JP6138642B2 - Absorption refrigerator - Google Patents

Description

  The present invention relates to an absorption refrigerator, and more particularly to an absorption refrigerator having improved efficiency.

  The absorption refrigerator cools cold water by removing the heat of vaporization from the cold water when the refrigerant to be absorbed by the absorption liquid changes phase from liquid to gas. The absorption refrigerator is composed of an evaporator that evaporates the refrigerant, an absorber that absorbs the vapor of the refrigerant generated in the evaporator with an absorbing liquid (concentrated solution) having a high concentration, and an absorbing liquid (diluted solution) that absorbs the refrigerant. And a condenser that condenses the vapor of the refrigerant separated by the regenerator and uses it as a refrigerant liquid that is conveyed to the evaporator. In order to improve efficiency, the absorption refrigerator is provided with a solution heat exchanger that performs heat exchange between the concentrated solution transported from the regenerator to the absorber and the dilute solution transported from the absorber to the regenerator. It is common. Some absorption refrigerators use steam (heat source steam) as a heating source for a dilute solution in a regenerator.

  In order to further improve the efficiency of an absorption refrigerator that uses heat source vapor, there is one that also recovers heat from a drain liquid that is generated by condensation of the heat source vapor as the dilute solution is heated in the regenerator. As such an absorption refrigerator, a drain heat recovery unit that recovers the heat of the drain liquid in the dilute solution and a solution heat exchanger that performs heat exchange between the dilute solution and the concentrated solution are installed in parallel to recover the drain heat. There is a flow rate control mechanism that controls the flow rate of the dilute solution supplied to the storage unit, and controls to reduce the flow rate of the dilute solution supplied to the drain heat recovery device as the load on the absorption refrigerator decreases. (For example, refer to Patent Document 1).

JP 2009-287805 A

  However, the absorption refrigerator described in Patent Document 1 can only improve efficiency during partial load operation in which the load of the absorption refrigerator is reduced, and cooling supplied to the absorber, for example, during operation near the full load. When the flow rate of the circulating absorption liquid decreases due to a decrease in the temperature of the water, for example, it becomes impossible to recover the amount of heat corresponding to the flow rate of the drain liquid.

  In view of the above-described problems, an object of the present invention is to provide an absorption refrigerator that has improved efficiency when the temperature of cooling water is lower than that during rated operation during operation near full load.

  In order to achieve the above object, the absorption refrigerator according to the first aspect of the present invention transfers heat by a cycle of a refrigerant accompanying phase change and an absorbing liquid mixed with the refrigerant, as shown in FIG. A first absorption liquid Sw and a heat source vapor H, and the first absorption liquid Sw is heated with heat held by the heat source vapor H to generate a refrigerant from the first absorption liquid Sw. A regenerator 30 that generates a second absorbent liquid Sa having a higher concentration than the first absorbent liquid Sw by evaporating Vg; and an absorbent liquid heat exchange that flows the first absorbent liquid Sw introduced into the regenerator 30 An absorption liquid heat recovery pipe 18B for flowing the first absorption liquid Sw introduced into the regenerator 30, and an absorption liquid heat recovery pipe 18B arranged in parallel with the absorption liquid heat exchange pipe 18A; A heat exchanger 81 disposed in the absorption liquid heat exchange pipe 18A, wherein the absorption liquid heat exchange A heat exchanger 81 for exchanging heat between the first absorbent Sw flowing through the pipe 18A and the second absorbent Sa derived from the regenerator 30, and heat disposed in the absorbent heat recovery pipe 18B A heat recovery unit 82 for recovering the heat of the drain liquid D generated by condensation of the heat source vapor H in the regenerator 30 to the first absorption liquid Sw flowing through the absorption liquid heat recovery pipe 18B; A throttle mechanism 85 disposed in the absorption liquid heat recovery pipe 18B, which allows a maximum flow rate larger than the rated flow rate to pass; a flow rate of the first absorption liquid Sw flowing through the absorption liquid heat exchange pipe 18A; A flow rate adjusting mechanism 84 that adjusts the ratio of the flow rate of the first absorbent liquid Sw flowing through the absorbent heat recovery pipe 18B to the heat recovery unit 82 having the flow rate of the drain liquid D introduced into the heat recovery unit 82. With an increase in the ratio of the first absorbing liquid Sw introduced to the flow rate A flow rate adjustment mechanism 84 that adjusts the ratio so that the ratio of the flow rate of the first absorbent liquid Sw flowing through the absorbent liquid heat recovery pipe 18B to the flow rate of the first absorbent liquid Sw flowing through the absorbent liquid heat exchange pipe 18A increases. With.

  If comprised in this way, the temperature of cooling water will become lower than at the time of rated operation, the flow volume of the absorption liquid which circulates will reduce, and the 1st introduced into the heat recovery device of the flow volume of the drain liquid introduced into a heat recovery device. When the ratio of the absorption liquid to the flow rate of the absorption liquid increases, it is possible to increase the amount of heat recovered from the drain liquid by increasing the flow rate of the first absorption liquid flowing through the absorption liquid heat recovery pipe up to the maximum flow rate, The efficiency of the absorption refrigerator can be improved.

  Moreover, when the absorption refrigerator according to the second aspect of the present invention is shown, for example, with reference to FIG. 1, in the absorption refrigerator 1 according to the first aspect of the present invention, the throttle mechanism 85 is an orifice.

  If comprised in this way, installation and adjustment (exchange) of an aperture mechanism will become easy.

  Moreover, the absorption refrigerator which concerns on the 3rd aspect of this invention, for example, as shown in FIG. 1, in the absorption refrigerator 1 which concerns on the said 1st aspect or 2nd aspect of this invention, of the heat exchanger 81, is shown. An exchange temperature detector 51 for detecting the temperature of the first absorbent liquid Sw flowing through the downstream absorbent heat exchanger tube 18A; and a first absorbent liquid flowing through the absorbent heat recovery pipe 18B downstream of the heat collector 82; A recovery temperature detector 52 for detecting the temperature of Sw; and a flow rate adjusting mechanism 84 so that the difference between the temperature detected by the replacement temperature detector 51 and the temperature detected by the recovery temperature detector 52 falls within a predetermined range. And a control device 60 for controlling.

  If comprised in this way, appropriate flow volume distribution can be performed simply.

  According to the present invention, the temperature of the cooling water is lower than that during the rated operation, the flow rate of the circulating absorption liquid is reduced, and the first flow rate of the drain liquid introduced into the heat recovery unit is introduced into the heat recovery unit. When the ratio of the absorption liquid to the flow rate of the absorption liquid increases, it is possible to increase the amount of heat recovered from the drain liquid by increasing the flow rate of the first absorption liquid flowing through the absorption liquid heat recovery pipe up to the maximum flow rate, The efficiency of the absorption refrigerator can be improved.

1 is a schematic system diagram of an absorption refrigerator according to an embodiment of the present invention. It is a graph which shows the relationship between the flow volume of a drain liquid, and the ratio of the dilute solution flow volume introduce | transduced into a drain heat recovery device and a solution heat exchanger. It is a graph which shows the relationship between the load factor of the absorption refrigerator which used the cooling water inlet temperature as a parameter, and the consumption rate of heat source steam, (A) is a dilute solution introduced into a drain heat recovery device with a load factor fall. (B) is a graph when the ratio of the flow rate to the flow rate of the dilute solution introduced into the solution heat exchanger is lowered, and (B) is introduced into the drain heat recovery device as the cooling water inlet temperature of the absorption chiller decreases. It is a graph at the time of increasing the ratio with respect to the flow volume of the dilute solution introduce | transduced into the solution heat exchanger of the flow volume of a dilute solution. It is a partial systematic diagram which shows the modification of a flow volume adjustment mechanism. (A) is a partial system diagram on the solution side of a double-effect absorption refrigerator of a parallel flow, and (B) is a partial system diagram on the solution side of a double-effect absorption refrigerator of a reverse flow.

  Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or similar members are denoted by the same or similar reference numerals, and redundant description is omitted.

First, with reference to FIG. 1, the absorption refrigerator 1 which concerns on embodiment of this invention is demonstrated. FIG. 1 is a schematic system diagram of the absorption refrigerator 1. The absorption refrigerator 1 includes an absorber 10, an evaporator 20, a regenerator 30, and a condenser 40 as main components that perform an absorption refrigeration cycle. In addition, the absorption refrigerator 1 includes a control device 60. The absorption refrigerator 1 is a device that causes heat transfer by circulating the refrigerant while undergoing a phase change with respect to the absorption liquid, and reduces the temperature of the cold water C that is a medium to be cooled. In the following description, the absorption liquid is referred to as “dilute solution Sw”, “concentrated solution Sa”, etc., depending on the properties and the position on the absorption refrigeration cycle, in order to facilitate discrimination on the absorption refrigeration cycle. When the properties and the like are not asked, they are collectively referred to as “solution S”. Further, regarding the refrigerant, in order to facilitate the distinction on the absorption refrigeration cycle, the “evaporator refrigerant vapor Ve”, “regenerator refrigerant vapor Vg”, “refrigerant liquid Vf” are selected according to the property and the position on the absorption refrigeration cycle. However, when the property or the like is unquestioned, it is generally referred to as “refrigerant V”. In the present embodiment, an LiBr aqueous solution is used as the solution S (mixture of the absorbent and the refrigerant), and water (H ₂ O) is used as the refrigerant V. You may use it in the combination of a solution (absorbent).

  The absorber 10 is a device that absorbs the evaporator refrigerant vapor Ve generated in the evaporator 20 with the concentrated solution Sa as the second absorbing liquid. The absorber 10 includes a cooling pipe 11 serving as a cooling water flow path through which the cooling water Q flows and a concentrated solution spray nozzle 12 that sprays the concentrated solution Sa toward the outer surface of the cooling pipe 11 inside the absorber can body 17. Have. The concentrated solution spray nozzle 12 is disposed above the cooling pipe 11 so that the sprayed concentrated solution Sa falls on the cooling pipe 11. In addition, the concentrated solution spraying nozzle 12 may be configured by a device (for example, a dropping device using a capillary phenomenon) that can supply the concentrated solution Sa to the outer surface of the cooling tube 11 other than the spray nozzle. The absorber 10 stores the dilute solution Sw as the first absorbent having a reduced concentration due to the sprayed concentrated solution Sa absorbing the evaporator refrigerant vapor Ve in the lower portion of the absorber can body 17. The cooling water Q is configured to take away heat absorbed when the solution Sa absorbs the evaporator refrigerant vapor Ve. A cooling water inlet pipe 11 a for introducing cooling water Q cooled by a cooling tower (not shown) outside the absorption refrigerator 1 is connected to one end of the cooling pipe 11. A cooling water communication pipe 58 is connected to the other end of the cooling pipe 11. The cooling water inlet pipe 11 a is provided with a cooling water thermometer 15 as a cooling water temperature detector that detects the temperature of the cooling water Q introduced into the cooling pipe 11. The cooling water thermometer 15 is connected to the control device 60 with a signal cable, and is configured to be able to transmit the detected temperature of the cooling water Q as a signal to the control device 60.

  The evaporator 20 is a device that cools the cold water C by evaporating the refrigerant liquid Vf with the heat of the cold water C to generate an evaporator refrigerant vapor Ve. The evaporator 20 has an evaporator pipe 21 serving as a cold water flow path through which the cold water C flows, and a refrigerant liquid spray nozzle 22 that sprays the refrigerant liquid Vf toward the outer surface of the evaporator pipe 21 inside the evaporator can body 27. doing. The refrigerant liquid spray nozzle 22 is disposed above the evaporation pipe 21 so that the sprayed refrigerant liquid Vf falls on the evaporation pipe 21. The refrigerant liquid spray nozzle 22 may be configured by an apparatus (for example, a dripping apparatus using a capillary phenomenon) that can supply the refrigerant liquid Vf to the outer surface of the evaporation pipe 21 other than the spray nozzle. Further, the evaporator 20 includes a refrigerant liquid pipe 28 that guides the refrigerant liquid Vf stored in the lower portion of the evaporator can body 27 to the refrigerant liquid spray nozzle 22, and the refrigerant liquid Vf in the refrigerant liquid pipe 28. And a refrigerant pump 29 to be sent to 22. The evaporator 20 cools the cold water C by taking the heat of vaporization for evaporating the refrigerant liquid Vf sprayed on the outer surface of the evaporator pipe 21 to become the evaporator refrigerant vapor Ve from the cold water C flowing in the evaporator pipe 21. The refrigerant liquid Vf that has not evaporated out of the sprayed refrigerant liquid Vf is stored in the lower portion of the evaporator can body 27.

  In the present embodiment, the absorber 10 and the evaporator 20 are disposed adjacent to each other, and the upper part of the absorber can body 17 and the upper part of the evaporator can body 27 communicate with each other. With such a configuration, the evaporator refrigerant vapor Ve generated inside the evaporator can body 27 can be guided to the inside of the absorber can body 17.

  The regenerator 30 is a device that introduces the diluted solution Sw and heats it to release the refrigerant V in the diluted solution Sw to generate a concentrated solution Sa. In the regenerator 30, the refrigerant V separated from the dilute solution Sw is in a vapor state, and the vapor of the refrigerant V is referred to as a regenerator refrigerant vapor Vg. The regenerator 30 includes a heating unit 31 that heats the diluted solution Sw and a regenerator can body 37 that stores the introduced solution S. The heating unit 31 is disposed inside the regenerator can body 37. The heating unit 31 is connected to a heat source steam pipe 32 that introduces the heat source steam H, and is configured to be able to heat the solution S with heat held by the introduced heat source steam H. In addition, a drain pipe 33 that discharges a drain liquid D generated by condensation of the heat source vapor H by applying heat to the solution S is connected to the heating unit 31.

  The condenser 40 is a device that introduces the regenerator refrigerant vapor Vg evaporated from the dilute solution Sw in the regenerator 30, cools and condenses, and generates the refrigerant liquid Vf to be sent to the evaporator 20. The condenser 40 has a condenser pipe 41, which is a member that forms a flow path of the cooling water Q, inside the condenser can body 47. One end of the condensing pipe 41 is connected to the other end of a cooling water communication pipe 58 whose one end is connected to the cooling pipe 11. The other end of the condensing pipe 41 is connected to a cooling water outlet pipe 41b for leading the cooling water Q toward a cooling tower (not shown) outside the absorption refrigerator 1. The cooling water Q flowing through the cooling water outlet pipe 41b is cooled by a cooling tower (not shown) and supplied to the cooling water inlet pipe 11a.

  The condenser can body 47 is disposed in the vicinity of the regenerator can body 37. In the present embodiment, the upper part of the regenerator can body 37 and the upper part of the condenser can body 47 communicate with each other via the regenerator refrigerant vapor channel 35. The condenser 40 introduces the regenerator refrigerant vapor Vg from the regenerator 30 via the regenerator refrigerant vapor flow path 35, causes the cooling water Q flowing through the condenser pipe 41 to take the heat of the regenerator refrigerant vapor Vg, and regenerates it. The refrigerant vapor Vg is condensed into the refrigerant liquid Vf. In the present embodiment, the condenser can body 47 and the regenerator can body 37 are disposed above the evaporator can body 27 and the absorber can body 17. The bottom or lower portion of the condenser can body 47 and the evaporator can body 27 are connected by a condensed refrigerant liquid pipe 48, and the refrigerant liquid Vf in the condenser can body 47 is evaporated by the difference between the position head and the internal pressure of both. It is configured so that it can be guided into the can body 27.

  The bottom or lower portion of the absorber can body 17 and the regenerator can body 37 are connected by a dilute solution tube 18. A solution pump 19 is disposed in the dilute solution pipe 18. The dilute solution pipe 18 branches into two parts, an exchange dilute solution pipe 18A as an absorption liquid heat exchange pipe and a recovered dilute solution pipe 18B as an absorption liquid heat recovery pipe on the downstream side of the solution pump 19. . The exchange dilute solution pipe 18 </ b> A and the recovered dilute solution pipe 18 </ b> B are integrated upstream of the regenerator can body 37. The absorption refrigerator 1 is configured so that the dilute solution Sw in the absorber can body 17 can be conveyed into the regenerator can body 37 by the solution pump 19. In the regenerator can body 37, as the introduced dilute solution Sw moves from the inlet to the outlet, the refrigerant V is detached from the dilute solution Sw to increase the concentration.

  A portion where the concentrated solution Sa of the regenerator can body 37 is led out and the concentrated solution spray nozzle 12 of the absorber 10 are connected by a concentrated solution tube 38. In the absorption refrigerator 1, the dilute solution Sw is conveyed to the regenerator can body 37 by the solution pump 19, and the concentrated solution Sa generated by the release of the refrigerant V in the regenerator can body 37 is passed through the concentrated solution tube 38. And is introduced into the concentrated solution spray nozzle 12. In the exchange dilute solution tube 18A and the concentrated solution tube 38, solution heat exchange as a heat exchanger that performs heat exchange between the dilute solution Sw flowing in the exchange dilute solution tube 18A and the concentrated solution Sa flowing in the concentrated solution tube 38 is performed. A device 81 is inserted and arranged. The recovered dilute solution pipe 18B and the drain pipe 33 serve as a heat recovery unit that recovers the heat of the drain liquid D flowing through the drain pipe 33 into the dilute solution Sw flowing through the recovered dilute solution pipe 18B and raises the temperature of the dilute solution Sw. The drain heat recovery device 82 is inserted and arranged.

  Further, in the recovered dilute solution pipe 18B, a minimum flow orifice 83 and a maximum flow orifice 85 as a throttling mechanism are arranged upstream from the drain heat recovery device 82 in this order as viewed in the flow direction of the dilute solution Sw. It is arranged. The minimum flow rate orifice 83 is formed to have a diameter through which the dilute solution Sw having the minimum flow rate in the recovered dilute solution pipe 18B flows. Here, the minimum flow rate is a flow rate of the dilute solution Sw that needs to be secured at a minimum. The maximum flow orifice 85 is formed to have a diameter through which the dilute solution Sw having the maximum flow rate in the recovered dilute solution pipe 18B flows. Here, the maximum flow rate is larger than the rated flow rate, and is the maximum flow rate that allows the recovered dilute solution pipe 18B to flow in relation to the inlet temperature of the cooling water Q, for example. The rated flow rate is an optimum flow rate of the dilute solution Sw that flows through the recovered dilute solution pipe 18B when the absorption refrigerator 1 is performing the rated operation. The rated operation is that the absorption refrigerator 1 is operated under the assumed use conditions. Examples of the assumed use conditions include the inlet temperature of the cooling water Q, the outlet temperature of the cold water C, and the pressure of the heat source steam H. .

  The recovered diluted solution pipe 18B is provided with a bypass pipe 18Bb so as to bypass the minimum flow orifice 83. The bypass pipe 18Bb is formed to have a diameter that allows the dilute solution Sw having the maximum flow rate to flow. The bypass pipe 18Bb is provided with a dilute solution flow rate control valve 84 as a flow rate adjusting mechanism. The dilute solution flow control valve 84 is configured to be able to arbitrarily adjust the flow rate of the dilute solution Sw flowing through the recovered dilute solution pipe 18B between the minimum flow rate and the maximum flow rate by adjusting the opening degree. ing. By adjusting the opening of the diluted solution flow rate control valve 84, the ratio between the flow rate of the diluted solution Sw flowing through the exchange diluted solution tube 18A and the flow rate of the diluted solution Sw flowing through the recovered diluted solution tube 18B can be adjusted. It is configured as follows.

  An exchange thermometer 51 serving as an exchange temperature detector for detecting the temperature of the dilute solution Sw derived from the solution heat exchanger 81 is provided in the exchange dilute solution pipe 18 </ b> A downstream of the solution heat exchanger 81. The exchange thermometer 51 is connected to the control device 60 with a signal cable, and is configured to be able to transmit the detected temperature of the diluted solution Sw as a signal to the control device 60. A recovery thermometer 52 as a recovery temperature detector that detects the temperature of the diluted solution Sw led out from the drain heat recovery device 82 is provided in the recovery diluted solution pipe 18B downstream of the drain heat recovery device 82. The recovery thermometer 52 is connected to the control device 60 through a signal cable, and is configured to transmit the detected temperature of the diluted solution Sw as a signal to the control device 60.

  The control device 60 is a device that controls the operation of the absorption refrigerator 1. The control device 60 is connected to the solution pump 19 and the refrigerant pump 29 by signal cables, respectively, and is configured to be able to control the start and stop of these. Further, the control device 60 is configured to receive a signal of the temperature of the cooling water Q from the cooling water thermometer 15. Further, the control device 60 is configured to be able to receive a temperature signal of the dilute solution Sw from each of the replacement thermometer 51 and the recovery thermometer 52. The control device 60 is connected to the dilute solution flow control valve 84 through a signal cable, and is configured to be able to adjust the opening degree of the dilute solution flow control valve 84. Moreover, the control apparatus 60 is comprised so that control of the absorption refrigerator 1 as demonstrated by the effect | action of the absorption refrigerator 1 mentioned later can be performed.

  With continued reference to FIG. 1, the operation of the absorption refrigerator 1 will be described. First, the operation at the time of steady operation of the absorption refrigerator 1 will be described. During the steady operation of the absorption refrigerator 1, the solution pump 19 and the refrigerant pump 29 are respectively operated according to commands from the control device 60. Looking at the cycle on the refrigerant V side, the regenerator refrigerant vapor Vg introduced from the regenerator 30 to the condenser 40 via the regenerator refrigerant vapor channel 35 is cooled and condensed by the cooling water Q flowing through the condenser pipe 41. The refrigerant liquid Vf is stored in the lower portion of the condenser can body 47. The cooling water Q that has cooled the regenerator refrigerant vapor Vg rises in temperature, is led out from the cooling water outlet pipe 41b, and is supplied to a cooling tower (not shown). The refrigerant liquid Vf in the condenser can body 47 is introduced into the evaporator can body 27 via the condensed refrigerant liquid pipe 48.

  The refrigerant liquid Vf introduced from the condenser can body 47 into the evaporator can body 27 is mixed with the refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 22 and not evaporated, and stored in the lower portion of the evaporator can body 27. The The refrigerant liquid Vf in the evaporator can body 27 flows through the refrigerant liquid pipe 28 to the refrigerant liquid spray nozzle 22 by the refrigerant pump 29. 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 C flowing through the evaporation pipe 21, and partially evaporates to become the evaporator refrigerant vapor Ve, and the absorber can It is introduced into the trunk 17. The cold water C deprived of heat by the sprayed refrigerant liquid Vf is led out from the evaporation pipe 21 with the temperature lowered, and is supplied to a place where the cold water C 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 condenser can body 47 and stored in the lower portion of the evaporator can body 27.

  Next, looking at the solution S side cycle of the absorption refrigerator 1, the dilute solution Sw in the absorber canister 17 first flows through the dilute solution pipe 18 by the solution pump 19, and the exchange dilute solution pipe 18 </ b> A and the recovered dilute solution are collected. After the temperature is increased by the solution heat exchanger 81 and the drain heat recovery device 82, the temperature is increased by the solution heat exchanger 81 and the drain heat recovery device 82, and then, in this embodiment, the temperature is again merged with one dilute solution tube 18 and introduced into the regenerator can body 37. Is done. The dilute solution Sw whose temperature has risen in each of the solution heat exchanger 81 and the drain heat recovery unit 82 is not merged into one dilute solution pipe 18 and is introduced into the regenerator can body 37 separately. May be. The dilute solution Sw introduced into the regenerator can body 37 is heated by the heat held by the heat source vapor H supplied to the heating unit 31, and the refrigerant V is released to become a concentrated solution Sa. On the other hand, the refrigerant V separated from the dilute solution Sw is sent as regenerator refrigerant vapor Vg into the condenser can body 47 via the regenerator refrigerant vapor channel 35. The concentrated solution Sa generated in the regenerator can body 37 flows through the concentrated solution tube 38 and heat exchanges with the dilute solution Sw in the solution heat exchanger 81 to reach the concentrated solution spray nozzle 12 after the temperature is lowered. In addition, the heat source vapor | steam H which gave the heat | fever to the solution S in the heating part 31 condenses, becomes the drain liquid D, flows through the drain pipe 33, and heat-exchanges with the dilute solution Sw in the drain heat recovery device 82, and temperature falls. After that, it is discharged out of the absorption refrigerator 1.

  The concentrated solution Sa reaching the concentrated solution spraying nozzle 12 is sprayed toward the cooling pipe 11, absorbs the evaporator refrigerant vapor Ve introduced from the evaporator 20, decreases in concentration, and becomes a diluted solution Sw. In the absorber can body 17, when the concentrated solution Sa absorbs the evaporator refrigerant vapor Ve, absorption heat is generated. The generated absorbed heat is removed by the cooling water Q flowing through the cooling pipe 11. The cooling water Q flowing through the cooling pipe 11 is deprived of absorbed heat, rises in temperature, is led to the cooling water communication pipe 58, and is supplied to the condensing pipe 41 of the condenser 40. The dilute solution Sw generated in the absorber can body 17 is stored in the absorber can body 17.

  In the present embodiment, the absorption refrigerator 1 acting as described above has an inlet temperature of the cooling water Q of 32 ° C., an outlet temperature of the cold water C of 7 ° C., and a load factor of 100% during rated operation. . In the absorption refrigerator 1, the control device 60 receives the temperature signal of the dilute solution Sw from each of the replacement thermometer 51 and the recovery thermometer 52, and detects the temperature detected by the replacement thermometer 51 and the recovery thermometer 52. The opening degree of the dilute solution flow control valve 84 is adjusted so that the difference from the measured temperature falls within a predetermined range. Specifically, when the temperature detected by the replacement thermometer 51 is higher than the temperature detected by the recovery thermometer 52, the dilute solution flow rate control is performed so that the flow rate of the dilute solution Sw flowing through the recovery dilute solution pipe 18B decreases. When the opening of the valve 84 is adjusted and, conversely, when the temperature detected by the recovery thermometer 52 is higher than the temperature detected by the replacement thermometer 51, the flow rate of the diluted solution Sw flowing through the recovered diluted solution pipe 18B is The opening degree of the diluted solution flow rate control valve 84 is adjusted so as to increase. By controlling the diluted solution flow rate control valve 84 in this way, the temperature of the diluted solution Sw introduced into the regenerator 30 can be maximized (the heat recovered by the diluted solution Sw can be maximized), and the heat recovery efficiency Can be improved. Note that the heat recovery efficiency increases as the difference between the temperature detected by the replacement thermometer 51 and the temperature detected by the recovery thermometer 52 approaches zero, so that the predetermined range is preferably zero. From the viewpoint of stability, the predetermined range may be appropriately set within an allowable range.

  Here, when the load of the absorption refrigerator 1 decreases without changing the inlet temperature of the cooling water Q and the outlet temperature of the cold water C, the control device 60 determines the difference between the internal pressure of the regenerator 30 and the internal pressure of the absorber 10. Relatedly, the discharge flow rate of the solution pump 19 is controlled so that the flow rate of the dilute solution Sw conveyed from the absorber 10 to the regenerator 30 is decreased. In addition, the flow rate and enthalpy of the drain liquid D discharged from the heating unit 31 of the regenerator 30 and introduced into the drain heat recovery unit 82 are reduced. When the flow rate and enthalpy of the drain liquid D introduced into the drain heat recovery device 82 are decreased, the amount of heat that can be recovered from the drain solution D in the drain heat recovery device 82 decreases, and thus the recovery thermometer 52 detects the heat. The temperature drops. When the temperature detected by the recovery thermometer 52 falls below a predetermined range from the temperature detected by the replacement thermometer 51, the control device 60 causes the diluted solution Sw of the recovered diluted solution pipe 18B to flow. The opening degree of the dilute solution flow control valve 84 is adjusted so that the flow rate decreases, so that the difference between the temperature detected by the replacement thermometer 51 and the temperature detected by the recovery thermometer 52 falls within a predetermined range. . In this way, when the load of the absorption refrigerator 1 is reduced, the flow rate of the diluted solution Sw flowing through the recovered diluted solution tube 18B is decreased to maximize the heat recovered by the diluted solution Sw introduced into the regenerator 30. To improve heat recovery efficiency.

  On the other hand, when the inlet temperature of the cooling water Q is lowered while the absorption refrigerator 1 is operating near the rated load, the internal pressure of the absorption refrigerator 1 is reduced, and the flow rate of the concentrated solution Sa is accordingly reduced. The flow rate of the dilute solution Sw is also reduced. In this case, the flow rate and enthalpy of the drain liquid D introduced into the drain heat recovery device 82 are slightly reduced, but the flow rate of the dilute solution Sw supplied to the drain heat recovery device 82 is further reduced, and the recovery temperature is reduced. The temperature detected by the total 52 increases. When the temperature detected by the recovery thermometer 52 rises beyond a predetermined range from the temperature detected by the replacement thermometer 51, the control device 60 causes the diluted solution Sw of the recovered diluted solution pipe 18B to flow. The opening degree of the dilute solution flow control valve 84 is adjusted so that the flow rate increases, so that the difference between the temperature detected by the replacement thermometer 51 and the temperature detected by the recovery thermometer 52 falls within a predetermined range. . The flow rate of the diluted solution Sw flowing through the recovered diluted solution tube 18B can be increased to the maximum flow rate. By restricting the increase in the flow rate of the dilute solution Sw flowing through the recovered dilute solution pipe 18B to the maximum flow rate by the maximum flow orifice 85, the flow rate of the dilute solution Sw flowing through the recovered dilute solution tube 18B is excessively increased for some reason. It is possible to prevent the temperature of the dilute solution Sw derived from the drain heat recovery unit 82 from being lowered. In this way, when the inlet temperature of the cooling water Q decreases, the flow rate of the dilute solution Sw flowing through the collective dilute solution tube 18B is increased so that the heat recovered by the dilute solution Sw introduced into the regenerator 30 is maximized. To improve heat recovery efficiency. Thus, in the present embodiment, the opening of the dilute solution flow control valve 84 is set so that the difference between the temperature detected by the replacement thermometer 51 and the temperature detected by the recovery thermometer 52 falls within a predetermined range. By adjusting, the ratio (D / Sw) of the flow rate of the drain liquid D introduced into the drain heat recovery unit 82 to the flow rate of the dilute solution Sw introduced into the drain heat recovery unit 82 becomes a predetermined ratio. ing. Here, the predetermined ratio is a ratio at which the amount of heat recovered by the dilute solution Sw introduced into the regenerator 30 can be increased as much as possible, and may have a permissible range.

  FIG. 2 shows the ratio (D / Sw) of the flow rate of the drain liquid D introduced into the drain heat recovery unit 82 to the dilute solution Sw introduced into the drain heat recovery unit 82, and the rare amount introduced into the drain heat recovery unit 82. The graph of the relationship with ratio (R) with respect to the flow volume of the dilute solution Sw introduced into the solution heat exchanger 81 of the flow volume of the solution Sw is shown. In the graph shown in FIG. 2, the relationship between the two is linear for simplicity of explanation, but it may not be linear depending on the characteristics of the dilute solution flow control valve 84. When the absorption refrigerator 1 is performing a rated operation, the ratio D / Sw is a rated point, and the ratio R at this time is a rated flow ratio Rr. When the load factor of the absorption refrigerator 1 decreases and the drain liquid D discharged from the heating unit 31 decreases, that is, the ratio D / Sw decreases, the dilute solution flow rate control valve by the control device 60 By the control of 84, the flow rate of the dilute solution Sw flowing through the recovered dilute solution pipe 18B decreases, that is, the ratio R decreases. When the flow rate of the dilute solution Sw flowing through the recovered dilute solution tube 18B becomes the minimum flow rate, the ratio R becomes the minimum flow rate ratio Rmin and does not decrease further. On the other hand, when the temperature of the cooling water Q supplied to the absorption refrigerator 1 is decreased and the flow rate of the dilute solution Sw is decreased and the ratio D / Sw is increased, the dilute solution flow rate control valve 84 of the control device 60 increases. The flow rate of the dilute solution Sw flowing through the recovered dilute solution tube 18B is increased by the control, that is, the ratio R is increased. When the flow rate of the dilute solution Sw flowing through the recovered dilute solution tube 18B reaches the maximum flow rate, the ratio R becomes the maximum flow rate ratio Rmax and does not increase further.

  FIG. 3A shows the load factor of the absorption chiller 1 and the heat source steam H, using the cooling water Q inlet temperature as a parameter when the ratio R is reduced as the load factor of the absorption chiller 1 is reduced. The graph of the relationship with the consumption rate is shown. In the figure, curve Q20 is when the cooling water Q inlet temperature is 20 ° C., curve Q32 is when the cooling water Q inlet temperature is 32 ° C., and the broken line is introduced into the drain heat recovery unit 82, respectively. When the ratio R of the flow rate of the dilute solution Sw to the flow rate of the dilute solution Sw introduced into the solution heat exchanger 81 is not changed from the rated point, the solid line indicates the case where the ratio R is decreased as the load factor decreases. Yes. As can be seen from FIG. 3A, during the partial load operation of the absorption chiller 1, the higher the cooling water Q inlet temperature and the lower the load factor, the greater the effect of reducing the steam consumption rate, that is, the efficiency. It has improved.

  FIG. 3B shows the load factor of the absorption chiller 1 and the heat source steam H with the ratio of the cooling water Q inlet temperature as a parameter when the ratio R is increased as the cooling water Q inlet temperature decreases. The graph of the relationship with a consumption rate is shown. In the figure, the curve Q20 is when the cooling water Q inlet temperature is 20 ° C., the curve Q32 is when the cooling water Q inlet temperature is 32 ° C., and the broken line in the curve Q20 is introduced into the drain heat recovery device 82. When the ratio R of the flow rate of the diluted solution Sw to the flow rate of the diluted solution Sw introduced into the solution heat exchanger 81 is not changed from the rated point, the solid line increases the ratio R as the cooling water Q inlet temperature decreases. Shows the case. As can be seen from FIG. 3 (B), during the rated operation of the absorption refrigerator 1, when the inlet temperature of the cooling water Q decreases, the higher the load factor, the greater the effect of reducing the steam consumption rate, that is, the efficiency is improved. ing.

  As explained above, according to the absorption refrigerator 1 according to the present embodiment, when the load decreases and the flow rate of the condensed drain liquid D decreases, or the inlet temperature of the cooling water Q decreases. When the flow rate of the dilute solution Sw decreases, the ratio of the flow rate of the dilute solution Sw flowing through the exchange dilute solution tube 18A and the flow rate of the dilute solution Sw flowing through the recovered dilute solution tube 18B according to the change in the ratio D / Sw. Therefore, the heat recovered by the dilute solution Sw introduced into the regenerator 30 can be maximized, and the efficiency can be improved. Further, when the ratio of the flow rate of the dilute solution Sw is adjusted, the dilute solution flow rate control valve 84 is set so that the difference between the temperature detected by the replacement thermometer 51 and the temperature detected by the recovery thermometer 52 falls within a predetermined range. Therefore, appropriate flow rate distribution can be easily performed.

  In the above description, the throttle mechanism is the maximum flow orifice 85, but it may be a valve (regardless of whether it is manual or automatic) whose opening degree can be adjusted. When the throttle mechanism is configured by a valve capable of adjusting the opening, the setting of the maximum flow rate can be changed as appropriate. On the other hand, when the throttle mechanism is constituted by the maximum flow orifice 85, it is possible to prevent the maximum flow rate from being changed by mistake. Even when the maximum flow orifice 85 is used, the setting of the maximum flow can be changed by replacing the orifice.

  In the above description, when adjusting the ratio between the flow rate of the dilute solution Sw flowing through the exchange dilute solution tube 18A and the flow rate of the dilute solution Sw flowing through the recovery dilute solution tube 18B, the temperature detected by the exchange thermometer 51 and the recovery temperature. The opening degree of the dilute solution flow rate control valve 84 is adjusted so that the difference from the temperature detected by the total 52 is within a predetermined range. However, with respect to the ratio of the dilute solution Sw flow rate during rated operation, Even if the opening degree of the dilute solution flow control valve 84 is adjusted so that the flow rate of the dilute solution Sw flowing through the recovered dilute solution pipe 18B increases as the temperature detected by the cooling water thermometer 15 decreases. Good. In this case, the replacement thermometer 51 and the recovery thermometer 52 may be omitted. Note that the cooling water thermometer 15 may be omitted when the control based on the temperature detected by the cooling water thermometer 15 is not performed.

In the above description, the flow rate adjustment mechanism is configured by the dilute solution flow rate control valve 84 that is disposed in the bypass pipe 18Bb that bypasses the minimum flow rate orifice 83 and can adjust the opening degree steplessly. It may be configured as follows.
FIG. 4 is a partial system diagram showing a modification of the flow rate adjusting mechanism. The difference between the modification shown in FIG. 4 and the configuration around the dilute solution flow control valve 84 shown in FIG. 1 is as follows. First, a rated flow orifice 184 through which a diluted solution Sw of a rated flow is passed is disposed in the recovered diluted solution pipe 18B between the minimum flow orifice 83 and the maximum flow orifice 85. A minimum bypass pipe 318B that bypasses the minimum flow orifice 83 (corresponding to the bypass pipe 18Bb in FIG. 1) is an electromagnetic that opens and closes the flow path of the minimum bypass pipe 318B instead of the dilute solution flow control valve 84 (see FIG. 1). A valve 283 is provided. The recovered dilute solution pipe 18B is provided with a rated bypass pipe 418B that bypasses the rated flow orifice 184. The rated bypass pipe 418B is provided with an electromagnetic valve 284 that opens and closes the flow path. The minimum bypass pipe 318B when the electromagnetic valve 283 is opened and the rated bypass pipe 418B when the electromagnetic valve 284 is opened are formed to have a diameter capable of flowing the dilute solution Sw having the maximum flow rate. In the modification shown in FIG. 4, the pipe connected to the recovered dilute solution pipe 18B between the minimum flow orifice 83 and the rated flow orifice 184 also serves as the minimum bypass pipe 318B and the rated bypass pipe 418B.

  In the modification shown in FIG. 4 configured as described above, when the flow rate of the dilute solution Sw flowing through the recovered dilute solution pipe 18B on the downstream side of the maximum flow orifice 85 is when the two electromagnetic valves 283 and 284 are opened. The maximum flow rate is obtained when the electromagnetic valve 283 is opened and the electromagnetic valve 284 is closed, and the minimum flow rate is obtained when at least the electromagnetic valve 283 is closed. As described above, in the modification shown in FIG. 4, the control device simply switches the opening and closing of the electromagnetic valve disposed in each bypass pipe, and the dilute solution having a flow rate selected from a plurality of preset flow rates. Sw can flow. In the modification shown in FIG. 4, the flow rate is selected from the three types of maximum flow rate, rated flow rate, and minimum flow rate, but an orifice with an arbitrarily set flow rate and a maximum flow rate that bypasses the orifice. By providing the recovered dilute solution pipe 18B with a set of a bypass pipe (with an on-off valve provided) through which the flow rate can flow, the range of flow rate selection can be expanded.

  In the above description, the configuration in which the cooling water Q is introduced into the condenser 40 after being introduced into the absorber 11 is exemplified. However, the cooling water Q is introduced into the absorber 11 after being introduced into the condenser 40. Alternatively, a configuration in which the absorber 10 and the condenser 40 are introduced in parallel may be employed.

In the above description, for the sake of easy understanding, the absorption refrigerator 1 has a single-effect configuration, but a multiple-effect absorption refrigerator having a plurality of regenerators or a plurality of evaporators having different operating pressures. / It can also be applied to an absorption refrigerator having an absorber.
FIG. 5 (A) is a partial system diagram on the solution side of the parallel flow double-effect absorption refrigerator 1A. The absorption refrigerator 1A is different from the absorption refrigerator 1 (see FIG. 1) mainly in the following points. In the absorption refrigerator 1A, the regenerator is divided into a high temperature regenerator 30H and a low temperature regenerator 30L. The absorption refrigerator 1A is configured such that the dilute solution Sw derived from the absorber 10 is supplied in parallel to the high temperature regenerator 30H and the low temperature regenerator 30L. In the high temperature regenerator 30H, the heating unit 31 for introducing the heat source steam H is provided in the high temperature regenerator 30H, and the flow rate of the introduced dilute solution Sw is heated with the heat source steam H so as to generate the high temperature concentrated solution SaH. It is configured. The low temperature regenerator 30L is configured to heat the introduced dilute solution Sw using the vapor of the refrigerant generated in the high temperature regenerator 30H as a heat source to generate a low temperature concentrated solution SaL. The dilute solution tube 18 is provided with a concentrated solution Sa obtained by mixing the high temperature concentrated solution SaH and the low temperature concentrated solution SaL, and a low temperature solution heat exchanger 81L for exchanging heat with the diluted solution Sw.

  A low temperature dilute solution pipe 18L that supplies dilute solution Sw to the low temperature regenerator 30L is connected to the dilute solution pipe 18 on the downstream side of the low temperature solution heat exchanger 81L. The dilute solution pipe 18 is branched into an exchange dilute solution pipe 18A and a recovered dilute solution pipe 18B on the downstream side of the branch portion with the low temperature dilute solution pipe 18L. The downstream structure of the branch portion of the exchange dilute solution pipe 18A and the recovered dilute solution pipe 18B is the same as that of the absorption refrigerator 1 (see FIG. 1), but for the distinction from the low temperature solution heat exchanger 81L, The heat exchanger disposed in the exchange dilute solution tube 18A is referred to as a high temperature solution heat exchanger 81H. The flow path for flowing the high temperature concentrated solution SaH derived from the high temperature regenerator 30H is referred to as a high temperature concentrated solution tube 38H. The high temperature concentrated solution pipe 38H is connected to the low temperature concentrated solution pipe 38L through which the low temperature concentrated solution SaL derived from the low temperature regenerator 30L flows, downstream of the high temperature solution heat exchanger 81H. The downstream side where the high temperature concentrated solution tube 38H and the low temperature concentrated solution tube 38L are connected is a concentrated solution tube 38 that guides the concentrated solution Sa to the absorber 10.

  In the absorption refrigerator 1A, the hot concentrated solution SaH corresponds to the second absorbing solution. Also in the absorption refrigerator 1A, when the flow rate of the condensate drain liquid D decreases due to a decrease in load, or when the cooling water inlet temperature decreases and the flow rate of the dilute solution Sw decreases, the exchange dilute solution tube Since the ratio between the flow rate of the dilute solution Sw flowing through 18A and the flow rate of the dilute solution Sw flowing through the recovered dilute solution tube 18B is adjusted, the heat recovered by the dilute solution Sw introduced into the high temperature regenerator 30H can be maximized. And efficiency can be improved.

  FIG. 5B is a partial system diagram on the solution side of the reverse-flow double-effect absorption refrigerator 1B. The absorption refrigerator 1B is different from the absorption refrigerator 1A (see FIG. 5A) mainly in the following points. The absorption refrigerator 1B is configured such that the dilute solution Sw derived from the absorber 10 is supplied to the low temperature regenerator 30L, and the low temperature concentrated solution SaL generated by the low temperature regenerator 30L is supplied to the high temperature regenerator 30H. ing. In the absorption refrigerator 1B, the absorber 10 and the low temperature regenerator 30L are connected by a low temperature dilute solution pipe 18L that conveys the dilute solution Sw. A low temperature solution pump 19L for pumping the dilute solution Sw and a low temperature solution heat exchanger 81L are disposed in the low temperature dilute solution pipe 18L. The low temperature regenerator 30L and the high temperature regenerator 30H are connected by a high temperature dilute solution pipe 18H that conveys the low temperature concentrated solution SaL toward the high temperature regenerator 30H. A low temperature concentrated solution tube 38L through which a part of the low temperature concentrated solution SaL flows is connected to the high temperature diluted solution tube 18H. The high temperature dilute solution pipe 18H is provided with a high temperature solution pump 19H on the downstream side of the connecting portion with the low temperature concentrated solution pipe 38L. The high-temperature dilute solution pipe 18H branches into an exchange dilute solution pipe 18A and a recovered dilute solution pipe 18B on the downstream side of the high-temperature solution pump 19H. The configuration downstream of the branch portion of the exchange dilute solution pipe 18A and the recovered dilute solution pipe 18B is the same as that of the absorption refrigerator 1A (see FIG. 5A). Further, a low-temperature heat recovery device may be provided in parallel with the low-temperature solution heat exchanger 81L, and the drain liquid D recovered by the heat recovery device 82 may be guided to the low-temperature heat recovery device for further heat recovery. In this case, the flow rate control similar to the control of the absorption liquid introduced into the heat recovery device 82 by the high temperature solution pump 19H may be performed on the low temperature heat recovery device arranged in parallel with the low temperature solution heat exchanger 81L. Good.

  In the absorption refrigerator 1B, the low-temperature concentrated solution SaL corresponds to the first absorption liquid, and the high-temperature concentrated solution SaH corresponds to the second absorption liquid. Also in the absorption refrigerator 1B, when the flow rate of the drain liquid D that is condensed due to a decrease in load decreases, or when the inlet temperature of the cooling water decreases and the flow rate of the diluted solution Sw decreases, the exchange diluted solution tube Since the ratio between the flow rate of the low temperature concentrated solution SaL flowing through 18A and the flow rate of the low temperature concentrated solution SaL flowing through the recovered diluted solution pipe 18B is adjusted, the heat recovered by the low temperature concentrated solution SaL introduced into the high temperature regenerator 30H is maximized. Can improve efficiency.

  When the flow rate of the condensate drain liquid D decreases due to a decrease in load, or when the cooling water inlet temperature decreases and the flow rate of the dilute solution Sw decreases, the exchange is performed according to the change in the ratio D / Sw. The configuration for adjusting the ratio between the flow rate of the first absorbent flowing through the dilute solution pipe 18A and the flow rate of the first absorbent flowing through the recovered dilute solution pipe 18B is the absorption refrigerator 1 shown in FIG. In addition to the absorption refrigerator 1A shown in FIG. 5B, the absorption refrigerator 1B shown in FIG. 5B, a series-effect double-effect absorption refrigerator, a multi-effect absorption refrigerator having three or more regenerators, or The present invention can also be applied to an absorption refrigerator having a plurality of evaporators / absorbers having different operating pressures.

1 Absorption Refrigerator 18A Exchange Diluted Solution Tube 18B Collected Diluted Solution Tube 30 Regenerator 60 Controller 81 Heat Exchanger 82 Heat Recovery Unit 84 Diluted Solution Flow Control Valve 85 Maximum Flow Orifice 91 Exchange Thermometer 92 Recovery Thermometer D Drain Solution H Heat source vapor Sa Concentrated solution Sw Dilute solution Vg Regenerator refrigerant vapor

Claims (3)

An absorption refrigerator that transfers heat by a cycle of a refrigerant accompanied by a phase change and an absorbing liquid mixed with the refrigerant;
The first absorption liquid and the heat source vapor are introduced, the first absorption liquid is heated by the heat held by the heat source vapor, and the refrigerant is evaporated from the first absorption liquid, thereby the first absorption liquid. A regenerator that produces a second absorbent having a higher concentration;
An absorption liquid heat exchange tube for flowing the first absorption liquid introduced into the regenerator;
An absorption liquid heat recovery pipe for flowing the first absorption liquid introduced into the regenerator, the absorption liquid heat recovery pipe disposed in parallel with the absorption liquid heat exchange pipe;
A heat exchanger disposed in the absorption liquid heat exchange pipe, wherein heat is generated by the first absorption liquid flowing through the absorption liquid heat exchange pipe and the second absorption liquid derived from the regenerator. A heat exchanger to effect exchange;
A heat recovery unit disposed in the absorption liquid heat recovery pipe, wherein the drain liquid generated by condensing the heat source vapor in the regenerator to the first absorption liquid flowing through the absorption liquid heat recovery pipe A heat recovery device for recovering heat;
A throttle mechanism disposed in the absorption liquid heat recovery pipe, wherein the throttle mechanism allows a maximum flow rate larger than a rated flow rate to pass;
An absorber configured so that the cooling water takes away the heat of absorption generated when the second absorbent absorbs the vapor of the refrigerant;
A flow rate adjusting mechanism that adjusts a ratio between a flow rate of the first absorption liquid flowing through the absorption liquid heat exchange tube and a flow rate of the first absorption liquid flowing through the absorption liquid heat recovery tube, the absorption refrigeration At the time of operation near the full load of the machine, the temperature of the cooling water is lower than that at the rated operation, and the flow rate of the first absorption liquid and the second absorption liquid is reduced, so that the heat recovery device is introduced. As the ratio of the flow rate of the drain liquid to the flow rate of the first absorption liquid introduced into the heat recovery device increases, the absorption liquid of the flow rate of the first absorption liquid flowing through the absorption liquid heat recovery pipe A flow rate adjusting mechanism that adjusts the ratio so that a ratio to a flow rate of the first absorbent flowing through the heat exchange pipe increases;
Absorption refrigerator. The throttling mechanism is an orifice;
The absorption refrigerator according to claim 1. An exchange temperature detector for detecting the temperature of the first absorbent flowing through the absorbent liquid heat exchange pipe on the downstream side of the heat exchanger;
A recovery temperature detector for detecting the temperature of the first absorption liquid flowing through the absorption liquid heat recovery pipe on the downstream side of the heat recovery apparatus;
A control device that controls the flow rate adjusting mechanism so that a difference between a temperature detected by the replacement temperature detector and a temperature detected by the recovery temperature detector falls within a predetermined range;
The absorption refrigerator according to claim 1 or 2.

Images