CN109974328A - Absorption type heat exchange system - Google Patents

Absorption type heat exchange system Download PDF

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Publication number
CN109974328A
CN109974328A CN201811552771.6A CN201811552771A CN109974328A CN 109974328 A CN109974328 A CN 109974328A CN 201811552771 A CN201811552771 A CN 201811552771A CN 109974328 A CN109974328 A CN 109974328A
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CN
China
Prior art keywords
absorption
condensation
fluid
temperature
evaporation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201811552771.6A
Other languages
Chinese (zh)
Inventor
竹村与四郎
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ebara Refrigeration Equipment and Systems Co Ltd
Original Assignee
Ebara Refrigeration Equipment and Systems Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to JP2017247654A priority Critical patent/JP2019113260A/en
Priority to JP2017-247654 priority
Application filed by Ebara Refrigeration Equipment and Systems Co Ltd filed Critical Ebara Refrigeration Equipment and Systems Co Ltd
Publication of CN109974328A publication Critical patent/CN109974328A/en
Pending legal-status Critical Current

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Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B15/00Sorption machines, plant, or systems, operating continuously, e.g. absorption type
    • F25B15/006Sorption machines, plant, or systems, operating continuously, e.g. absorption type with cascade operation
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B30/00Heat pumps
    • F25B30/04Heat pumps of the sorption type
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B30/00Heat pumps
    • F25B30/06Heat pumps characterised by the source of low potential heat
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B33/00Boilers; Analysers; Rectifiers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B37/00Absorbers; Adsorbers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B39/00Evaporators; Condensers
    • F25B39/02Evaporators
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B39/00Evaporators; Condensers
    • F25B39/04Condensers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25BREFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT-PUMP SYSTEMS
    • F25B41/00Fluid-circulation arrangements
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28DHEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28DHEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0068Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for refrigerant cycles
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00Adapting or protecting infrastructure or their operation
    • Y02A30/27Relating to heating, ventilation or air conditioning [HVAC] technologies
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02BCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62Absorption based systems

Abstract

Absorption type heat exchange system provided by the invention keeps the outlet temperature for being heated fluid higher than the inlet temperature of heating source fluid.Absorption type heat exchange system has: making to be heated the first absorption portion, the second absorption portion, the first condensation part, the second condensation part that the temperature of fluid rises;The first evaporation part, the second evaporation part, the first reproducing unit, the second reproducing unit for reducing the temperature of heating source fluid;And in the heat exchange department for flowing out and carrying out between fluid and the heating source fluid of a part from the heating source fluid branch towards before each evaporation part and the importing of each reproducing unit to being heated before the inflow of each absorption portion heat exchange from each condensation part, pass through the absorption heat pump cycle of absorbing liquid and refrigerant, the pressure and temperature of the inside of first evaporation part are higher than the first condensation part, the pressure and temperature of the inside of second evaporation part are higher than the second condensation part, and the fluid that is heated flowed out from heat exchange department is flowed into each absorption portion.

Description

Absorption type heat exchange system
Technical field
The present invention relates to absorption type heat exchange systems, more particularly to so that the outlet temperature of cryogen compares high temperature fluid The high mode of inlet temperature, the absorption type heat exchange system of heat exchange is carried out between two fluids.
Background technique
Heat exchanger is widely used as carrying out the device of heat exchange between the fluid of high temperature and the fluid of low temperature.At two In the heat exchanger for directly carrying out heat exchange between fluid, the outlet temperature of the fluid of low temperature can not be made to become the fluid than high temperature The high temperature of inlet temperature (for example, referring to patent document 1).
Patent document 1: No. 5498809 bulletins of Japanese Patent No. (referring to Fig.1 1 etc.)
As a purposes of heat exchanger, enumerates and heat extraction is recycled.Heat extraction is to be not used and discarded heat, therefore If the outlet temperature of the fluid for the low temperature that can make recycling heat extraction and increase temperature becomes than comprising the high temperature including heat extraction Fluid the high temperature of inlet temperature, then make the range utilized broaden.
Summary of the invention
The present invention in view of above-mentioned project, and it is an object of the present invention to provide it is a kind of can make the fluid for being equivalent to low temperature be heated stream The high absorption type heat exchange system of the inlet temperature of the heating source fluid of fluid of the outlet temperature of body than being equivalent to high temperature.
To achieve the goals above, for the absorption type heat exchange system of the 1st aspect of the present invention, such as Fig. 1 institute Show have: the first absorption portion A1, by absorbing liquid Sa absorb refrigerant steam Ve1 when release absorption heat and make by The temperature for heating fluid FL rises;Second absorption portion A2 is released when absorbing the steam Ve2 of refrigerant by absorbing liquid Sa It absorbs heat and increase the temperature for being heated fluid FL;First condensation part C1 is condensed by the steam Vg1 of refrigerant and is become The condensation heat released when refrigerant liquid Vf1 rises the temperature for being heated fluid FL;Second condensation part C2, by system The condensation heat that the steam Vg2 of cryogen is released when condensing and becoming refrigerant liquid Vf2, makes to be heated in the temperature of fluid FL It rises;First evaporation part E1 is directly or indirectly imported from at least one party of the first condensation part C1 and the second condensation part C2 Refrigerant liquid Vf, and capture imported refrigerant liquid Vf evaporation from heating source fluid FH and become to the first absorption portion A1 Required evaporation latent heat when the steam Ve1 of the refrigerant of supply, so that making the temperature of heating source fluid FH reduces;Second evaporation Portion E2 directly or indirectly imports refrigerant liquid from at least one party of the first condensation part C1 and the second condensation part C2 Vf, and capture imported refrigerant liquid Vf evaporation from heating source fluid FH and become the refrigeration supplied to the second absorption portion A2 Required evaporation latent heat when the steam Ve2 of agent, so that making the temperature of heating source fluid FH reduces;First reproducing unit G1, from At least one party of first absorption portion A1 and the second absorption portion A2 directly or indirectly import absorbing liquid Sw, from heating source fluid FH captures to generate to the steam Vg1 of the first condensation part C1 refrigerant supplied and heats to the absorbing liquid Sw imported And refrigerant is made to be detached from required heat from absorbing liquid Sw, so that making the temperature of heating source fluid FH reduces;Second reproducing unit G2, Absorbing liquid Sw is directly or indirectly imported from at least one party of the first absorption portion A1 and the second absorption portion A2, from heating source stream Body FH captures to generate to the steam Vg2 of the second condensation part C2 refrigerant supplied and adds to the absorbing liquid Sw imported Heat simultaneously makes refrigerant be detached from required heat from absorbing liquid Sw, so that making the temperature of heating source fluid FH reduces;And heat exchange department 80, make to flow into from the first condensation part C1 and the second condensation part C2 outflow to the first absorption portion A1 and the second absorption portion A2 It is preceding be heated fluid FL, with from towards the first evaporation part E1, the second evaporation part E2, the first reproducing unit G1 and the second reproducing unit Heat exchange, the absorption type heat are carried out between the heating source fluid FHs of a part of the heating source fluid FH branch before G2 importing Exchange system is constituted are as follows: by the absorption heat pump cycle of absorbing liquid and refrigerant, so that the pressure of the inside of the first evaporation part E1 Power and temperature are than the first condensation part C1 high, and the pressure and temperature of the inside of the second evaporation part E2 are than the second condensation part C2 high; In such a way that make to flow out from heat exchange department 80 is heated fluid FL to the first absorption portion A1 and the second absorption portion A2 inflow, structure At the flow path for being heated fluid FL.
If constituting in this wise, the temperature for being heated fluid flowed out from the first absorption portion and the second absorption portion can be made Temperature than the heating source fluid before flowing into the first evaporation part, the second evaporation part, the first reproducing unit and the second reproducing unit is high.
In addition, for the absorption type heat exchange system of the 2nd aspect of the present invention, such as shown in Fig. 1, at above-mentioned On the basis of the absorption type heat exchange system 1 of the first method of invention, so that the heating source fluid flowed out from heat exchange department 80 FHs and the heating source stream flowed out from the first evaporation part E1, the second evaporation part E2, the first reproducing unit G1 and the second reproducing unit G2 The mode at the interflow body FH, constitutes the flow path of heating source fluid FH.
If constituting in this wise, the flow of the heating source fluid passed in and out relative to absorption type heat exchange system can be made flat Weighing apparatus.
To achieve the goals above, for the absorption type heat exchange system of the 3rd aspect of the present invention, such as Fig. 2 institute Show have: the first absorption portion A1, by absorbing liquid Sa absorb refrigerant steam Ve1 when release absorption heat and make by The temperature for heating fluid FL rises;Second absorption portion A2 is released when absorbing the steam Ve2 of refrigerant by absorbing liquid Sa It absorbs heat and increase the temperature for being heated fluid FL;First condensation part C1 is condensed by the steam Vg1 of refrigerant and is become The condensation heat released when refrigerant liquid Vf1 rises the temperature for being heated fluid FL;Second condensation part C2, by refrigeration The condensation heat that the steam Vg2 of agent is released when condensing and becoming refrigerant liquid Vf2 rises the temperature for being heated fluid FL;The One evaporation part E1 directly or indirectly imports refrigerant from at least one party of the first condensation part C1 and the second condensation part C2 Liquid Vf captures imported refrigerant liquid Vf evaporation from heating source fluid FH and becomes the system supplied to the first absorption portion A1 Required evaporation latent heat when the steam Ve1 of cryogen, so that making the temperature of heating source fluid FH reduces;Second evaporation part E2, Refrigerant liquid Vf is directly or indirectly imported from at least one party of the first condensation part C1 and the second condensation part C2, from heating Source stream body FH captures imported refrigerant liquid Vf evaporation and becomes the steam Ve2 to the second absorption portion A2 refrigerant supplied When required evaporation latent heat, so that making the temperature of heating source fluid FH reduces;First reproducing unit G1, from the first absorption portion A1 And second at least one party of absorption portion A2 directly or indirectly import absorbing liquid Sw, capture from heating source fluid FH for life The absorbing liquid Sw imported is heated at the steam Vg1 of the refrigerant supplied to the first condensation part C1 and make refrigerant from Absorbing liquid Sw is detached from required heat, so that making the temperature of heating source fluid FH reduces;Second reproducing unit G2, from the first absorption portion At least one party of A1 and the second absorption portion A2 directly or indirectly import absorbing liquid Sw, from heating source fluid FH capture in order to It generates to the steam Vg2 of the second condensation part C2 refrigerant supplied and the absorbing liquid Sw imported is heated and makes refrigerant Required heat is detached from from absorbing liquid Sw, so that making the temperature of heating source fluid FH reduces;And heat exchange department 80, make from first Condensation part C1 and the second condensation part C2 flows out and is heated stream to before the first absorption portion A1 and the second absorption portion A2 inflow Body FL and the heating source stream flowed out from the first evaporation part E1, the second evaporation part E2, the first reproducing unit G1 and the second reproducing unit G2 Heat exchange is carried out between body FH, the absorption type heat exchange system is constituted are as follows: passes through the absorption heat pump of absorbing liquid and refrigerant Circulation, so that the pressure and temperature of the inside of the first evaporation part E1 are than the first condensation part C1 high, the inside of the second evaporation part E2 Pressure and temperature than the second condensation part C2 high so that from heat exchange department 80 flow out be heated fluid FL to the first absorption portion The mode that A1 and the second absorption portion A2 is flowed into constitutes the flow path for being heated fluid FL.
If constituting in this wise, the temperature for being heated fluid flowed out from the first absorption portion and the second absorption portion can be made Temperature than the heating source fluid before flowing into the first evaporation part, the second evaporation part, the first reproducing unit and the second reproducing unit is high.
In addition, for the absorption type heat exchange system of the 4th aspect of the present invention, such as shown in Fig. 1, at above-mentioned On the basis of the absorption type heat exchange system 1 of any one mode in first method~Third Way of invention, so that from first The absorbing liquid Sw of at least one party of absorption portion A1 and the second absorption portion A2 outflow is directly or indirectly to the first reproducing unit G1 It is flowed into parallel with the second reproducing unit G2, the absorbing liquid flowed out from at least one party of the first reproducing unit G1 and the second reproducing unit G2 The mode that Sa is directly or indirectly flowed into the first absorption portion A1 and the second absorption portion A2 in parallel, constitutes the stream of absorbing liquid Road.
If constituting in this wise, the concentration for being able to suppress absorbing liquid excessively rises.
In addition, for the absorption type heat exchange system of the 5th aspect of the present invention, such as shown in Fig. 3, at above-mentioned In the absorption type heat exchange system 3 of any one mode in first method~Third Way of invention, so that from the first absorption portion At least one party of A1 and the second absorption portion A2 directly or indirectly flow into the first reproducing unit G1 or the second reproducing unit G2 Absorbing liquid flowed in series in the first reproducing unit G1 and the second reproducing unit G2, from the first reproducing unit G1 and the second reproducing unit The absorbing liquid that at least one party of G2 directly or indirectly flows into the first absorption portion A1 or the second absorption portion A2 is inhaled first The mode that receipts portion A1 and the second absorption portion A2 flow in series, constitutes the flow path of absorbing liquid.
If constituting in this wise, the concentration difference of absorbing liquid can be made to become larger and increase output.
In addition, for the absorption type heat exchange system of the 6th aspect of the present invention, such as shown in Fig. 4, at above-mentioned In the absorption type heat exchange system 4 of any one mode in first method~Third Way of invention, have: the first absorbing liquid is followed Circulation road 14,34 so that from the first absorption portion A1 flow out absorbing liquid Sw1 flowed into the first reproducing unit G1 and from first again The mode that is flowed into the first absorption portion A1 of absorbing liquid Sa1 of life portion G1 outflow, make absorbing liquid the first absorption portion A1 and first again It is recycled between life portion G1;With the second absorbing liquid circulation stream 18,38 so that from the second absorption portion A2 flow out absorbing liquid Sw2 The mode that is flowed into the second absorption portion A2 of absorbing liquid Sa2 for flowing into the second reproducing unit G2 and being flowed out from the second reproducing unit G2, Recycle absorbing liquid between the second absorption portion A2 and the second reproducing unit G2.
If constituting in this wise, multiple independent system roads of the absorption heat pump cycle with absorbing liquid and refrigerant Diameter, so as to carry out control management to multiple absorption heat pump cycles.
In addition, for the absorption type heat exchange system of the 7th aspect of the present invention, such as shown in Fig. 1, at above-mentioned On the basis of the absorption type heat exchange system 1 of any one mode in the first method of invention~the 6th mode, so as to be heated The mode that fluid FL flows in series in the first absorption portion A1 and the second absorption portion A2 constitutes the flow path for being heated fluid FL.
If constituting in this wise, it can make to be heated fluid with two step-up temperatures, being added for higher temperature can be taken out Hot fluid.
In addition, for the absorption type heat exchange system of the 8th aspect of the present invention, such as shown in Fig. 5, at above-mentioned In the absorption type heat exchange system 5 of any one mode in the first method of invention~the 7th mode, so that heating source fluid FH The first reproducing unit G1 or the first evaporation part E1 is flowed at first, and is steamed in suitable order in the first reproducing unit G1, first The mode that hair portion E1, the second reproducing unit G2 and the second evaporation part E2 flow in series constitutes the flow path of heating source fluid FH, with Make to be heated fluid FL after flowing through the first condensation part C1 and the second condensation part C2 in series to the first absorption portion A1 or Two absorption portion A2 are flowed into, and after heating source fluid FH flows through the first evaporation part E1 the case where the second evaporation part E2 flows Under, it is heated fluid FL and flows through the mode flowed after the second absorption portion A2 in the first absorption portion A1, and so that in heating source fluid FH is flowed through after the second evaporation part E2 in the case where the first evaporation part E1 flowing, is heated after fluid FL flows through the first absorption portion A1 In the mode of the second absorption portion A2 flowing, the flow path for being heated fluid FL is constituted.
If constituting in this wise, in heating source fluid at first to being capable of increasing in the case where the inflow of the first reproducing unit from adding Heat source fluid is to being heated the heat of fluid movement and can be improved the temperature for being heated fluid of outflow, in heating source fluid At first to the first evaporation part flow into the case where, in addition to from heating source fluid towards be heated fluid mobile heat increase with And outflow is heated except the high temperature of fluid, is able to suppress the dense of the first reproducing unit and the absorbing liquid in the second reproducing unit The rising of degree, crystallizes so as to avoid absorbing liquid from being excessively concentrated.
In addition, for the absorption type heat exchange system of the 9th aspect of the present invention, such as shown in Fig. 6 and Fig. 7, In the absorption type heat exchange system 6,7 of any of the first method of aforementioned present invention~the 6th mode mode, it is configured to carry out At least one of constitute below, it may be assumed that carry out with by heating source fluid FH to the first evaporation part E1, the second evaporation part E2, first At least two modes imported in parallel in reproducing unit G1 and the second reproducing unit G2 constitute the flow path (example of heating source fluid FH As referring to Fig. 7);With will be heated fluid FL to the first absorption portion A1 and the second absorption portion A2 import in parallel (not shown) and It is heated at least one party's that fluid FL is imported to the first condensation part C1 and the second condensation part C2 in parallel in (referring for example to Fig. 6) Mode constitutes the flow path for being heated fluid FL.
If constituting in this wise, heating source fluid can be reduced and be heated the resistance of the flow path of at least one party of fluid Power.
In addition, for the absorption type heat exchange system of the 10th aspect of the present invention, such as shown in Fig. 8, at above-mentioned In the absorption type heat exchange system 1A of any one mode in the first method of invention~the 9th mode, have: first is raw and cold again Solidifying tank body 30, in a manner of being connected to the first reproducing unit G1 with the first condensation part C1, receiving the first reproducing unit G1 and first is cold Solidifying portion C1;The is accommodated in a manner of being connected to the second reproducing unit G2 with the second condensation part C2 with the second regeneration condensation tank body 40 Two reproducing unit G2 and the second condensation part C2.
If constituting in this wise, it is able to suppress the enlargement of device, and is able to suppress from each reproducing unit to condensation part and moves The increase of the flow resistance of the steam of dynamic refrigerant, so as to improve the efficiency as absorption heat pump cycle.
In addition, for the absorption type heat exchange system of the 11st aspect of the present invention, such as shown in Fig. 8, above-mentioned On the basis of the absorption type heat exchange system 1A of the 10th aspect of the present invention, have: first absorbs evaporation tank body 10, so that the The mode that one absorption portion A1 is connected to the first evaporation part E1 accommodates the first absorption portion A1 and the first evaporation part E1;It is absorbed with second Tank body 20 is evaporated, in a manner of being connected to the second absorption portion A2 with the second evaporation part E2, accommodates the second absorption portion A2 and second Evaporation part E2, the first regeneration condensation tank body 30 are configured at position different in horizontal direction from the second regeneration condensation tank body 40, The top of first regeneration condensation tank body 30 and the second regeneration condensation tank body 40 absorbs evaporation tank body 10 and the configured with first Two absorb evaporation tank body 20.
If constituting in this wise, it can ensure the flowing of absorbing liquid and inhibit the enlargement of device.
In addition, for the absorption type heat exchange system of the 12nd aspect of the present invention, for example, Fig. 9 (A), Fig. 9 (B), Shown in Fig. 9 (D), on the basis of the absorption type heat exchange system of the tenth mode of aforementioned present invention, the first absorption portion A1 receiving In the tank body different from the first evaporation part E1, the second absorption portion A2 is contained in the tank body different from the second evaporation part E2.
If constituting in this wise, in the case where the first absorption portion and/or the second absorption portion are damaged, can compare Relatively easily only replace the absorption portion being damaged.
In addition, for the absorption type heat exchange system of the 13rd aspect of the present invention, such as shown in Figure 11, above-mentioned In the absorption type heat exchange system 9 of any one mode in the 1st aspect of the present invention~the 12nd mode, have: third absorbs Portion A3, the absorption released when absorbing the steam Ve3 of refrigerant by absorbing liquid Sa is hot and makes the temperature for being heated fluid FL Rise;Third condensation part C3, the condensation released when becoming refrigerant liquid Vf3 by the steam Vg3 condensation of refrigerant Heat and the temperature for making to be heated fluid FL rises;Third evaporation part E3, from the first condensation part C1, the second condensation part C2 and At least one of three condensation part C3 directly or indirectly imports refrigerant liquid Vf, captures from heating source fluid FH and to be imported Refrigerant liquid Vf evaporation and required evaporation latent heat when becoming to the steam Ve3 of the third absorption portion A3 refrigerant supplied, from And reduce the temperature of heating source fluid FH;And third reproducing unit G3, from the first absorption portion A1, the second absorption portion A2 and At least one of third absorption portion A3 directly or indirectly imports absorbing liquid Sw, capture from heating source fluid FH in order to generate to Third condensation part C3 supply refrigerant steam Vg3 and the absorbing liquid Sw imported is heated and makes refrigerant from absorption Heat needed for liquid Sw is detached from is configured to the absorption by absorbing liquid and refrigerant so that making the temperature of heating source fluid FH reduces Formula heat pump cycle, so that the pressure and temperature of the inside of third evaporation part E3 are than third condensation part C3 high, 80 structure of heat exchange department It is inhaled as being flowed out from the first condensation part C1, the second condensation part C2 and third condensation part C3 to the first absorption portion A1, second The fluid FL that is heated before receipts portion A2 and third absorption portion A3 is flowed into is flowed into, so as to be heated stream from what heat exchange department 80 flowed out The mode that body FL is flowed into the first absorption portion A1, the second absorption portion A2 and third absorption portion A3, composition are heated fluid FL's Flow path.
If constituting in this wise, the temperature for being heated fluid can be made further up.
In accordance with the invention it is possible to make from the temperature ratio for being heated fluid that the first absorption portion and the second absorption portion are flowed out to The temperature of heating source fluid before first evaporation part, the second evaporation part, the first reproducing unit and the inflow of the second reproducing unit is high.
Detailed description of the invention
Fig. 1 is the exemplary system figure of the absorption type heat exchange system of first embodiment of the invention.
Fig. 2 is the exemplary system figure of the absorption type heat exchange system of second embodiment of the present invention.
Fig. 3 is the exemplary system figure of the absorption type heat exchange system of third embodiment of the present invention.
Fig. 4 is the exemplary system figure of the absorption type heat exchange system of the 4th embodiment of the invention.
The exemplary system figure of the absorption type heat exchange system of 5th embodiment Fig. 5 of the invention.
Fig. 6 is the exemplary system figure of the absorption type heat exchange system of sixth embodiment of the invention.
Fig. 7 is the exemplary system figure of the absorption type heat exchange system of the 7th embodiment of the invention.
Fig. 8 is the outline structure of absorption type heat exchange system involved in the variation of first embodiment of the invention Figure.
Fig. 9 (A)~Fig. 9 (D) is matching for each tank body in the absorption type heat exchange system for indicate embodiments of the present invention The skeleton diagram for the change set.
Figure 10 is the schematic structural diagram of the absorption type heat exchange system of the 8th embodiment of the invention.
Figure 11 is the exemplary system figure of the absorption type heat exchange system of the 9th embodiment of the invention.
Figure 12 is the exemplary system figure of the absorption type heat exchange system of the tenth embodiment of the invention.
Description of symbols: 1,1A, 2,3,4,5,6,7,8,9,10... absorption type heat exchange system;10... first absorbs Evaporate tank body;14... the first weak solution effuser;18... the second weak solution effuser;20... second absorbs evaporation tank body; 30... the first regeneration condensation tank body;34... the first concentrated solution effuser;38... the second concentrated solution effuser;40... second again The solidifying tank body of raw food;A1... the first absorber;A2... the second absorber;A3... third absorber;C1... the first condenser; C2... the second condenser;C3... third condenser;E1... the first evaporator;E2... the second evaporator;E3... third is evaporated Device;G1... the first regenerator;G2... Second reactivator;G3... third regenerator;FH... high temperature fluid;FL... low temperature stream Body;Sa... concentrated solution;Sa1... the first concentrated solution;Sa2... the second concentrated solution;Sa3... third concentrated solution;Sw... dilute molten Liquid;Sw1... the first weak solution;Sw2... the second weak solution;Sw3... third weak solution;Ve1... the first evaporator refrigerant Steam;Ve2... the second evaporator refrigerant steam;Ve3... third evaporator refrigerant steam;Vf... refrigerant liquid; Vf1... the first refrigerant liquid;Vf2... second refrigerant liquid;Vf3... third refrigerant liquid;Vg1... the first regeneration Device refrigerant vapour;Vg2... Second reactivator refrigerant vapour;Vg3... third regenerator refrigerant vapour.
Specific embodiment
Hereinafter, the embodiments of the present invention will be described with reference to the drawings.In addition, in the various figures, for same to each other or The comparable component of person marks same or similar appended drawing reference, and the repetitive description thereof will be omitted.
Firstly, being illustrated referring to Fig.1 to the absorption type heat exchange system 1 of first embodiment of the invention.Fig. 1 is to inhale The exemplary system figure of receipts formula heat-exchange system 1.Absorption type heat exchange system 1 is the absorption type heat using absorbing liquid と refrigerant と Pump circulation carries out cryogen FL in the mode for keeping the outlet temperature of cryogen FL higher than the inlet temperature of high temperature fluid FH With the system of the heat exchange of high temperature fluid FH.Here, cryogen FL is as making in temperature in absorption type heat exchange system 1 The fluid of the object risen, is equivalent to and is heated fluid.High temperature fluid FH is that temperature reduces in absorption type heat exchange system 1 Fluid is equivalent to heating source fluid.As the example of cryogen FL, enumerate for heating or as other absorption The heat source of the heat resource equipments such as refrigeration machine, absorption heat pump is come the fluid that utilizes.As the example of high temperature fluid FH, enumerate by steel The fluid of the discharges such as factory, power plant, manufacturing process, factory.Absorption type heat exchange system 1 has composition and carries out absorbing liquid and refrigeration First absorber A1 of the capital equipment of the absorption heat pump cycle of agent, the second absorber A2, the first evaporator E1, the second evaporation Device E2, the first regenerator G1, Second reactivator G2, the first condenser C1 and the second condenser C2, and have heat exchange department 80。
In the present specification, about absorbing liquid, for the ease of the difference on heat pump circulating system, with character, heat pump cycle It accordingly calls for " weak solution Sw ", " the first weak solution Sw1 ", " concentrated solution Sa ", " the second concentrated solution Sa2 " position in system Deng, but " absorbing liquid S " can be referred to as when keeping aloof from character etc..Similarly, about refrigerant, for the ease of heat pump circulating system On difference, accordingly called with the position on character, heat pump circulating system for " the first evaporator refrigerant steam Ve1 ", " the Two regenerator refrigerant vapour Vg2 ", " refrigerant liquid Vf ", " the first refrigerant liquid Vf1 " etc., but keeping aloof from character etc. When can be referred to as " refrigerant V ".In the present embodiment, it is used as absorbing liquid S (mixture of absorbent and refrigerant V) LiBr aqueous solution uses water (H as refrigerant V2O)。
First absorber A1 is that the first evaporator refrigerant generated by the first evaporator E1 is absorbed using concentrated solution Sa The equipment of steam Ve1 is equivalent to the first absorption portion.First absorber A1 includes the flow path for constituting cryogen FL in inside First absorbs heat conducting pipe 11;The the first absorber solution supplied with the surface that concentrated solution Sa is absorbed heat conducting pipe 11 to first supplies Device 12.First absorber A1 is supplied dense from the surface that the first absorber solution supplying device 12 absorbs heat conducting pipe 11 to first Solution S a is generated when concentrated solution Sa absorbs the first evaporator refrigerant steam Ve1 and becomes the first weak solution Sw1 and is absorbed heat. The cryogen FL for being configured to flow in the first absorption heat conducting pipe 11 is by absorption warm, so that cryogen FL is heated. In the first absorber solution supplying device 12, it is connected with one end of concentrated solution Sa the first concentrated solution ingress pipe 13 imported.? The lower part (typical for be bottom) of first absorber A1 is connected with for the first dilute of the first weak solution Sw1 outflow stockpiled One end of solution effuser 14.
First evaporator E1 is that refrigerant liquid Vf is made to evaporate and generate the first evaporator system using the heat of high temperature fluid FH The equipment of refrigerant vapor Ve1 is equivalent to the first evaporation part.First evaporator E1 has in the inside of the tank body of the first evaporator E1 Constitute the first evaporation heat source tube 21 of the flow path of high temperature fluid FH.First evaporator E1 is in the inside of the tank body of the first evaporator E1 Without the nozzle for making refrigerant liquid Vf disperse.Therefore, the first evaporation heat source tube 21 is accumulated in the first evaporator E1 to be immersed in The intracorporal refrigerant liquid Vf of tank in mode (flooded evaporator) is arranged.First evaporator E1 is configured to using first Evaporation heat source tube 21 in flow high temperature fluid FH heat make 21 periphery of the first evaporation heat source tube refrigerant liquid Vf evaporate and Generate the first evaporator refrigerant steam Ve1.In the first evaporator E1, it is connected with and internally supplies the first of refrigerant liquid Vf One end of refrigerant liquid ingress pipe 23.
First absorber A1 and the first evaporator E1 is contained in the first absorption in mode adjacent in the horizontal direction and steams Send out tank body (hereinafter referred to as " first absorbs evaporation tank body 10 ").In the inside that first absorbs evaporation tank body 10, being provided with will be internal Space is greatly classified into two the first absorption evaporation walls 19.It is absorbed in evaporation tank body 10 first, to clip the first absorption steaming The mode of hair wall 19 is provided with the first absorber A1 in a side, and another party is provided with the first evaporator E1.It absorbs and steams from first The first of the first side evaporator E1 that hair wall 19 rises absorbs the tank body that evaporation tank body 10 constitutes the first evaporator E1.First absorbs steaming Hair wall 19 is set as in a manner of being connected to the first absorber A1 on top with the first evaporator E1, does not absorb evaporator with first The top surface of body 10 contacts.That is, first absorb evaporation wall 19 first absorb evaporation tank body 10 removing top two sidewalls and Bottom absorbs evaporation tank body 10 with first and contacts.According to this structure, it is absorbed in evaporation tank body 10 first, the first evaporation Device refrigerant vapour Ve1 can be mobile from the first evaporator E1 to the first absorber A1.
Second absorber A2 is that the second evaporator refrigerant generated by the second evaporator E2 is absorbed using concentrated solution Sa The equipment of steam Ve2 is equivalent to the second absorption portion.Second absorber A2 includes the flow path for constituting cryogen FL in inside Second absorbs heat conducting pipe 15;The the second absorber solution supplied with the surface that concentrated solution Sa is absorbed heat conducting pipe 15 to second supplies Device 16.Second absorber A2 is constituted identically as the first absorber A1, and the second absorption heat conducting pipe 15 and the second absorber are molten Liquid supplying device 16 corresponds respectively to the first absorption heat conducting pipe 11 and the first absorber solution supplying device 12.Second absorber A2 is supplied concentrated solution Sa from the surface that the second absorber solution supplying device 16 absorbs heat conducting pipe 15 to second, in concentrated solution Sa It is generated when absorbing the second evaporator refrigerant steam Ve2 and becoming the second weak solution Sw2 and absorbs heat.It is configured to absorb second and leads The cryogen FL flowed in heat pipe 15 is by absorption warm, so that cryogen FL is heated.Second absorbs heat conducting pipe 15 One end is connect with one end of the first absorption heat conducting pipe 11 by absorber cryogen connecting tube 71.It is supplied in the second absorber solution To device 16, it is connected with one end of concentrated solution Sa the second concentrated solution ingress pipe 17 imported.In the lower part of the second absorber A2 (being bottom for typical), is connected with one end of the second weak solution effuser 18 for the second weak solution Sw2 outflow stockpiled.
Second evaporator E2 is that refrigerant liquid Vf is made to evaporate and generate the second evaporator system using the heat of high temperature fluid FH The equipment of refrigerant vapor Ve2 is equivalent to the second evaporation part.Second evaporator E2 has in the inside of the tank body of the second evaporator E2 Constitute the second evaporation heat source tube 25 of the flow path of high temperature fluid FH.Second evaporator E2 is constituted identically as the first evaporator E1, Second evaporation heat source tube 25 corresponds to the first evaporation heat source tube 21.Second evaporator E2 is configured to evaporate heat source tube using second The heat of the high temperature fluid FH flowed in 25 makes the refrigerant liquid Vf on 25 periphery of the second evaporation heat source tube evaporate and generate second and steam Send out device refrigerant vapour Ve2.One end of first evaporation heat source tube 21 and one end of the second evaporation heat source tube 25 pass through evaporator height Warm fluid connecting line 72 connects.In the second evaporator E2, it is connected with the second refrigerant liquid for internally supplying refrigerant liquid Vf One end of body ingress pipe 27.
Second absorber A2 and the second evaporator E2 is contained in the second absorption in mode adjacent in the horizontal direction and steams Send out tank body (hereinafter referred to as " second absorbs evaporation tank body 20 ").In the inside that second absorbs evaporation tank body 20, being provided with will be internal Space is greatly classified into two the second absorption evaporation walls 29.It is absorbed in evaporation tank body 20 second, to clip the second absorption steaming The mode of hair wall 29 is provided with the second absorber A2 in a side, and another party is provided with the second evaporator E2.It absorbs and steams from second The second of the second side evaporator E2 that hair wall 29 rises absorbs the tank body that evaporation tank body 20 constitutes the second evaporator E2.Second absorbs steaming Hair wall 29 is set as in a manner of being connected to the second absorber A2 on top with the second evaporator E2, does not absorb evaporator with second The top surface of body 20 contacts.That is, second absorb evaporation wall 29 second absorb evaporation tank body 20 removing top two sidewalls and Bottom absorbs evaporation tank body 20 with second and contacts.According to this structure, it is absorbed in evaporation tank body 20 second, the second evaporation Device refrigerant vapour Ve2 can be mobile from the second evaporator E2 to the second absorber A2.
First regenerator G1 be the weak solution Sw of the absorbing liquid S relatively low as concentration is carried out heating concentration and make its Regenerated equipment in concentration, is equivalent to the first reproducing unit.First regenerator G1 includes the high temperature for making to be heated to weak solution Sw Fluid FH regenerates heat source tube 31 the first of internal flow;It is supplied with the surface that weak solution Sw is regenerated heat source tube 31 to first First regenerator solution supplying device 32.First regenerator G1 is configured to, and supplies from the first regenerator solution supplying device 32 Weak solution Sw is heated by the high temperature fluid FH flowed in the first regeneration heat source tube 31, so that refrigerant V is evaporated from weak solution Sw And generate the first concentrated solution Sa1 that concentration rises.First regenerator G1 is configured to stockpile the first concentrated solution Sa1 generated In lower part.It is configured to condense as the first regenerator refrigerant vapour Vg1 to first from the vaporized refrigerant V of weak solution Sw Device C1 is mobile.In the first regenerator solution supplying device 32, it is connected with the first weak solution ingress pipe 33 for importing weak solution Sw One end.In the lower part (being bottom for typical) of the first regenerator G1, it is connected with the first concentrated solution Sa1 outflow for being stockpiled The first concentrated solution effuser 34 one end.In the first concentrated solution effuser 34, it is equipped and pressure is carried out to the first concentrated solution Sa1 First concentrated solution of conveying pumps 34p.
First condenser C1 is to make to be steamed by the first regenerator refrigerant that the first regenerator G1 is generated using cryogen FL The equipment that gas Vg1 cooling condensed and became the first refrigerant liquid Vf1, is equivalent to the first condensation part.First condenser C1 is The inside of the tank body of one condenser C1 has the first condensation heat conducting pipe 41 flowed for cryogen FL.First condenser C1 is constituted To import the first regenerator refrigerant vapour Vg1 generated by the first regenerator G1, being flowed in the first condensation heat conducting pipe 41 What cryogen FL was released when being condensed by the first regenerator refrigerant vapour Vg1 and becoming the first refrigerant liquid Vf1 Condensation heat, so that cryogen FL is heated and temperature rising.Second in the lower part of the first condenser C1 (is bottom for typical Portion), it is connected with one end of the first refrigerant liquid effuser 44 for the first refrigerant liquid Vf1 outflow stockpiled.? One refrigerant liquid effuser 44 is equipped and carries out pressure-feed first refrigerant liquid pump to the first refrigerant liquid Vf1 44p。
It is raw and cold again that first regenerator G1 and the first condenser C1 in mode adjacent is in the horizontal direction contained in first Solidifying tank body (hereinafter referred to as " the first regeneration condensation tank body 30 ").In the inside of the first regeneration condensation tank body 30, being provided with will be internal Space is substantially divided into two the first regeneration condenser walls 39.It is raw and cold again to clip first in the first regeneration condensation tank body 30 The mode of solidifying wall 39, is provided with the first regenerator G1 in a side, another party is provided with the first condenser C1.It is raw and cold again from first First regeneration condensation tank body 30 of the first side condenser C1 that solidifying wall 39 rises constitutes the tank body of the first condenser C1.First is raw and cold again Solidifying wall 39 is set as in a manner of being connected to the first regenerator G1 on top with the first condenser C1, does not regenerate drainer with first The top surface of body 30 contacts.That is, first regeneration condenser wall 39 first regeneration condensation tank body 30 removing top two sidewalls and Bottom is contacted with the first regeneration condensation tank body 30.According to this structure, in the first regeneration condensation tank body 30, the first regeneration Device refrigerant vapour Vg1 can be mobile from the first regenerator G1 to the first condenser C1.
Second reactivator G2 is to carry out heating concentration to weak solution Sw and make its regenerated equipment in concentration, is equivalent to the Two reproducing units.Second reactivator G2 include the high temperature fluid FH that makes to heat weak solution Sw internal flow second again Heat source capsule 35;With the Second reactivator solution supplying device for supplying weak solution Sw to the surface of the second regeneration heat source tube 35 36.Second reactivator G2 is constituted identically as the first regenerator G1, and the second regeneration heat source tube 35 and Second reactivator solution supply The first regeneration heat source tube 31 and the first regenerator solution supplying device 32 are corresponded respectively to device 36.Second reactivator G2 structure Become, the high temperature that the weak solution Sw supplied from Second reactivator solution supplying device 36 is flowed in the second regeneration heat source tube 35 Fluid FH heating, so that refrigerant V generates the second concentrated solution Sa2 that concentration rises from weak solution Sw evaporation.Second regeneration Device G2 is configured to the second concentrated solution Sa2 generated being accumulated in lower part.It is configured to make from the vaporized refrigerant V of weak solution Sw It is mobile to the second condenser C2 for Second reactivator refrigerant vapour Vg2.One end and first of second regeneration heat source tube 35 is again One end of heat source capsule 31 is connected by regenerator high temperature fluid connecting tube 73.In Second reactivator solution supplying device 36, even It is connected to one end of weak solution Sw the second weak solution ingress pipe 37 imported.(it is for typical in the lower part of Second reactivator G2 Bottom), it is connected with one end of the second concentrated solution effuser 38 for the second concentrated solution Sa2 outflow stockpiled.It is dense molten second Liquid stream outlet pipe 38 pumps 38p configured with pressure-feed second concentrated solution is carried out to the second concentrated solution Sa2.
Second condenser C2 is to steam the Second reactivator refrigerant generated by Second reactivator G2 using cryogen FL The equipment that gas Vg2 cooling condensed and became second refrigerant liquid Vf2, is equivalent to the second condensation part.Second condenser C2 is The inside of the tank body of two condenser C2 has the second condensation heat conducting pipe 45 flowed for cryogen FL.Second condenser C2 and One condenser C1 is constituted in the same manner, and the second condensation heat conducting pipe 45 corresponds to the first condensation heat conducting pipe 41.Second condenser C2 is constituted To import the Second reactivator refrigerant vapour Vg2 generated by Second reactivator G2, being flowed in the second condensation heat conducting pipe 45 What cryogen FL was released when being condensed by the Second reactivator refrigerant vapour Vg2 and becoming second refrigerant liquid Vf2 Condensation heat, so that cryogen FL is heated and temperature rising.One end of second condensation heat conducting pipe 45 and the first condensation heat conducting pipe 41 one end is connected by condenser cryogen connecting tube 74.In the lower part (typical for be bottom) of the second condenser C2, It is connected with one end of the second refrigerant liquid effuser 48 for the second refrigerant liquid Vf2 outflow stockpiled.In the second system Cryogen liquid effuser 48 is equipped and carries out pressure-feed second refrigerant liquid pump 48p to second refrigerant liquid Vf2.
It is raw and cold again that Second reactivator G2 and the second condenser C2 in mode adjacent is in the horizontal direction contained in second Solidifying tank body (hereinafter referred to as " the second regeneration condensation tank body 40 ").In the inside of the second regeneration condensation tank body 40, being provided with will be internal Space is substantially divided into two the second regeneration condenser walls 49.It is raw and cold again to clip second in the second regeneration condensation tank body 40 The mode of solidifying wall 49, is provided with Second reactivator G2 in a side, another party is provided with the second condenser C2.It is raw and cold again from second Second regeneration condensation tank body 40 of the second side condenser C2 that solidifying wall 49 rises constitutes the tank body of the second condenser C2.Second is raw and cold again Solidifying wall 49 is set as in a manner of being connected to Second reactivator G2 on top with the second condenser C2, does not regenerate drainer with second The top surface of body 40 contacts.That is, second regeneration condenser wall 49 second regeneration condensation tank body 40 removing top two sidewalls and Bottom is contacted with the second regeneration condensation tank body 40.According to this structure, in the second regeneration condensation tank body 40, the second regeneration Device refrigerant vapour Vg2 can be mobile from Second reactivator G2 to the second condenser C2.
In the present embodiment, the first absorber A1 first absorption heat conducting pipe 11, be connected with absorber low temperature The end of the opposite side in the end of one end of fluid connecting line 71, is connected with cryogen effuser 53.Cryogen outflow Pipe 53 is the pipe for constituting the flow path for the cryogen FL flowing after heating.In addition, the second absorption of the second absorber A2 is thermally conductive The end of the side opposite with the end of one end for being connected with absorber cryogen connecting tube 71 of pipe 15 and the first condenser The side opposite with the end of one end for being connected with condenser cryogen connecting tube 74 of the first condensation heat conducting pipe 41 of C1 End is connected by absorption condensation cryogen connecting tube 81.In addition, the first evaporator E1 first evaporation heat source tube 21 with Be connected with the opposite side in end of one end of evaporator high temperature fluid connecting tube 72 end and Second reactivator G2 second The end for regenerating the side opposite with the end of one end for being connected with regenerator high temperature fluid connecting tube 73 of heat source tube 35 passes through Regeneration high-temp fluid connecting line 75 is evaporated to connect.In addition, the second evaporator E2 second evaporation heat source tube 25, be connected with The end of the opposite side in the end of one end of evaporator high temperature fluid connecting tube 72, is connected with high temperature heat source effuser 56.It is high Temperature-heat-source effuser 56 is constituted for being used as heat source and the pipe of the flow path for the high temperature fluid FH flowing that temperature reduces.In addition, The first condenser C1 first condensation heat conducting pipe 41, be connected with condenser cryogen connecting tube 74 one end end The end of opposite side is connected with one end of absorption condensation cryogen connecting tube 81 as described above.In addition, cold second The second condensation heat conducting pipe 45 of condenser C2, opposite with the end of one end for being connected with condenser cryogen connecting tube 74 one The end of side is connected with the cryogen ingress pipe 57 for constituting the flow path for the cryogen FL flowing before being heated.
In addition, the first regenerator G1 first regeneration heat source tube 31, be connected with regenerator high temperature fluid connecting tube The end of the opposite side in the end of 73 one end, is connected with high temperature heat source ingress pipe 52.High temperature heat source ingress pipe 52 is to constitute The pipe for the flow path that high temperature fluid FH before reducing to temperature is guided.In high temperature heat source ingress pipe 52, it is provided in inside The high temperature heat source valve 52v that the flow of the high temperature fluid FH of flowing is adjusted.The other end and heat of high temperature heat source ingress pipe 52 are handed over It is connected to high temperature fluid together with the other end of branch pipe 82 and flows into pipe 55.High temperature fluid, which flows into pipe 55, to be constituted for part high-temperature stream The pipe of the flow path of high temperature fluid FH flowing before body FHs shunting.Part high temperature fluid FHs is the stream from high temperature fluid FH branch Body, entity are high temperature fluid FH, but in view of its purposes, for ease of description and as another address.It flows into and manages in high temperature fluid The high temperature fluid FH of 55 flowings is configured to a part and shunts and flow into hot friendship branch pipe 82, remaining flows into high temperature heat source ingress pipe 52.In hot friendship branch pipe 82, it is provided with and the heat exchange that the flow of the part high temperature fluid FHs in internal flow is adjusted is used Branch valve 82v.Hot friendship is connected to high temperature fluid stream with the other end of branch pipe 82 together with the other end of high temperature heat source effuser 56 Outlet pipe 59.High temperature fluid effuser 59 is composition for flowing through the part high temperature fluid FHs of hot friendship branch pipe 82 and in high temperature heat source The pipe of the flow path of high temperature fluid FH flowing behind the interflow high temperature fluid FH that effuser 56 flows.
In the present embodiment, heat exchange department 80 is disposed in absorption condensation cryogen connecting tube 81 and hot friendship branch pipe 82, it is configured to make in the cryogen FL of the flowing of absorption condensation cryogen connecting tube 81 and in the portion of hot friendship branch pipe 82 flowing High temperature fluid FHs is divided to carry out heat exchange.It is made of shell and tube heat exchanger but it is also possible to be board-like for 80 typical case of heat exchange department The equipment that heat exchanger etc. carries out heat exchange between two fluids.
In addition, in the present embodiment, the other end of the first weak solution effuser 14 and the second weak solution effuser 18 The other end is connected to one end of weak solution collecting fitting 61.In the other end of weak solution collecting fitting 61, it is connected with the first weak solution and leads Enter the other end of pipe 33 and the other end of the second weak solution ingress pipe 37.According to this structure, it is configured to absorb from first First weak solution Sw1 of device A1 outflow is with the interflow the second weak solution Sw2 from the second absorber A2 outflow and as weak solution Sw After flowing through weak solution collecting fitting 61, weak solution Sw is flowed into the first regenerator G1 and Second reactivator G2 in parallel respectively.This Sample is configured to the first regenerator G1 and Second reactivator G2 respectively from the first absorber A1 and in the present embodiment Two absorber A2 are introduced directly into weak solution Sw.Here, it is introduced directly into and refers to not mainly setting via composition absorption heat pump cycle Import to standby other equipment.
In addition, in the present embodiment, the other end of the first concentrated solution effuser 34 and the second concentrated solution effuser 38 The other end is connected to one end of concentrated solution collecting fitting 63.In the other end of concentrated solution collecting fitting 63, it is connected with the first concentrated solution and leads Enter the other end of pipe 13 and the other end of the second concentrated solution ingress pipe 17.According to this structure, it is configured to regenerate from first First concentrated solution Sa1 of device G1 outflow is with the interflow the second concentrated solution Sa2 from Second reactivator G2 outflow and as concentrated solution Sa After flowing through concentrated solution collecting fitting 63, concentrated solution Sa is flowed into the first absorber A1 and the second absorber A2 in parallel respectively.This Sample is configured to the first absorber A1 and the second absorber A2 respectively from the first regenerator G1 and in the present embodiment Two regenerator G2 are introduced directly into concentrated solution Sa.In weak solution collecting fitting 61 and concentrated solution collecting fitting 63, it is provided in weak solution The solution heat exchanger 62 of heat exchange is carried out between Sw and concentrated solution Sa.
In addition, in the present embodiment, the other end and second refrigerant liquid flow of the first refrigerant liquid effuser 44 The other end of outlet pipe 48 is connected to one end of refrigerant liquid collecting fitting 64.In the other end of refrigerant liquid collecting fitting 64, even It is connected to the other end of the first refrigerant liquid ingress pipe 23 and the other end of second refrigerant liquid ingress pipe 27.According to such Structure, in the first refrigerant liquid Vf1 flowed out from the first condenser C1 and the second refrigerant from the second condenser C2 outflow Liquid Vf2 collaborates after flowing through refrigerant liquid collecting fitting 64 as refrigerant liquid Vf, and refrigerant liquid Vf is respectively to first Evaporator E1 and the second evaporator E2 are flowed into parallel.In this way, in the present embodiment, be configured to the first evaporator E1 and Second evaporator E2 is introduced directly into refrigerant liquid Vf from the first condenser C1 and the second condenser C2 respectively.
In the example depicted in figure 1, first absorbs the evaporation absorption evaporation regeneration condensation of tank body 20, first of tank body 10, second The regeneration condensation tank body 40 of tank body 30, second in the state of being respectively horizontal, by along it is vertical become a column up and down in a manner of it is longitudinal It stacks, and absorbs evaporation tank body according to the first regeneration condensation regeneration condensation tank body 40, first of tank body 30, second from bottom to top 10, second absorbs being arranged in order for evaporation tank body 20.Although Fig. 1 is in fact, can also be formed as Fig. 1 such configuration Exemplary system figure, therefore can also suitably change and respectively set on the basis of the connection relationship of the flow path of fluid is kept intact Standby configuration.As long as can ensure the installation space of above-mentioned piping between each tank body.
For absorption type heat exchange system 1, in steady running, the pressure and temperature of the inside of the first absorber A1 It spends the pressure for becoming the inside than the first regenerator G1 and temperature is high, the pressure and temperature of the inside of the second absorber A2 become Must be higher than the pressure and temperature of the inside of Second reactivator G2, the pressure and temperature of the inside of the first evaporator E1 become to compare The pressure and temperature of the inside of first condenser C1 are high, and the pressure and temperature of the inside of the second evaporator E2 become than second The pressure and temperature of the inside of condenser C2 are high.In absorption type heat exchange system 1, the first absorber A1, the first evaporator E1, the second absorber A2, the second evaporator E2, the first regenerator G1, the first condenser C1, Second reactivator G2, the second condensation Device C2 becomes the structure of second of absorption heat pump.
The effect of absorption type heat exchange system 1 is illustrated with continued reference to Fig. 1.Firstly, to the absorption of refrigerant side Heat pump cycle is illustrated.In the first condenser C1, receive through the vaporized first regenerator refrigeration of the first regenerator G1 Agent steam Vg1 keeps the first regenerator refrigerant vapour Vg1 cooling using the cryogen FL flowed in the first condensation heat conducting pipe 41 And condense, to become the first refrigerant liquid Vf1.At this point, cryogen FL is cold by the first regenerator refrigerant vapour Vg1 The condensation heat that is released when solidifying and temperature rises.Condensed first refrigerant liquid Vf1 by the first refrigerant liquid pump 44p into Row pressure is conveyed and is flowed in the first refrigerant liquid effuser 44.In the second condenser C2, receiving passes through Second reactivator The vaporized Second reactivator refrigerant vapour Vg2 of G2 makes the using the cryogen FL flowed in the second condensation heat conducting pipe 45 Two regenerator refrigerant vapour Vg2 are cooling and condense, to become second refrigerant liquid Vf2.At this point, cryogen FL by The condensation heat that releases when Second reactivator refrigerant vapour Vg2 is condensed and temperature rises.In the present embodiment, cryogen FL flows after flowing through the second condensation heat conducting pipe 45 through condensing heat conducting pipe 41 first by condenser cryogen connecting tube 74, Therefore the temperature when the first condensation heat conducting pipe 41 flows is higher than the temperature when the second condensation heat conducting pipe 45 flows, the first condensation The internal pressure of the second condenser of inner pressure ratio C2 of device C1 is high.Condensed second refrigerant liquid Vf2 is by second refrigerant liquid pump 48p carries out pressure conveying and flows in second refrigerant liquid effuser 48.In the flowing of the first refrigerant liquid effuser 44 First refrigerant liquid Vf1 and second refrigerant liquid effuser 48 flow second refrigerant liquid Vf2 separately flow into Refrigerant liquid collecting fitting 64, and it is mixed to refrigerant liquid Vf.Refrigerant liquid in refrigerant liquid collecting fitting 64 Body Vf is shunted to the first refrigerant liquid ingress pipe 23 with second refrigerant liquid ingress pipe 27.It is imported in the first refrigerant liquid The refrigerant liquid that pipe 23 flows is flowed into the first evaporator E1.On the other hand, it is flowed in second refrigerant liquid ingress pipe 27 Dynamic refrigerant liquid is flowed into the second evaporator E2.
Flow into the high temperature fluid FH that the refrigerant liquid Vf of the first evaporator E1 is flowed in the first evaporation heat source tube 21 It heats and evaporates, become the first evaporator refrigerant steam Ve1.At this point, the high-temperature stream flowed in the first evaporation heat source tube 21 Body FH takes heat by force by refrigerant liquid Vf and temperature reduces.The the first evaporator refrigerant steam Ve1 generated by the first evaporator E1 It is mobile to the first absorber A1 being connected to the first evaporator E1.On the other hand, the refrigerant liquid of the second evaporator E2 is flowed into Body Vf is heated and evaporated by the high temperature fluid FH flowed in the second evaporation heat source tube 25, becomes the second evaporator refrigerant steam Ve2.At this point, the high temperature fluid FH that flows takes heat by force by refrigerant liquid Vf in the second evaporation heat source tube 25 and temperature reduces.By The second evaporator refrigerant steam Ve2 that second evaporator E2 is generated is moved to the second absorber A2 being connected to the second evaporator E2 It is dynamic.High temperature fluid FH is after flowing through the first evaporation heat source tube 21 through evaporating heat source second by evaporator high temperature fluid connecting tube 72 Pipe 25 flows, therefore the temperature when the first evaporation heat source tube 21 flows is than the temperature when the second evaporation heat source tube 25 flows The internal pressure of height, the second evaporator of inner pressure ratio E2 of the first evaporator E1 is high.
Then, the absorption heat pump cycle of solution side is illustrated.In the first absorber A1, by from the first absorber Solution supplying device 12 supplies concentrated solution Sa, and the concentrated solution Sa of the supply is absorbed from mobile the first next evaporation of the first evaporator E1 Device refrigerant vapour Ve1.The concentrated solution Sa concentration for absorbing the first evaporator refrigerant steam Ve1 reduces and becomes first dilute molten Liquid Sw1.In the first absorber A1, is generated when concentrated solution Sa absorbs the first evaporator refrigerant steam Ve1 and absorb heat.By Absorption heat is heated in the cryogen FL that the first absorption heat conducting pipe 11 flows, and the temperature of cryogen FL rises.Absorb the One evaporator refrigerant steam Ve1 and the first weak solution Sw1 that concentration is reduced from the first concentrated solution Sa1 is accumulated in the first absorption The lower part of device A1.
In the second absorber A2, by from the second absorber solution supplying device 16 supply concentrated solution Sa, the supply it is dense Solution S a is absorbed from mobile the second next evaporator refrigerant steam Ve2 of the second evaporator E2.Absorb the second evaporator refrigeration The concentrated solution Sa concentration of agent steam Ve2 reduces and becomes the second weak solution Sw2.In the second absorber A2, inhaled in concentrated solution Sa It is generated when receiving the second evaporator refrigerant steam Ve2 and absorbs heat.Using absorption heat, absorb what heat conducting pipe 15 flowed to second Cryogen FL is heated, so that the temperature of cryogen FL rises.After cryogen FL flows through the second absorption heat conducting pipe 15 Via absorber cryogen connecting tube 71 first absorb heat conducting pipe 11 flow, therefore from the first absorber A1 flow out and Temperature when cryogen effuser 53 flows is higher than the temperature when absorber cryogen connecting tube 71 flows, and can make low Warm fluid FL more heats up.Absorb the second evaporator refrigerant steam Ve2 and that concentration is reduced from concentrated solution Sa is second dilute molten Liquid Sw2 is accumulated in the second lower part absorber A2.
The the first weak solution Sw1 generated from the first absorber A1 is flowed out to the first weak solution effuser 14, is absorbed by second The second weak solution Sw2 that device A2 is generated is flowed out to the second weak solution effuser 18.The of the flowing of the first weak solution effuser 14 One weak solution Sw1 and the second weak solution effuser 18 flowing the second weak solution Sw2 separately flow into weak solution collecting fitting 61, And it is mixed to weak solution Sw.Weak solution collecting fitting 61 flow weak solution Sw in solution heat exchanger 62 with it is dense molten Liquid Sa, which carries out heat exchange and temperature, to be reduced, backward first weak solution ingress pipe 33 and the shunting of the second weak solution ingress pipe 37.? First weak solution ingress pipe 33 flowing weak solution Sw by from the first regenerator solution supplying device 32 into the first regenerator G1 Supply.On the other hand, in the weak solution Sw of the second weak solution ingress pipe 37 flowing by from Second reactivator solution supplying device 36 It is supplied into Second reactivator G2.
In the first regenerator G1, the weak solution Sw that is supplied from the first regenerator solution supplying device 32 by first again The high temperature fluid FH that heat source capsule 31 flows is heated, and the refrigerant in the weak solution Sw supplied evaporates and becomes the first concentrated solution Sa1, and it is accumulated in the lower part of the first regenerator G1.At this point, the high temperature fluid FH flowed in the first regeneration heat source tube 31 is dilute Solution S w takes heat by force and temperature reduces.The refrigerant evaporated from weak solution Sw is as the first regenerator refrigerant vapour Vg1 to first Condenser C1 is mobile.On the other hand, in Second reactivator G2, what is supplied from Second reactivator solution supplying device 36 is dilute molten Liquid Sw is heated in the second high temperature fluid FH for being flowed of regeneration heat source tube 35, the refrigerant evaporation in the weak solution Sw supplied and As the second concentrated solution Sa2, and it is accumulated in the lower part of Second reactivator G2.At this point, flowed in the second regeneration heat source tube 35 High temperature fluid FH takes heat by force by weak solution Sw and temperature reduces.Freeze from the vaporized refrigerant of weak solution Sw as Second reactivator Agent steam Vg2 is mobile to the second condenser C2.
The the first concentrated solution Sa1 generated from the first regenerator G1 is flowed out to the first concentrated solution effuser 34, by the second regeneration The second concentrated solution Sa2 that device G2 is generated is flowed out to the second concentrated solution effuser 38.Pressure conveying is carried out by the first concentrated solution pump 34p And the first concentrated solution effuser 34 flowing the first concentrated solution Sa1 and by the second concentrated solution pump 38p carry out pressure conveying and Concentrated solution collecting fitting 63 is separately flowed into the second concentrated solution Sa2 of the second concentrated solution effuser 38 flowing, and is mixed to Concentrated solution Sa.Concentrated solution Sa in concentrated solution collecting fitting 63 carries out heat exchange with weak solution Sw in solution heat exchanger 62 and warm After degree rises, shunted to the first concentrated solution ingress pipe 13 and the second concentrated solution ingress pipe 17.It is flowed in the first concentrated solution ingress pipe 13 Dynamic concentrated solution Sa is supplied from the first absorber solution supplying device 12 into the first absorber A1, and is held repeatedly afterwards The above-mentioned circulation of row.On the other hand, it is supplied in the concentrated solution Sa of the second concentrated solution ingress pipe 17 flowing from the second absorber solution It is supplied to device 16 into the second absorber A2, and executes above-mentioned circulation repeatedly afterwards.
Specific example is enumerated, during carrying out absorption heat pump cycle as described above to absorbing liquid S and refrigerant V , the variation of the temperature of cryogen FL and high temperature fluid FH is illustrated.If flowing into the height that pipe 55 flows in high temperature fluid Warm fluid FH is 95 DEG C, then the high temperature fluid FH and part high temperature fluid FHs after shunting also are respectively 95 DEG C.In high temperature heat source 95 DEG C of the high temperature fluid FH that ingress pipe 52 flows is when the first regeneration heat source tube 31 of the first regenerator G1 is flowed by weak solution Sw takes heat by force and temperature reduces, and flows into Second reactivator G2 via regenerator high temperature fluid connecting tube 73 later, and second Heat is taken by force by weak solution Sw when the second regeneration heat source tube 35 of regenerator G2 flows, if reaching evaporation regeneration high-temp fluid connecting line 75 Then temperature is reduced to 88 DEG C.Later, the first steaming is being flowed through in the high temperature fluid FH that evaporation regeneration high-temp fluid connecting line 75 flows Hair device E1 first evaporation heat source tube 21 when by refrigerant liquid Vf take by force heat and temperature reduce, later via evaporator high temperature fluid Connecting tube 72 and flow into the second evaporator E2, and the second evaporator E2 second evaporation heat source tube 25 flow when by refrigerant Liquid Vf takes heat by force, and temperature is reduced to 81 DEG C if reaching high temperature heat source effuser 56.In addition, flowing into 55 branch of pipe from high temperature fluid And the part high temperature fluid FHs for flowing into hot friendship branch pipe 82 flows towards heat exchange department 80 and flows into heat exchange department 80.
On the other hand, it if being 32 DEG C in the cryogen FL that cryogen ingress pipe 57 flows, is imported in cryogen When the cryogen FL that pipe 57 flows flows through the second condensation heat conducting pipe 45 of the second condenser C2, Second reactivator refrigerant is obtained The condensation heat that steam Vg2 is released when condensing and becoming refrigerant liquid Vf rises to temperature, later via condenser low temperature Fluid connecting line 74 and flow into the first condenser C1, in the first condensation heat conducting pipe 41 for flowing through the first condenser C1, obtain the The condensation heat that one regenerator refrigerant vapour Vg1 is released when condensing and becoming refrigerant liquid Vf, if it is low to reach absorption condensation Then temperature rises to 53 DEG C to warm fluid connecting line 81.It is flowed into the cryogen FL that absorption condensation cryogen connecting tube 81 flows Heat exchange department 80.In heat exchange department 80, in the cryogen FL for flowing through absorption condensation cryogen connecting tube 81 and heat is flowed through Heat exchange is carried out between the part high temperature fluid FHs of friendship branch pipe 82, the temperature of 53 DEG C of cryogen FL rises to 92 DEG C, and 95 DEG C part high temperature fluid FHs temperature to 56 DEG C reduce.Temperature is reduced to 56 DEG C of part high temperature fluid FHs to continue to hand in heat It is flowed with branch pipe 82, collaborates with 81 DEG C of the high temperature fluid FH flowed in high temperature heat source effuser 56, become 75 DEG C of high-temperature stream Body FH is simultaneously flowed in high temperature fluid effuser 59 and is discharged from absorption type heat exchange system 1.On the other hand, temperature rises to 92 DEG C Cryogen FL from absorption condensation cryogen connecting tube 81 to the second absorber A2 second absorb heat conducting pipe 15 flow into, When flowing through the second absorption heat conducting pipe 15, obtains concentrated solution Sa and absorb the absorption heat generated when the second evaporator refrigerant steam Ve2 And temperature rises, and flows into the first absorber A1 via absorber cryogen connecting tube 71 later, is flowing through the first absorber When the first of A1 absorbs heat conducting pipe 11, obtains concentrated solution Sa and absorbs the absorption heat generated when the first evaporator refrigerant steam Ve1, Temperature rises to 111 DEG C if reaching cryogen effuser 53.At this point, the first evaporator E1 high temperature fluid FH's flowed The temperature of high temperature fluid FH of the temperature than flowing in the second evaporator E2 is high, therefore the second evaporator E2 and the second absorber A2 Internal pressure and temperature it is lower than the internal pressure and temperature of the first evaporator E1 and the first absorber A1, if cryogen FL is pressed According to being sequentially introduced into from the second absorber A2 to the first absorber A1, then can make by the low of each absorber A2, A1 heat temperature raising The temperature of warm fluid FL successively increases.Field is utilized by direction in 111 DEG C of the cryogen FL that cryogen effuser 53 flows It is supplied.
In absorption type heat exchange system 1, in order to set up temperature relation as described above, determine to import in high temperature heat source The ratio between the flow for the high temperature fluid FH that pipe 52 flows and the flow of part high temperature fluid FHs that is flowed in hot friendship branch pipe 82, with And flow the ratio between of the flow of cryogen FL relative to part high temperature fluid FHs.In the present embodiment, by high temperature fluid FH 4:1 is substantially set as with the flow-rate ratio of part high temperature fluid FHs.In addition, relatively, if increasing the flow of part high temperature fluid FHs More, then the temperature of the cryogen FL flowed out from heat exchange department 80 increases, if the flow of part high temperature fluid FHs is made to tail off, The temperature of the cryogen FL flowed out from heat exchange department 80 is lower.In addition, in the present embodiment, by cryogen FL and part The flow-rate ratio of high temperature fluid FHs is set as about 1:1.Here, each for high temperature fluid FH, part high temperature fluid FHs, cryogen FL From flow-rate ratio for, piping, discharge orifice of size used according to pre-determined value etc. can be used to fix, can be with structure As being able to use valve (triple valve of high temperature heat source valve 52v and heat exchange branch valve 82v or their substitution) etc. and It automatically or manually adjusts, in the case where automatic adjustment, can also be pre-set in control device setting (not shown) Storage device (not shown), be also configured to be carried out at any time by the input unit (not shown) for being set to control device Setting.In such manner, it is possible to make (111 DEG C) of the temperature ratios of the cryogen FL flowed out from absorption type heat exchange system 1 to absorption type heat The high temperature fluid FH's that exchange system 1 flows into is (95 DEG C) of temperature high.Here, absorption type heat exchange system 1 can be considered as making height A heat exchanger of heat exchange is carried out between warm fluid FH and cryogen FL.In previous heat exchanger, if making low temperature Fluid the thick high temperature of flow fluid flow it is few, then the outlet temperature of the fluid of low temperature can be made close to the fluid of high temperature Inlet temperature, but can not be higher than the inlet temperature of the fluid of high temperature.About this point, exchanged in the absorption type heat of present embodiment In system 1, as described above, the temperature ratio of the cryogen FL flowed out from absorption type heat exchange system 1 can be made to absorption The temperature for the high temperature fluid FH that heat-exchange system 1 flows into is high, to be suitable for the long distance delivery of hot fluid.
As described above, absorption type heat exchange system 1 according to the present embodiment is absorbed via second of performance The first absorber A1, the second absorber A2, the first evaporator E1, the second evaporator E2, the first regenerator of the function of formula heat pump The absorption heat pump cycle of G1, Second reactivator G2, the first condenser C1, the absorbing liquid S in the second condenser C2 and refrigerant V And the heat exchange of high temperature fluid FH Yu cryogen FL are carried out indirectly, and part height is directly carried out in heat exchange department 80 The heat exchange of warm fluid FHs (high temperature fluid FH) and cryogen FL, so as to take by force in cryogen FL from high temperature fluid FH After heat, keep the temperature of the cryogen FL flowed out from absorption type heat exchange system 1 higher than the temperature of the high temperature fluid FH of inflow. In addition, due to having the first absorber A1 and the second absorber A2, to can make low compared with absorber is one situation The temperature of warm fluid FL rises.In addition, it is cold that the first condenser C1 and second will have been passed through in absorption type heat exchange system 1 The cryogen FL of condenser C2 is imported to the first absorber A1 and the second absorber A2 and increase the temperature of cryogen FL, Therefore the cooling water to necessitate in second of absorption heat pump is not needed, the attendant equipment for not needing to be accompanied by this is (cooling Water pump, cooling tower etc.).In addition, existing unlike second of absorption heat pump in absorption type heat exchange system 1 to cooling The condensation heat of first condenser C1 and the second condenser C2 are used for the heating of cryogen FL, therefore energy by the heat that water is given up Enough it is equal to the large-scale heat exchanger of than second absorption heat pump of efficiency (COP) high (substantially 2 times or so).
Next, being illustrated referring to absorption type heat exchange system 2 of the Fig. 2 to second embodiment of the present invention.Fig. 2 is The exemplary system figure of absorption type heat exchange system 2.Absorption type heat exchange system 2 and absorption type heat exchange system 1 (referring to Fig.1) phase Than not being from relative to the first evaporator E1, the second evaporator in the high temperature fluid FH flowed into heat exchange department 80 in general survey The part high temperature fluid FHs (referring to Fig.1) of high temperature fluid FH branch before E2, the first regenerator G1, Second reactivator G2 inflow, But the aspect of the high temperature fluid FH after flowing out is different.It is accompanied by this, the structure of absorption type heat exchange system 2 is mainly below Aspect is different from the structure of absorption type heat exchange system 1 (referring to Fig.1).In absorption type heat exchange system 2, it is not provided with and is inhaling The hot friendship branch pipe 82 for being equipped with heat exchange branch valve 82v being arranged in receipts formula heat-exchange system 1 (referring to Fig.1), with This is also not provided with high temperature heat source valve 52v.In addition, heat exchange department 80 is configured to that hot friendship is replaced to be configured at high-temperature stream with 82 ground of branch pipe Body effuser 59 flows the cryogen FL flowed in absorption condensation cryogen connecting tube 81 in high temperature fluid effuser 59 Dynamic high temperature fluid FH carries out heat exchange.The structure other than the above and absorption type heat exchange system 1 of absorption type heat exchange system 2 (referring to Fig.1) identical.In addition, high temperature fluid flows into pipe 55 and high temperature heat source ingress pipe 52, there is no the tie point branches in the two Piping (heat hand over use branch pipe 82 (referring to Fig.1)), thus can with one integrated mass be constituted, but for the ease of being exchanged with absorption type heat System 1 (referring to Fig.1) compares, and retains the address of the two.Similarly, high temperature heat source effuser 56 and high temperature fluid effuser 59 can also with one integrated mass be constituted, but retain the address of the two.
In the absorption type heat exchange system 2 constituted in this way, in the first regenerator G1, Second reactivator G2, the first evaporation Compared with the high temperature fluid FH of device E1, the second evaporator E2 flowing is with absorption type heat exchange system 1 (referring to Fig.1) the case where, with portion The amount correspondingly flow increase for dividing high temperature fluid FHs (referring to Fig.1) non-branch, is flowing through high temperature heat source effuser 56 and high temperature Fluid effuser 59 and to heat exchange department 80 flow into when, become the temperature 82 lower than absorption type heat exchange system 1 (referring to Fig.1) ℃.On the other hand, cold in the second condenser C2 and first in 32 DEG C of cryogen FL of the flowing of cryogen ingress pipe 57 Temperature rises to 58 DEG C and reaches condensation cryogen connecting tube 81 in condenser C1, and flows into heat exchange department 80.In heat exchange In portion 80, in the high temperature fluid FH for flowing through high temperature fluid effuser 59 and the low temperature for flowing through absorption condensation cryogen connecting tube 81 Heat exchange is carried out between fluid FL, the temperature of 82 DEG C of high temperature fluid FH is reduced to 77 DEG C, the temperature of 58 DEG C of cryogen FL Rise to 79 DEG C.Flow-rate ratio by the high temperature fluid FH and cryogen FL of heat exchange department 80 is about 4:1.In this way, heat exchange High temperature fluid FH and the flow-rate ratio of cryogen FL in portion 80 is bigger, therefore can be improved the heating conduction of heat exchange department 80 And reduce the heat-conducting area of every heat exchange amount.The high temperature fluid FH that temperature is reduced to 77 DEG C and flows out from heat exchange department 80 continues High temperature fluid effuser 59 is flowed and is discharged from absorption type heat exchange system 1.Temperature rises to 79 DEG C and flows from heat exchange department 80 Cryogen FL and absorption type heat exchange system 1 (referring to Fig.1) out flows into the first absorber A1 in the same manner, inhales by first It receives after device A1 and the second absorber A2 and temperature rise to 104 DEG C, flows through cryogen effuser 53 and supplied to using place It gives.In absorption type heat exchange system 2, the temperature of the cryogen FL to be heated up by heat exchange department 80 is lower, therefore to low temperature The temperature for the cryogen FL that fluid effuser 53 flows out is lower than absorption type heat exchange system 1 (referring to Fig.1), from high temperature fluid FH The heat given to cryogen FL also tails off.Absorption type heat exchange system 2 can be with absorption type heat exchange system 1 (referring to figure 1) in the same manner, make the temperature of the cryogen FL flowed out from absorption type heat exchange system 2 than the temperature of the high temperature fluid FH of inflow Height, and increase the temperature of cryogen FL compared with absorber is one situation.
Next, being illustrated referring to absorption type heat exchange system 3 of the Fig. 3 to third embodiment of the present invention.Fig. 3 is The exemplary system figure of absorption type heat exchange system 3.Absorption type heat exchange system 3 and absorption type heat exchange system 1 (referring to Fig.1) phase Than in general survey, the type of flow of the liquid of absorbing liquid S and refrigerant V and the sequence of flow of cryogen FL and ratio are steamed The sequence of flow for sending out the high temperature fluid FH of 75 downstream of regeneration high-temp fluid connecting line is different.It is accompanied by this, absorption type heat is handed over The structure for changing system 3 is mainly different from the structure of absorption type heat exchange system 1 (referring to Fig.1) at aspect below.Absorption In heat-exchange system 3, it is configured to the second weak solution effuser for the second weak solution Sw2 flowing flowed out from the second absorber A2 18 other end is connect with the first absorber solution supplying device 12 of the first absorber A1, makes the second weak solution Sw2 to first Absorber A1 supply.In addition, being configured to the first weak solution stream for the first weak solution Sw1 flowing flowed out from the first absorber A1 The other end of outlet pipe 14 is connect with the Second reactivator solution supplying device 36 of Second reactivator G2, make the first weak solution Sw1 to Second reactivator G2 supply.In addition, it is dense molten to be configured to flow for the second concentrated solution Sa2 flowed out from Second reactivator G2 second The other end of liquid stream outlet pipe 38 is connect with the first regenerator solution supplying device 32 of the first regenerator G1, makes the second concentrated solution Sa2 is supplied to the first regenerator G1.It is not provided with the second concentrated solution pump 38p (referring to Fig.1) in the second concentrated solution effuser 38, the Two concentrated solution Sa2 are flowed by gravity from Second reactivator G2 to the first regenerator G1.In addition, being configured to supply from the first regenerator The other end of the first concentrated solution effuser 34 of the first concentrated solution Sa1 flowing of G1 outflow and the second of the second absorber A2 absorb Device solution supplying device 16 connects, and supplies the first concentrated solution Sa1 to the second absorber A2.In absorption type heat exchange system 2, The concentration for being configured to the first weak solution Sw1 is lower than the second weak solution Sw2, and the concentration of the second concentrated solution Sa2 is than the first weak solution Sw1 The concentration of height, the first concentrated solution Sa1 is lower than the first concentrated solution Sa1 than the concentration of the second concentrated solution Sa2 high, the second weak solution Sw2. According to this structure, absorbing liquid S is according to the second absorber A2, the first absorber A1, Second reactivator G2, the first regenerator G1 Sequential series flow, and return again to the second absorber A2 from the first regenerator G1 and speed change concentration variation side is followed Ring.At this point, importing absorbing liquid S directly to Second reactivator G2 from the first absorber A1, from the second absorber A2 via first Absorber A1 and imported indirectly to Second reactivator G2, and via Second reactivator G2 and indirectly from the first absorber A1 It is imported to the first regenerator G1, from the second absorber A2 via the first absorber A1 and Second reactivator G2 and indirectly to the One regenerator G1 is imported.In addition, importing absorbing liquid S directly to the second absorber A2 from the first regenerator G1, from the second regeneration Device G2 is imported via the first regenerator G1 and indirectly to the second absorber A2, and is absorbed from the first regenerator G1 via second Device A2 and indirectly to the first absorber A1 import, from Second reactivator G2 via the first regenerator G1 and the second absorber A2 And it is imported indirectly to the first absorber A1.Here, the capital equipment referred to via absorption heat pump cycle is constituted is imported indirectly Other equipment and import.
In addition, being configured to the second refrigerant liquid for flowing out from the second condenser C2 in absorption type heat exchange system 3 The other end of the second refrigerant liquid effuser 48 of Vf2 flowing is connect with the first condenser C1, makes second refrigerant liquid Vf2 It is supplied to the first condenser C1.Second refrigerant liquid pump 48p is not provided with (referring to figure in second refrigerant liquid effuser 48 1), second refrigerant liquid Vf2 is flowed by gravity from the second condenser C2 to the first condenser C1.In addition, be configured to for from The other end and second of first refrigerant liquid effuser 44 of the first refrigerant liquid Vf1 flowing of the first condenser C1 outflow Evaporator E2 connection, supplies the first refrigerant liquid Vf1 to the second evaporator E2.In addition, in absorption type heat exchange system 3 In, it is provided with and supplies a part for being accumulated in the first refrigerant liquid Vf1 of the second evaporator E2 to the first evaporator E1 Evaporator refrigerant liquid ingress pipe 28.According to this structure, refrigerant V is in addition to from the first evaporator E1 to the first absorber Outside A1 and the part flowed from the second evaporator E2 to the second absorber A2 respectively as steam (Ve1, Ve2), according to second Flow to the sequential series of condenser C2, the first condenser C1, the second evaporator E2, the first evaporator E1.It is handed in absorption type heat It changes in system 3, is not provided with the first concentrated solution ingress pipe 13, second being arranged in absorption type heat exchange system 1 (referring to Fig.1) Concentrated solution ingress pipe 17, the first refrigerant liquid ingress pipe 23, second refrigerant liquid ingress pipe 27, the first weak solution ingress pipe 33, the second weak solution ingress pipe 37, weak solution collecting fitting 61, concentrated solution collecting fitting 63 and refrigerant liquid collecting fitting 64.Cause This, solution heat exchanger 62 is not set in weak solution collecting fitting 61 (referring to Fig.1) and concentrated solution collecting fitting 63 (referring to Fig.1), And it is set to the first weak solution effuser 14 and the first concentrated solution effuser 34.
Also, in absorption type heat exchange system 3, cryogen ingress pipe 57 is not condensed with the second of the second condenser C2 Heat conducting pipe 45 connects, and connect with one end of the first condensation heat conducting pipe 41 of the first condenser C1.The of the second condenser C2 The end of two condensation heat conducting pipes 45, opposite with the end for being connected with condenser cryogen connecting tube 74 sides, is connected with One end of absorption condensation cryogen connecting tube 81.The other end of absorption condensation cryogen connecting tube 81 not with the second absorber The second of A2 absorbs heat conducting pipe 15 and connects, and connect with one end of the first absorption heat conducting pipe 11 of the first absorber A1.Second The second of absorber A2 absorbs heat conducting pipe 15, opposite with the end for being connected with absorber cryogen connecting tube 71 side End is connected with one end of cryogen effuser 53.According to this structure, the low temperature flowed in cryogen ingress pipe 57 Fluid FL according to the first condenser C1, the second condenser C2, the first absorber A1, the second absorber A2 sequential series flow And reach cryogen effuser 53.In addition, one end is connected to the second regeneration heat source tube 35 in absorption type heat exchange system 3 The other end of evaporation regeneration high-temp fluid connecting line 75 do not connect with the first of the first evaporator E1 the evaporation heat source tube 21, and with One end connection of the second evaporation heat source tube 25 of second evaporator E2.The first evaporator E1 first evaporation heat source tube 21, The end of the side opposite with the end for being connected with evaporator high temperature fluid connecting tube 72, is connected with high temperature heat source effuser 56 One end.According to this structure, in evaporation regeneration high-temp after flowing through the first regenerator G1 and Second reactivator G2 in series The high temperature fluid FH that fluid connecting line 75 flows according to the second evaporator E2, the first evaporator E1 sequential series flow and arrive Up to high temperature heat source effuser 56.The structure other than the above and the 1 (reference of absorption type heat exchange system of absorption type heat exchange system 3 It is Fig. 1) identical.
The absorption type heat exchange system 3 constituted in this way is preferably, in the temperature of the cryogen FL of the second condenser C2 flowing The temperature for spending the cryogen FL than flowing in the first condenser C1 is high, thus Second reactivator G2 and the second condenser C2 The internal pressure of inner pressure ratio the first regenerator G1 and the first condenser C1 are high, thus Second reactivator G2 and the first regenerator G1 it Between generate the difference of internal pressure, and flow absorbing liquid S from Second reactivator G2 to the first regenerator G1.Similarly, it is also preferred that making to make Cryogen liquid Vf is flowed from the second condenser C2 to the first condenser C1.By the temperature of the Second reactivator G2 absorbing liquid S heated The temperature of absorbing liquid S than being heated by the first regenerator G1 is low, thus because absorbing liquid S the lower Second reactivator G2 of temperature, Then in the higher first regenerator G1 flowing of temperature, thus absorbing liquid S is heated twice according to the sequence of temperature from low to high, It can be improved the concentration of absorbing liquid S and increase thermal output.Additionally, it is preferred that the internal pressure of the second absorber A2 and the second evaporator E2 Internal pressure than the first absorber A1 and the first evaporator E1 is high, to produce between the second absorber A2 and the first absorber A1 The difference of raw internal pressure, flows absorbing liquid S from the second absorber A2 to the first absorber A1.Similarly, it is also preferred that making refrigerant liquid Body Vf is flowed from the second evaporator E2 to the first evaporator E1.By the temperature ratio of the second absorber A2 cooling absorbing liquid S by the The temperature of one absorber A1 cooling absorbing liquid S is high, thus because absorbing liquid S exists in the higher second absorber A2 of temperature, then The lower first absorber A1 flowing of temperature, thus absorbing liquid S is cooled twice according to the sequence of temperature from high to low, can drop The concentration of low absorption liquid S and increase thermal output.In this way, in absorption type heat exchange system 3, absorbing liquid S is from the second absorber A2 It flows to the first absorber A1 and is flowed in series from Second reactivator G2 to the first regenerator G1 in series, therefore can make The concentration difference of absorbing liquid S becomes larger and increases output.
Next, being illustrated referring to absorption type heat exchange system 4 of the Fig. 4 to the 4th embodiment of the invention.Fig. 4 is The exemplary system figure of absorption type heat exchange system 4.Absorption type heat exchange system 4 and absorption type heat exchange system 2 (referring to Fig. 2) phase Than in general survey, absorbing liquid S is different with the type of flow of the liquid of refrigerant V and the sequence of flow of high temperature fluid FH.Companion With in this, the structure of absorption type heat exchange system 4 mainly in the following areas with absorption type heat exchange system 2 (referring to Fig. 2) Structure is different.In absorption type heat exchange system 4, it is configured to the first weak solution Sw1 flowing for flowing out from the first absorber A1 The other end of the first weak solution effuser 14 connect with the first regenerator solution supplying device 32 of the first regenerator G1, make One weak solution Sw1 is supplied to the first regenerator G1.In addition, being configured to the first concentrated solution Sa1 for flowing out from the first regenerator G1 The other end of the first concentrated solution effuser 34 of flowing is connect with the first absorber solution supplying device 12 of the first absorber A1, Supply the first concentrated solution Sa1 to the first absorber A1.In absorption type heat exchange system 4, the first weak solution Sw1 and first Concentrated solution Sa1 is recycled between the first absorber A1 and the first regenerator G1 when changing concentration, the first weak solution effuser 14 And first concentrated solution effuser 34 and the first absorber A1 and the first regenerator G1 cooperatively constitute the first absorbing liquid and follow Circulation road.In addition, being configured to the second weak solution Sw2 stream for flowing out from the second absorber A2 in absorption type heat exchange system 4 The dynamic other end of the second weak solution effuser 18 is connect with the Second reactivator solution supplying device 36 of Second reactivator G2, is made Second weak solution Sw2 is supplied to Second reactivator G2.In addition, being configured to the second concentrated solution for flowing out from Second reactivator G2 The other end of second concentrated solution effuser 38 of Sa2 flowing and the second absorber solution supplying device 16 of the second absorber A2 connect It connects, supplies the second concentrated solution Sa2 to the second absorber A2.In absorption type heat exchange system 4, the second weak solution Sw2 and Second concentrated solution Sa2 is recycled between the second absorber A2 and Second reactivator G2 when changing concentration, the outflow of the second weak solution Pipe 18 and the second concentrated solution effuser 38 and the second absorber A2 and Second reactivator G2 cooperatively constitute the second absorption Liquid recycle stream road.In addition, in absorption type heat exchange system 4, it is instead of solution heat exchanger 62 (referring to Fig. 2), dilute first Solution effuser 14 and the first concentrated solution effuser 34 are provided with the first solution heat exchanger 62A, and in the second weak solution Effuser 18 and the second concentrated solution effuser 38 are provided with the second solution heat exchanger 62B.
In addition, being configured to the first refrigerant liquid for flowing out from the first condenser C1 in absorption type heat exchange system 4 The other end of first refrigerant liquid effuser 44 of Vf1 flowing is connect with the first evaporator E1, makes the first refrigerant liquid Vf1 It is supplied to the first evaporator E1.In addition, be configured to flow for the second refrigerant liquid Vf2 that flow out from the second condenser C2 the The other end of two refrigerant liquid effusers 48 is connect with the second evaporator E2, makes second refrigerant liquid Vf2 to the second evaporation Device E2 supply.In absorption type heat exchange system 4, refrigerant V as first systematic, the first refrigerant liquid of Bian Gaihuan Vf1, First evaporator refrigerant steam Ve1, the first regenerator refrigerant vapour Vg1 and phase side are steamed in the first condenser C1, first Device E1, the first absorber A1, the first regenerator G1 circulation are sent out, as second system, Bian Gaihuan second refrigerant liquid Vf2, Second evaporator refrigerant steam Ve2, Second reactivator refrigerant vapour Vg2 and phase side are steamed in the second condenser C2, second Send out device E2, the second absorber A2, Second reactivator G2 circulation.
Also, in absorption type heat exchange system 4, high temperature heat source ingress pipe 52 be connected to high temperature fluid flow into pipe 55 The end of the opposite side in end do not connect with the first regeneration heat source tube 31 of the first regenerator G1, and with the first evaporator E1 First evaporation heat source tube 21 one end connection.In the other end of the first evaporation heat source tube 21, it is connected with the first connecting tube of heat source 76 one end.The other end of the first connecting tube of heat source 76 is connect with one end of the first regeneration heat source tube 31 of the first regenerator G1. In the other end of the first regeneration heat source tube 31, it is connected with one end of heat source intermediate connection tube 77.Heat source intermediate connection tube 77 it is another One end is connect with one end of the second evaporation heat source tube 25 of the second evaporator E2.In the other end of the second evaporation heat source tube 25, even It is connected to one end of the second connecting tube of heat source 78.The other end of the second connecting tube of heat source 78 and the second regenerated heat of Second reactivator G2 One end of source capsule 35 connects.In the other end of the second regeneration heat source tube 35, it is connected with one end of high temperature heat source effuser 56, high temperature The other end of heat source effuser 56 is connect with the end of high temperature fluid effuser 59.According to this structure, it is led in high temperature heat source Enter the high temperature fluid FH of the flowing of pipe 52 according to the first evaporator E1, the first regenerator G1, the second evaporator E2, Second reactivator G2 Sequential series flow and reach high temperature heat source effuser 56.In addition, being not provided in absorption type heat exchange system 4 Evaporator high temperature fluid connecting tube 72, the regenerator high temperature fluid connecting tube being arranged in absorption type heat exchange system 2 (referring to Fig. 2) 73, regeneration high-temp fluid connecting line 75 is evaporated.The structure other than the above of absorption type heat exchange system 4 and absorption heat exchange series System 2 (referring to Fig. 2) is identical.The absorption type heat exchange system 4 constituted in this way has the absorption heat pump of absorbing liquid S and refrigerant V Multiple absorption heat pump cycles can be controlled and be managed by two independent system paths of circulation.In addition, for height For the temperature of warm fluid FH, the first regenerator G1 is lower than the first evaporator E1, therefore is able to suppress in the first regenerator G1 The rising of the concentration of absorbing liquid S and avoid absorbing liquid S from being excessively concentrated.
Next, being illustrated referring to absorption type heat exchange system 5 of the Fig. 5 to the 5th embodiment of the invention.Fig. 5 is The exemplary system figure of absorption type heat exchange system 5.Absorption type heat exchange system 5 and absorption type heat exchange system 4 (referring to Fig. 4) phase Than in general survey, the state of the sequence of flow of high temperature fluid FH and the high temperature fluid FH flowed into heat exchange department 80 are different.Companion With in this, the structure of absorption type heat exchange system 5 is mainly at aspect below and absorption type heat exchange system 4 (referring to Fig. 4) Structure is different.In absorption type heat exchange system 5, heat is handed over branch pipe 82 and absorption type heat exchange system 1 (referring to Fig.1) in the same manner Configuration is configured in the cryogen FL for flowing through absorption condensation cryogen connecting tube 81 in heat exchange department 80 and flows through hot friendship Heat exchange is carried out between the part high temperature fluid FHs of branch pipe 82.In addition, high temperature heat source ingress pipe 52 be connected to high-temperature stream Body flows into the end of pipe 55 and the hot friendship opposite side in the end of branch pipe 82 not the first heat of evaporation with the first evaporator E1 Source capsule 21 connects, and connect with one end of the first regeneration heat source tube 31 of the first regenerator G1.First evaporation heat source tube 21, The end of the side opposite with the end for being connected to the first heat source connecting tube 76, is connected with one end of heat source intermediate connection tube 77. The other end of heat source intermediate connection tube 77 is not connect with the second evaporation heat source tube 25 of the second evaporator E2, and and Second reactivator One end connection of the second regeneration heat source tube 35 of G2.Second evaporation heat source tube 25, be connected to Secondary Heat Source connecting tube 78 The opposite side in end end, be connected with one end of high temperature heat source effuser 56, the other end of high temperature heat source effuser 56 It is connect with hot friendship with the end of branch pipe 82 and high temperature fluid effuser 59.According to this structure, in high temperature heat source ingress pipe 52 flowing high temperature fluid FH according to the first regenerator G1, the first evaporator E1, Second reactivator G2, the second evaporator E2 it is suitable Sequence flows in series and reaches high temperature heat source effuser 56.The structure other than the above of absorption type heat exchange system 5 with it is absorption Heat-exchange system 4 (referring to Fig. 4) is identical.The absorption type heat exchange system 5 constituted in this way is identical as absorption type heat exchange system 4 Ground, two independent system paths of the absorption heat pump cycle with absorbing liquid S and refrigerant V, so as to multiple suctions Receipts formula heat pump cycle is controlled and is managed.In addition, in absorption type heat exchange system 5, for the temperature of high temperature fluid FH For, flowed into the first regenerator G1 it is high when ratio is flowed into the first evaporator E1, to Second reactivator G2 inflow when ratio to the High when two evaporator E2 are flowed into, the concentration of the first regenerator G1 and the respective absorbing liquid S of Second reactivator G2 compare absorption type heat Exchange system 4 (referring to Fig. 4) is high, therefore according to operating condition, the temperature after capable of making the heating of cryogen FL is than absorption Heat-exchange system 4 (referring to Fig. 4) is high and increases thermal output.
In Fig. 4 and absorption type heat exchange system shown in fig. 54,5, there are have absorber, evaporator, again It gives birth to and wants to make the temperature of heating subject fluid into one under the situation of device, condenser each one second of the absorption heat pump both set In the case that step is got higher, also can have second of absorber, evaporator, regenerator, condenser each one by being newly arranged Absorption heat pump and by high temperature fluid FH and cryogen FL it is each piping connect as shown in the embodiment and to control System processed applies micro change to constitute.
Next, being illustrated referring to absorption type heat exchange system 6 of the Fig. 6 to sixth embodiment of the invention.Fig. 6 is The exemplary system figure of absorption type heat exchange system 6.Absorption type heat exchange system 6 and absorption type heat exchange system 1 (referring to Fig.1) phase Than in general survey, the type of flow than the cryogen FL of heat exchange department 80 on the upstream side is different.It is accompanied by this, absorption type heat The structure of exchange system 6 is mainly different from the structure of absorption type heat exchange system 1 (referring to Fig.1) at aspect below.It is absorbing In formula heat-exchange system 6, cryogen ingress pipe 57 is in branched halfway at the first cryogen ingress pipe 57A and the second low temperature stream One end of the first condensation heat conducting pipe 41 of body ingress pipe 57B, the first cryogen ingress pipe 57A and the first condenser C1 is connect, Second cryogen ingress pipe 57B is connect with one end of the second condensation heat conducting pipe 45 of the second condenser C2.It is led in the first condensation The other end of heat pipe 41 is connected with one end of the first absorption condensation cryogen connecting tube 81A, in the second condensation heat conducting pipe 45 The other end is connected with one end of the second absorption condensation cryogen connecting tube 81B.First absorption condensation cryogen connecting tube 81A The other end be connected to together with the other end of the second absorption condensation cryogen connecting tube 81B absorption condensation cryogen connection One end of pipe 81, the other end of absorption condensation cryogen connecting tube 81 is after 80s with the second absorber A2's by heat exchange department Second absorbs the end connection of heat conducting pipe 15.In absorption type heat exchange system 6, it is not provided in absorption type heat exchange system 1 (referring to Fig.1) the condenser cryogen connecting tube 74 being arranged in.According to this structure, it is flowed in cryogen ingress pipe 57 Cryogen FL be split into the first cryogen ingress pipe 57A and the second cryogen ingress pipe 57B, to the first condenser C1 And second condenser C2 flow in parallel and respectively to the first absorption condensation cryogen connecting tube 81A and the second absorption condensation Cryogen connecting tube 81B outflow, collaborates again later and reaches absorption condensation cryogen connecting tube 81.Absorption type heat exchange The structure other than the above of system 6 is identical as absorption type heat exchange system 1 (referring to Fig.1).It is handed in the absorption type heat constituted in this way It changes in system 6, cryogen FL can be made to shunt and the flow resistance when the first condenser C1 and the second condenser C2 flows It is smaller than absorption type heat exchange system 1 (referring to Fig.1), suitable for the lesser feelings of pressure difference permitted when flowing cryogen FL Condition.
Next, being illustrated referring to absorption type heat exchange system 7 of the Fig. 7 to the 7th embodiment of the invention.Fig. 7 is The exemplary system figure of absorption type heat exchange system 7.Absorption type heat exchange system 7 and absorption type heat exchange system 4 (referring to Fig. 4) phase Than in general survey, the type of flow of high temperature fluid FH is different.Be accompanied by this, the structure of absorption type heat exchange system 7 mainly with Under the structure of aspect and absorption type heat exchange system 4 (referring to Fig. 4) it is different.In absorption type heat exchange system 7, it is not provided with High temperature heat source ingress pipe 52 (referring to Fig. 4), one end of the first high temperature heat source ingress pipe 52A and the second high temperature heat source ingress pipe 52B One end be connected to high temperature fluid flow into pipe 55.The of the other end of first high temperature heat source ingress pipe 52A and the first evaporator E1 One end connection of one evaporation heat source tube 21, the other end of the second high temperature heat source ingress pipe 52B and the second of the second evaporator E2 are steamed One end connection of fever source capsule 25.The first regenerator G1 the first regeneration heat source tube 31, be connected with heat source first and connect The end of the opposite side in the end of pipe 76 is connected with one end of the first high temperature heat source effuser 56A.Second reactivator G2's The end of second regeneration heat source tube 35, opposite with the end for being connected with the second connecting tube of heat source 78 side, is connected with second One end of high temperature heat source effuser 56B.The other end of first high temperature heat source effuser 56A and the second high temperature heat source effuser 56B The other end be connected to high temperature fluid effuser 59.In absorption type heat exchange system 7, it is not provided in absorption heat exchange series The high temperature heat source effuser 56 and heat source intermediate connection tube 77 being arranged in system 4 (referring to Fig. 4).According to this structure, in height Warm fluid flows into the high temperature fluid FH that pipe 55 flows and is split into the first high temperature heat source ingress pipe 52A and the second high temperature heat source ingress pipe 52B, flowed in parallel to the first evaporator E1 and the first regenerator G1 and the second evaporator E2 and Second reactivator G2 and It is flowed out respectively to the first high temperature heat source effuser 56A and the second high temperature heat source effuser 56B, collaborates later and reach high temperature fluid Effuser 59, and flowed towards heat exchange department 80.The structure other than the above and absorption type heat of absorption type heat exchange system 7 are handed over It is identical to change system 4 (referring to Fig. 4).In the absorption type heat exchange system 7 constituted in this way, high temperature fluid FH can be made and first Flow resistance when evaporator E1 and the first regenerator G1 and the second evaporator E2 and Second reactivator G2 flows is than absorbing Formula heat-exchange system 4 (referring to Fig. 4) is small, suitable for the lesser situation of pressure difference permitted when flowing high temperature fluid FH.This Outside, in the example shown in Fig. 7, the side in two high temperature fluid FH that pipe 55 shunts is flowed into from the first evaporation from high temperature fluid Device E1 is flowed to the first regenerator G1, another party from the second evaporator E2 to Second reactivator G2 flow, but can also with a side from First regenerator G1 is flowed to the first evaporator E1, and another party is flowed from Second reactivator G2 to the second evaporator E2.Alternatively, It can be split into 4 parts by the high temperature fluid FH that pipe 55 flows is flowed at high temperature fluid and steamed to the first regenerator G1, first Hair device E1, Second reactivator G2, the second evaporator E2 4 positions supply in parallel, in this case, each regenerator can be made And flow resistance when each evaporator The high temperature fluid FH flowing is minimum.
Next, the absorption type heat exchange system referring to involved in variation of the Fig. 8 to first embodiment of the invention 1A is illustrated.Fig. 8 is the schematic structural diagram of absorption type heat exchange system 1A.Absorption type heat exchange system 1A is relative to absorption The process of heat-exchange system 1 (referring to Fig.1), fluid (absorbing liquid S, refrigerant V, cryogen FL, high temperature fluid FH) is identical, but More specifically show the configuration of each equipment.In this variation, it absorbs in evaporation tank body 10 first by the first absorber A1 Separate with the first evaporator E1, but replaces first to be formed as the first container for evaporation with absorbing evaporation wall 19 (referring to Fig.1) 19A.For first absorbs evaporation tank body 10, internal the first absorber A1 and the first evaporator E1 are contained in vertical It is arranged above and below.In this variation, the first evaporator E1 configuration is on the first absorber A1.Constitute the of the first evaporator E1 One evaporation heat source tube 21 is contained in the first container for evaporation 19A of opened upper end.It, can also be in addition, in the first container for evaporation 19A First refrigerant liquid body feeding 22 is set in the top of the first evaporation heat source tube 21, makes refrigerant liquid Vf from upper direction the The entirety of one evaporation heat source tube 21 is dispersed.In the first refrigerant liquid body feeding 22, it is connected with the importing of the first refrigerant liquid Pipe 23.Since the first evaporator E1 is configured at the top of the first absorber A1, so as to prevent the suction in the first absorber A1 It receives liquid S and to the first evaporator E1 internal leakage the refrigerant liquid Vf in the first evaporator E1 is contaminated.In addition, inhaling In receipts formula heat-exchange system 1A, is absorbed in evaporation tank body 20 second and separate the second absorber A2 and the second evaporator E2 Come, but replaces second to be formed as the second container for evaporation 29A with absorbing evaporation wall 29 (referring to Fig.1).Evaporator is absorbed for second It is identical as the first absorption evaporation tank body 10 for body 20, it is contained in the second internal evaporator E2 and is configured at the second absorber A2 Vertical top.The the second evaporation heat source tube 25 for constituting the second evaporator E2 is contained in the second container for evaporation 29A of opened upper end. In the second container for evaporation 29A, second refrigerant liquid corresponding with the first refrigerant liquid body feeding 22 also can be set Feedway 26.First, which absorbs evaporation tank body 10, is configured at position different in horizontal direction from the second absorption evaporation tank body 20. Position when different positions refers to vertical view in horizontal direction is different, adjacent in the horizontal direction in this variation or be close to Ground configuration.In this variation, it is configured to the height of the first absorption heat conducting pipe 11 and the second absorption respective topmost of heat conducting pipe 15 Spend identical, the first absorber solution supplying device 12 and the second absorber solution supplying device 16 are configured at identical height.This In described identical height include the equal height of essence (supply pressure of concentrated solution Sa it is different and reach the first absorber A1 with And second the respective thermal output of absorber A2 different degree within the allowable range range).Similarly, it is configured to the first evaporation Heat source tube 21 is identical as the second evaporation height of the respective topmost of heat source tube 25, the first refrigerant liquid body feeding 22 and the Two refrigerant liquid body feedings 26 are configured at identical height.
In addition, in absorption type heat exchange system 1A, by the first regenerator G1 and the in the first regeneration condensation tank body 30 One condenser C1 separates, but is formed as the first condensing container 39A with replacing the first regeneration condenser wall 39 (referring to Fig.1).It is right For the first regeneration condensation tank body 30, internal the first regenerator G1 and the first condenser C1 are contained in vertical row up and down Column.In this variation, the first condenser C1 configuration is on the first regenerator G1.Constitute the first condensation of the first condenser C1 Heat conducting pipe 41 is contained in the first condensing container 39A of opened upper end.Since the first condenser C1 is configured at the first regenerator G1's Top, so as to prevent the absorbing liquid S in the first regenerator G1 from making the first condenser C1 to the first condenser C1 internal leakage Interior refrigerant liquid Vf is contaminated.In addition, in absorption type heat exchange system 1A, it will in the second regeneration condensation tank body 40 Second reactivator G2 separates with the second condenser C2, but is formed as with replacing the second regeneration condenser wall 49 (referring to Fig.1) Second condensing container 49A.Second regeneration condensation tank body 40 is identical as the first regeneration condensation tank body 30, and it is cold to be contained in internal second Condenser C2 is configured in the vertical top of Second reactivator G2.The the second condensation heat conducting pipe 45 for constituting the second condenser C2 is contained in The open second condensing container 49A in portion.First regeneration condensation tank body 30 and the second regeneration condensation tank body 40 are configured in level side Different position upwards abuts in the horizontal direction in this variation or closely configures.In this variation, it is configured to First regeneration heat source tube 31 is identical as the second regeneration height of the respective topmost of heat source tube 35, the first regenerator solution supply dress It sets 32 and is configured at identical height with Second reactivator solution supplying device 36.Identical height mentioned here includes substantial (supply pressure of weak solution Sw is different and reaches the first regenerator G1 and the respective thermal output of Second reactivator G2 for equal height The range of different degree within the allowable range).Similarly, it is configured to the first condensation heat conducting pipe 41 and the second condensation heat conducting pipe 45 The height of respective topmost is identical.In addition, the first regeneration condensation tank body that is adjacent in the horizontal direction or closely configuring 30 and second regeneration condensation tank body 40 top, configured with it is adjacent in the horizontal direction or closely configure first absorb Evaporate tank body 10 and the second absorption evaporation tank body 20.In addition, in absorption type heat exchange system 1A, instead of being handed in absorption type heat It changes the first concentrated solution pump 34p for being disposed in the first concentrated solution effuser 34 being arranged in system 1 (referring to Fig.1) and is disposed in the The second concentrated solution pump 38p of two concentrated solution effusers 38, it is provided with the concentrated solution pump 63p for being disposed in concentrated solution collecting fitting 63. In addition, instead of be disposed in the first refrigerant liquid effuser 44 the being arranged in the absorption type heat exchange system 1 (referring to Fig.1) One refrigerant liquid pumps 44p and with being disposed in the second refrigerant liquid pump 48p of second refrigerant liquid effuser 48, is arranged There is the refrigerant liquid pump 64p for being disposed in refrigerant liquid collecting fitting 64.The knot of absorption type heat exchange system 1A other than the above Structure is identical as absorption type heat exchange system 1 (referring to Fig.1).For the absorption type heat exchange system 1A constituted in this way, first Absorber solution supplying device 12 and the second absorber solution supplying device 16 are configured at identical height, therefore can make to apply In towards the first absorber solution supplying device 12 and the pressure-feed concentrated solution Sa of the second absorber solution supplying device 16 Pressure is close, is able to suppress the discharge pressure of concentrated solution pump 63p.Similarly, it is able to suppress and makes refrigerant liquid Vf towards first The discharge of cryogen fluid Supplying apparatus 22 and the pressure-feed refrigerant liquid of second refrigerant fluid Supplying apparatus 26 pump 64p Pressure.In addition, the first absorption heat conducting pipe 11 is identical as the second absorption height of the respective topmost of heat conducting pipe 15, therefore it is able to suppress Pressure applied is conveyed in order to carry out pressure to cryogen FL.Similarly, the first evaporation heat source tube 21 and the second heat of evaporation The height of the respective topmost of source capsule 25 is identical, therefore is able to suppress to carry out what pressure conveying was applied to high temperature fluid FH Pressure.In addition, if absorbing evaporation tank body 10 and the second absorption evaporation tank body 20 and the first regeneration condensation tank body 30 first And second only consider the peace of the first weak solution effuser 14 and the second weak solution effuser 18 between regeneration condensation tank body 40 Dress height, thus make the first absorption evaporation tank body 10 and second absorb evaporation tank body 20 with first regeneration condense tank body 30 and Second regeneration condensation tank body 40 is closely constituted, then is able to suppress height and apparatus structure is made to become compact.
As described above, from the vaporized first regenerator refrigerant vapour of the first weak solution Sw1 in the first regenerator G1 Vg1 is mobile to the first condenser C1, if therefore by the first regenerator G1 and the first condenser C1 as absorption type heat shown in FIG. 1 is handed over System 1 is changed to configure in mode adjacent in the horizontal direction like that or as absorption type heat exchange system 1A shown in Fig. 8 It is closely configured up and down vertical, so that the first regenerator G1 and the first condenser C1 are housed in the first regeneration condensation tank body 30 Interior, then the first regenerator G1 and the first condenser C1 is close, therefore can compactly constitute, and can make the first regenerator system Refrigerant vapor Vg1 makes the first regenerator refrigerant from the flow path that the first regenerator G1 is flowed towards the first condenser C1 to be most short The flow resistance of steam Vg1 flowing is minimum.It is directed to the first regenerator refrigerant vapour Vg1 as a result, can will be regenerated first The difference (pressure difference) of the pressure and the pressure condensed in the first condenser C1 evaporated in device G1 is substantially eliminated, so as to mention The high thermal efficiency as absorption heat pump cycle.In addition, the pressure difference is smaller, then got over as the thermal efficiency of absorption heat pump cycle It is high.It similarly, can be compact if Second reactivator G2 and the second condenser C2 are housed in the second regeneration condensation tank body 40 Ground is constituted, and is directed to Second reactivator refrigerant vapour Vg2, can by the pressure evaporated in Second reactivator G2 with the The difference (pressure difference) of the pressure condensed in two condenser C2 is substantially eliminated, to improve the thermal effect as absorption heat pump cycle Rate.
In addition, to each portion (the first suction for executing the capital equipment of absorption heat pump cycle of absorbing liquid and refrigerant is constituted Receive device A1, second evaporator E2 etc.) structure of tank body that is accommodated and configuration can for example generate Fig. 9 (A)~Fig. 9 (D) Shown such various change.Fig. 9 (A)~Fig. 9 (D) only specifically indicates the structure and configuration of the tank body in each portion of receiving, and And omit the structure for indicating the peripheries such as piping.In above-mentioned absorption type heat exchange system 1A (referring to Fig. 8), make first raw and cold again Solidifying tank body 30 is abutted in the horizontal direction with the second regeneration condensation tank body 40 or is closely configured, and first raw and cold again at this The top of solidifying tank body 30 and the second regeneration condensation tank body 40, configured with making, tank body 10 is evaporated in the first absorption and the second absorption is evaporated Component made of tank body 20 is abutted in the horizontal direction or closely configured.On the other hand, in the example shown in Fig. 9 (A), So that the first evaporator E1 and the first absorber A1 is not housed within the first absorption evaporation tank body 10 (referring to Fig. 8) and is contained in difference interiorly Independent tank body is constituted, and the second evaporator E2 and the second absorber A2 is made to be not housed within the second absorption evaporation 20 (reference of tank body It is contained in tank body independently interiorly Fig. 8) to constitute.Moreover, in the top of the first regeneration condensation tank body 30 configured with receiving The tank body of second absorber A2, in the top that contains the tank body of second absorber A2 configured with having accommodated the second evaporator The tank body of E2, and the tank body for having accommodated the first absorber A1 is configured in the top of the second regeneration condensation tank body 40, it is accommodating There is the top of the tank body of first absorber A1 to be configured with the tank body for having accommodated the first evaporator E1.In such manner, it is possible to make receiving The tank body of first absorber A1 is independently configured with the tank body for having accommodated the second absorber A2 relative to other tank bodies, therefore can Only by the tank body for having accommodated the first absorber A1 or the tank body of the second absorber A2 is accommodated and other tank bodies are cut off and are easy It is replaced, to easily can only be carried out in the case where the first absorber A1 or the second absorber A2 are damaged Contain the replacement of the tank body of the absorber of the damage.
It is raw and cold again first in the example shown in Fig. 9 (B) relative to example shown in Fig. 9 (A) as another example The top of solidifying tank body 30 and the second regeneration condensation tank body 40, makes the tank body for containing the first evaporator E1 and contains the first suction The tank body for receiving device A1 adjacently configures in the horizontal direction, and makes the tank body for containing the second evaporator E2 and contain second The tank body of absorber A2 adjacently configures in the horizontal direction.In such manner, it is possible to inhibit the height of absorption type heat exchange system.This In, the tank body for containing the first absorber A1 can also be made relative to the first regeneration condensation tank body 30 not above and in level side Adjacently configure upwards, make to contain the tank body of the second absorber A2 relative to the second regeneration condensation tank body 40 not above and It is adjacently configured in horizontal direction.Furthermore, the tank body for containing the first absorber A1 can also be made, contain the first steaming The tank body and first regeneration condensation this 3 tank bodies of tank body 30 for sending out device E1 adjacently configure in the horizontal direction, make to contain the The tank body of two absorber A2, the tank body for containing the second evaporator E2 and second regeneration condensation this 3 tank bodies of tank body 40 are in water It square adjacently configures upwards.In such manner, it is possible to further suppress the height of absorption type heat exchange system.No matter in addition, making to accommodate Have the tank body of the first absorber A1 and contain the first evaporator E1 tank body which can be vertical along vertical direction for top It plays configuration and configures it adjacently in the horizontal direction with the first regeneration condensation tank body 30, no matter making to contain the second absorber A2 Tank body with contain the second evaporator E2 tank body which be top, can along vertical direction erect configuration and by its with Second regeneration condensation tank body 40 adjacently configures in the horizontal direction.
In addition, making the first regeneration condensation tank body 30 and the first absorption evaporation tank body 10 exist in the example shown in Fig. 9 (C) It abuts in horizontal direction or closely configures, absorb the upper of evaporation tank body 10 in the first regeneration condensation tank body 30 and first Side makes the second regeneration condensation tank body 40 absorb the adjoining in the horizontal direction of evaporation tank body 20 with second or closely configure.This Sample respectively constitutes the circulation loop of absorbing liquid S between the first regenerator G1 and the first absorber A1 and the second regeneration In the case where between device G2 and the second absorber A2, the first regenerator G1 with the first absorber A1 match by the level under identical height Set, there is no need to by the first concentrated solution Sa1 from the first regenerator G1 to pressure-feed first concentrated solution of the first absorber A1 The discharge pressure for pumping 34p (referring to Fig. 4), applies and presses caused by the difference as the setting height of the first regenerator G1 and the first absorber A1 Head is poor, can reduce the discharge pressure of the first concentrated solution pump 34p.Similarly, Second reactivator G2 is with the second absorber A2 identical Height under horizontal arrangement, there is no need to the second concentrated solution Sa2 is defeated from Second reactivator G2 to the second absorber A2 pressure The discharge pressure of the second solution pump 38p (referring to Fig. 4) sent, applies the setting height by Second reactivator G2 and the second absorber A2 Difference caused by head difference, can reduce the discharge pressure of the second solution pump 38p.
In addition, in the example shown in Fig. 9 (D), making the first evaporator E1 and first relative to example shown in Fig. 9 (C) Absorber A1 is not housed in the first absorption evaporation tank body 10 and constitutes as independent tank body, makes the second evaporator E2 and second Absorber A2 is not housed in the second absorption evaporation tank body 20 and constitutes as independent tank body.In addition, the first suction will be contained The tank body and the first regeneration condensation tank body 30 for receiving device A1 adjacently configure in the horizontal direction, will contain the tank of the second absorber A2 Body adjacently configures in the horizontal direction with the second regeneration condensation tank body 40.In addition, containing the tank body of the first absorber A1 Top is configured with the tank body for having accommodated the first evaporator E1, in the top for containing the tank body of the second absorber A2 configured with receiving The tank body of second evaporator E2.In such manner, it is possible to make the tank body for containing the first absorber A1 and contain the second absorber The tank body of A2 is independently configured relative to other tank bodies, therefore will can only accommodate the tank body or receipts of the first absorber A1 The tank body for having held the second absorber A2 cuts off with other tank bodies and is easy to be replaced, thus the feelings being damaged in absorber Under condition, the replacement of the absorber of the damage easily can be only carried out.It, can also be in addition, configured for shown in Fig. 9 (D) The tank body for containing the first evaporator E1 is not configured to the top for containing the tank body of the first absorber A1 and in the horizontal direction It adjacently configures, the tank body for containing the second evaporator E2 can also be configured to the tank body for containing the second absorber A2 Top and adjacently configure in the horizontal direction.Alternatively, the tank body for containing the first evaporator E1 can also be made and contain first The configuration up and down of the tank body of absorber A1 is reverse, makes the tank body for containing the second evaporator E2 and contains the second absorber A2's The configuration up and down of tank body is reverse, to rise from below in the height direction, according to tank body, the receiving for containing the first evaporator E1 Have the tank body of the first absorber A1, the tank body for containing the second evaporator E2, contain the second absorber A2 tank body sequence It is configured along vertical direction.
Next, the absorption type heat exchange system 8 of 0 pair of the 8th embodiment of the invention is illustrated referring to Fig.1.Figure 10 It is the schematic structural diagram of absorption type heat exchange system 8.Absorption type heat exchange system 8 and absorption type heat exchange system 1A are (referring to figure 8) it compares, in general survey, the type of flow of high temperature fluid FH is different.It is accompanied by this, the structure of absorption type heat exchange system 8 is main It is different from the structure of absorption type heat exchange system 1A (referring to Fig. 8) at aspect below.In absorption type heat exchange system 8, with Absorption type heat exchange system 2 (referring to Fig. 2) in the same manner, hand over by the not set heat for being equipped with heat exchange branch valve 82v (referring to Fig. 8) With branch pipe 82 (referring to Fig. 8), it is accompanied by this also not set high temperature heat source valve 52v (referring to Fig. 8), in addition heat exchange department 80 replaces heat It hands over and is configured at high temperature fluid effuser 59 with branch pipe 82 (referring to Fig. 8).In addition, in absorption type heat exchange system 8, Gao Wenre The end of the side opposite with the high temperature fluid inflow end of pipe 55 is connected to of source ingress pipe 52 is not with the first regenerator G1's First regeneration heat source tube 31 connects, and connect with one end of the first evaporation heat source tube 21 of the first evaporator E1.In the second evaporation The end of the side opposite with the end for being connected to evaporator high temperature fluid connecting tube 72 of heat source tube 25, it is not connected to have Gao Wenre Source stream outlet pipe 56, and it is connected with one end of evaporation regeneration high-temp fluid connecting line 75.Evaporate regeneration high-temp fluid connecting line 75 The other end is not connect with the second regeneration heat source tube 35, and is connect with one end of the first regeneration heat source tube 31.Heat source is regenerated second The end of pipe 35, opposite with the end for being connected to regenerator high temperature fluid connecting tube 73 side, is connected with high temperature heat source stream One end of outlet pipe 56.According to this structure, in the high temperature fluid FH of the flowing of high temperature heat source ingress pipe 52 according to the first evaporator Flows and reach high temperature heat source effuser to the sequential series of E1, the second evaporator E2, the first regenerator G1, Second reactivator G2 56.The structure other than the above of absorption type heat exchange system 8 is identical as absorption type heat exchange system 1A (referring to Fig. 8).Such structure At absorption type heat exchange system 8 compared with absorption type heat exchange system 1A (referring to Fig. 8), to Second reactivator G2 and first The temperature for the high temperature fluid FH that regenerator G1 is imported is corresponding to by the first evaporator E1 and the second hectic amount of evaporator E2 Ground is lower, therefore is able to suppress the rising of the concentration of Second reactivator G2 and the absorbing liquid S in the first regenerator G1, can keep away Exempt from absorbing liquid S to be excessively concentrated and crystallize.
In the explanation of various embodiments so far, it is illustrated each of high temperature fluid FH and cryogen FL Kind sequence of flow, but the sequence of flow of these fluids is not limited to illustrate, such as can also suitably change as shown below.? It is configured to each equipment of the high temperature fluid FH to the first regenerator G1, Second reactivator G2, the first evaporator E1, the second evaporator E2 In the case where flowing in series, also it is configured to flow into the first regenerator G1 or the first evaporator E1 at first.Here, in height In the case that warm fluid FH flows into the first regenerator G1 at first, for after the high temperature fluid FH that the first regenerator G1 flows out The type of flow for, if indicating sequence of flow by appended drawing reference for ease of description and only, become (1) G2, E1, E2, (2) G2, E2, E1, (3) E1, G2, E2, (4) E1, E2, G2, (5) E2, G2, E1, any one of (6) E2, E1, G2.On the other hand, In the case where high temperature fluid FH flows into the first evaporator E1 at first, for the high temperature fluid FH's that is flowed out from the first evaporator E1 For the type of flow later, if only indicating sequence of flow by appended drawing reference, become (7) E2, G1, G2, (8) E2, G2, G1, (9) G1, E2, G2, (10) G2, E2, G1, (11) G1, G2, E2, any one of (12) G2, G1, E2.More than high temperature fluid FH When stating any mode and flowing in series, for the sequence of flow of cryogen FL, if no matter the first regenerator G1 And how and only the sequence of Second reactivator G2 is conceived to the sequence of the first evaporator E1 and the second evaporator E2, then may be used Be configured to high temperature fluid FH according to the first evaporator E1, the second evaporator E2 sequential flowing in the case where, cryogen FL is steamed in high temperature fluid FH according to the second evaporator E2, first according to the sequential flowing of the second absorber A2, the first absorber A1 Send out device E1 sequential flowing in the case where, cryogen FL according to the first absorber A1, the second absorber A2 sequential flowing.Separately Outside, though than the cryogen FL of heat exchange department 80 on the upstream side make the first condenser C1 and the second condenser C2 which It can first flow in series, but if no matter how and only the sequence of the first evaporator E1 and the second evaporator E2 be conceived to The sequence of first regenerator G1 and Second reactivator G2, then be preferably configured as high temperature fluid FH according to the first regenerator G1, In the case where the sequential flowing of Second reactivator G2, cryogen FL according to the second condenser C2, the first condenser C1 sequence Flowing, high temperature fluid FH according to Second reactivator G2, the first regenerator G1 sequential flowing in the case where, cryogen FL is pressed According to the sequential flowing of the first condenser C1, the second condenser C2.If being constituted with above-mentioned either type, high temperature fluid FH at first In the case where flowing into the first regenerator G1, it is capable of increasing the heat mobile to cryogen FL from high temperature fluid FH, and energy The temperature of enough cryogen FL for improving outflow.On the other hand, the feelings flowed at first to the first evaporator E1 in high temperature fluid FH Under condition, in addition to the high temperature of the cryogen FL of increase and the outflow of the mobile heat from high temperature fluid FH towards cryogen FL Except change, additionally it is possible to inhibit the rising of the concentration of the absorbing liquid S in the first regenerator G1 and Second reactivator G2, so as to Absorbing liquid S is avoided excessively to be concentrated and crystallize.
Next, the absorption type heat exchange system 9 of 1 pair of the 9th embodiment of the invention is illustrated referring to Fig.1.Figure 11 It is the exemplary system figure of absorption type heat exchange system 9.Absorption type heat exchange system 9 and absorption type heat exchange system 1 (referring to Fig.1) It compares, other than the structure of absorption type heat exchange system 1 (referring to Fig.1), is mainly having third absorber A3, third evaporation Device E3, third regenerator G3, third condenser C3 point on it is different.It also include different structures with the main difference, It is described below.Third absorber A3 is equivalent to third absorption portion, has third and absorbs heat conducting pipe 311 and third absorption Device solution supplying device 312, and it is connected with third concentrated solution ingress pipe 313 and third weak solution effuser 314.Third is inhaled It receives device A3 and surrounding structure is constituted identically as the first absorber A1, third absorbs heat conducting pipe 311, third absorber solution Feedway 312, third concentrated solution ingress pipe 313, third weak solution effuser 314 are respectively equivalent in the first absorber A1 First absorbs heat conducting pipe 11, the first absorber solution supplying device 12, the first concentrated solution ingress pipe 13, the first weak solution effuser 14.Third evaporator E3 is equivalent to third evaporation part, has third evaporation heat source tube 321, and be connected with third refrigerant liquid Body ingress pipe 323.Third evaporator E3 and surrounding structure are constituted identically as the first evaporator E1, and third evaporates heat source tube 321, the first evaporation heat source tube 21, first that third refrigerant liquid ingress pipe 323 is respectively equivalent in the first evaporator E1 is made Cryogen liquid ingress pipe 23.Third absorber A3 and third evaporator E3 is contained in third and absorbs evaporation tank body 310, imitates the One absorbs evaporation tank body 10, and the two absorbs evaporation wall 319 by third and divides.Third regenerator G3 is equivalent to third reproducing unit, tool Standby third regeneration heat source tube 331 and third regenerator solution supplying device 332, and it is connected with third weak solution ingress pipe 333 With the third concentrated solution effuser 334 for being equipped with third concentrated solution pump 334p.Third regenerator G3 and surrounding structure and the One regenerator G1 is constituted in the same manner, and third regeneration heat source tube 331, third regenerator solution supplying device 332, third weak solution are led Enter pipe 333, third concentrated solution effuser 334, third concentrated solution pump 334p are respectively equivalent in the first regenerator G1 first again Heat source capsule 31, the first regenerator solution supplying device 32, the first weak solution ingress pipe 33, the first concentrated solution effuser 34, One concentrated solution pumps 34p.Third condenser C3 is equivalent to third condensation part, has third condensation heat conducting pipe 341, and be connected with and match If the third refrigerant liquid effuser 344 of third refrigerant liquid pump 344p.Third condenser C3 and surrounding structure It constitutes identically as the first condenser C1, third condenses heat conducting pipe 341, third refrigerant liquid effuser 344, third refrigerant Liquid pump 344p be respectively equivalent in the first condenser C1 first condensation heat conducting pipe 41, the first refrigerant liquid effuser 44, First refrigerant liquid pumps 44p.Third regenerator G3 and third condenser C3 is contained in third regeneration condensation tank body 330, effect Imitative first regeneration condensation tank body 30, the two are divided by third regeneration condenser wall 339.
In the present embodiment, one end be connected to the other end of the third weak solution effuser 314 of third absorber A3 with The connection of second weak solution effuser 18 is collaborated from the third absorber A3 third weak solution Sw3 flowed out and the second weak solution Sw2. In addition, one end is connected to the other end of the third concentrated solution ingress pipe 313 of third absorber solution supplying device 312 and second dense Solution ingress pipe 17 connects, and supplies in a part of the concentrated solution Sa of the second concentrated solution ingress pipe 17 flowing to third absorber A3 It gives.In addition, one end is connected to the other end and second refrigerant liquid of the third refrigerant liquid ingress pipe 323 of third evaporator E3 Body ingress pipe 27 connects, the refrigerant liquid Vf that second refrigerant liquid ingress pipe 27 flows a part to third evaporator E3 supply.In addition, one end is connected to the other end and the first concentrated solution stream of the third concentrated solution effuser 334 of third regenerator G3 Outlet pipe 34 connects, and collaborates from the third regenerator G3 third concentrated solution Sa3 flowed out and the first concentrated solution Sa1.In addition, one end connects In the other end and the first weak solution ingress pipe 33 of the third weak solution ingress pipe 333 of third regenerator solution supplying device 332 Connection is supplied in a part of the weak solution Sw of the first weak solution ingress pipe 33 flowing to third regenerator G3.In addition, one end connects The other end and the first refrigerant liquid effuser 44 for being connected to the third refrigerant liquid effuser 344 of third condenser C3 connect It connects, collaborates from the third condenser C3 third refrigerant liquid Vf3 flowed out and the first refrigerant liquid Vf1.
Third absorber A3 is configured when from the flow direction of cryogen FL in the first absorber A1 and the second absorber Between A2.In absorption type heat exchange system 9, heat conducting pipe 11 is absorbed instead of in absorption type heat exchange system 1 (referring to Fig.1) first Ground is connect (referring to Fig.1) by absorber cryogen connecting tube 71 with the second absorption heat conducting pipe 15, and first absorbs heat conducting pipe 11 Heat conducting pipe 311 is absorbed with third connect by the first absorber cryogen connecting tube 71A, and the second absorption heat conducting pipe 15 and Third absorbs heat conducting pipe 311 and passes through the second absorber cryogen connecting tube 71B connection.In addition, third condenser C3 is from low Configuration is between the first condenser C1 and the second condenser C2 when the flow direction observation of warm fluid FL.In absorption type heat exchange system 9 In, pass through condensation instead of the first condensation heat conducting pipe 41 in absorption type heat exchange system 1 (referring to Fig.1) and the second condensation heat conducting pipe 45 Device cryogen connecting tube 74 (referring to Fig.1) connection ground, the first condensation heat conducting pipe 41 and third condensation heat conducting pipe 341 pass through first Condenser cryogen connecting tube 74A connection, and the second condensation heat conducting pipe 45 and third condensation heat conducting pipe 341 are cold by second Condenser cryogen connecting tube 74B connection.According to this structure, it is pressed in the cryogen FL that cryogen ingress pipe 57 flows According to the second condenser C2, third condenser C3, the first condenser C1, heat exchange department 80, the second absorber A2, third absorber Flows and reach cryogen effuser 53 to the sequential series of A3, the first absorber A1.Third evaporator E3 is from high-temperature stream Configuration is between the first evaporator E1 and the second evaporator E2 when the flow direction observation of body FH.In absorption type heat exchange system 9, generation Pass through evaporator height for the first evaporation heat source tube 21 in absorption type heat exchange system 1 (referring to Fig.1) and the second evaporation heat source tube 25 Warm fluid connecting line 72 (referring to Fig.1) connection ground, the first evaporation heat source tube 21 and third evaporation heat source tube 321 pass through the first evaporation Device high temperature fluid connecting tube 72A connection, and the second evaporation heat source tube 25 and third evaporation heat source tube 321 pass through the second evaporator The 72B connection of high temperature fluid connecting tube.Third regenerator G3 is configured when from the flow direction of high temperature fluid FH in the first regenerator Between G1 and Second reactivator G2.In absorption type heat exchange system 9, instead of in absorption type heat exchange system 1 (referring to Fig.1) Heat source capsule 31 connect ground by regenerator high temperature fluid connecting tube 73 with the second regeneration heat source tube 35 (referring to Fig.1) again and again, the Heat source capsule 31 is connect with third regeneration heat source tube 331 by the first regenerator high temperature fluid connecting tube 73A again and again, and second Regeneration heat source tube 35 is connect with third regeneration heat source tube 331 by Second reactivator high temperature fluid connecting tube 73B.According in this way Structure, high temperature heat source ingress pipe 52 flow high temperature fluid FH according to the first regenerator G1, third regenerator G3, second again Flows and reach high temperature heat source stream to the sequential series of raw device G2, the first evaporator E1, third evaporator E3, the second evaporator E2 Outlet pipe 56.The structure other than the above of absorption type heat exchange system 9 is identical as absorption type heat exchange system 1 (referring to Fig.1).
In the absorption type heat exchange system 9 constituted as described above, cryogen FL followed by the second condenser C2, Third condenser C3, the first condenser C1 and be heated three times, after being heated by heat exchange department 80, further followed by Second absorber A2, third absorber A3, the first absorber A1 and be heated three times, therefore can make in cryogen effuser The temperature of the cryogen FL of 53 flowings is than absorption type heat exchange system 1 (referring to Fig.1) height.In addition, being flowed in the first evaporator E1 The temperature of high temperature fluid FH of the temperature of dynamic high temperature fluid FH than flowing in third evaporator E3 is high, flows in third evaporator E3 The temperature of high temperature fluid FH of the temperature of dynamic high temperature fluid FH than flowing in the second evaporator E2 is high, therefore for each evaporator And for internal pressure/temperature of each absorber, internal pressure/temperature of the second evaporator E2 and the second absorber A2 are minimum, then According in internal pressure/temperature of third evaporator E3 and third absorber A3, the first evaporator E1 and the first absorber A1 Pressure/temperature sequence increases, if being sequentially introduced into cryogen FL according to this, can make by the low temperature of each absorber heat temperature raising The temperature of fluid FL successively increases.In addition it is also possible to have added third absorber A3, third evaporator E3, third regenerator G3, third condenser C3 structure on the basis of, the 4th absorber, the 4th evaporator, the 4th regenerator, the 4th cold is further set Condenser is arranged the 4th between the first absorber A1 and the first evaporator E1 and third absorber A3 and third evaporator E3 Absorber and the 4th evaporator are condensed in the first regenerator G1 and the first condenser C1 and third regenerator G3 and third 4th regenerator and the 4th condenser are set between device C3, if constituting in this wise, cryogen FL is heated four times and energy Enough temperature improved after heating.
Next, the absorption type heat exchange system 10 of 2 pairs of the tenth embodiments of the invention is illustrated referring to Fig.1.Figure 12 be the exemplary system figure of absorption type heat exchange system 10.Absorption type heat exchange system 10 and the 4 (reference of absorption type heat exchange system It Fig. 4) compares, other than the structure of absorption type heat exchange system 4 (referring to Fig. 4), is mainly having third absorber A3, third Evaporator E3, third regenerator G3, third condenser C3 point on it is different.It also include different knots with the main difference Structure is described below.Third absorber A3 and third evaporator E3 substantially with the 9 (reference of absorption type heat exchange system Third absorber A3 and third evaporator E3 in Figure 11) are constituted in the same manner, are drawn being contained in by third absorption evaporation wall 319 It is also general that the third divided, which absorbs on the point of evaporation tank body 310, but is connect with third absorber solution supplying device 312 Be not third concentrated solution ingress pipe 313 (referring to Fig.1 1) but third concentrated solution effuser 334, connect with third evaporator E3 Be not third refrigerant liquid ingress pipe 323 (referring to Fig.1 1) but it is different on the point of third refrigerant liquid effuser 344. Third regenerator G3 and third condenser C3 substantially with the third regenerator G3 in absorption type heat exchange system 9 (referring to Fig.1 1) And third condenser C3 is constituted in the same manner, is being contained in the third regeneration condensation tank body divided by third regeneration condenser wall 339 It is also general on 330 point, but is not that third weak solution imports what is connect with third regenerator solution supplying device 332 Pipe 333 (referring to Fig.1 1) but it is different on the point of third weak solution effuser 314.In absorption type heat exchange system 10, do not set It is equipped with the weak solution collecting fitting 61 (referring to Fig.1 1) being arranged in absorption type heat exchange system 9 (referring to Fig.1 1) and concentrated solution is closed Flow tube 63 (referring to Fig.1 1).In absorption type heat exchange system 10, third weak solution Sw3 and third concentrated solution Sa3 are in third It is recycled between absorber A3 and third regenerator G3 when changing concentration, third weak solution effuser 314 and third concentrated solution Effuser 334 and third absorber A3 and third regenerator G3 cooperatively constitute third absorbing liquid circulation stream.In addition, In absorption type heat exchange system 10, it is molten that third weak solution effuser 314 and third concentrated solution effuser 334 are provided with third Liquid heat exchanger 62C.In addition, refrigerant V becomes as third system and changes third refrigerant liquid Vf3, third evaporator system Refrigerant vapor Ve3, the first regenerator refrigerant vapour Vg3 and phase side are inhaled in third condenser C3, third evaporator E3, third Receive device A3, third regenerator G3 circulation.
Third absorber A3 is configured when from the flow direction of cryogen FL in the first absorber A1 and the second absorber Between A2.In absorption type heat exchange system 10, heat conducting pipe is absorbed instead of in absorption type heat exchange system 4 (referring to Fig. 4) first 11 connect ground by absorber cryogen connecting tube 71 with the second absorption heat conducting pipe 15 (referring to Fig. 4), and first absorbs heat conducting pipe 11 absorb heat conducting pipe 311 with third is connect by the first absorber cryogen connecting tube 71A, and second absorbs heat conducting pipe 15 Heat conducting pipe 311 is absorbed with third to connect by the second absorber cryogen connecting tube 71B.In addition, third condenser C3 from When the flow direction observation of cryogen FL, configure between the first condenser C1 and the second condenser C2.In absorption heat exchange series In system 10, pass through instead of the first condensation heat conducting pipe 41 in absorption type heat exchange system 4 (referring to Fig. 4) and the second condensation heat conducting pipe 45 Condenser cryogen connecting tube 74 (referring to Fig. 4) connection ground, the first condensation heat conducting pipe 41 pass through with third condensation heat conducting pipe 341 First condenser cryogen connecting tube 74A connection, and the second condensation heat conducting pipe 45 and third condensation heat conducting pipe 341 pass through the Two condenser cryogen connecting tube 74B connections.According to this structure, the cryogen flowed in cryogen ingress pipe 57 FL is absorbed according to the second condenser C2, third condenser C3, the first condenser C1, heat exchange department 80, the second absorber A2, third Flows and reach cryogen effuser 53 to the sequential series of device A3, the first absorber A1.Third evaporator E3 and third Regenerator G3 when from the flow direction of high temperature fluid FH, steam in the first evaporator E1 and the first regenerator G1 and second by configuration It sends out between device E2 and Second reactivator G2.In absorption type heat exchange system 10, instead of the 4 (reference of absorption type heat exchange system The first regeneration heat source tube 31 connect ground, the first regenerated heat by heat source intermediate connection tube 77 with the second evaporation heat source tube 25 in Fig. 4) Source capsule 31 and third evaporation heat source tube 321 connects by the first heat source intermediate connection tube 77A, and second evaporate heat source tube 25 and Third regenerates heat source tube 331 and passes through Secondary Heat Source intermediate connection tube 77B connection.Third evaporates heat source tube 321 and third regenerated heat Source capsule 331 is connected by heat source third connecting tube 79.According to this structure, the high-temperature stream flowed in high temperature heat source ingress pipe 52 Body FH is according to the first evaporator E1, the first regenerator G1, third evaporator E3, third regenerator G3, the second evaporator E2, second Flows and reach high temperature heat source effuser 56 to the sequential series of regenerator G2.Absorption type heat exchange system 10 it is other than the above Structure is identical as absorption type heat exchange system 4 (referring to Fig. 4).
In the absorption type heat exchange system 10 constituted in this way, in the same manner with absorption type heat exchange system 4 (referring to Fig. 4), Multiple (3) independent system paths with absorbing liquid S Yu the absorption heat pump cycle of refrigerant V, in addition to can be to multiple Except absorption heat pump cycle is controlled and managed, cryogen FL is followed by the second condenser C2, third condenser C3, the first condenser C1 and be heated three times, and after being heated by heat exchange department 80, further inhaled followed by second Receive device A2, third absorber A3, the first absorber A1 and be heated three times, therefore can make cryogen effuser 53 flow Cryogen FL temperature it is higher than absorption type heat exchange system 4 (referring to Fig. 4).In addition, in the height of the first evaporator E1 flowing The temperature of high temperature fluid FH of the temperature of warm fluid FH than flowing in third evaporator E3 is high, in the height of third evaporator E3 flowing The temperature of high temperature fluid FH of the temperature of warm fluid FH than flowing in the second evaporator E2 is high, therefore for each evaporator and respectively For internal pressure/temperature of absorber, internal pressure/temperature of the second evaporator E2 and the second absorber A2 are minimum, then according to Internal pressure/temperature of internal pressure/temperature of three evaporator E3 and third absorber A3, the first evaporator E1 and the first absorber A1 Sequence increase, if being sequentially introduced into cryogen FL according to this, can make by the cryogen FL of each absorber heat temperature raising Temperature successively increase.In addition it is also possible to have added third absorber A3, third evaporator E3, third regenerator G3, third On the basis of the structure of condenser C3, the 4th absorber, the 4th evaporator, the 4th regenerator, the 4th condenser are further set, and And setting the 4th is inhaled between the second absorber A2 and the second evaporator E2 and third regenerator G3 and third condenser C3 Device, the 4th evaporator, the 4th regenerator, the 4th condenser are received, if constituting in this wise, cryogen FL is heated four times and energy Enough temperature improved after heating.
In the above description, cryogen FL is in the first absorber A1, the second absorber A2 and third absorber A3 It flows, but can also flow in parallel in series.Alternatively, replacing or therewith together, cryogen FL is mainly first Condenser C1, the second condenser C2 and third condenser C3 flow in series, but can also flow in parallel.If low temperature stream Body FL flows in parallel in each absorber A1, A2, A3 and/or each condenser C1, C2, C3, then can make in each absorber The case where flow resistance when A1, A2, A3 and/or each condenser C1, C2, C3 flow is than flowing in series is small, suitable for making Cryogen FL permitted pressure difference lesser situation when flowing.
In the above description, in absorption type heat exchange system 1,2,3,4,5,6,7,9,10, the first evaporator E1, Two evaporator E2 and third evaporator E3 are full-liquid type but it is also possible to be fallig film.Evaporator is set to flow down liquid film In the case where formula, as the first refrigerant liquid body feeding 22 or second refrigerant liquid in absorption type heat exchange system 1A, 8 Like that, the top setting in evaporator supplies the refrigerant liquid body feeding of refrigerant liquid Vf to body feeding 26, The end for the refrigerant liquid pipe connecting with evaporator is set to be connected to refrigerant liquid body feeding in the case where full-liquid type. Alternatively, it is also possible to be arranged to refrigerant liquid body feeding supply evaporator lower part refrigerant liquid Vf piping and Pump.Conversely, evaporator can also be made absorption in the absorption type heat exchange system 1A for making evaporator fallig film, 8 Full-liquid type as heat-exchange system 1 etc..
In the above description, in absorption type heat exchange system 1,1A, 3,5,6,9, from the portion that heat exchange department 80 flows out High temperature fluid FHs is divided to flow out with from the first regenerator G1, Second reactivator G2, the first evaporator E1 and the second evaporator E2 The interflow high temperature fluid FH, however, you can also not with from the first regenerator G1, Second reactivator G2, first evaporator E1, Yi Ji The high temperature fluid FH of two evaporator E2 outflow collaborates ground, flows into the system different from the system for flowing out high temperature fluid FH.Into one For step, in the above description, to heat exchange department 80 flow into part high temperature fluid FHs from high temperature fluid FH branch, but It can be from the system introducing different from high temperature fluid FH.In such manner, it is possible to utilize diversified heat.
In the above description, it in absorption type heat exchange system 1A, 1B, absorbs in evaporation tank body 10 first by first Evaporator E1 is configured at the top of the first absorber A1, absorbs in evaporation tank body 20 second second evaporator E2 being configured at the First condenser C1 is configured at the upper of the first regenerator G1 in the first regeneration condensation tank body 30 by the top of two absorber A2 Second condenser C2, is configured at the top of Second reactivator G2 by side in the second regeneration condensation tank body 40, but can also be the One absorbs the top that the first absorber A1 is configured to the first evaporator E1 in evaporation tank body 10, absorbs evaporation tank body 20 second The middle top that second absorber A2 is configured to the second evaporator E2, by the first regenerator G1 in the first regeneration condensation tank body 30 It is configured at the top of the first condenser C1, Second reactivator G2 is configured at the second condenser in the second regeneration condensation tank body 40 The top of C2.
In the above description, in absorption type heat exchange system 9,10, make cryogen FL according to the second condenser C2, Flow to the sequential series of third condenser C3, the first condenser C1, but can also in contrast according to the first condenser C1, Flow to the sequential series of third condenser C3, the second condenser C2.In addition, making low temperature stream in absorption type heat exchange system 9 Body FL according to the first absorber A1, third absorber A3, the second absorber A2 sequential series flow, but can also phase therewith Instead according to the second absorber A2, third absorber A3, the first absorber A1 sequential series flow.In addition, absorption In heat-exchange system 10, make cryogen FL according to the sequence string of the second absorber A2, third absorber A3, the first absorber A1 The flowing of connection ground, but can also be in contrast according to the sequence string of the first absorber A1, third absorber A3, the second absorber A2 The flowing of connection ground.

Claims (16)

1. a kind of absorption type heat exchange system, which is characterized in that have:
First absorption portion, the absorption released when absorbing the steam of refrigerant by absorbing liquid is hot and makes the temperature for being heated fluid Degree rises;
Second absorption portion, the absorption released when absorbing the steam of refrigerant by absorbing liquid is hot and makes the temperature for being heated fluid Degree rises;
First condensation part, the condensation heat released when becoming refrigerant liquid by the steam condensation of refrigerant, makes to be added The temperature of hot fluid rises;
Second condensation part, the condensation heat released when becoming refrigerant liquid by the steam condensation of refrigerant, makes to be added The temperature of hot fluid rises;
First evaporation part is directly or indirectly led from at least one party of first condensation part and second condensation part Enter the refrigerant liquid, and captures the refrigerant liquid evacuator body imported from heating source fluid and become to described first Required evaporation latent heat when the steam of the refrigerant of absorption portion supply, so that the temperature of the heating source fluid be made to drop It is low;
Second evaporation part is directly or indirectly led from at least one party of first condensation part and second condensation part Enter the refrigerant liquid, and captures the refrigerant liquid evacuator body imported from heating source fluid and become to described second Required evaporation latent heat when the steam of the refrigerant of absorption portion supply, so that the temperature of the heating source fluid be made to drop It is low;
First reproducing unit is directly or indirectly led from at least one party in first absorption portion and second absorption portion Enter the absorbing liquid, and captures from heating source fluid in order to generate the steam of the refrigerant supplied to first condensation part And the absorbing liquid imported is heated and refrigerant is made to be detached from required heat from the absorbing liquid, to make described add The temperature of heat source fluid reduces;
Second reproducing unit is directly or indirectly led from at least one party in first absorption portion and second absorption portion Enter the absorbing liquid, capture from heating source fluid in order to generate to second condensation part supply the refrigerant steam and The absorbing liquid imported is heated and refrigerant is made to be detached from required heat from the absorbing liquid, to make the heating The temperature of source stream body reduces;And
Heat exchange department, make from first condensation part and second condensation part outflow and to first absorption portion and Second absorption portion flow into before it is described be heated fluid, with from towards first evaporation part, second evaporation part, institute The heating source of a part of the heating source fluid branch before stating the first reproducing unit and second reproducing unit importing Heat exchange is carried out between fluid,
The absorption type heat exchange system is constituted are as follows: by the absorption heat pump cycle of the absorbing liquid and the refrigerant, is made Pressure and the temperature for obtaining the inside of first evaporation part are higher than first condensation part, the inside of second evaporation part Pressure and temperature are higher than second condensation part,
So that from fluid is heated to first absorption portion and second absorption portion described in heat exchange department outflow The mode of inflow is heated the flow path of fluid described in composition.
2. absorption type heat exchange system according to claim 1, which is characterized in that
So that from the heat exchange department flow out the heating source fluid, with from first evaporation part, second evaporation part, The mode at the heating source fluid interflow of first reproducing unit and second reproducing unit outflow, constitutes the heating source The flow path of fluid.
3. a kind of absorption type heat exchange system, which is characterized in that have:
First absorption portion, the absorption released when absorbing the steam of refrigerant by absorbing liquid is hot and makes the temperature for being heated fluid Degree rises;
Second absorption portion, the absorption released when absorbing the steam of refrigerant by absorbing liquid is hot and makes the temperature for being heated fluid Degree rises;
First condensation part, the condensation heat that releases when being condensed by the steam of refrigerant and becoming refrigerant liquid and make to be added The temperature of hot fluid rises;
Second condensation part, the condensation heat that releases when being condensed by the steam of refrigerant and becoming refrigerant liquid and make to be added The temperature of hot fluid rises;
First evaporation part is directly or indirectly led from at least one party of first condensation part and second condensation part Enter the refrigerant liquid, and captures the refrigerant liquid evacuator body imported from heating source fluid and become to described first Required evaporation latent heat when the steam of the refrigerant of absorption portion supply, so that making the temperature of the heating source fluid reduces;
Second evaporation part is directly or indirectly led from at least one party of first condensation part and second condensation part Enter the refrigerant liquid, captures the refrigerant liquid evacuator body imported from heating source fluid and become to described second and inhale Required evaporation latent heat when the steam of the refrigerant of receipts portion supply, so that making the temperature of the heating source fluid reduces;
First reproducing unit is directly or indirectly led from at least one party in first absorption portion and second absorption portion Enter the absorbing liquid, and captures from heating source fluid in order to generate the steam of the refrigerant supplied to first condensation part And the absorbing liquid imported is heated and refrigerant is made to be detached from required heat from the absorbing liquid, to make described add The temperature of heat source fluid reduces;
Second reproducing unit is directly or indirectly led from at least one party in first absorption portion and second absorption portion Enter the absorbing liquid, and captures from heating source fluid in order to generate the steam of the refrigerant supplied to second condensation part And the absorbing liquid imported is heated and refrigerant is made to be detached from required heat from the absorbing liquid, to make described add The temperature of heat source fluid reduces;And
Heat exchange department, make from first condensation part and second condensation part outflow and to first absorption portion and Second absorption portion flow into before it is described be heated fluid, with from first evaporation part, second evaporation part, described the Heat exchange is carried out between one reproducing unit and the heating source fluid of second reproducing unit outflow,
The absorption type heat exchange system is constituted are as follows: by the absorption heat pump cycle of the absorbing liquid and the refrigerant, is made Pressure and the temperature for obtaining the inside of first evaporation part are higher than first condensation part, the inside of second evaporation part Pressure and temperature are higher than second condensation part,
So that from fluid is heated to first absorption portion and second absorption portion described in heat exchange department outflow The mode of inflow is heated the flow path of fluid described in composition.
4. absorption type heat exchange system according to claim 2, which is characterized in that
So that from at least one party in first absorption portion and second absorption portion flow out the absorbing liquid directly or It is flowed into parallel indirectly to first reproducing unit and second reproducing unit, from first reproducing unit and described second The absorbing liquid of at least one party's outflow of reproducing unit is directly or indirectly absorbed to first absorption portion and described second The mode that portion flows into parallel constitutes the flow path of the absorbing liquid.
5. absorption type heat exchange system according to claim 3, which is characterized in that
So that from at least one party in first absorption portion and second absorption portion flow out the absorbing liquid directly or It is flowed into parallel indirectly to first reproducing unit and second reproducing unit, from first reproducing unit and described second The absorbing liquid of at least one party's outflow of reproducing unit is directly or indirectly absorbed to first absorption portion and described second The mode that portion flows into parallel constitutes the flow path of the absorbing liquid.
6. absorption type heat exchange system according to claim 2, which is characterized in that
So as to directly or indirectly be flowed into from at least one party in first absorption portion and second absorption portion described The absorbing liquid of first reproducing unit or second reproducing unit is in first reproducing unit and the second reproducing unit string The flowing of connection ground directly or indirectly flows into described from at least one party of first reproducing unit and second reproducing unit The absorbing liquid in the first absorption portion or second absorption portion is gone here and there in first absorption portion and second absorption portion The mode of connection ground flowing, constitutes the flow path of the absorbing liquid.
7. absorption type heat exchange system according to claim 3, which is characterized in that
So as to directly or indirectly be flowed into from at least one party in first absorption portion and second absorption portion described The absorbing liquid of first reproducing unit or second reproducing unit is in first reproducing unit and the second reproducing unit string The flowing of connection ground directly or indirectly flows into described from at least one party of first reproducing unit and second reproducing unit The absorbing liquid in the first absorption portion or second absorption portion is gone here and there in first absorption portion and second absorption portion The mode of connection ground flowing, constitutes the flow path of the absorbing liquid.
8. absorption type heat exchange system according to claim 2, which is characterized in that have:
First absorbing liquid circulation stream, so that the absorbing liquid flowed out from first absorption portion is to first reproducing unit Inflow and the mode flowed into from the absorbing liquid that first reproducing unit flows out to first absorption portion, make the absorption Liquid recycles between first absorption portion and first reproducing unit;With
Second absorbing liquid circulation stream, so that the absorbing liquid flowed out from second absorption portion is to second reproducing unit Inflow and the mode flowed into from the absorbing liquid that second reproducing unit flows out to second absorption portion, make the absorption Liquid recycles between second absorption portion and second reproducing unit.
9. absorption type heat exchange system according to claim 3, which is characterized in that have:
First absorbing liquid circulation stream, so that the absorbing liquid flowed out from first absorption portion is to first reproducing unit Inflow and the mode flowed into from the absorbing liquid that first reproducing unit flows out to first absorption portion, make the absorption Liquid recycles between first absorption portion and first reproducing unit;With
Second absorbing liquid circulation stream, so that the absorbing liquid flowed out from second absorption portion is to second reproducing unit Inflow and the mode flowed into from the absorbing liquid that second reproducing unit flows out to second absorption portion, make the absorption Liquid recycles between second absorption portion and second reproducing unit.
10. absorption type heat exchange system described according to claim 1~any one of 9, which is characterized in that
In a manner of being heated fluid described in making and be flowed in series in first absorption portion and second absorption portion, constitute The flow path for being heated fluid.
11. absorption type heat exchange system according to claim 10, which is characterized in that
So that the heating source fluid flows into first reproducing unit or first evaporation part at first, and according to appropriate Sequence flows in series in first reproducing unit, first evaporation part, second reproducing unit and second evaporation part Dynamic mode constitutes the flow path of the heating source fluid,
So that described be heated fluid after flowing through first condensation part and second condensation part in series to described One absorption portion or second absorption portion flow into, and described after the heating source fluid flows through first evaporation part In the case that second evaporation part is flowed, described be heated after fluid flows through second absorption portion is flowed in first absorption portion Mode, and so that after the heating source fluid flows through second evaporation part first evaporation part flow the case where Under, the fluid that is heated flows through the mode flowed behind first absorption portion in second absorption portion, constitutes described is added The flow path of hot fluid.
12. absorption type heat exchange system described according to claim 1~any one of 9, which is characterized in that
Be configured to carry out following at least one of constitute, it may be assumed that carry out with by the heating source fluid to first evaporation part, At least two mode structures imported in parallel in second evaporation part, first reproducing unit and second reproducing unit At the flow path of the heating source fluid;With to be heated fluid in parallel with second absorption portion to first absorption portion by described Ground import and it is described be heated fluid imported in parallel to first condensation part and second condensation part at least one The mode of side is heated the flow path of fluid described in composition.
13. absorption type heat exchange system described according to claim 1~any one of 9, which is characterized in that have:
First regeneration condensation tank body, in a manner of being connected to first reproducing unit with first condensation part, described in receiving First reproducing unit and first condensation part;With
Second regeneration condensation tank body, in a manner of being connected to second reproducing unit with second condensation part, described in receiving Second reproducing unit and second condensation part.
14. absorption type heat exchange system according to claim 13, which is characterized in that have:
First absorbs evaporation tank body, in a manner of being connected to first absorption portion with first evaporation part, described in receiving First absorption portion and first evaporation part;With
Second absorbs evaporation tank body, in a manner of being connected to second absorption portion with second evaporation part, described in receiving Second absorption portion and second evaporation part,
The first regeneration condensation tank body is configured at position different in horizontal direction from the second regeneration condensation tank body,
It absorbs and steams configured with described first in the top of the first regeneration condensation tank body and the second regeneration condensation tank body Send out tank body and the second absorption evaporation tank body.
15. absorption type heat exchange system according to claim 13, which is characterized in that
First absorption portion is contained in the tank body different from first evaporation part,
Second absorption portion is contained in the tank body different from second evaporation part.
16. absorption type heat exchange system described according to claim 1~any one of 9, which is characterized in that have:
Third absorption portion, the absorption released when absorbing the steam of refrigerant by absorbing liquid is hot and makes the temperature for being heated fluid Degree rises;
Third condensation part, the condensation heat for condensing by the steam of refrigerant and releasing when becoming refrigerant liquid make to be heated The temperature of fluid rises;
Third evaporation part, from least one of first condensation part, second condensation part and the third condensation part The refrigerant liquid is directly or indirectly imported, and captures the refrigerant liquid evacuator body imported from heating source fluid And become evaporation latent heat required when the steam of the refrigerant supplied to third absorption portion, to make the heating source The temperature of fluid reduces;And
Third reproducing unit, from least one of first absorption portion, second absorption portion and third absorption portion The absorbing liquid is directly or indirectly imported, and is captured from heating source fluid in order to generate to third condensation part supply The steam of the refrigerant and the absorbing liquid imported is heated and make refrigerant from the absorbing liquid disengaging needed for Heat, so that making the temperature of the heating source fluid reduces,
The absorption type heat exchange system is constituted are as follows: by the absorption heat pump cycle of the absorbing liquid and the refrigerant, is made Pressure and the temperature for obtaining the inside of the third evaporation part are higher than the third condensation part,
The heat exchange department be configured to for from first condensation part, the second condensation part and the third condensation part flow out and to The fluid that is heated before first absorption portion, second absorption portion and third absorption portion flow into flows into,
So that from the heat exchange department outflow described in be heated fluid to first absorption portion, second absorption portion and The mode that third absorption portion flows into is heated the flow path of fluid described in composition.
CN201811552771.6A 2017-12-25 2018-12-18 Absorption type heat exchange system Pending CN109974328A (en)

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JP2019113260A (en) * 2017-12-25 2019-07-11 荏原冷熱システム株式会社 Absorption type heat exchange system

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Publication number Priority date Publication date Assignee Title
KR100746241B1 (en) * 2006-06-20 2007-08-03 한국지역난방공사 Low temperature water two-stage absorbtion type refrigerator
CN101261054A (en) * 2007-12-29 2008-09-10 清华大学 Great temperature rising absorption type heat pump units
CN102032706A (en) * 2009-09-30 2011-04-27 三洋电机株式会社 Absorbing type refrigerator
CN105352079A (en) * 2015-11-24 2016-02-24 东南大学 Independent temperature and humidity processing air conditioner system driven by low-level thermal energy
CN107328132A (en) * 2017-06-30 2017-11-07 荏原冷热系统(中国)有限公司 A kind of second-kind absorption-type heat pump
CN209801851U (en) * 2017-12-25 2019-12-17 荏原冷热系统株式会社 Absorption heat exchange system

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100746241B1 (en) * 2006-06-20 2007-08-03 한국지역난방공사 Low temperature water two-stage absorbtion type refrigerator
CN101261054A (en) * 2007-12-29 2008-09-10 清华大学 Great temperature rising absorption type heat pump units
CN102032706A (en) * 2009-09-30 2011-04-27 三洋电机株式会社 Absorbing type refrigerator
CN105352079A (en) * 2015-11-24 2016-02-24 东南大学 Independent temperature and humidity processing air conditioner system driven by low-level thermal energy
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CN209801851U (en) * 2017-12-25 2019-12-17 荏原冷热系统株式会社 Absorption heat exchange system

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