JP4602734B2 - Two-stage temperature rising type absorption heat pump - Google Patents

Description

  The present invention relates to a two-stage temperature rising absorption heat pump that converts exhaust heat energy into a high-temperature medium (high-temperature water, high-temperature steam, etc.) using an absorption heat pump, and more particularly to a two-stage temperature rising absorption heat pump with improved start-up characteristics. Is.

  Conventionally, this type of two-stage temperature rising type absorption heat pump is disclosed in Patent Document 1. FIG. 1 is a diagram showing a configuration example of a two-stage temperature rising type absorption heat pump disclosed in Patent Document 1. In FIG. As shown in FIG. 1, the two-stage temperature rising type absorption heat pump includes a high temperature absorber A2, a low temperature absorber A1, a high temperature evaporator E2, a low temperature evaporator E1, a regenerator G, a condenser C, and a high temperature solution heat exchanger X2. The low-temperature solution heat exchanger X1 is provided as a main component device.

  As the equipment on the solution side, a solution pump 101 that sends the concentrated solution of the regenerator G to the high-temperature absorber A2, a concentrated solution tube 102, a diluted solution tube 103, an intermediate concentration diluted solution tube 104, a first pressure reducing valve 105, and a second pressure reducing valve 106, a first hot water pipe 107 provided in the regenerator G, a control valve 108 provided on the inlet side of the first hot water pipe 107, a second hot water pipe 109 provided in the high temperature absorber A2, the first 2. Temperature sensor 110 for detecting the outlet temperature provided on the outlet side of the hot water pipe 109, a liquid level sensor 111 for detecting the liquid level of the low temperature absorber A1, a first spray 112 opened in the low temperature absorber A1 and high temperature absorption. A second spray 113 opening in the vessel A2 is provided.

  As the refrigerant side equipment, a refrigerant pump 114 that sends refrigerant from the condenser C to the low temperature evaporator E1 and the high temperature evaporator E2, a refrigerant pipe 115, 116, 117, a spray 118 that opens to the low temperature evaporator E1, and an opening to the high temperature evaporator E2. A spray 119, a liquid level sensor 120 for detecting the liquid level of the low temperature evaporator E1, a liquid level sensor 130 for detecting the liquid level of the high temperature evaporator E2, a control valve 121 for controlling the flow rate of refrigerant supplied to the spray 118, and the spray 119. A control valve 122 for controlling the flow rate of refrigerant supplied to the condenser C, a cold water pipe 123 provided in the condenser C, a third hot water pipe 124 provided in the low temperature evaporator E1, and an inlet of the third hot water pipe 124. A control valve 125 is provided.

  The equipment for connecting the solution side and the refrigerant side includes a communication pipe 126 that guides the refrigerant vapor generated in the regenerator G to the condenser C, and a supply pipe 127 that supplies the refrigerant vapor generated in the low-temperature evaporator E1 to the low-temperature absorber A1. The supply pipe 128 that supplies the refrigerant vapor generated in the high-temperature evaporator E2 to the high-temperature absorber A2, the inside of the low-temperature absorber A1 and the inside of the high-temperature evaporator E2 are connected in an endless manner, and the temperature is lowered by circulating water therein. A heat transfer tube 129 for supplying the heat obtained in the absorber A1 into the high temperature evaporator E2 is provided. The control valve 108 and the control valve 125 are controlled by a detection signal of the temperature sensor 110 on the outlet side of the second hot water pipe 109.

  Heat energy such as warm drainage is supplied to the first hot water pipe 107 and the third hot water pipe 124 as heat source hot water, and the thermal energy supplied by the temperature difference between the cooling water supplied to the cold water pipe 123 of the condenser C is obtained. The absorption heat and the boiling point of the solution are used to raise the temperature of the heat medium in two steps to increase the temperature in the high-temperature absorber A2 to extremely high temperature, and the hot water separately supplied to the second hot water pipe 109 is heated. Thus, hot water having a high utility value that cannot be obtained by the conventional cycle is obtained.

FIG. 2 shows an absorption cycle diagram (hereinafter referred to as “series flow”) of the flow on the solution side of the two-stage temperature rising type absorption heat pump having the above configuration. In this series flow, a normal solution circulation system is established when the start-up is completed and normal operation is performed and each device has a pressure distribution as a heat pump. That is, the concentrated solution concentrated by the regenerator G is sent to the high-temperature absorber A2 having a high refrigerant vapor pressure by the solution pump 101, and the intermediate-concentration solution having an intermediate concentration is transferred from the high-temperature absorber A2 to the low-temperature absorber A1. Dilute solution diluted with the low temperature absorber A1 flows from the low temperature absorber A1 to the regenerator G with the refrigerant vapor pressure difference between the two.
Japanese Patent Publication No.58-18574

  In the above series flow, the solution is not supplied to the low-temperature absorber at the start-up, and the cooling medium of the low-temperature absorber A1 is heated by the condensation heat of the refrigerant vapor from the low-temperature evaporator E1, and this cooling medium Is lower than the evaporation temperature of the low temperature evaporator E1. In the high-temperature evaporator E2, refrigerant vapor is generated using this cooling medium as a heat source, or the cooling medium itself becomes refrigerant vapor and is absorbed by the high-temperature absorber A2. Therefore, the refrigerant vapor pressure of the high temperature absorber A2 is lower than the vapor pressure of the low temperature absorber A1 (same as the vapor pressure of the low temperature steam generator E1). The flow of the intermediate concentration solution to the absorber A1 does not occur. If the height of the high temperature absorber A2 is suppressed, the startup cannot be performed or the startup time is required.

  Patent Document 1 also shows solution-side equipment such as an absorption cycle diagram shown in FIG. 3 (hereinafter referred to as “reverse flow”) and an absorption cycle diagram shown in FIG. 4 (hereinafter referred to as “parallel flow”). Has been. Since the solution is introduced into the low-temperature absorber A1 at the start of operation, the cooling medium of the low-temperature absorber A1 becomes higher than the refrigerant temperature of the low-temperature evaporator E1, and the solution can be circulated. However, the reverse flow of FIG. 3 has a problem that two solution pumps are required. On the other hand, in the parallel flow of FIG. 4, only one solution pump may be used, but the concentration ranges of the low-temperature absorber A1 and the high-temperature absorber A2 become large, and the outlet concentrations of both absorbers become almost dilute solution concentrations. The solution temperature at the vessel outlet is lower than the series flow of FIG. 2 or the solution temperature of FIG. That is, there is a problem that the temperature raising capability as a heat pump is reduced.

  The present invention has been made in view of the above points, eliminates the above-mentioned problems, suppresses the height of the machine of the heat pump, and is excellent in temperature rise performance and start-up characteristics. Particularly, the high temperature medium is in the form of high temperature steam. It aims at providing the two-stage temperature rising type absorption heat pump which can be obtained by this.

In order to achieve the above object, the invention described in claim 1 mainly includes a high temperature absorber, a low temperature absorber, a high temperature evaporator, a low temperature evaporator, a regenerator, a condenser, a high temperature solution heat exchanger, and a low temperature solution heat exchanger. Comprising as a component device, introducing the concentrated solution of the regenerator into the high temperature absorber via the heated side of the low temperature solution heat exchanger and the heated side of the high temperature solution heat exchanger, The condensed refrigerant liquid is introduced into the low temperature evaporator and the high temperature evaporator, the refrigerant vapor generated in the low temperature evaporator is introduced into the low temperature absorber, and the refrigerant vapor generated in the high temperature evaporator is introduced into the high temperature absorber. An intermediate concentration solution in which the refrigerant vapor is absorbed into the concentrated solution by the high temperature absorber to an intermediate concentration is introduced into the low temperature side absorber via the heating side of the high temperature solution heat exchanger, and the low temperature Absorbing refrigerant vapor in the intermediate concentration solution with an absorber The solution thus obtained is introduced into the regenerator via the heating side of the low-temperature solution heat exchanger, the refrigerant vapor generated in the regenerator is introduced into the condenser, and the temperature is increased by two stages. A two-stage temperature rising type absorption heat pump, wherein a part of the concentrated solution from the regenerator heated by the low temperature solution heat exchanger and introduced into the high temperature absorber is branched , It mixes , introduce | transduces into the said low temperature absorber, The heat | fever which a refrigerant | coolant vapor | steam is absorbed by this mixed solution and generate | occur | produces is supplied to the high temperature evaporator, It is characterized by the above-mentioned.

According to a second aspect of the invention, the two-stage heating type absorption heat pump of claim 1, heating the heated medium in a solution of the hot absorber, characterized in that the vapor.

The invention according to claim 3 is the two-stage temperature rising type absorption heat pump according to claim 1 or 2 , wherein the flow rate of the concentrated solution introduced by branching to the low-temperature absorber is the total concentrated flow from the regenerator. It is characterized by being 5-50% of the solution flow rate.

According to the invention described in claim 1, a part of the concentrated solution from the regenerator heated by the low temperature solution heat exchanger and introduced into the high temperature absorber is branched , mixed with the total flow rate of the intermediate concentration solution, and Since it was introduced into the low-temperature absorber and the heat generated by the refrigerant vapor being absorbed into the mixed solution was supplied into the high-temperature evaporator , the solution temperature of the low-temperature absorber was higher than the refrigerant temperature of the low-temperature evaporator even during startup. also becomes a high temperature, therefore the difference between the high temperature absorber in vapor pressure and low temperature absorber the vapor pressure is increased, the intermediate concentration solution in the hot absorber easily flows to the cold absorber, the height of the absorption refrigerator In addition, it is possible to provide a two-stage temperature rising type absorption heat pump excellent in temperature rising performance and starting characteristics.

According to the second aspect of the present invention, since the heated medium is heated with the solution of the high-temperature absorber to form steam, the high-temperature medium is obtained with the heated medium with a small flow rate, and the heated medium is supplied. Can save power.

According to the invention described in claim 3 , since the flow rate of the concentrated solution introduced after being branched into the low-temperature absorber is 5 to 50% of the total concentrated solution flow rate from the regenerator, it takes time to start. Even if the introduction of the concentrated solution is continued after the completion of the start-up, the decrease in the heating capability can be ignored.

  Embodiments of the present invention will be described below with reference to the drawings.

  FIG. 5 is a diagram showing a configuration example of a two-stage temperature rising type absorption heat pump according to the present invention. As shown in the figure, the two-stage temperature rising type absorption heat pump is composed mainly of a high temperature absorber AH, a low temperature absorber A, a high temperature evaporator EH, a low temperature evaporator E, a regenerator G, a condenser C, and a high temperature solution heat exchange. And a low-temperature solution heat exchanger X1.

  The concentrated solution of the regenerator G is introduced into the high temperature absorber AH by the solution pump 1 through the concentrated solution tube 2, the heated side of the low temperature solution heat exchanger X1, and the heated side of the high temperature solution heat exchanger X2. It has become. The condensed refrigerant liquid in the condenser C is introduced by the refrigerant pump 3 through the refrigerant pipe 4 and the control valve 5 into the low temperature evaporator E, and through the refrigerant pipe 4 and the control valve 6 into the high temperature evaporator EHS. ing. The refrigerant vapor generated in the low temperature evaporator E is introduced into the low temperature absorber A through the flow path 7, and the refrigerant vapor generated in the high temperature evaporator EHS is introduced into the high temperature absorber AH through the flow path 8. It has become.

  The spray 9 is arranged in the high temperature absorber AH, the concentrated solution introduced by the concentrated solution tube 2 is sprayed from the spray 9 into the high temperature absorber AH, and the refrigerant vapor from the high temperature evaporator EHS is sprayed. The concentrated solution is absorbed into the concentrated solution to become an intermediate concentration solution, and the concentrated solution passing through the concentrated solution tube 2 through the heating side of the intermediate concentration solution tube 10 and the high temperature solution heat exchanger X2 is heated. 12 is introduced into the low-temperature absorber A. The introduced intermediate concentration solution is sprayed from the spray 13 disposed in the low temperature absorber A. As a result, the refrigerant vapor from the low temperature evaporator E is absorbed by the intermediate concentration solution and becomes a dilute solution.

  The dilute solution in the low temperature absorber A is introduced into the regenerator G through the dilute solution pipe 14 and the heating side of the low temperature solution heat exchanger X1, and the regenerator is supplied from the spray 15 provided in the regenerator G. It is spread | dispersed on the hot water pipe | tube 16 arrange | positioned in G. The sprayed dilute solution is heated by the hot water 203 supplied to the hot water pipe 16, and refrigerant vapor is generated and concentrated to become a concentrated solution. The generated refrigerant vapor is introduced into the condenser C through the flow path 17 and is cooled and condensed by the cooling water 204 passing through the cold water pipe 18 disposed in the condenser C to be a condensed refrigerant liquid.

  Inside each of the low temperature absorber A and the high temperature evaporator EHS, heat exchange pipes 20 and 21 are disposed, and the heat exchange pipes 20 and 21 are connected to the working medium transport pipes 19 and 19 for circulation. The working medium circulates through the heat exchange pipes 20 and 21 by the pump 22. Due to the circulation of the working medium, the heat generated in the low temperature absorber A is sent to the high temperature evaporator EHS. A spray 23 is disposed in the high-temperature evaporator EHS, and a refrigerant liquid introduced through the control valve 6 is supplied to the spray 23 and circulated. Further, the refrigerant liquid in the high-temperature evaporator EHS is also supplied to the spray 23 by the refrigerant pump 24. By spraying the refrigerant liquid from the spray 23 onto the heat exchanging pipe 21, the refrigerant liquid is heated and evaporated by the working medium circulating in the heat exchanging pipe 21, and the evaporated refrigerant vapor flows as described above. It is introduced into the high-temperature absorber AH through the path 8.

  Further, a hot water pipe 25 is disposed in the low temperature evaporator E, the refrigerant liquid in the low temperature evaporator E is heated by the hot water supplied to the hot water pipe, and the generated refrigerant vapor is absorbed at a low temperature as described above. Introduced into vessel A. Further, the concentrated solution sent through the concentrated solution pipe 2 is heated through the heated side of the low temperature solution heat exchanger X1, and then partially branched by the branch pipe 26 and introduced into the low temperature absorber A. It has become. The flow rate of the concentrated solution to be introduced is restricted by the orifice 27.

  The high temperature absorber AH is provided with a liquid level sensor 28 for detecting the liquid level, and the detection signal of the liquid level sensor 28 is input to the inverter 29 so that the rotation speed of the solution pump 1 can be controlled. ing. Further, the low-temperature absorber A is provided with a liquid level sensor 30 for detecting the outlet liquid level, and a detection signal of the liquid level sensor 30 is input to the control valve 12 so that the opening degree can be controlled. . Further, the low-temperature evaporator E is provided with a liquid level sensor 31 for detecting the liquid level, and a detection signal of the liquid level sensor 31 is input to the control valve 5 so that the opening degree can be controlled. Further, the high temperature evaporator EHS is provided with a liquid level sensor 32 for detecting the liquid level, and a detection signal of the liquid level sensor 32 is inputted to the control valve 6 so that the opening degree thereof can be controlled.

  A pipe 33 for supplying water as a medium to be heated is disposed in the high-temperature absorber AH. Water is supplied from the gas-liquid separator 35 to the pipe 33 by the pump 34 and heated, and the generated steam passes through the pipe 36. Then, it is guided to the gas-liquid separator 35 and the steam 201 is discharged from the steam discharge pipe 37. The gas-liquid separator 35 is supplied with water 202 as a heating medium through a water supply pipe 39 by a water supply pump 38. Water 202 passing through the water supply pipe 39 is heated by the heat exchanger 40 with hot water 203 passing through the hot water pipe 41, heated by the dilute solution passing through the dilute solution pipe 14 by the heat exchanger 42, and introduced into the gas-liquid separator 35. It has come to be. The gas-liquid separator 35 is provided with a liquid level sensor 43 for detecting the liquid level, and the detection signal is input to an inverter of a feed water pump 38 driven by an inverter (not shown), for example, so that the pump rotation speed can be controlled. It has become.

  In the two-stage temperature rising absorption heat pump configured as described above, hot water 203 as a heat source is supplied to the hot water pipe 16 of the regenerator G and the hot water pipe 25 of the low temperature evaporator E, and cooling water 204 is supplied to the cold water pipe of the condenser C. To do. After the concentrated solution in the regenerator G is heated by the low temperature solution heat exchanger X1 by the solution pump 1, a part is branched by the branch pipe 26 to the low temperature absorber A, and the rest is heated by the high temperature solution heat exchanger X2. To the high temperature absorber AH via the side. In the high-temperature absorber AH, the concentrated solution is sprayed from the spray 9 and absorbs the vapor from the high-temperature evaporator EHS to generate heat of absorption, and the concentrated solution becomes a diluted intermediate-concentration solution, and high-temperature solution heat exchange It is led to the low-temperature absorber A via the heating side of the vessel X2. In the low temperature absorber A, the concentrated solution branched by the branch pipe 26 and the intermediate concentration solution from the high temperature absorber AH are mixed, sprayed from the spray 13 and absorbs the refrigerant vapor from the low temperature evaporator E to generate absorption heat. Diluted into a dilute solution. The dilute solution returns to the regenerator G via the heating side of the low temperature solution heat exchanger X1.

  The cooling side of the low temperature absorber A is a heat supply part of the high temperature evaporator EHS. That is, the working medium passing through the heat exchanging pipe 20 is heated by the absorption heat generated by absorbing the refrigerant vapor from the low temperature evaporator E in the mixed solution sprayed by the absorber spray 13, and the heated operation is performed. The medium is sent to the heat exchange pipe 21 of the high temperature evaporator EHS, the absorption heat generated by the low temperature absorber A is supplied to the high temperature evaporator EHS, and the refrigerant liquid sprayed on the heat exchange pipe 21 by the spray 23 is supplied. It comes to heat. In the low temperature evaporator E, the refrigerant liquid is heated by the hot water passing through the hot water pipe 25, and refrigerant vapor is generated.

  As described above, since the concentrated solution is also supplied to the low temperature absorber as described above, the refrigerant vapor from the low temperature evaporator E is absorbed, the temperature of the dilute solution rises, and the working medium passing through the heat exchange pipe 20 is heated. Is done. This temperature is higher than the vapor of the low temperature evaporator E, and the refrigerant vapor dispersed and evaporated on the heat exchange pipe 21 by the spray 23 in the high temperature evaporator EH is higher than the vapor of the low temperature evaporator E. Thus, the vapor pressure of the high temperature evaporator EHS is higher than that of the low temperature evaporator. The high temperature absorber AH is at the same pressure as the high temperature evaporator EHS, and the low temperature absorber is at the same pressure as the low temperature evaporator E. Therefore, the vapor pressure of the high temperature absorber AH is higher than that of the low temperature absorber A, and the flow of the solution from the high temperature absorber AH to the low temperature absorber A is ensured.

  The flow rate of the concentrated solution branched by the branch tube 26 and introduced into the low temperature absorber A is set to about 5 to 50% of the flow rate of the concentrated solution supplied from the regenerator G through the concentrated solution tube 2. When the flow rate of the concentrated solution is small, startup takes time, but even if the concentrated solution introduction is continued even after the startup is completed, a decrease in the temperature rise capability can be ignored. FIG. 6 is an absorption cycle diagram when the concentrated solution introduction is continued even after the start-up is completed (the absorption cycle diagram shown in FIG. 2). On the other hand, when the flow rate of the concentrated solution is large, it is necessary to stop the concentrated solution introduction after the start-up is completed. If the introduction of the concentrated solution is continued, the temperature rise capability is greatly reduced, and is about the same as the parallel flow (see FIG. 4).

  In the two-stage temperature rising type absorption heat pump, the concentrated solution branched from the concentrated solution tube 2 and introduced into the low temperature absorber A is mixed with the intermediate concentration solution from the high temperature absorber AH and introduced into the low temperature absorber A. However, the position may be changed separately so that the concentrated solution is first mixed into the inlet portion and the intermediate concentration solution is mixed from the intermediate portion.

  The flow of the concentrated solution is controlled by controlling the rotational speed of the solution pump 1 by the output of the liquid level sensor so that the outlet liquid level of the high temperature absorber AH becomes substantially constant, and the concentrated solution at the outlet of the regenerator G is heated to a high temperature. It is sent to the absorber AH. The intermediate concentration solution flow rate from the high temperature absorber AH to the low temperature absorber A is controlled by the detection output of the liquid level sensor 30 so that the outlet liquid level of the high temperature absorber AH is substantially constant. The opening degree of the valve 12 is controlled, and the solution flow rate from the high temperature absorber AH is adjusted.

  FIG. 7 is a view showing another configuration example of the two-stage temperature rising type absorption heat pump according to the present invention. In FIG. 7, the same reference numerals as those in FIG. 5 denote the same or corresponding parts. 7 differs from that of FIG. 5 in that the high-temperature evaporator EHS and the low-temperature absorber A in FIG. 5 are configured separately and are used for heat exchange through the working medium transport pipes 19 and 19. The heat of the low-temperature absorber A is transferred to the high-temperature evaporator EHS by the working medium circulating through the pipe 20 and the heat exchange pipe 21, but in FIG. 7, the high-temperature evaporator EHS and the low-temperature absorber A are integrated. The refrigerant liquid of the high-temperature evaporator EHS is sent to the heat exchange pipe 45 of the low-temperature absorber A through the refrigerant transport pipe 44, and is evaporated by heating to send the refrigerant vapor to the high-temperature evaporator EHS through the refrigerant transport pipe 44. Reference numeral 46 denotes a baffle provided inside the high temperature evaporator EHS.

  In the two-stage temperature rising type absorption heat pump shown in FIG. 7, since the concentrated solution is also supplied to the low temperature absorber A at the start-up, the refrigerant vapor from the low temperature evaporator E is absorbed, the temperature of the diluted solution rises, The refrigerant liquid passing through the replacement pipe 45 is heated. This heating temperature is higher than the vapor of the low temperature evaporator E, the evaporated refrigerant vapor is higher than the vapor of the low temperature evaporator E, and the vapor pressure of the high temperature evaporator EHS is higher than that of the low temperature evaporator. become. The high temperature absorber AH is at the same pressure as the high temperature evaporator EHS, and the low temperature absorber is at the same pressure as the low temperature evaporator E. Therefore, the vapor pressure of the high temperature absorber AH is higher than that of the low temperature absorber A, and the flow of the solution from the high temperature absorber AH to the low temperature absorber A is ensured.

  The flow rate of the concentrated solution branched by the branch tube 26 and introduced into the low temperature absorber A is set to about 5 to 50% of the flow rate of the concentrated solution supplied from the regenerator G through the concentrated solution tube 2. When the flow rate of the concentrated solution is small, startup takes time, but even if the concentrated solution introduction is continued even after the startup is completed, a decrease in the temperature rise capability can be ignored. The absorption cycle diagram when the introduction of the concentrated solution is continued even after the start-up is completed is the same as FIG. On the other hand, when the flow rate of the concentrated solution is large, it is necessary to provide a valve in the branch pipe 26 and stop the concentrated solution introduction after the start-up is completed.

  The refrigerant level level of the high-temperature evaporator EHS is detected by the liquid level sensor 32, and the detection signal is input to the control valve 6, and the opening degree is adjusted so that the refrigerant level of the high-temperature evaporator EHS becomes a set value. Control. By constructing the two-stage temperature rising type absorption heat pump as shown in FIG. 7, compared with FIG. 5, a circulating pump 22 for circulating the working medium in order to send the heat of the low temperature absorber A to the high temperature evaporator EHS or a high temperature The refrigerant pump 24 that circulates the refrigerant liquid of the evaporator EHS is not necessary, the configuration is simplified, and the manufacturing cost and running cost are reduced. Further, it is possible to eliminate temperature loss when heat exchange is performed between the working medium and the refrigerant by EHS.

  Although the embodiments of the present invention have been described above, the present invention is not limited to the above-described embodiments, and various modifications can be made within the scope of the technical idea described in the claims and the specification and drawings. Is possible. For example, in the above-described embodiment, a gas-liquid separator is provided, and steam generated by heating water as a medium to be heated by the high-temperature absorber AH is led to discharge the vapor 201 separated by gas-liquid. It is not necessary to provide a liquid separator. Moreover, you may make it obtain in the form of a high temperature liquid instead of heating a to-be-heated medium in the form of a vapor | steam.

It is a figure which shows the structural example of the conventional two-step temperature rising type absorption heat pump. It is a figure which shows the example of the solution side absorption cycle diagram of a two-step temperature rising type absorption heat pump. It is a figure which shows the example of the solution side absorption cycle diagram of a two-step temperature rising type absorption heat pump. It is a figure which shows the example of the solution side absorption cycle diagram of a two-step temperature rising type absorption heat pump. It is a figure which shows the structural example of the two-step temperature rising type absorption heat pump which concerns on this invention. Example 1 It is a figure which shows the example of the solution side absorption cycle diagram of the two-step temperature rising type absorption heat pump which concerns on this invention. It is a figure which shows the structural example of the two-step temperature rising type absorption heat pump which concerns on this invention. (Example 2)

Explanation of symbols

AH high temperature absorber A low temperature absorber EH high temperature evaporator E low temperature evaporator G regenerator C condenser X1 low temperature solution heat exchanger X2 high temperature solution heat exchanger 1 solution pump 2 concentrated solution tube 3 refrigerant pump 4 refrigerant tube 5 control valve 6 control valve 7 flow path 8 flow path 9 spray 10 medium concentration solution pipe 11 check valve 12 control valve 13 spray 14 dilute solution pipe 15 spray 16 hot water pipe 17 flow path 18 cold water pipe 19 working medium transport pipe 20 heat exchange pipe DESCRIPTION OF SYMBOLS 21 Heat exchange pipe 22 Circulation pump 23 Spray 24 Refrigerant pump 25 Hot water pipe 26 Branch pipe 27 Orifice 28 Liquid level sensor 29 Inverter 30 Liquid level sensor 31 Liquid level sensor 32 Liquid level sensor 33 Piping 34 Pump 35 Gas-liquid separator 36 Piping 37 Steam exhaust pipe 38 Water supply pump 39 Water supply pipe 40 Heat exchanger 41 Hot water pipe 42 Heat exchanger 43 Liquid Sensor 44 refrigerant conveying tube 45 heat exchange tubes 46 baffles

Claims (3)

High temperature absorber, low temperature absorber, high temperature evaporator, low temperature evaporator, regenerator, condenser, high temperature solution heat exchanger, low temperature solution heat exchanger are equipped as main components,
The concentrated solution of the regenerator is introduced into the high temperature absorber via the heated side of the low temperature solution heat exchanger and the heated side of the high temperature solution heat exchanger, and the condensed refrigerant liquid of the condenser is introduced into the low temperature Introducing into the evaporator and the high temperature evaporator, introducing the refrigerant vapor generated in the low temperature evaporator into the low temperature absorber, introducing the refrigerant vapor generated in the high temperature evaporator into the high temperature absorber, and the high temperature absorber In the concentrated solution, the refrigerant solution is absorbed and the intermediate concentration solution having an intermediate concentration is introduced into the low temperature side absorber via the heating side of the high temperature solution heat exchanger, and the intermediate concentration is A solution that has absorbed a refrigerant vapor into the solution to become a dilute solution is introduced into the regenerator via the heating side of the low-temperature solution heat exchanger, and the refrigerant vapor generated in the regenerator is introduced into the condenser. Two-stage temperature rising type absorption heat po A-flops,
A portion of the concentrated solution from the regenerator heated by the low temperature solution heat exchanger and introduced into the high temperature absorber is branched , mixed with the total flow rate of the intermediate concentration solution and introduced into the low temperature absorber , A two-stage temperature rising type absorption heat pump characterized in that heat generated by absorption of refrigerant vapor in a mixed solution is supplied into a high-temperature evaporator . In the two-stage temperature rising type absorption heat pump according to claim 1 ,
A two-stage temperature rising type absorption heat pump, wherein a medium to be heated is heated with a solution of the high-temperature absorber to form a vapor. In the two-stage temperature rising type absorption heat pump according to claim 1 or 2 ,
A two-stage temperature rising type absorption heat pump characterized in that the flow rate of the concentrated solution introduced by branching into the low-temperature absorber is 5 to 50% of the total concentrated solution flow rate from the regenerator.

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