JP6907438B2 - Absorption heat exchange system - Google Patents

Description

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

Heat exchangers are widely used as devices for exchanging heat between hot and cold fluids. In a heat exchanger in which heat exchange is performed directly between two fluids, the outlet temperature of the cold fluid cannot be set higher than the inlet temperature of the hot fluid (see, for example, Patent Document 1).

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

One of the uses of heat exchangers is to recover exhaust heat. Since the exhaust heat is the 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 the heat including the exhaust heat and lowers the temperature. If the temperature can be raised, the range of utilization will be expanded.

In view of the above problems, it is an object of the present invention to provide an absorption type heat exchange system capable of raising the outlet temperature of the fluid to be heated, which raises the temperature, to be higher than the inlet temperature of the heating source fluid, which lowers the temperature. do.

In order to achieve the above object, in the absorption type heat exchange system according to the first aspect of the present invention, for example, as shown in FIG. 1, the absorption liquid Sa absorbs the vapor vapor Ve of the refrigerant and the concentration is lowered. The absorption unit 10 that raises the temperature of the first heated fluid RP by the absorbed heat released when it becomes Sw; the second by the condensed heat released when the vapor Vg of the refrigerant condenses into the refrigerant liquid Vf. Condensing unit 40 that raises the temperature of the fluid GP to be heated; Necessary when the refrigerant liquid Vf is introduced from the condensing unit 40 and the introduced refrigerant liquid Vf evaporates to become the vapor vapor Ve of the refrigerant supplied to the absorbing unit 10. Evaporation unit 20 that lowers the temperature of the heating source fluid RS by removing the latent heat of evaporation from the heating source fluid RS; the dilute solution Sw is introduced from the absorption unit 10, the introduced dilute solution Sw is heated, and the refrigerant is supplied from the dilute solution Sw. It is provided with a regenerating unit 30 that lowers the temperature of the heating source fluid RS by removing the heat required for removing Vg to obtain a concentrated solution Sa having an increased concentration from the heating source fluid RS; By the absorption heat pump cycle with the refrigerants Ve, Vf, and Vg, the absorption unit 10 has a higher internal pressure and temperature than the regeneration unit 30, and the evaporation unit 20 has an internal pressure and temperature higher than that of the condensing unit 40. It is configured to introduce a part of the heat source fluid branched from the heat source fluid RA before being introduced into the evaporation unit 20 and the regeneration unit 30 into the absorption unit 10 as the first heated fluid RP. There is.

With this configuration, a part of the heating source fluid branched from the heating source fluid before being introduced into the evaporating section and the regenerating section is introduced into the absorbing section as the first heated fluid, so that the fluid flows out from the absorbing section. The temperature of the first fluid to be heated can be made higher than the temperature of the heating source fluid before being introduced into the evaporating part and the regenerating part.

Further, the absorption type heat exchange system according to the second aspect of the present invention is shown by referring to FIG. 1, for example, from the absorption unit 10 in the absorption type heat exchange system 1 according to the first aspect of the present invention. The flow rate of the heating source fluid RS flowing into the evaporating section 20 and the regenerating section 30 and flowing into the absorbing section 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 is set.

With this configuration, the temperature of the first fluid to be heated flowing out of the absorption unit can be adjusted.

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

Further, the absorption heat exchange system according to the fourth aspect of the present invention has, for example, as shown in FIG. 2, the absorption heat according to any one of the first to third aspects of the present invention. In the exchange system 2, a part of the second heated fluid GPd branched from the second heated fluid GP flowing out from the condensing unit 40 is introduced into the absorbing unit 10 before the first heated fluid RP. A partially heated fluid bypass flow path 48 is provided.

With this configuration, the system configuration can be simplified.

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

With this configuration, the balance between the temperature and flow rate of the first fluid to be heated flowing out of the absorption unit can be adjusted.

Further, 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 according to any one of the first to fifth aspects of the present invention. In the exchange system 3, the refrigerant heat exchanges heat between the refrigerant liquid Vf conveyed from the condensing unit 40 to the evaporating unit 20 and the heating source fluid RS flowing out from at least one of the evaporating unit 20 and the regenerating unit 30. The exchanger 99 is provided.

With this configuration, the temperature of the heat source fluid flowing out of the absorption heat exchange system can be lowered, and the amount of heat recovered from the heat source fluid in the absorption heat exchange system can be increased.

According to the present invention, a part of the heating source fluid branched from the heating source fluid before being introduced into the evaporating part and the regenerating part is introduced into the absorbing part as the first heated fluid, so that the fluid flows out from the absorbing part. The temperature of the first fluid to be heated can be made higher than the temperature of the heating source fluid before being introduced into the evaporating part and the regenerating part.

It is a schematic system diagram of the absorption type heat exchange system which concerns on 1st Embodiment of this invention. It is a schematic system diagram of the absorption type heat exchange system which concerns on the 2nd Embodiment of this invention. It is a schematic system diagram of the absorption type heat exchange system which concerns on 3rd Embodiment of this invention. It is a schematic system diagram of the absorption type heat exchange system which concerns on the modification of 1st Embodiment of this invention.

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

First, the absorption heat exchange system 1 according to the first embodiment of the present invention will be described with reference to FIG. FIG. 1 is a schematic system diagram of the absorption heat exchange system 1. The absorption heat exchange system 1 utilizes the absorption heat pump cycle of the absorption liquid and the refrigerant, and the temperature of the temperature-increasing target fluid RP flowing out from the absorption heat exchange system 1 toward the heat utilization equipment HCF is used as a driving heat source. This is a system in which 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-increasing target fluid RP is a fluid that is a target for raising the temperature in the absorption heat exchange system 1, and corresponds to the first fluid to be heated. The drive heat source fluid RS is a fluid whose temperature drops in the absorption heat exchange system 1, and corresponds to a heat source fluid. The absorption heat exchange system 1 comprises an absorber 10, an evaporator 20, and a regenerator 30 that constitute a main device in which an absorption heat pump cycle of an absorption liquid S (Sa, Sw) and a 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 condensing unit, respectively.

In the present specification, in order to facilitate the distinction of the absorbent liquid on the heat pump cycle, it is referred to as "rare solution Sw" or "concentrated solution Sa" depending on the properties and the position on the heat pump cycle. Etc. are collectively referred to as "absorbent solution S". Similarly, regarding the refrigerant, in order to facilitate the distinction 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 unquestioned, they are collectively referred to as "refrigerant V". In the present embodiment, a LiBr aqueous solution is used as the absorbing liquid S (mixture of the absorbing agent and the refrigerant V), and water (H ₂ O) is used as the refrigerant V.

The absorber 10 has a heat transfer tube 12 that constitutes a flow path of the fluid RP to be heated, 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 tube 12 has a temperature rise fluid introduction pipe 51 connected to one end and a temperature rise fluid outflow pipe 19 connected to the other end. The temperature-increasing fluid introduction pipe 51 is a pipe that constitutes a flow path that guides the temperature-increasing fluid RP to the heat transfer tube 12. The temperature-increasing fluid introduction pipe 51 is provided with a temperature-increasing fluid valve 51v for adjusting the flow rate of the fluid to be heated RP flowing inside. The temperature-increasing fluid outflow pipe 19 is a pipe that constitutes a flow path through which the fluid RP to be heated by the absorber 10 flows. The absorber 10 generates heat of absorption 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 a dilute solution Sw. The heat absorption target fluid RP flowing through the heat transfer tube 12 receives heat, and the temperature rise target fluid RP is heated.

The evaporator 20 has a heat source pipe 22 that constitutes 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. Therefore, the heat source pipe 22 is arranged 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 pipe 52 is connected to one end of the heat source pipe 22. The drive heat source introduction pipe 52 is a pipe that constitutes 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 regulates 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 that constitutes a flow path through which the combined heat source fluid RA flows. The merging heat source fluid RA flowing through the heat source fluid inflow pipe 55 is configured to split and flow into the temperature rising fluid introduction pipe 51 and the drive heat source introduction pipe 52. That is, the temperature-increasing target fluid RP flowed into the temperature-increasing fluid introduction pipe 51 of the merging heat source fluid RA, and the driving heat source fluid RS flowed into the driving heat source introduction pipe 52 of the merging heat source fluid RA. It is a thing. The evaporator 20 is configured so that the refrigerant liquid Vf around the heat source pipe 22 evaporates with 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 for supplying the refrigerant liquid Vf is connected to the evaporator can body 21 in the evaporator can body 21.

The absorber 10 and the evaporator 20 communicate with each other. By communicating 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 has a heat source tube 32 for flowing a driving heat source fluid RS for heating the dilute solution Sw, and a dilute solution supply device 33 for supplying the dilute solution Sw to the surface of the heat source tube 32. The drive heat source fluid RS flowing in the heat source pipe 32 is the drive 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 drive heat source connecting pipe 25 through which the drive heat source fluid RS flows. A drive heat source outflow pipe 39 is connected to an end opposite to the end to which the drive heat source connecting pipe 25 of the heat source pipe 32 of the regenerator 30 is connected. The drive heat source outflow pipe 39 is a pipe that constitutes a flow path that guides the drive heat source fluid RS to the outside of the regenerator 30. In the regenerator 30, the dilute solution Sw supplied from the dilute solution supply device 33 is heated by the driving heat source fluid RS, so that the refrigerant V evaporates from the dilute solution Sw to generate a concentrated solution Sa having an increased concentration. It is configured as follows. The refrigerant V evaporated from the dilute solution Sw is configured to move to the condenser 40 as the 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. A low temperature heat source introduction pipe 57 constituting a flow path for guiding the low temperature heat source fluid GP to the heat transfer tube 42 is connected to one end of the heat transfer tube 42. One end of the low temperature heat source outflow pipe 49 constituting the flow path through which the low temperature heat source fluid GP flowing out from the condenser 40 flows is connected to the other end of the heat transfer tube 42. 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 constituting a flow path through which the combined heat source fluid RA in which the drive heat source fluid RS flowing through the drive heat source outflow pipe 39 and the low temperature heat source fluid GP flowing through the low temperature heat source outflow pipe 49 merge. .. The condenser 40 introduces the regenerator refrigerant steam 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 this is condensed into the refrigerant liquid Vf. Therefore, the low-temperature heat source fluid GP is configured to be heated. The low temperature heat source fluid GP corresponds to the second heated fluid. The regenerator 30 and the condenser 40 are integrally formed with the can body of the regenerator 30 and the condenser can body 41 so as to communicate with each other. By communicating 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 of the regenerator 30 in which the concentrated solution Sa 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. A solution pump 35p for pumping the concentrated solution Sa is provided in the concentrated solution tube 35. The portion of the absorber 10 in which 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. A solution heat exchanger 38 for exchanging heat between the concentrated solution Sa and the dilute solution Sw is provided in the concentrated solution tube 35 and the dilute solution tube 36. 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 type 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 higher than those inside the condenser 40. It will be 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-class absorption heat pump.

The heat source fluid inflow pipe 55 and the heat source fluid outflow pipe 59 are connected to the heat source equipment HSF in the present embodiment. The heat source equipment HSF is equipment that recovers exhaust heat from, for example, a steel mill or a power plant. In the present embodiment, the heat source equipment HSF heats the combined heat source fluid RA taken in from the heat source fluid outflow pipe 59 with exhaust heat to raise the temperature and supplies it 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 equipment HCF. The heat utilization equipment HCF uses, for example, the introduced heat for heating or as a heat source for heat source equipment such as other absorption chillers and absorption heat pumps. In the present embodiment, the heat utilization facility HCF utilizes the heat possessed by the temperature-increasing target fluid RP introduced from the temperature-increasing fluid outflow pipe 19, and removes heat from the temperature-increasing target fluid RP to remove the fluid whose temperature has decreased. It flows out to the low temperature heat source introduction pipe 57 as the low temperature heat source fluid GP.

Subsequently, with 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. The condenser 40 receives the regenerator refrigerant vapor Vg evaporated by the regenerator 30, and the regenerator refrigerant vapor Vg is cooled and condensed by the low-temperature heat source fluid GP flowing through the heat transfer tube 42 to become the refrigerant liquid Vf. At this time, the temperature of the low-temperature heat source fluid GP rises due to the heat of condensation 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 drive heat source fluid RS flowing in the heat source pipe 22 and evaporates to become the evaporator refrigerant steam Ve. At this time, the temperature of the drive heat source fluid RS is lowered by being deprived of heat by the refrigerant liquid Vf. The evaporator refrigerant vapor Ve generated in the evaporator 20 moves to the absorber 10 communicating 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 concentration of the concentrated solution Sa that has absorbed the evaporator refrigerant vapor Ve decreases to become a dilute solution Sw. In the absorber 10, absorption heat is generated when the concentrated solution Sa absorbs the evaporator refrigerant vapor Ve. The absorbed heat heats the temperature-increasing target fluid RP flowing through the heat transfer tube 12, and the temperature of the temperature-increasing target fluid RP rises. The temperature-increasing target fluid RP flowing through the heat transfer tube 12 is originally the same confluent heat source fluid RA as the source of the drive heat source fluid RS introduced into the heat source tube 22 of the evaporator 20. Therefore, the temperature of the temperature-increasing target fluid RP flowing through the temperature-increasing fluid outflow pipe 19 is higher than that of the drive heat source fluid RS flowing into the evaporator 20 and the regenerator 30 by the amount heated by the absorber 10. The concentration of the concentrated solution Sa that has absorbed the evaporator refrigerant vapor Ve in the absorber 10 decreases to become a dilute solution Sw, which is stored in the lower part of the absorber 10. The stored dilute solution Sw flows through the dilute solution tube 36 toward the regenerator 30 due to the difference in internal pressure between the absorber 10 and the regenerator 30, and heats with the concentrated solution Sa in the solution heat exchanger 38 to raise the temperature. It drops to reach the regenerator 30.

The dilute solution Sw sent to the regenerator 30 is supplied from the dilute solution supply device 33, heated by the driving heat source fluid RS flowing through the heat source tube 32, and the refrigerant in the supplied dilute solution Sw evaporates to concentrate the concentrated solution Sa. And is stored in the lower part of the regenerator 30. At this time, the temperature of the driving heat source fluid RS is lowered by being deprived of heat by the dilute solution Sw. The drive 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 by the solution pump 35p to the concentrated solution supply device 13 of the absorber 10 via the concentrated solution pipe 35. The concentrated solution Sa flowing through the concentrated solution tube 35 exchanges heat with the dilute solution Sw in the solution heat exchanger 38, flows into the absorber 10 after the temperature rises, is supplied from the concentrated solution supply device 13, and so on. Repeat the cycle of.

Changes in temperature of the fluid to be heated and the fluid to be heated in the process in which the absorption liquid S and the refrigerant V perform the absorption heat pump cycle as described above will be described with reference to specific examples. In the combined heat source fluid RA at 95 ° C. that flows out of the heat source equipment HSF and flows through the heat source fluid inflow pipe 55, the temperature-increasing target fluid RP and the driving heat source fluid RS that are separated are each 95 ° C. The 95 ° C. drive heat source fluid RS flowing through the drive 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 88 ° C. when reaching the drive heat source communication pipe 25. Decreases. After that, the drive heat source fluid RS flowing through the drive heat source connecting pipe 25 is deprived of heat by the dilute solution Sw when flowing through the heat source pipe 32 of the regenerator 30, and when it reaches the drive heat source outflow pipe 39, the temperature reaches 80 ° C. descend.

On the other hand, the temperature-increasing target fluid RP flowing through the temperature-increasing fluid introduction tube 51 obtains the absorbed heat generated by the concentrated solution Sa absorbing the evaporator refrigerant vapor Ve when flowing through the heat transfer tube 12 of the absorber 10. When the temperature rises to the temperature rising fluid outflow pipe 19, the temperature rises to 100 ° C. The temperature of the fluid RP to be heated at 100 ° C. flowing through the temperature-increasing fluid outflow pipe 19 flows into the heat utilization equipment HCF and the heat is utilized to lower the temperature. The fluid whose temperature has dropped due to the use of heat in the heat utilization facility HCF flows out to the low temperature heat source introduction pipe 57 as the low temperature heat source fluid GP at 30 ° C. The 30 ° C. low-temperature heat source fluid GP flowing through the low-temperature heat source introduction tube 57 releases the heat of condensation when the regenerator refrigerant vapor Vg condenses into the refrigerant liquid Vf when flowing through the heat transfer tube 42 of the condenser 40. As a result, when the low temperature heat source outflow pipe 49 is reached, 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 mixes with the 80 ° C. driving heat source fluid RS flowing through the driving heat source outflow pipe 39 to become a 60 ° C. confluent heat source fluid RA to form the heat source fluid outflow pipe 59. It flows. In the present embodiment, by mixing the low temperature heat source fluid GP of the low temperature heat source outflow pipe 49 and the drive heat source fluid RS of the drive heat source outflow pipe 39, the heated fluid and the heat source fluid entering and exiting the absorption type heat exchange system 1 are subjected to. The flow rate is balanced. The 60 ° C. confluent heat source fluid RA flowing through the heat source fluid outflow pipe 59 flows into the heat source equipment HSF to recover the exhaust heat and raise the temperature. The combined heat source fluid RA whose temperature has risen in the heat utilization equipment HCF flows out to the heat source fluid inflow pipe 55 at 95 ° C., and thereafter, the above flow is repeated.

In the absorption type heat exchange system 1, the temperature of the fluid to be heated RP flowing out from the absorber 10 is a predetermined temperature (a temperature suitable for use in the heat utilization equipment HCF) by establishing the above-mentioned temperature relationship. In this embodiment, the ratio of the flow rate of the fluid to be heated RP flowing through the temperature raising fluid introduction tube 51 and the flow rate of the drive heat source fluid RS flowing through the drive heat source introduction tube 52 is determined so as to be 100 ° C.). ing. In the present embodiment, the flow rate ratio of the temperature-increasing target fluid RP and the driving heat source fluid RS is approximately 1: 1. If the flow rate of the fluid to be heated is relatively small, the temperature of the fluid RP to be heated will be relatively high, and if the flow rate of the fluid RP to be heated is increased, the temperature of the fluid RP to be heated will be low. Here, the flow rate ratio between the temperature-increasing target fluid RP flowing through the temperature-increasing fluid introduction pipe 51 and the drive heat source fluid RS flowing through the drive heat source introduction pipe 52 is a storage device (not shown) provided in the control device (not shown). It may be set in advance, or it may be configured to be set at any time by an input device (not shown) provided in the control device. In the present embodiment, the flow rate ratio between the temperature-increasing target fluid RP and the drive heat source fluid RS is adjusted by adjusting the opening degrees of the temperature-increasing fluid valve 51v and the drive heat source valve 52v. The opening degree of the temperature rising fluid valve 51v and the drive heat source valve 52v is typically adjusted automatically by a signal from the control device based on the flow rate ratio set in the control device described above, but it depends on the control device. The opening may be adjusted manually without this. Instead of the heating fluid valve 51v and the driving heat source valve 52v, a three-way valve may be provided at the connection portion between the heating fluid introduction pipe 51, the driving heat source introduction pipe 52, and the heat source fluid inflow pipe 55.

An overview of the flow of the heat source fluid (merged heat source fluid RA) and the heated fluid (heat temperature target fluid RP, low temperature heat source fluid GP) that enters and exits the absorption type heat exchange system 1 described so far is absorbed. In the type heat exchange system 1, the combined heat source fluid RA that flows out from the heat source equipment HSF and flows into the absorption type heat exchange system 1 at 95 ° C. flows out from the absorption type heat exchange system 1 at 60 ° C. and flows into the heat source equipment HSF. The low-temperature heat source fluid GP that flows out of the heat utilization equipment HCF and flows into the absorption type heat exchange system 1 at 30 ° C. flows out from the absorption type heat exchange system 1 as the temperature rise target fluid RP at 100 ° C. and heat utilization equipment. It is flowing into the HCF. If the combined heat source fluid RA that flows in and out of the heat source equipment HSF is used as the heat source fluid, and the temperature-increasing target fluid RP and low-temperature heat source fluid GP that flow in and out of the heat-utilizing equipment HCF are taken as heated fluids, they are absorbed. The formula heat exchange system 1 can be regarded as having a heat exchange action between the heating source fluid and the heated fluid, and the temperature of the heating source fluid is changed from the temperature of the heated fluid into which the heated fluid flows. The amount of heat required to heat to a higher temperature can be regarded as a heat exchange system that flows out after being deprived of the heating source fluid. The higher the temperature of the fluid to be heated (fluid RP to be heated) flowing out from the absorption type heat exchange system 1, the more the temperature difference between the inlet and outlet of the fluid to be heated with respect to the absorption type heat exchange system 1 is calculated from the inlet and outlet temperature difference of the heating source fluid. Can also be expanded to reduce the flow rate of the fluid to be heated (fluid RP to be heated). Further, the flow rate of the combined heat source fluid RA flowing out of the absorption heat exchange system 1 and flowing into the heat source equipment HSF is equal to the flow rate of the combined heat source fluid RA flowing out of the heat source equipment HSF and flowing into the absorption heat exchange system 1. Then, the flow rate of the temperature-increasing target fluid RP flowing out of the absorption heat exchange system 1 and flowing into the heat utilization device HCF and the flow rate of the low-temperature heat source fluid GP flowing out of the heat utilization device HCF and flowing into the absorption heat exchange system 1. When is equal, it is considered that both the heating source fluid and the heated fluid flow into and out of the absorption heat exchange system 1 as an independent system partitioned in the absorption heat exchange system 1. This makes it clearer to see the absorption heat exchange system 1 as a heat exchanger. As shown in the present embodiment, the combined heat source fluid RA flowing out of the absorption type heat exchange system 1 passes through the heat source equipment HSF and is heated, and then returns to the absorption type heat exchange system 1 to return to the absorption type heat exchange system. It is preferable that the temperature-increasing target fluid RP flowing out of 1 passes through the heat utilization equipment HCF and consumes heat, and then returns to the absorption-type heat exchange system 1 as the low-temperature heat source fluid GP.

It should be noted that the condenser 40 is assumed that the fluid flowing in and out of the heat utilization equipment HCF (heated fluid) is not split and merged with the fluid flowing in and out of the heat source equipment HSF (heating source fluid). When the low temperature heat source fluid GP flowing through the heat transfer tube 42 of the above is set as an independent system so as to flow through the heat transfer tube 12 of the absorber 10, the low temperature heat source fluid GP flowing through the heat transfer tube 42 of the condenser 40 is used in the absorber 10. Before flowing into the heat transfer tube 12, the heat is exchanged with the driving heat source fluid RS flowing out from the evaporator 20 and the regenerator 30 or the driving heat source fluid RS before flowing into the evaporator 20 and the regenerator 30 to heat and raise the temperature. You will need a heat exchanger. On the other hand, as in the present embodiment, the fluid flowing in and out of the heat utilization facility HCF (heated fluid) is split and merged with the fluid flowing in and out of the heat source facility HSF (heating source fluid). Then, the heat exchanger provided in the case of the above assumption becomes unnecessary, and the system configuration can be simplified. By eliminating the need for the heat exchanger provided in the above assumption, it is possible to avoid the temperature drop of the fluid to be heated due to the heat dissipation loss from the heat exchanger and the heat exchange temperature efficiency of less than 1, and the heat efficiency of the heat exchanger. Can be eliminated. Further, the installation space of the heat exchanger, the piping for the fluid to enter and exit the heat exchanger, and the maintenance and inspection work of the heat exchanger can be omitted. Further, in the absorption type heat exchange system 1 according to the present embodiment, a fluid (heated fluid) having a temperature lower than the fluid flowing out to the heat source equipment HSF (heat source fluid) is introduced from the heat utilization equipment HCF to introduce the heat source equipment. A fluid (heated fluid) having a temperature higher than the fluid introduced from the HSF (heat source fluid) can flow out to the heat utilization facility HCF, and heat can be effectively utilized, and the absorption type heat exchange system 1 The temperature difference between the inlet and outlet of the fluid to be heated can be increased to reduce the flow rate of the fluid to be heated.

As described above, according to the absorption type heat exchange system 1 according to the present embodiment, the temperature rise target is such that the temperature of the outflow target fluid RP is higher than the temperature of the drive heat source fluid RS to be introduced. The fluid RP can be heated, and the temperature-increasing target fluid RP having a higher utility value than the driving heat source fluid RS can be supplied to the outside. Further, the temperature-increasing target fluid RP heated by the absorber 10 is branched from the confluent 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 to drive the heat source fluid. Since it is merged with the RS, the device configuration is simplified without heat exchange between the driving heat source fluid RS and the low temperature heat source fluid GP, that is, without providing a large heat exchanger, and the temperature rise target is relatively high. Fluid RP can be supplied (outflowed). Further, rather than the temperature difference between the inlet and outlet of the drive heat source fluid RS flowing into and out of the absorption type heat exchange system 1, the temperature of the low temperature heat source fluid GP flowing into and out of the absorption type heat exchange system 1 and the temperature of the fluid to be heated RP flowing out. The difference between the temperature and the temperature can be increased, and the flow rate of the fluid RP to be heated to be supplied to the heat utilization facility HCF can be reduced by the amount of the large temperature difference, and the transport power can be reduced.

Next, the absorption heat exchange system 2 according to the second embodiment of the present invention will be described with reference to FIG. FIG. 2 is a schematic system diagram of the absorption heat exchange system 2. The absorption heat exchange system 2 differs 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 heating fluid introduction pipe 51. The low-temperature heat source bypass pipe 48 is a fluid to be heated that flows through the temperature-increasing fluid introduction pipe 51 before the part of the low-temperature heat source fluid GP that flows out of the condenser 40 and flows through the low-temperature heat source outflow pipe 49 flows into the absorber 10. It 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 represented by the reference numeral GPd to distinguish it 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 regulates the flow rate of the low-temperature heat source fluid GPd flowing inside. On the other hand, the low temperature heat source outflow pipe 49 on the downstream side of the connection with the low temperature heat source bypass pipe 48 is provided with a low temperature heat source valve 49v for adjusting 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 configuration 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).

The absorption heat exchange system 2 configured as described above adjusts the opening degrees of the low temperature heat source bypass valve 48v and the low temperature heat source valve 49v in addition to the action of the absorption heat exchange system 1 (see FIG. 1). A part GPd of the low-temperature heat source fluid GP heated by the condenser 40 is mixed with the temperature-increasing 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. Although it is automatically performed by the above, the opening degree may be adjusted manually without depending on the control device. By adjusting the flow rate of the low-temperature heat source fluid GPd to be mixed with the temperature-increasing target fluid RP, the temperature and / or the flow rate of the temperature-heating target fluid RP flowing through the temperature-increasing 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 outflow of the heat source fluid so that the temperature of the temperature-increasing 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 outflow 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-increasing target fluid RP flowing through the temperature-increasing fluid outflow pipe 19 decreases and the flow rate increases, so that the low-temperature heat source bypass pipe If the flow rate of the low-temperature heat source fluid GPd flowing through 48 is reduced, the temperature of the temperature-increasing target fluid RP flowing through the temperature-increasing 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-increasing target fluid RP flowing through the temperature-increasing fluid outflow pipe 19 decreases but the flow rate increases as described above. The amount of heat possessed by the temperature-increasing target fluid RP flowing through the outflow pipe 19 can be increased.

Next, the absorption heat exchange system 3 according to the 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 differs 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 heading from the condenser 40 to the evaporator 20 and the fluid including the driving heat source fluid RS flowing out of the regenerator 30. In the present embodiment, the drive heat source fluid RS before merging with the low temperature heat source fluid GP is subjected to heat exchange with the refrigerant liquid Vf, but heat exchange is performed between the merging heat source fluid RA and the refrigerant liquid Vf. It may be that. The refrigerant heat exchanger 99 is arranged in the refrigerant liquid pipe 45 and the drive heat source outflow pipe 39 on the downstream side of the refrigerant pump 46. A shell-and-tube type or plate type heat exchanger is used as the refrigerant heat exchanger 99. The configuration 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 the absorption heat exchange system 3 configured as described above, in addition to the action of the absorption heat exchange system 2 (see FIG. 2), the refrigerant liquid Vf from the condenser 40 to the evaporator 20 and the regenerator 30 Heat exchange is performed with the outflowing drive heat source fluid RS, the temperature of the refrigerant liquid Vf rises, and the temperature of the drive heat source fluid RS decreases. Since the temperature of the refrigerant liquid Vf flowing out of the refrigerant heat exchanger 99 rises and flows into the evaporator 20, the amount of heat required for evaporation in the evaporator 20 can be suppressed. On the other hand, the drive heat source fluid RS flowing out of the refrigerant heat exchanger 99 flows out of the absorption heat exchange system 3 after the temperature drops and mixes with the low temperature heat source fluid GP, and the drive heat source in the absorption heat exchange system 3 The amount of heat recovered from the fluid RS can be increased. Although not shown, the refrigerant heat exchanger 99 can also be applied to the absorption heat exchange system 1 (see FIG. 1).

In the above description, the drive heat source fluid RS that has flowed from the heat source fluid inflow pipe 55 into the drive heat source introduction pipe 52 flows through the heat source pipe 22 of the evaporator 20 and then through the heat source pipe 32 of the regenerator 30, that is, the evaporator 20. As shown in the absorption type heat exchange system 1A according to the modified example of the first embodiment of FIG. 4, the drive heat source introduction pipe 52 is used as the heat source pipe 32 of the regenerator 30. The drive heat source outflow pipe 39 may be connected to the heat source pipe 22 of the evaporator 20 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 with the heat source pipe 22 of the evaporator 20 and the heat source pipe 32 of the regenerator 30. If the drive 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 drive heat source fluid RS flows from the evaporator 20 to the regenerator 30 in series, the concentration of the absorption liquid S is suppressed from being excessively increased, and the absorption liquid S is less likely to crystallize. Further, if the driving heat source fluid RS flows in parallel with the evaporator 20 and the regenerator 30, it is possible to suppress an increase in the concentration of the absorbing liquid S while improving the COP. As described above, regardless of whether the drive heat source fluid RS that has flowed into the drive 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-increasing target fluid RP that has flowed into the tube 51 is introduced into the heat transfer tube 12 of the absorber 10. The drive heat source fluid RS flows in series from the heat source tube 32 of the regenerator 30 to the heat source tube 22 of the evaporator 20, or flows in parallel to the heat source tube 22 of the evaporator 20 and the heat source tube 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 drive 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 allowed to flow. 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 to join the fluid flowing out from the heat utilization facility HCF into the drive heat source fluid RS while forming an independent system.

In the above description, the heating source fluid (merged heat source fluid RA, driving heat source fluid RS) and the fluid to be heated (heat temperature target fluid RP, low temperature heat source fluid GP) are the same type of fluid because they are split and merged. The fluid to be applied may be a heat medium liquid 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 adopted, it may be applied up 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 it may be a flowing liquid film type. When the evaporator is of the flow-down 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 in the case of the full liquid type, it is connected to the evaporator can body 21. The end of the refrigerant liquid pipe 45 may be connected to the refrigerant liquid supply device. Further, a pipe and a pump for supplying the refrigerant liquid Vf at the lower part of the evaporator can body 21 to the refrigerant liquid supply device may be provided.

In the above description, an 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 has been described, but these may be configured in multiple stages. For example, when the absorption heat pump cycle is a two-stage temperature rise type, the absorber 10 and the evaporator 20 are represented by a high temperature absorber on the high temperature side (hereinafter, for convenience of explanation, the reference numeral “10” is added with “H”. ) And the high temperature evaporator (hereinafter, represented by adding "H" to the reference numeral "20" for convenience of explanation) and the low temperature absorber on the low temperature side (hereinafter, for convenience of explanation, the reference numeral "10" is represented by "L"). It may be divided into a low temperature evaporator (hereinafter, for convenience of explanation, it is represented by adding “L” to the reference numeral “20”). 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 upper part 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 are typically communicated at the top so that the vapor of the refrigerant V of the low temperature evaporator 20L can be transferred to the low temperature absorber 10L. The temperature-increasing target fluid RP separated from the merging 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 drive heat source fluid RS separated 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 with the absorbed heat when the absorbing liquid S absorbs the vapor of the refrigerant V moved from the low temperature evaporator 20L, and the refrigerant V in the high temperature evaporator 20H. The vapor 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. Is 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 tube 99 Coolant heat exchanger GP Low temperature heat source fluid RP Heat temperature target fluid RS Driven heat source fluid Sa concentrated solution Sw Rare Solution Ve Evaporator Fluid Steam Vf Fluid Liquid Vg Regenerator Fluid Steam

Claims (6)

Absorption heat exchange system;
With an absorbing part that raises the temperature of the first fluid to be heated by the absorbed heat released when the absorbing liquid absorbs the vapor of the refrigerant and becomes a dilute solution with a reduced concentration;
With a condensing part that raises the temperature of the second fluid to be heated by the heat of condensation released when the vapor of the refrigerant condenses into a refrigerant liquid;
The heating source is introduced by introducing the refrigerant liquid from the condensing portion, and removing the latent heat of vaporization required when the introduced refrigerant liquid evaporates to become vapor of the refrigerant supplied to the absorbing portion from the heating source fluid. With an evaporative part that lowers the temperature of the fluid;
The dilute solution is introduced from the absorption unit, and the heat required for heating the introduced dilute solution to separate the refrigerant from the dilute solution to obtain a concentrated solution having an increased concentration is taken from the heating source fluid. Equipped with a regenerator that lowers the temperature of the heating source fluid;
Due to the absorption heat pump cycle of the absorbing liquid and the refrigerant, the internal pressure and temperature of the absorbing portion are higher than those of the regenerating portion, and the internal pressure and temperature of the evaporating portion are higher than those of the condensed portion. Configured;
The heat source fluid supplied to the evaporation unit and the regeneration unit is supplied from a heat source facility outside the absorption heat exchange system;
A part of the heat source fluid branched from the heat source fluid supplied from the heat source equipment and before being introduced into the evaporation unit and the regeneration unit is introduced into the absorption unit as the first heated fluid. It was configured as;
Absorption heat exchange system.
The flow rate of the heating source fluid flowing into the evaporating part and the regenerating part and the first covering on the absorbing part so that the temperature of the first heated fluid flowing out from the absorbing part becomes a predetermined temperature. The ratio to the flow rate of the heating source fluid flowing in as the heating fluid was set;
The absorption heat exchange system according to claim 1. The second heated fluid flowing out of the condensing section was configured to mix with the heating source fluid flowing out of at least one of the evaporation section and the regeneration section;
The absorption heat exchange system according to claim 1 or 2. A partial cover that merges a part of the second heated fluid branched from the second heated fluid flowing out of the condensing portion with the first heated fluid before being introduced into the absorbing portion. Equipped with a heated fluid bypass flow path;
The absorption heat exchange system according to any one of claims 1 to 3. From at least one of the evaporating part and the regenerating part of the second heated fluid flowing out from the condensing part so that the temperature of the first heated fluid flowing out from the absorbing part becomes a predetermined temperature. The ratio of the flow rate mixed with the outflowing heating source fluid to the flow rate flowing 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 evaporating unit and the heating source fluid flowing out from at least one of the evaporating unit and the regenerating unit is provided;
The absorption heat exchange system according to any one of claims 1 to 5.

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