JP2019035560A - Absorption type heat exchange system - Google Patents

Abstract

To provide an absorption type heat exchange system for making outlet temperature of a heated fluid raising temperature higher than inlet temperature of a heat source fluid reducing temperature.SOLUTION: An absorption type heat exchange system 1 includes: an absorption part 10 for raising temperature of a first heated fluid RP by absorption heat emitted when an absorbent liquid Sa absorbs refrigerant vapor Ve; a condensation part 40 for raising temperature of a heated fluid GP by condensation heat emitted when refrigerant vapor Vg becomes a refrigerant liquid Vf; a steam part 20 for taking away evaporative latent heat required when the refrigerant liquid Vf evaporates and becomes the refrigerant vapor Ve, from a heat source fluid RS; and a reproduction part 30 for taking away heat required for heating a diluted solution Sw to bring to a concentrated solution Sa, from a heat source fluid RS. The absorption part 10 has inner pressure and temperature higher than those of the reproduction part 30 due to an absorption heat pump cycle of the absorbent liquid and the refrigerant, and a part of the heat source fluid branched from a heat source fluid RA before introducing to the vaporization part 20 and the reproduction part 30 is introduced as the first heated fluid RP to the absorption part 10.SELECTED DRAWING: Figure 1

Description

  The present invention relates to an absorption heat exchange system, and more particularly, to an absorption heat exchange system in which heat is exchanged between two fluids so that an outlet temperature of a fluid whose temperature is increased is higher than an inlet temperature of a fluid whose temperature is decreased.

  A heat exchanger is widely used as a device for exchanging heat between a hot fluid and a cold fluid. In a heat exchanger in which heat is directly exchanged between two fluids, the outlet temperature of the low temperature fluid cannot be higher than the inlet temperature of the high temperature fluid (see, for example, Patent Document 1).

Japanese Patent No. 5498809 (see FIG. 11 etc.)

  One application of heat exchangers is to recover waste heat. Since exhaust heat is heat that is discarded without being used, the outlet temperature of the fluid that recovers the exhaust heat and raises the temperature is higher than the inlet temperature of the fluid that loses heat and includes the exhaust heat. If the temperature can be increased, the range of utilization will expand.

  In view of the above-described problems, the present invention has an object to provide an absorption heat exchange system that can increase the outlet temperature of the heated fluid that raises the temperature higher than the inlet temperature of the heating source fluid that lowers the temperature. To do.

  In order to achieve the above object, the absorption heat exchange system according to the first aspect of the present invention is a dilute solution in which, for example, as shown in FIG. An absorption section 10 that raises the temperature of the first heated fluid RP by the absorbed heat released when it becomes Sw; and a second heat by the condensation heat released when the refrigerant vapor Vg condenses into the refrigerant liquid Vf. Condensing section 40 for raising the temperature of the fluid GP to be heated; Necessary when introducing the refrigerant liquid Vf from the condensing section 40 and evaporating the introduced refrigerant liquid Vf into the refrigerant vapor Ve supplied to the absorption section 10 Evaporating part 20 for lowering the temperature of heating source fluid RS by taking away the latent heat of evaporation from heating source fluid RS; introducing diluted solution Sw from absorbing part 10; heating the introduced diluted solution Sw; refrigerant from diluted solution Sw Vg was released and the concentration increased A regenerator 30 that lowers the temperature of the heating source fluid RS by removing the heat necessary to obtain the solution Sa from the heating source fluid RS; an absorption heat pump of the absorbing liquids Sa and Sw and the refrigerants Ve, Vf, and Vg Depending on the cycle, the absorption unit 10 has a higher internal pressure and temperature than the regeneration unit 30, and the evaporation unit 20 is configured to have a higher internal pressure and temperature than the condensation unit 40; the evaporation unit 20 and the regeneration unit 30. A part of the heating source fluid branched from the heating source fluid RA before being introduced into the absorber is introduced into the absorber 10 as the first heated fluid RP.

  With this configuration, a part of the heating source fluid branched from the heating source fluid before being introduced into the evaporation unit and the regeneration unit is introduced into the absorption unit as the first heated fluid, and thus flows out of the absorption unit. The temperature of the first heated fluid can be made higher than the temperature of the heating source fluid before being introduced into the evaporation unit and the regeneration unit.

  Moreover, when the absorption heat exchange system according to the second aspect of the present invention is shown with reference to FIG. 1, for example, in the absorption heat exchange system 1 according to the first aspect of the present invention, from the absorption unit 10. The flow rate of the heating source fluid RS flowing into the evaporation unit 20 and the regeneration unit 30 and the absorption unit 10 as the first heated fluid RP so that the temperature of the first heated fluid RP that has flowed out becomes a predetermined temperature. The ratio with the flow rate of the heating source fluid RP to be set is set.

  If comprised in this way, the temperature of the 1st to-be-heated fluid which flowed out from the absorption part can be adjusted.

  Further, the absorption heat exchange system according to the third aspect of the present invention is, for example, as shown in FIG. 1, in the absorption heat exchange system 1 according to the first aspect or the second aspect of the present invention. The second heated fluid GP flowing out from the section 40 is configured to mix with the heating source fluid RS flowing out from at least one of the evaporation section 20 and the regeneration section 30.

  With this configuration, it is possible to balance the flow rate of the heating source fluid flowing into the absorption heat exchange system and the flow rate of the heating source fluid flowing out of the absorption heat exchange system.

  In addition, the absorption heat exchange system according to the fourth aspect of the present invention is, for example, as shown in FIG. 2, the absorption heat heat according to any one of the first to third aspects of the present invention. In the exchange system 2, the first heated fluid RP before introducing a part of the second heated fluid GPd branched from the second heated fluid GP flowing out from the condensing unit 40 into the absorption unit 10. And a partially heated fluid bypass channel 48 to be joined.

  With this configuration, the system configuration can be simplified.

  Moreover, when the absorption heat exchange system according to the fifth aspect of the present invention is shown, for example, with reference to FIG. 2, in the absorption heat exchange system 2 according to the fourth aspect of the present invention, from the absorption unit 10. A heating source that has flowed out of at least one of the evaporation unit 20 and the regeneration unit 30 of the second heated fluid GP that has flowed out from the condensing unit 40 so that the temperature of the first heated fluid RP that has flowed out becomes a predetermined temperature. The ratio between the flow rate mixed with the fluid RS and the flow rate flowing through the partially heated fluid bypass flow path 48 is set.

  If comprised in this way, the balance of the temperature and flow volume of the 1st to-be-heated fluid which flowed out from the absorption part can be adjusted.

  In addition, the absorption heat exchange system according to the sixth aspect of the present invention is, for example, as shown in FIG. 3, the absorption heat heat according to any one of the first to fifth aspects of the present invention. In the exchange system 3, refrigerant heat causing heat exchange between the refrigerant liquid Vf conveyed from the condenser 40 to the evaporator 20 and the heating source fluid RS flowing out from at least one of the evaporator 20 and the regenerator 30. An exchange 99 is provided.

  If comprised in this way, the temperature of the heating source fluid which flows out out of an absorption heat exchange system can be lowered | hung, and the quantity of heat collect | recovered from a heating source fluid in an absorption heat exchange system can be increased.

  According to the present invention, since a part of the heating source fluid branched from the heating source fluid before being introduced into the evaporation unit and the regeneration unit is introduced into the absorption unit as the first heated fluid, it flows out of the absorption unit The temperature of the first heated fluid can be made higher than the temperature of the heating source fluid before being introduced into the evaporation unit and the regeneration unit.

1 is a schematic system diagram of an absorption heat exchange system according to a first embodiment of the present invention. It is a typical systematic diagram of the absorption heat exchange system which concerns on the 2nd Embodiment of this invention. It is a typical systematic diagram of the absorption heat exchange system which concerns on the 3rd Embodiment of this invention. It is a typical systematic diagram of the absorption heat exchange system which concerns on the modification of the 1st Embodiment of this invention.

  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 heat exchange system 1 which concerns on the 1st Embodiment of this invention is demonstrated. FIG. 1 is a schematic system diagram of an absorption heat exchange system 1. The absorption heat exchange system 1 uses the absorption heat pump cycle of the absorption liquid and the refrigerant, and the temperature of the temperature increase target fluid RP flowing out from the absorption heat exchange system 1 toward the heat utilization device HCF is used as a drive heat source. In this system, heat is transferred so as to be higher than the temperature of the drive heat source fluid RS flowing into the absorption heat exchange system 1. Here, the temperature increase target fluid RP is a fluid to be increased in temperature in the absorption heat exchange system 1 and corresponds to a first heated fluid. The driving heat source fluid RS is a fluid whose temperature decreases in the absorption heat exchange system 1 and corresponds to a heating source fluid. The absorption heat exchange system 1 includes an absorber 10, an evaporator 20, and a regenerator 30 that constitute main equipment in which an absorption heat pump cycle of the absorbing liquid S (Sa, Sw) and the refrigerant V (Ve, Vg, Vf) is performed. , And a condenser 40. The absorber 10, the evaporator 20, the regenerator 30, and the condenser 40 correspond to an absorption unit, an evaporation unit, a regeneration unit, and a condensation unit, respectively.

In the present specification, the absorption liquid is referred to as “dilute solution Sw”, “concentrated solution Sa” or the like in accordance with the property or the position on the heat pump cycle in order to facilitate distinction on the heat pump cycle. In general, the term “absorbing liquid S” is used. Similarly, regarding the refrigerant, in order to easily distinguish on the heat pump cycle, “evaporator refrigerant vapor Ve”, “regenerator refrigerant vapor Vg”, “refrigerant liquid Vf”, etc., depending on the properties and the position on the heat pump cycle. However, when the properties and the like are not asked, they are collectively referred to as “refrigerant V”. In the present embodiment, an LiBr aqueous solution is used as the absorbing liquid S (a mixture of the absorbent and the refrigerant V), and water (H ₂ O) is used as the refrigerant V.

  The absorber 10 includes a heat transfer tube 12 that constitutes a flow path of the temperature increase target fluid RP and a concentrated solution supply device 13 that supplies the concentrated solution Sa to the surface of the heat transfer tube 12. The heat transfer pipe 12 has one end connected to the temperature rising fluid introduction pipe 51 and the other end connected to the temperature rising fluid outflow pipe 19. The temperature rising fluid introduction pipe 51 is a pipe constituting a flow path for guiding the temperature rising target fluid RP to the heat transfer pipe 12. The temperature rising fluid introduction pipe 51 is provided with a temperature rising fluid valve 51v for adjusting the flow rate of the temperature rising target fluid RP flowing inside. The temperature rising fluid outflow pipe 19 is a pipe constituting a flow path for flowing the temperature rising target fluid RP heated by the absorber 10. The absorber 10 generates absorbed heat when the concentrated solution Sa is supplied from the concentrated solution supply device 13 to the surface of the heat transfer tube 12 and the concentrated solution Sa absorbs the evaporator refrigerant vapor Ve to become the diluted solution Sw. The absorption target fluid RP that flows through the heat transfer pipe 12 receives the absorbed heat, and the temperature increase target fluid RP is heated.

  The evaporator 20 has a heat source pipe 22 constituting a flow path of the driving heat source fluid RS inside the evaporator can body 21. The evaporator 20 does not have a nozzle for spraying the refrigerant liquid Vf inside the evaporator can body 21. For this reason, the heat source pipe 22 is disposed so as to be immersed in the refrigerant liquid Vf stored in the evaporator can body 21 (full liquid evaporator). A drive heat source introduction tube 52 is connected to one end of the heat source tube 22. The drive heat source introduction pipe 52 is a pipe constituting a flow path that guides the drive heat source fluid RS to the heat source pipe 22. The drive heat source introduction pipe 52 is provided with a drive heat source valve 52v that adjusts the flow rate of the drive heat source fluid RS flowing inside. The other end of the drive heat source introduction pipe 52 is connected to the heat source fluid inflow pipe 55 together with the other end of the temperature rising fluid introduction pipe 51. The heat source fluid inflow pipe 55 is a pipe constituting a flow path through which the combined heat source fluid RA flows. The combined heat source fluid RA flowing through the heat source fluid inflow pipe 55 is divided and flows into the temperature rising fluid introduction pipe 51 and the drive heat source introduction pipe 52. That is, the temperature increase target fluid RP flows into the temperature rising fluid introduction pipe 51 of the combined heat source fluid RA, and the drive heat source fluid RS flows into the drive heat source introduction pipe 52 of the combined heat source fluid RA. Is. The evaporator 20 is configured such that the refrigerant liquid Vf around the heat source pipe 22 is evaporated by the heat of the driving heat source fluid RS flowing in the heat source pipe 22 to generate the evaporator refrigerant vapor Ve. A refrigerant liquid pipe 45 that supplies the refrigerant liquid Vf into the evaporator can body 21 is connected to the evaporator can body 21.

  The absorber 10 and the evaporator 20 are in communication with each other. By connecting the absorber 10 and the evaporator 20, the evaporator refrigerant vapor Ve generated in the evaporator 20 can be supplied to the absorber 10.

  The regenerator 30 includes a heat source pipe 32 that flows a driving heat source fluid RS that heats the dilute solution Sw, and a dilute solution supply device 33 that supplies the dilute solution Sw to the surface of the heat source pipe 32. The driving heat source fluid RS flowing in the heat source pipe 32 is the driving heat source fluid RS after flowing in the heat source pipe 22 of the evaporator 20. The heat source pipe 22 of the evaporator 20 and the heat source pipe 32 of the regenerator 30 are connected by a driving heat source communication pipe 25 that flows the driving heat source fluid RS. A drive heat source outflow pipe 39 is connected to the end of the heat source pipe 32 of the regenerator 30 opposite to the end to which the drive heat source communication pipe 25 is connected. The drive heat source outflow pipe 39 is a pipe constituting a flow path that guides the drive heat source fluid RS to the outside of the regenerator 30. In the regenerator 30, when the dilute solution Sw supplied from the dilute solution supply device 33 is heated by the driving heat source fluid RS, the concentrated solution Sa having an increased concentration is generated from the dilute solution Sw by evaporating the refrigerant V. It is configured as follows. The refrigerant V evaporated from the dilute solution Sw is configured to move to the condenser 40 as a regenerator refrigerant vapor Vg.

  The condenser 40 has a heat transfer tube 42 through which the low-temperature heat source fluid GP flows inside the condenser can body 41. One end of the heat transfer tube 42 is connected to a low temperature heat source introduction tube 57 that constitutes a flow path for guiding the low temperature heat source fluid GP to the heat transfer tube 42. The other end of the heat transfer tube 42 is connected to one end of a low temperature heat source outflow tube 49 that constitutes a flow path through which the low temperature heat source fluid GP flowing out of the condenser 40 flows. The other end of the low temperature heat source outflow pipe 49 is connected to the heat source fluid outflow pipe 59 together with the other end of the drive heat source outflow pipe 39. The heat source fluid outflow pipe 59 is a pipe that forms a flow path through which the combined heat source fluid RA, in which the driving heat source fluid RS flowing through the driving heat source outflow pipe 39 and the low temperature heat source fluid GP flowing through the low temperature heat source outflow pipe 49 merge, flows. . The condenser 40 introduces the regenerator refrigerant vapor Vg generated in the regenerator 30, and the low-temperature heat source fluid GP flowing in the heat transfer tube 42 receives the heat of condensation released when the vapor is condensed and becomes the refrigerant liquid Vf. Thus, the low-temperature heat source fluid GP is configured to be heated. The low-temperature heat source fluid GP corresponds to a second heated fluid. The can body of the regenerator 30 and the condenser can body 41 are integrally formed so that the regenerator 30 and the condenser 40 communicate with each other. By connecting the regenerator 30 and the condenser 40, the regenerator refrigerant vapor Vg generated in the regenerator 30 can be supplied to the condenser 40.

  The portion where the concentrated solution Sa of the regenerator 30 is stored and the concentrated solution supply device 13 of the absorber 10 are connected by a concentrated solution tube 35 through which the concentrated solution Sa flows. The concentrated solution pipe 35 is provided with a solution pump 35p that pumps the concentrated solution Sa. The portion of the absorber 10 where the dilute solution Sw is stored and the dilute solution supply device 33 are connected by a dilute solution tube 36 through which the dilute solution Sw flows. The concentrated solution tube 35 and the diluted solution tube 36 are provided with a solution heat exchanger 38 that performs heat exchange between the concentrated solution Sa and the diluted solution Sw. The portion of the condenser 40 in which the refrigerant liquid Vf is stored and the evaporator can body 21 are connected by a refrigerant liquid pipe 45 through which the refrigerant liquid Vf flows. The refrigerant liquid pipe 45 is provided with a refrigerant pump 46 that pumps the refrigerant liquid Vf.

  In the absorption heat exchange system 1, during steady operation, the pressure and temperature inside the absorber 10 are higher than the pressure and temperature inside the regenerator 30, and the pressure and temperature inside the evaporator 20 are It becomes higher than the internal pressure and temperature. In the absorption heat exchange system 1, the absorber 10, the evaporator 20, the regenerator 30, and the condenser 40 are configured as a second type absorption heat pump.

  In this embodiment, the heat source fluid inflow pipe 55 and the heat source fluid outflow pipe 59 are connected to the heat source equipment HSF. The heat source facility HSF is a facility that recovers exhaust heat from, for example, an ironworks or a power plant. In the present embodiment, the heat source facility HSF heats the combined heat source fluid RA taken from the heat source fluid outflow pipe 59 with exhaust heat to increase the temperature and supplies the heat source fluid RA to the heat source fluid inflow pipe 55. In the present embodiment, the temperature rising fluid outflow pipe 19 and the low temperature heat source introduction pipe 57 are connected to the heat utilization facility HCF. The heat utilization facility HCF is used, for example, to use introduced heat for heating or as a heat source for heat source devices such as other absorption refrigerators and absorption heat pumps. In the present embodiment, the heat utilization facility HCF uses the heat held by the temperature rise target fluid RP introduced from the temperature rise fluid outflow pipe 19, and removes the fluid whose temperature has been lowered by taking heat away from the temperature rise target fluid RP. It flows out to the low-temperature heat source introduction pipe 57 as the low-temperature heat source fluid GP.

  With continued reference to FIG. 1, the operation of the absorption heat exchange system 1 will be described. First, the absorption heat pump cycle on the refrigerant side will be described. In the condenser 40, the regenerator refrigerant vapor Vg evaporated in the regenerator 30 is received, and the regenerator refrigerant vapor Vg is cooled and condensed by the low-temperature heat source fluid GP flowing through the heat transfer pipe 42 to become a refrigerant liquid Vf. At this time, the temperature of the low-temperature heat source fluid GP rises due to the condensation heat released when the regenerator refrigerant vapor Vg condenses. The condensed refrigerant liquid Vf is sent to the evaporator can body 21 by the refrigerant pump 46. The refrigerant liquid Vf sent to the evaporator can body 21 is heated by the driving heat source fluid RS flowing in the heat source pipe 22 and evaporated to become the evaporator refrigerant vapor Ve. At this time, the driving heat source fluid RS is deprived of heat by the refrigerant liquid Vf, and the temperature is lowered. The evaporator refrigerant vapor Ve generated in the evaporator 20 moves to the absorber 10 that communicates with the evaporator 20.

  Next, the absorption heat pump cycle on the solution side will be described. In the absorber 10, the concentrated solution Sa is supplied from the concentrated solution supply device 13, and the supplied concentrated solution Sa absorbs the evaporator refrigerant vapor Ve that has moved from the evaporator 20. The concentrated solution Sa that has absorbed the evaporator refrigerant vapor Ve is reduced in concentration to become a diluted solution Sw. In the absorber 10, heat of absorption is generated when the concentrated solution Sa absorbs the evaporator refrigerant vapor Ve. Due to this absorbed heat, the temperature increase target fluid RP flowing through the heat transfer tube 12 is heated, and the temperature of the temperature increase target fluid RP rises. The temperature rising target fluid RP flowing through the heat transfer tube 12 is originally the same combined heat source fluid RA as the source of the driving heat source fluid RS introduced into the heat source tube 22 of the evaporator 20. Therefore, the temperature of the temperature rising target fluid RP flowing through the temperature rising fluid outflow pipe 19 is higher than that of the driving heat source fluid RS flowing into the evaporator 20 and the regenerator 30 by the amount heated by the absorber 10. The concentrated solution Sa that has absorbed the evaporator refrigerant vapor Ve by the absorber 10 is reduced in concentration to become the diluted solution Sw, and is stored in the lower part of the absorber 10. The stored diluted solution Sw flows through the diluted solution tube 36 toward the regenerator 30 due to the difference in internal pressure between the absorber 10 and the regenerator 30, and heat-exchanges with the concentrated solution Sa in the solution heat exchanger 38, so that the temperature is increased. Decreases and reaches the regenerator 30.

  The dilute solution Sw sent to the regenerator 30 is supplied from the dilute solution supply device 33 and heated by the driving heat source fluid RS flowing through the heat source pipe 32, and the refrigerant in the supplied dilute solution Sw evaporates to concentrate the concentrated solution Sa. And stored in the lower part of the regenerator 30. At this time, the drive heat source fluid RS is deprived of heat by the dilute solution Sw, and the temperature decreases. The driving heat source fluid RS flowing through the heat source pipe 32 has passed through the heat source pipe 22 of the evaporator 20. The refrigerant V evaporated from the dilute solution Sw moves to the condenser 40 as the regenerator refrigerant vapor Vg. The concentrated solution Sa stored in the lower part of the regenerator 30 is pumped to the concentrated solution supply device 13 of the absorber 10 through the concentrated solution tube 35 by the solution pump 35p. The concentrated solution Sa flowing through the concentrated solution pipe 35 is heat-exchanged with the diluted solution Sw by the solution heat exchanger 38 and then rises in temperature, and then flows into the absorber 10 and supplied from the concentrated solution supply device 13. Repeat the cycle.

  A change in the temperature of the heated fluid and the heating source fluid in the process in which the absorbing liquid S and the refrigerant V perform the absorption heat pump cycle as described above will be described with a specific example. The 95 ° C. combined heat source fluid RA flowing out of the heat source facility HSF and flowing through the heat source fluid inflow pipe 55 has the divided temperature rising target fluid RP and the driving heat source fluid RS at 95 ° C., respectively. The 95 ° C. driving heat source fluid RS flowing through the driving heat source introduction pipe 52 is deprived of heat by the refrigerant liquid Vf when flowing through the heat source pipe 22 of the evaporator 20 and reaches a temperature of 88 ° C. when reaching the driving heat source communication pipe 25. Decreases. Thereafter, the driving heat source fluid RS flowing through the driving heat source communication pipe 25 is deprived of heat by the dilute solution Sw when flowing through the heat source pipe 32 of the regenerator 30, and reaches a temperature of 80 ° C. when reaching the driving heat source outflow pipe 39. descend.

  On the other hand, the temperature rising target fluid RP flowing through the temperature rising fluid introduction pipe 51 obtains the heat of absorption generated when the concentrated solution Sa absorbs the evaporator refrigerant vapor Ve when flowing through the heat transfer pipe 12 of the absorber 10. When the temperature rising fluid outflow pipe 19 is reached, the temperature rises to 100 ° C. The 100 ° C. temperature increase target fluid RP that flows through the temperature increase fluid outflow pipe 19 flows into the heat utilization facility HCF and heat is used to lower the temperature. The fluid whose temperature has been lowered by using heat in the heat utilization facility HCF flows out to the low temperature heat source introduction pipe 57 as a low temperature heat source fluid GP at 30 ° C. The low-temperature heat source fluid GP at 30 ° C. flowing through the low-temperature heat source introduction pipe 57 generates the condensation heat released when the regenerator refrigerant vapor Vg is condensed into the refrigerant liquid Vf when flowing through the heat transfer pipe 42 of the condenser 40. When the temperature reaches the low-temperature heat source outflow pipe 49, the temperature rises to 40 ° C.

  The 40 ° C. low-temperature heat source fluid GP flowing through the low-temperature heat source outflow pipe 49 is mixed with the 80 ° C. drive heat source fluid RS flowing through the drive heat source outflow pipe 39 to become a combined heat source fluid RA at 60 ° C. Flowing. In the present embodiment, the low temperature heat source fluid GP in the low temperature heat source outflow pipe 49 and the drive heat source fluid RS in the drive heat source outflow pipe 39 are mixed, so that the heated fluid and the heat source fluid entering and exiting the absorption heat exchange system 1 are mixed. The flow is balanced. The combined heat source fluid RA at 60 ° C. flowing through the heat source fluid outlet pipe 59 flows into the heat source facility HSF, recovers exhaust heat, and rises in temperature. The combined heat source fluid RA whose temperature has increased in the heat utilization facility HCF flows out to the heat source fluid inlet pipe 55 at 95 ° C., and thereafter repeats the above-described flow.

  In the absorption heat exchange system 1, the temperature relationship as described above is established, and the temperature of the temperature increase target fluid RP flowing out from the absorber 10 is a predetermined temperature (a temperature suitable for use in the heat utilization facility HCF). In this embodiment, the ratio of the flow rate of the temperature rising target fluid RP flowing through the temperature rising fluid introduction pipe 51 and the flow rate of the driving heat source fluid RS flowing through the driving heat source introduction pipe 52 is determined so as to be 100 ° C. ing. In the present embodiment, the flow rate ratio between the temperature increase target fluid RP and the drive heat source fluid RS is approximately 1: 1. In addition, when the flow rate of the temperature increase target fluid RP is relatively decreased, the temperature of the temperature increase target fluid RP increases, and when the flow rate of the temperature increase target fluid RP is increased, the temperature of the temperature increase target fluid RP decreases. Here, the flow rate ratio between the temperature rising target fluid RP flowing through the temperature rising fluid introduction pipe 51 and the driving heat source fluid RS flowing through the driving heat source introduction pipe 52 is a storage device (not shown) provided in the control device (not shown). May be set in advance, or may be configured as needed by an input device (not shown) provided in the control device. In the present embodiment, the flow rate ratio between the temperature increase target fluid RP and the drive heat source fluid RS is adjusted by adjusting the opening degrees of the temperature increase fluid valve 51v and the drive heat source valve 52v. The adjustment of the opening degree of the temperature raising fluid valve 51v and the drive heat source valve 52v is typically performed automatically by a signal from the control device based on the flow rate ratio set in the control device described above. It is good also as adjusting an opening degree manually. Instead of the temperature rising fluid valve 51v and the driving heat source valve 52v, a three-way valve may be provided at the connecting portion of the temperature rising fluid introduction pipe 51, the driving heat source introduction pipe 52, and the heat source fluid inflow pipe 55.

  The flow of the heating source fluid (merging heat source fluid RA) and the fluid to be heated (temperature increase target fluid RP, low temperature heat source fluid GP) entering and exiting the absorption heat exchange system 1 described so far is absorbed. In the heat exchanger system 1, the combined heat source fluid RA flowing out from the heat source facility HSF and flowing into the absorption heat exchange system 1 at 95 ° C. flows out from the absorption heat exchange system 1 at 60 ° C. and flows into the heat source facility HSF. The low-temperature heat source fluid GP flowing out from the heat utilization facility HCF and flowing into the absorption heat exchange system 1 at 30 ° C. flows out from the absorption heat exchange system 1 at 100 ° C. as the temperature increase target fluid RP. It flows into HCF. When the combined heat source fluid RA flowing into and out of the heat source facility HSF is regarded as a heating source fluid, and the temperature rising target fluid RP and the low temperature heat source fluid GP flowing into and out of the heat utilization device HCF are regarded as heated fluids, they are absorbed. The heat exchange system 1 can be regarded as performing a heat exchange action between the heating source fluid and the fluid to be heated, and the temperature of the heating source fluid is changed from the temperature of the fluid to be heated by the fluid to be heated. It can be regarded as a heat exchanging system that flows out after depriving the heating source fluid of the amount of heat that can be heated to a higher temperature. The higher the temperature of the heated fluid that flows out of the absorption heat exchange system 1 (the temperature increase target fluid RP), the greater the difference in the inlet / outlet temperature of the heated fluid relative to the absorption heat exchange system 1 from the inlet / outlet temperature difference of the heating source fluid. And the flow rate of the fluid to be heated (temperature rising target fluid RP) can be reduced. Further, the flow rate of the combined heat source fluid RA flowing out from the absorption heat exchange system 1 and flowing into the heat source facility HSF is equal to the flow rate of the combined heat source fluid RA flowing out from the heat source facility HSF and into the absorption heat exchange system 1 And the flow rate of the temperature-rising fluid RP that flows out from the absorption heat exchange system 1 and flows into the heat utilization device HCF, and the flow rate of the low-temperature heat source fluid GP that flows out from the heat utilization device HCF and flows into the absorption heat exchange system 1 Are equal to each other, it is considered that both the heating source fluid and the fluid to be heated flow into and out of the absorption heat exchange system 1 as independent systems partitioned in the absorption heat exchange system 1. It becomes clearer to view the absorption heat exchange system 1 as a heat exchanger. As shown in the present embodiment, the combined heat source fluid RA that has flowed out of the absorption heat exchange system 1 passes through the heat source facility HSF and is heated, and then returns to the absorption heat exchange system 1, so that the absorption heat exchange system It is preferable that the temperature-up target fluid RP flowing out from 1 passes through the heat utilization device HCF and is returned to the absorption heat exchange system 1 as the low-temperature heat source fluid GP after the heat is consumed.

  Note that the fluid that flows in and out of the heat utilization facility HCF (heated fluid) is not shunted and merged with the fluid that flows in and out of the heat source facility HSF (heating source fluid). In the case where the low-temperature heat source fluid GP that has flowed through the heat transfer tube 42 is an independent system so as to flow to the heat transfer tube 12 of the absorber 10, the low-temperature heat source fluid GP that has flowed through the heat transfer tube 42 of the condenser 40 Before flowing into the heat transfer tube 12, heat is exchanged with the driving heat source fluid RS flowing out of the evaporator 20 and the regenerator 30 or with the driving heat source fluid RS before flowing into the evaporator 20 and the regenerator 30, and the temperature is raised by heating. A heat exchanger is required. On the other hand, as in the present embodiment, the fluid flowing into and out of the heat utilization facility HCF (heated fluid) is divided and joined to the fluid flowing into and out of the heat source facility HSF (heating source fluid). As a result, the heat exchanger provided in the case of the above assumption is unnecessary, and the system configuration can be simplified. By eliminating the need for a heat exchanger provided in the case of the above assumption, a heat loss by the heat exchanger and a temperature drop of the fluid to be heated due to the heat exchange temperature efficiency being less than 1 are avoided, and the heat efficiency by the heat exchanger Can be eliminated. Furthermore, the installation space for the heat exchanger, the piping for the fluid to enter and exit the heat exchanger, and the maintenance and inspection work for the heat exchanger can also be omitted. Further, in the absorption heat exchange system 1 according to the present embodiment, a fluid (heated fluid) having a temperature lower than the fluid (heating source fluid) flowing out to the heat source facility HSF is introduced from the heat utilization facility HCF, and the heat source facility A fluid (heated fluid) having a temperature higher than that of the fluid introduced from the HSF (heating source fluid) can flow out to the heat utilization facility HCF, so that the heat can be used effectively, and the absorption heat exchange system 1 The flow rate of the fluid to be heated can be reduced by expanding the temperature difference between the inlet and outlet of the fluid to be heated.

  As described above, according to the absorption heat exchange system 1 according to the present embodiment, the temperature rise target is set so that the temperature of the temperature rise target fluid RP flowing out is higher than the temperature of the driving heat source fluid RS to be introduced. The fluid RP can be heated, and the temperature increase target fluid RP having a higher utility value than the driving heat source fluid RS can be supplied to the outside. In addition, the temperature increase target fluid RP heated by the absorber 10 is branched from the combined heat source fluid RA, and the low temperature heat source fluid GP heated by the condenser 40 is passed through the evaporator 20 and the regenerator 30 as a driving heat source fluid. Since it is merged with RS, the heat source fluid RS and the low-temperature heat source fluid GP do not exchange heat, that is, without providing a large heat exchanger, the device configuration is simplified, and the temperature is increased at a relatively high temperature. The fluid RP can be supplied (outflowed). Further, the temperature of the low temperature heat source fluid GP flowing into the absorption heat exchange system 1 and the temperature of the temperature rising target fluid RP flowing out from the inlet / outlet temperature difference of the drive heat source fluid RS flowing into and out of the absorption heat exchange system 1. And the flow rate of the temperature-rising fluid RP supplied to the heat utilization facility HCF can be reduced by an amount corresponding to the large temperature difference, and the conveyance power can be reduced.

  Next, with reference to FIG. 2, an absorption heat exchange system 2 according to a second embodiment of the present invention will be described. FIG. 2 is a schematic system diagram of the absorption heat exchange system 2. The absorption heat exchange system 2 is different from the absorption heat exchange system 1 (see FIG. 1) mainly in the following points. The absorption heat exchange system 2 is provided with a low-temperature heat source bypass pipe 48 that connects the low-temperature heat source outflow pipe 49 and the heated fluid introduction pipe 51. The low temperature heat source bypass pipe 48 is part of the low temperature heat source fluid GP flowing out from the condenser 40 and flowing through the low temperature heat source outflow pipe 49, and the temperature rising target fluid flowing through the temperature rising fluid introduction pipe 51 before flowing into the absorber 10. This is a pipe that joins the RP and corresponds to a partially heated fluid bypass flow path. Hereinafter, for convenience of explanation, the low-temperature heat source fluid GP flowing through the low-temperature heat source bypass pipe 48 may be particularly expressed by a symbol GPd to be distinguished from the low-temperature heat source fluid GP flowing through the low-temperature heat source outflow pipe 49. The low temperature heat source bypass pipe 48 is provided with a low temperature heat source bypass valve 48v that adjusts the flow rate of the low temperature heat source fluid GPd flowing inside. On the other hand, a low-temperature heat source outlet pipe 49 downstream of the connection with the low-temperature heat source bypass pipe 48 is provided with a low-temperature heat source valve 49v that adjusts the flow rate of the low-temperature heat source fluid GP flowing inside. Instead of the low temperature heat source bypass valve 48v and the low temperature heat source valve 49v, a three-way valve may be provided at the connection portion between the low temperature heat source outflow pipe 49 and the low temperature heat source bypass pipe 48. The structure of the absorption heat exchange system 2 other than the above is the same as that of the absorption heat exchange system 1 (see FIG. 1).

  In addition to the action of the absorption heat exchange system 1 (see FIG. 1), the absorption heat exchange system 2 configured as described above adjusts the opening of the low temperature heat source bypass valve 48v and the low temperature heat source valve 49v, A part GPd of the low-temperature heat source fluid GP heated by the condenser 40 is mixed with the temperature increase target fluid RP before flowing into the absorber 10. The adjustment of the opening degree of the low-temperature heat source bypass valve 48v and the low-temperature heat source valve 49v is typically a signal from the control device based on the flow rate ratio set in the control device (not shown) as in the absorption heat exchange system 1. However, the opening degree may be manually adjusted without using the control device. By adjusting the flow rate of the low-temperature heat source fluid GPd to be mixed with the temperature increase target fluid RP, the temperature and / or flow rate of the temperature increase target fluid RP flowing through the temperature increase fluid outflow pipe 19 can be adjusted. In the present embodiment, the flow rate of the low-temperature heat source fluid GPd flowing through the low-temperature heat source bypass pipe 48 and the heat source fluid outflow so that the temperature of the temperature increase target fluid RP flowing out from the absorber 10 becomes a predetermined temperature and / or flow rate. The ratio of the flow rate of the low-temperature heat source fluid GP flowing through the low-temperature heat source outlet pipe 49 toward the pipe 59 is determined. If the flow rate of the low temperature heat source fluid GPd flowing through the low temperature heat source bypass pipe 48 is relatively increased, the temperature of the temperature rising target fluid RP flowing through the temperature rising fluid outflow pipe 19 decreases and the flow rate increases, and the low temperature heat source bypass pipe If the flow rate of the low-temperature heat source fluid GPd flowing through 48 is decreased, the temperature of the temperature-rising fluid RP flowing through the temperature-rising fluid outflow pipe 19 rises and the flow rate decreases. When the flow rate of the low temperature heat source fluid GPd flowing through the low temperature heat source bypass pipe 48 is increased, the temperature of the temperature increase target fluid RP flowing through the temperature increase fluid outflow pipe 19 decreases as described above, but the flow rate increases. The amount of heat held by the temperature rising target fluid RP flowing through the outflow pipe 19 can be increased.

  Next, an absorption heat exchange system 3 according to a third embodiment of the present invention will be described with reference to FIG. FIG. 3 is a schematic system diagram of the absorption heat exchange system 3. The absorption heat exchange system 3 is different from the absorption heat exchange system 2 (see FIG. 2) mainly in the following points. The absorption heat exchange system 3 includes a refrigerant heat exchanger 99 in addition to the configuration of the absorption heat exchange system 2 (see FIG. 2). The refrigerant heat exchanger 99 is a device that exchanges heat between the refrigerant liquid Vf that travels from the condenser 40 toward the evaporator 20 and the fluid that includes the driving heat source fluid RS that has flowed out of the regenerator 30. In the present embodiment, the drive heat source fluid RS before joining the low-temperature heat source fluid GP is exchanged with the refrigerant liquid Vf, but heat exchange is performed between the merged heat source fluid RA and the refrigerant liquid Vf. It is good as well. The refrigerant heat exchanger 99 is disposed in the refrigerant liquid pipe 45 and the drive heat source outflow pipe 39 on the downstream side of the refrigerant pump 46. As the refrigerant heat exchanger 99, a shell and tube type or a plate type heat exchanger is used. The structure of the absorption heat exchange system 3 other than the above is the same as that of the absorption heat exchange system 2 (see FIG. 2).

  In addition to the action of the absorption heat exchange system 2 (see FIG. 2), the absorption heat exchange system 3 configured as described above includes the refrigerant liquid Vf from the condenser 40 toward the evaporator 20 and the regenerator 30. Heat exchange is performed with the driving heat source fluid RS that has flowed out, the temperature of the refrigerant liquid Vf increases, and the temperature of the driving heat source fluid RS decreases. Since the refrigerant liquid Vf flowing out from the refrigerant heat exchanger 99 rises in temperature and flows into the evaporator 20, the amount of heat necessary for evaporation in the evaporator 20 can be suppressed. On the other hand, the driving heat source fluid RS that has flowed out of the refrigerant heat exchanger 99 flows out of the absorption heat exchange system 3 after the temperature is lowered and mixed with the low-temperature heat source fluid GP, and the driving heat source in the absorption heat exchange system 3 The amount of heat recovered from the fluid RS can be increased. In addition, although illustration is abbreviate | omitted, the refrigerant | coolant heat exchanger 99 is applicable also to the absorption heat exchange system 1 (refer FIG. 1).

  In the above description, the driving heat source fluid RS flowing into the driving heat source introduction pipe 52 from the heat source fluid inflow pipe 55 flows through the heat source pipe 32 of the regenerator 30 after flowing through the heat source pipe 22 of the evaporator 20, that is, the evaporator 20. However, the drive heat source introduction pipe 52 is connected to the heat source pipe 32 of the regenerator 30 as shown in the absorption heat exchange system 1A according to the modification of the first embodiment of FIG. And the drive heat source outflow pipe 39 may be connected to the heat source pipe 22 of the evaporator 20 so as to flow in series from the heat source pipe 32 of the regenerator 30 to the heat source pipe 22 of the evaporator 20. May flow in parallel to the heat source tube 22 of the evaporator 20 and the heat source tube 32 of the regenerator 30. When the driving heat source fluid RS flows from the regenerator 30 to the evaporator 20 in series, there is an advantage that the COP of the absorption heat exchange system 1 is improved. As shown in FIG. 1, when the driving heat source fluid RS flows in series from the evaporator 20 to the regenerator 30, the concentration of the absorbing liquid S is prevented from excessively rising and the absorbing liquid S is difficult to crystallize. Further, if the driving heat source fluid RS flows in parallel to the evaporator 20 and the regenerator 30, an increase in the concentration of the absorbing liquid S can be suppressed while improving the COP. As described above, even if the driving heat source fluid RS flowing into the driving heat source introduction pipe 52 first flows into either the heat source pipe 22 of the evaporator 20 or the heat source pipe 32 of the regenerator 30, the temperature rising fluid is introduced. The temperature increase target fluid RP that has flowed into the pipe 51 is introduced into the heat transfer pipe 12 of the absorber 10. The driving heat source fluid RS flows in series from the heat source pipe 32 of the regenerator 30 to the heat source pipe 22 of the evaporator 20, or flows in parallel to the heat source pipe 22 of the evaporator 20 and the heat source pipe 32 of the regenerator 30. Can also be applied to the absorption heat exchange system 2 (see FIG. 2) and the absorption heat exchange system 3 (see FIG. 3).

  In the above description, the low-temperature heat source fluid GP that has flowed out of the condenser 40 is merged with the driving heat source fluid RS that has flowed out of the evaporator 20 and the regenerator 30, but the fluid flowing in the heat transfer tube 42 of the condenser 40 is used. While using an independent system, the low-temperature heat source introduction pipe 57 may be connected to the drive heat source outflow pipe 39 and the heat source fluid outflow pipe 59 so that the fluid flowing out from the heat utilization equipment HCF is merged with the drive heat source fluid RS.

  In the above description, the heating source fluid (merging heat source fluid RA, driving heat source fluid RS) and the heated fluid (temperature increase target fluid RP, low temperature heat source fluid GP) are the same kind of fluid because they are divided and merged. The fluid to be applied may be a liquid for a heat medium or a chemical liquid in addition to hot water. In particular, when a heat medium liquid or a chemical liquid having a boiling point higher than that of water is employed, it can be applied to a high temperature range without applying a high pressure to the fluid in order to suppress boiling of the fluid.

  In the above description, the evaporator 20 is a full liquid type, but may be a falling liquid film type. In the case where the evaporator is a falling liquid film type, a refrigerant liquid supply device for supplying the refrigerant liquid Vf is provided in the upper part of the evaporator can body 21 and connected to the evaporator can body 21 in the case of the full liquid type. What is necessary is just to connect the edge part of the refrigerant liquid pipe | tube 45 which had been connected to the refrigerant liquid supply apparatus. Further, a pipe and a pump for supplying the refrigerant liquid Vf below the evaporator can body 21 to the refrigerant liquid supply device may be provided.

  In the above description, the example in which the absorber 10, the evaporator 20, the regenerator 30, and the condenser 40 in which the absorption heat pump cycle is performed is configured in a single stage, may be configured in multiple stages. For example, when the absorption heat pump cycle is a two-stage temperature rising type, the absorber 10 and the evaporator 20 are represented by a high-temperature side high-temperature absorber (hereinafter, for convenience of explanation, “10” is added with “H”. ) And a high-temperature evaporator (hereinafter, “H” is added to the reference numeral “20” for convenience of explanation) and a low-temperature absorber on the low temperature side (hereinafter, “L” is assigned to the reference numeral “10” for convenience of explanation). And a low-temperature evaporator (hereinafter, for convenience of explanation, reference numeral “20” is added with “L”). The high temperature absorber 10H has a higher internal pressure than the low temperature absorber 10L, and the high temperature evaporator 20H has a higher internal pressure than the low temperature evaporator 20L. The high temperature absorber 10H and the high temperature evaporator 20H typically communicate with each other at the top so that the vapor of the refrigerant V of the high temperature evaporator 20H can be moved to the high temperature absorber 10H. The low-temperature absorber 10L and the low-temperature evaporator 20L typically communicate with each other at the top so that the vapor of the refrigerant V in the low-temperature evaporator 20L can be moved to the low-temperature absorber 10L. The temperature increase target fluid RP that is branched from the combined heat source fluid RA does not flow into the low temperature absorber 10L but flows into the high temperature absorber 10H and is heated by the high temperature absorber 10H. The driving heat source fluid RS branched from the combined heat source fluid RA is introduced into the low temperature evaporator 20L without being introduced into the high temperature evaporator 20H. The low-temperature absorber 10L heats the refrigerant liquid Vf in the high-temperature evaporator 20H by absorption heat when the absorbing liquid S absorbs the vapor of the refrigerant V that has moved from the low-temperature evaporator 20L, and the refrigerant V enters the high-temperature evaporator 20H. The generated vapor V of the refrigerant V in the high-temperature evaporator 20H moves to the high-temperature absorber 10H and is absorbed by the absorption liquid S in the high-temperature absorber 10H, and the temperature-up target fluid RP Configured to heat.

1, 1A, 2, 3 Absorption heat exchange system 10 Absorber 20 Evaporator 30 Regenerator 40 Condenser 48 Low temperature heat source bypass pipe 99 Refrigerant heat exchanger GP Low temperature heat source fluid RP Temperature increase target fluid RS Drive heat source fluid Sa Concentrated solution Sw Dilute solution Ve Evaporator refrigerant vapor Vf Refrigerant liquid Vg Regenerator refrigerant vapor

Claims (6)

An absorber that raises the temperature of the first heated fluid by the absorbed heat released when the absorbing liquid absorbs the vapor of the refrigerant to become a diluted solution having a reduced concentration;
A condensing unit that raises the temperature of the second heated fluid by the condensation heat released when the vapor of the refrigerant condenses into a refrigerant liquid;
The heating source is provided by introducing the refrigerant liquid from the condensing unit and removing the latent heat of evaporation required when the introduced refrigerant liquid evaporates and becomes the vapor of the refrigerant supplied to the absorption unit from the heating source fluid. An evaporation section for lowering the temperature of the fluid;
The dilute solution is introduced from the absorption part, and the introduced dilute solution is heated to remove the refrigerant from the dilute solution to take away the heat necessary to obtain a concentrated solution from the heating source fluid. A regeneration unit for lowering the temperature of the heating source fluid;
By the absorption heat pump cycle of the absorption liquid and the refrigerant, the absorption unit has an internal pressure and temperature higher than the regeneration unit, and the evaporation unit has an internal pressure and temperature higher than the condensation unit. Composed;
A part of the heating source fluid branched from the heating source fluid before being introduced into the evaporation unit and the regeneration unit is introduced into the absorption unit as the first heated fluid;
Absorption heat exchange system. The flow rate of the heating source fluid flowing into the evaporating unit and the regeneration unit and the first heated target fluid so that the temperature of the first heated fluid flowing out from the absorbing unit becomes a predetermined temperature. A ratio with the flow rate of the heating source fluid flowing as heating fluid was set;
The absorption heat exchange system according to claim 1. The second heated fluid that has flowed out of the condensing unit is mixed with the heating source fluid that has flowed out of at least one of the evaporation unit and the regeneration unit;
The absorption heat exchange system according to claim 1 or 2. A partial cover that joins a part of the second heated fluid branched from the second heated fluid that has flowed out of the condensing unit to the first heated fluid before being introduced into the absorption unit. Comprising a heated fluid bypass channel;
The absorption heat exchange system according to any one of claims 1 to 3. From at least one of the evaporation unit and the regeneration unit of the second heated fluid that has flowed out of the condensing unit such that the temperature of the first heated fluid that has flowed out of the absorbing unit becomes a predetermined temperature. The ratio of the flow rate to mix with the heated source fluid that flowed out and the flow rate through the partially heated fluid bypass flow path was set;
The absorption heat exchange system according to claim 4. A refrigerant heat exchanger that exchanges heat between the refrigerant liquid conveyed from the condensing unit to the evaporation unit and the heating source fluid flowing out from at least one of the evaporation unit and the regeneration unit;
The absorption heat exchange system according to any one of claims 1 to 5.

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