber and high-pressure evaporator with a vertical tube and exchange heat. Maximizing the heat transfer surface is important. In the case of a conventional horizontal tube group in which a plurality of heat transfer tubes are horizontally arranged, the solution sprayed on the upper part of the horizontal tube group can be allowed to flow down to the adjacent heat transfer tubes while moving to each other outside the heat transfer tubes. Because it can be done, it is easy to get the heat transfer surface wet.

On the other hand, in the case of a vertical tube, it is necessary to wet the heat transfer surface with the solution supplied to each vertical tube, but since it cannot be moved to the adjacent heat transfer tube, the supplied solution flows down almost linearly. It will be. Therefore, in order to increase the wet heat transfer surface and maximize the effective heat transfer area that can contribute to heat exchange, it is an effective means to increase the amount of solution supplied to each vertical tube.

That is, the amount of solution spray required to sufficiently wet the heat transfer surface of the horizontal tube group and the heat transfer surface of the vertical tube is different, and the vertical tube requires a larger amount of solution spray than the horizontal tube group.

In the technique of Patent Document 1, since the solution is circulated in the order of the high pressure absorber and the low pressure absorber, the amount of solution sprayed by the high pressure absorber and the low pressure absorber is almost the same, so that the vertical tube is used. The heat transfer surface of the low pressure absorber cannot be sufficiently wetted.

On the other hand, in the technique of Patent Document 2, a solution obtained by merging a solution from a high-pressure regenerator and a solution from a low-pressure regenerator is branched and distributed to a high-pressure absorber and a low-pressure absorber for circulation. Patent Document 2 describes a configuration in which a spraying device is provided on the upper part of both the high-pressure absorber and the low-pressure absorber, the heat transfer medium flows inside the heat transfer tube, and the solution flows down outside the heat transfer tube. It can be presumed that both the spirit level and the low-pressure absorber are composed of a group of horizontal tubes. That is, the low-pressure absorber of Patent Document 2 has a configuration different from that of the vertical tube, and the technique of Patent Document 2 cannot cope with the vertical tube.

Therefore, it is an object of the present invention that the amount of solution sprayed by the low pressure absorber can be increased more than that of the high pressure absorber, the wet heat transfer surface of the vertical tube through which the solution flows can be increased, and the effective heat transfer can contribute to heat exchange. It is to provide an absorption chiller capable of maximizing the heat area.

In order to achieve the above object, the absorption chiller according to one embodiment of the present invention includes a low pressure evaporator, a low pressure absorber, a high pressure evaporator, a high pressure absorber, a condenser, a regenerator, a refrigerant pump, and a solution pump. The low-pressure absorber and the high-pressure evaporator have heat transfer tubes extending substantially vertically, the inside of each heat transfer tube constitutes the high-pressure evaporator, and the outside of each heat transfer tube constitutes the low-pressure absorber. The solution pipe connected to the regenerator and for sending the solution concentrated in the regenerator to the high-pressure absorber and the low-pressure absorber has a branch portion, and the solution is transferred from the branch portion to the high-pressure absorber. It is branched into a solution pipe for sending and a solution pipe for sending the solution to the low pressure absorber.

According to the present invention, the amount of solution sprayed by the low pressure absorber can be increased as compared with the high pressure absorber, the wet heat transfer surface of the vertical tube through which the solution flows can be increased, and the effective heat transfer area can contribute to heat exchange. It is possible to provide an absorption chiller that can maximize the heat.

It is a cycle system diagram of the absorption chiller which concerns on 1st Embodiment. The graph which shows the performance characteristic of the flow-down liquid film type regenerator. It is a cycle system diagram of the absorption chiller which concerns on 2nd Embodiment.

Hereinafter, embodiments of the present invention will be described with reference to the drawings. In each figure, the parts with the same reference numerals indicate the same or corresponding parts.

1st Embodiment FIG. 1 is a cycle system diagram of the absorption chiller 100 according to the first embodiment of the present invention.

The absorption chiller 100 includes a regenerator 1, a condenser 4, a high pressure absorber 6, a high pressure evaporator 16, a low pressure absorber 15, a low pressure evaporator 18, a solution heat exchanger 26, 27, a refrigerant pump 21, 22, and a solution. It is equipped with pumps 23, 24, 25 and the like. In the figure, A indicates a branching portion of the solution, and B indicates a merging portion of the solution.

A plurality of horizontally arranged heat transfer tubes 3 are provided inside the regenerator 1, and a solution spraying device 2 is arranged above the heat transfer tubes 3. The regenerator 1 is a flowing liquid film type heat exchanger. Inside the condenser 4, a plurality of horizontally arranged heat transfer tubes 5 are provided. The regenerator 1 and the condenser 4 communicate with each other through a steam passage 28. A solution pipe 29 is connected to the bottom of the regenerator 1. The solution pipe 29 extends to the branch portion A via the solution pump 25 and the solution heat exchanger 27. A solution pipe 30 is connected to one side of the branch portion A, and a solution pipe 31 is connected to the other side. The solution pipe 30 is connected to a solution spraying device 7 provided on the upper part of the high pressure absorber 6. The solution pipe 30 is provided with a flow rate adjusting valve 39. The solution pipe 31 is connected to the solution spraying device 12 provided on the upper part of the low pressure absorber 15 via the solution heat exchanger 26. By the flow control valve 39, the pressure loss of the solution flowing through the solution pipe 30 from the branch portion A to the high pressure absorber 6 is set to be larger than the pressure loss of the solution flowing through the solution pipe 31 from the branch portion A to the low pressure absorber 15. To. The heat transfer tube 3 does not have to be exactly horizontal as long as it can exhibit its function, and may be substantially horizontal (substantially horizontal).

Inside the high-voltage absorber 6, a plurality of horizontally arranged heat transfer tubes 8 are provided. A solution pipe 33 is connected to the bottom of the high pressure absorber 6. The solution pipe 33 extends to the confluence portion B via the solution pump 24.

The low-pressure absorber 15 and the high-pressure evaporator 16 are integrally configured, and the internal space of each is divided by pipe plates 10, 11, partition walls 40, and the like. A plurality of vertically arranged vertical tubes (heat transfer tubes) 14 groups are supported by the tube plates 10 and 11. The upper end and the lower end of each vertical tube 14 are supported by the tube plates 10 and 11, the inside of each vertical tube 14 communicates with the inside of the high pressure evaporator 16, and the outside (outer peripheral surface) of each vertical tube 14 is. It is located in the low pressure absorber 15. Note that vertical means perpendicular to the horizontal plane, that is, vertical. Further, as long as the function as the heat transfer tube 14 can be exhibited, it does not have to be exactly vertical, and it may be substantially vertical (substantially vertical).

The low pressure absorber 15 is provided with a solution spraying device 12 through which the vertical tubes 14 penetrate, with the outside of the plurality of vertical tubes 14 serving as a heat transfer surface. A solution pipe 34 is connected to the bottom of the low pressure absorber 15. The solution pipe 34 extends to the confluence portion B via the solution pump 23 and the solution heat exchanger 26. At the confluence B, the solution pipes 32, 33, and 34 are connected to each other. The solution pipe 32 extends from the confluence portion B to the regenerator 1 via the solution heat exchanger 27, and is connected to the solution spraying device 2 provided above the regenerator 1.

The high-pressure evaporator 16 has a configuration in which the inside of a plurality of vertical tubes 14 serves as a heat transfer surface, the upper and lower sides of the vertical tubes 14 are opened inside, and the high-pressure absorber 6 and the gas phase portion communicate with each other via the eliminator 9. ing. A refrigerant pipe 35 is connected to the high-pressure evaporator 16. A refrigerant pipe 37 and a communication pipe 38 are connected to the bottom of the high-pressure evaporator 16. The refrigerant pipe 37 extends to the upper part of the high-pressure evaporator 16 via the refrigerant pump 22 and is connected to the refrigerant spraying device 17 of the high-pressure evaporator 16. The communication pipe 38 extends to the bottom of the low pressure evaporator 18.

A plurality of horizontally arranged heat transfer tubes 20 are provided inside the low-pressure evaporator 18, a refrigerant spraying device 19 is arranged at the upper part, and the low-pressure absorber 15 and the gas phase portion communicate with each other via the eliminator 13. ing. A communication pipe 38 and a refrigerant pipe 36 are connected to the bottom of the low-pressure evaporator 18. The refrigerant pipe 36 extends to the upper part of the low-pressure evaporator 18 via the refrigerant pump 21 and is connected to the refrigerant spraying device 19 of the low-pressure evaporator 18. In the present embodiment, the refrigerant is, for example, water, and the solution is, for example, an aqueous solution of lithium bromide.

The operation of the absorption chiller 100 configured in this way is as follows.

The solution sprayed from the solution spraying device 2 of the regenerator 1 is heated by a heating medium flowing inside the heat transfer tube 3 while flowing down the outside of the heat transfer tube 3, generates refrigerant vapor, and the solution is concentrated. The concentrated solution is sent to the solution heat exchanger 27 by the solution pump 25 in the solution pipe 29, exchanges heat with the solution flowing in the solution pipe 32, is cooled, and then branches at the branch portion A. One of the solutions branched at the branch portion A flows through the solution pipe 30 and is sent to the solution spraying device 7 of the high pressure absorber 6, and the other flows through the solution pipe 31 and is sent to the solution heat exchanger 26 and has a low pressure. It exchanges heat with the solution from the absorber 15, is cooled, and is sent to the solution spraying device 12 of the low pressure absorber 15. The pressure loss of the solution flowing through the solution pipe 30 from the branch portion A to the high pressure absorber 6 is set to be larger than the pressure loss of the solution flowing through the solution pipe 31 from the branch portion A to the low pressure absorber 15. As a result, the amount of the solution flowing through the solution pipe 31 becomes larger than the amount of the solution flowing through the solution pipe 30.

The solution sprayed from the solution spraying device 7 in the high-pressure absorber 6 absorbs the refrigerant vapor from the high-pressure evaporator 16 while flowing down the outside of the heat transfer tube 8, and the concentration becomes thin. The absorbed heat generated by the absorption of the refrigerant is cooled by the cooling water flowing in the heat transfer tube 8. The solution whose concentration has been reduced by absorbing the refrigerant vapor is temporarily stored in the lower part of the high pressure absorber 6, flows through the solution pipe 33, and is sent to the confluence portion B by the solution pump 24.

In the low pressure absorber 15, the solution from the solution spraying device 12 is supplied to the outer surface of the vertical tube 14. The solution absorbs the refrigerant vapor from the low pressure evaporator 18 while flowing down the outer surface of the vertical pipe 14. The absorbed heat generated by the refrigerant absorption is used for heating the refrigerant of the high-pressure evaporator 16 flowing down in the vertical pipe 14. The solution that has absorbed the refrigerant vapor and whose concentration has become thin is temporarily stored in the lower part of the low pressure absorber 15, sent to the solution heat exchanger 26 by the solution pump 23 in the solution pipe 34, and is absorbed by the low pressure from the branch portion A. It exchanges heat with the solution in the solution pipe 31 sent to the vessel 15, raises the temperature, and is sent to the confluence portion B. In the merging section B, the solutions from the high-pressure absorber 6 and the low-pressure absorber 15 merge, and the solution heat exchanger 27 exchanges heat with the solution from the regenerator 1 to raise the temperature, and then the solution spraying device of the regenerator 1 Sent to 2.

On the other hand, the refrigerant vapor generated in the regenerator 1 is sent to the condenser 4 through the steam passage 28, cooled by the cooling water flowing in the tube of the heat transfer tube 5, and condensed and liquefied on the outer surface of the heat transfer tube 5. The condensed refrigerant liquid is guided from the bottom of the condenser 4 to the high-pressure evaporator 16 through the refrigerant pipe 35.

A part of the refrigerant liquid stored in the lower part of the high-pressure evaporator 16 flows through the communication pipe 38 and is sent to the low-pressure evaporator 18, and the rest is sent to the refrigerant spraying device 17 in the upper part of the high-pressure evaporator 16 by the refrigerant pump 22.

The refrigerant liquid sprayed from the refrigerant spraying device 17 flows down the inner surface of the pipe from the opening at the upper part of the vertical pipe 14, and is heated and evaporated by the absorption heat from the solution of the low pressure absorber 15 flowing down the outside of the pipe. The evaporated refrigerant vapor is sent from the upper and lower openings of the vertical pipe 14 to the high pressure absorber 6 through the eliminator 9. The refrigerant liquid that could not be completely evaporated on the inner surface of the vertical pipe 14 is stored in the lower part of the high pressure evaporator 16.

Further, the refrigerant liquid sent from the high-pressure evaporator 16 to the low-pressure evaporator 18 through the communication pipe 38 is sent to the refrigerant spraying device 19 above the low-pressure evaporator 18 by the refrigerant pump 21 in the refrigerant pipe 36.

The refrigerant liquid of the refrigerant spraying device 19 is sprayed to the outside of the heat transfer tube 20, takes heat from the cold water flowing in the heat transfer tube 20, evaporates, and is sent to the low pressure absorber 15 through the eliminator 13. The refrigerant liquid that could not be completely evaporated on the heat transfer tube 20 is stored in the lower part of the low pressure evaporator 18.

As described above, in the absorption chiller 100 according to the present embodiment, the absorption heat of the solution absorbed by the refrigerant vapor on the outer surface of the vertically installed vertical pipe 14 flows down the inner surface of the vertical pipe 14. Since the liquid is directly cooled by the latent heat of evaporation, the heat loss between the low pressure absorber 15 and the high pressure evaporator 16 can be reduced, which can contribute to the miniaturization of the apparatus.

According to the absorption chiller 100, the low-pressure absorber 15 and the high-pressure evaporator 16 have a plurality of vertically extending vertical tubes (heat transfer tubes) 14, and the inside of each vertical tube 14 constitutes the high-pressure evaporator 16. The outside of each vertical tube 14 constitutes the low pressure absorber 15. The solution pipe 29 connected to the regenerator 1 and for sending the solution concentrated in the regenerator 1 to the high-pressure absorber 6 and the low-pressure absorber 15 has a branch portion A, and the high-pressure absorber 6 is connected to the branch portion A. The solution pipe 30 for sending the solution to the low pressure absorber 15 and the solution pipe 31 for sending the solution to the low pressure absorber 15 are branched.

According to such a configuration, the inflow amount of the solution into the low pressure absorber 15 can be increased as compared with the high pressure absorber 6. In the low pressure absorber 15 composed of the vertical pipes 14, the adjacent vertical pipes 14 cannot move to each other, so that the solution supplied to each vertical pipe 14 flows down the heat transfer surface substantially linearly. Become. Therefore, with such a configuration, the amount of solution supplied to each vertical tube 14 (liquid film flow rate) can be increased, the heat transfer surface can be wetted, and the effective heat transfer area can be maximized.

Further, the solution pipe 30 for sending the solution from the branch portion A to the high pressure absorber 6 is provided with a flow rate adjusting valve 39 as a flow rate adjusting means. The pressure loss of the solution from the branch portion A to the high pressure absorber 6 can be easily made larger than the pressure loss of the solution from the branch portion A to the low pressure absorber 15, and the pressure loss from the high pressure absorber 6 to the low pressure absorber 15 can be easily increased. The inflow of the solution can be increased. Further, since the amount of solution circulation to the high-pressure absorber 6 and the low-pressure absorber 15 can be arbitrarily adjusted, it is possible to arrange the equipment with a degree of freedom. The flow rate adjusting means capable of making the pressure loss of the solution from the branch portion A to the high pressure absorber 6 larger than the pressure loss of the solution from the branch portion A to the low pressure absorber 15 is limited to the flow rate adjusting valve 39. However, it may be an orifice or other means.

Further, the solution heat exchange on the high temperature side that exchanges heat between the solution pipe 29 for sending the solution from the regenerator 1 to the branch portion A and the solution pipe 32 for sending the solution from the low pressure absorber 15 to the regenerator 1. On the low temperature side, heat exchange is performed between the vessel 27, the solution pipe 31 for sending the solution from the branch portion A to the low pressure absorber 15, and the solution pipe 34 for sending the solution from the low pressure absorber 15 to the regenerator 1. A solution heat exchanger is further provided, and the branch portion A is located between the solution heat exchanger 27 on the high temperature side and the solution heat exchanger 26 on the low temperature side. As a result, it is possible to supply a solution amount suitable for the high-pressure absorber 6 in which the heat transfer tube 8 is horizontally arranged and the low-pressure absorber 15 in which the heat transfer tube 14 is vertically arranged. It is possible to efficiently absorb the refrigerant vapor.

Further, in the solution pipes 32 and 34 for sending the solution from the low pressure absorber 15 to the regenerator 1, a solution pump 23 is provided between the low pressure absorber 15 and the solution heat exchanger 26 on the low temperature side, and the low temperature side is provided. A solution pipe 33 extending from the high-pressure absorber 6 and provided with a solution pump 24 is provided between the solution heat exchanger 26 and the solution heat exchanger 27 on the high temperature side. It is connected.

As a result, in the confluence portion B, the solution from the high pressure absorber 6 is pressurized by the solution pump 24 to prevent backflow, and the solution from the low pressure absorber 15 is heated by the solution heat exchanger 26 to increase the pressure. It can prevent self-evaporation caused by the temperature difference of the solution from the absorber 6 and can operate without disturbing the circulation of the solution.

Further, the regenerator 1 has a plurality of horizontally arranged heat transfer tubes 3, and is configured such that the solution guided to the regenerator 1 flows out of the heat transfer tube 3 in a flow-down liquid film system. FIG. 2 is a diagram showing the relationship between the flow rate of solution spraying in the regenerator 1 as a flowing liquid film type heat exchanger and the heat transfer coefficient outside the tube of the heat transfer tube 3. The horizontal axis shows the flow rate of solution spraying, and the vertical axis shows the heat transfer coefficient outside the heat transfer tube. As shown in FIG. 2, when the solution spray flow rate is increased, the thermal conductivity outside the tube increases.

In the present embodiment, the amount of solution flowing into the regenerator 1 is the amount obtained by merging the solutions from the high-pressure absorber 6 and the low-pressure absorber 15. That is, the amount of solution flowing into the regenerator 1 can be made larger than that in the case where the high-pressure absorber 6 and the low-pressure absorber 15 flow in this order as in Patent Document 1. When the regenerator 1 is a heat transfer tube 3 in which the regenerator 1 is horizontally arranged and the solution exchanges heat outside the heat transfer tube 3 by a flowing liquid film type as in the present embodiment, as shown in FIG. 2, the solution spraying amount is proportional to the increase. The heat transfer coefficient outside the tube can be improved. Therefore, in the present embodiment, the solution inflow amount can be set to be suitable for the vertical tube 14 of the low pressure absorber 15 and the heat transfer tube 8 horizontally arranged in the high pressure absorber 6, and the solution inflow amount to the regenerator 1 can be set. By increasing the amount, the heat transfer coefficient outside the tube can be improved.

2nd Embodiment FIG. 3 is a cycle system diagram of the absorption chiller 110 according to the second embodiment of the present invention.

The same configuration as the absorption chiller 100 according to the first embodiment will be omitted, and only different parts will be described. As shown in FIG. 3, an ejector 50 is provided between the solution heat exchanger 26 on the low temperature side and the solution heat exchanger 27 on the high temperature side, and the ejector 50 has a solution pipe 33 extending from the high pressure absorber 6. It is connected.

The solution from the high pressure absorber 6 is sent to the ejector 50 via the solution pipe 33. The solution from the low pressure absorber 15 is sent to the ejector 50 by the solution pump 23 in the solution pipe 34 via the solution heat exchanger 26. The ejector 50 uses the solution pressurized by the solution pump 23 from the low-pressure absorber 15 as a driving liquid, and sucks the solution from the high-pressure absorber 6 to join them. The merged solution is sent to the regenerator 1 via the solution heat exchanger 27 in the solution pipe 32.

As a result, the solution pump 24 of the first embodiment can be replaced with the ejector 50, so that the cost can be reduced and the power consumption can be reduced.

The present invention is not limited to the above-described embodiment. Those skilled in the art can make various additions and changes within the scope of the present invention.

For example, if the solution from the regenerator 1 is sprayed in parallel with the vertical tube 14 of the low pressure absorber 15 and the heat transfer tube 8 arranged horizontally of the high pressure absorber 6, FIGS. 1 and 3 show. It is not limited to the cycle system diagram. That is, as long as the device has the solution circulation paths of FIGS. 1 and 3, it may have a plurality of regenerators 1 or a combination of a plurality of cycles, and has the same operation as that of the above embodiment.・ Effects can be obtained.

1: Regenerator 2, 7, 12: Solution sprayer 3, 5, 8, 20: Multiple horizontally arranged heat transfer tubes 4: Condenser 6: High pressure absorber 9, 13: Eliminator 10, 11: Pipe plate 14: Vertical pipe 15: Low pressure absorber 16: High pressure evaporator 17, 19: Refrigerant sprayer 18: Low pressure evaporator 21, 22: Refrigerant pump 23, 24, 25: Solution pump 26, 27: Solution heat exchanger 28: Steam passages 29, 30, 31, 32, 33, 34: Solution pipes 35, 36, 37: Refrigerant pipes 38: Communication pipes 50: Ejectors

Claims (3)

Equipped with low pressure evaporator, low pressure absorber, high pressure evaporator, high pressure absorber, condenser, regenerator, refrigerant pump, and solution pump,
The low-pressure absorber and the high-pressure evaporator have a heat transfer tube extending substantially vertically, the inside of each heat transfer tube constitutes the high-pressure evaporator, and the outside of each heat transfer tube constitutes the low-pressure absorber.
The solution pipe connected to the regenerator and for sending the solution concentrated by the regenerator to the high-pressure absorber and the low-pressure absorber has a branch portion, and the solution is sent from the branch portion to the high-pressure absorber. Branch into a solution pipe for sending the solution to the low pressure absorber and a solution pipe for sending the solution to the low pressure absorber.
A solution heat exchanger on the high temperature side that exchanges heat between a solution pipe for sending a solution from the regenerator to the branch portion and a solution pipe for sending a solution from the low pressure absorber to the regenerator. ,
A solution heat exchanger on the low temperature side that exchanges heat between a solution pipe for sending a solution from the branch portion to the low pressure absorber and a solution pipe for sending a solution from the low pressure absorber to the regenerator. When,
Further prepare
The branch portion is located between the high temperature side solution heat exchanger and the low temperature side solution heat exchanger.
In the solution pipe for sending the solution from the low pressure absorber to the regenerator, a solution pump is provided between the low pressure absorber and the solution heat exchanger on the low temperature side, and the solution heat exchanger on the low temperature side is provided. An ejector is provided between the and the solution heat exchanger on the high temperature side, and a solution pipe extending from the high pressure absorber is connected to the ejector.
The ejector is an absorption chiller that merges a solution from the low pressure absorber with a solution from the high pressure absorber and sends it to the regenerator via a solution heat exchanger on the high temperature side . The absorption chiller according to claim 1, wherein a flow rate adjusting means is provided in a solution pipe for sending a solution from the branch portion to the high pressure absorber. The regenerator has a heat transfer tube arranged substantially horizontally, and the solution guided to the regenerator is configured to flow down the outside of the heat transfer tube in a flow-down liquid film system, claim 1 or 2 . Absorption chiller described in.

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