CN205536654U - Stack heat pump and refrigeration cycle's absorption formula cold water machine - Google Patents

Stack heat pump and refrigeration cycle's absorption formula cold water machine Download PDF

Info

Publication number
CN205536654U
CN205536654U CN201620015304.XU CN201620015304U CN205536654U CN 205536654 U CN205536654 U CN 205536654U CN 201620015304 U CN201620015304 U CN 201620015304U CN 205536654 U CN205536654 U CN 205536654U
Authority
CN
China
Prior art keywords
outlet
heat
cold
pipeline
hot
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.)
Expired - Fee Related
Application number
CN201620015304.XU
Other languages
Chinese (zh)
Inventor
周轶松
周鼎
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.)
SHANGHAI DISEN ENERGY TECHNOLOGY Co Ltd
Original Assignee
SHANGHAI DISEN ENERGY TECHNOLOGY 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
Application filed by SHANGHAI DISEN ENERGY TECHNOLOGY Co Ltd filed Critical SHANGHAI DISEN ENERGY TECHNOLOGY Co Ltd
Priority to CN201620015304.XU priority Critical patent/CN205536654U/en
Application granted granted Critical
Publication of CN205536654U publication Critical patent/CN205536654U/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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]
    • Y02B30/52Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
    • 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

The utility model relates to a stack heat pump and refrigeration cycle's absorption formula cold water machine, the first order to third level evaporation unit mainly act on the concentration of weak solution, and the flash steam latent heat flash distillation of one -level generated steam and supplies back one -level utilization before back one -level was then utilized, and the heat source input of the first order is got back to to steam that the fourth stage generated after mechanical internal heat booster pump heats, and not enough heat source adopts to be had absorption heat pump to generate hot water to incorporate the steam system that regenerates into through the vapor generation system. The whole retrieval and utilizations of operation process high temperature heat of condensation and some low -temperature condensation heat of cryogen steam, simultaneously because its the hot break of regeneration steam that generates and temperature increase only consume less electric energy just by multistage use, thus the energy consumption that has significantly reduced, the utility model discloses a energy efficiency ratio reaches COP=18 (per hour obtain cold volume 3489kw, consume electric quantity 180kw), the emission of high temperature heat of condensation, hot driving have reduced 60% and the cooling water quantity.

Description

A kind of superposition heat pump and the absorption cooling-water machine of kind of refrigeration cycle
[technical field]
This utility model relates to a kind of complete power-actuated multistage weak solution method for concentration, complete at process of refrigerastion Portion absorbs high temperature water as refrigerant steam condensation discharge heat and is back to refrigeration system, the low temperature agent of part reuse simultaneously Water vapour discharge heat is used for driving heat pump to generate new heat energy and supplements partial heat energy needed for refrigeration system, thus obtains Obtain the absorption type refrigerating unit of ultrahigh energy efficiency ratio.
[background technology]
Traditional absorption-type refrigerating method has had the production history of last 100 years, uses the heating power finalized the design almost Process and equipment;In actual use, with the most use is to follow for the lithium bromide absorbing type refrigeration of air-conditioning Ring and for freezing, the ammonia absorption type kind of refrigeration cycle of air-conditioning.Recent decades is due to by " Montreal Agreement " The impact of regulation, reduces the use of fluorine carbide, and utilizes waste heat as driving heat source to reducing carbon emission The meaning having, absorption-type refrigerating method has obtained bigger popularization and development, such as open source literature CN200510060377.7 " multiple-energy-source drive lithium bromide refrigerating air conditioner " proposes make use of solar energy, Microwave and fuel oil (gas) various energy resources, carry in CN101871702A " double heat source high-efficiency absorption refrigerating plant " Going out the Application way of double thermal source, CN103438605A " absorbs and heat exchange type Absorption Cooling System occurs " and proposes The solar energy method as thermal source, Japan Patent 2009-236440 " Gas heat pup type air Conditioning device or refrigerating device " and 2009-236441 " Heat pup type Refrigerating device " develop with gas engine used heat as air-conditioning, the absorption system of refrigeration machine thermal source Cooling method.This kind of refrigerating method is applied to the utilization of low temperature exhaust heat more.But these improvement all can not improve absorption The Energy Efficiency Ratio of formula kind of refrigeration cycle itself.
Up-to-date GB 29540-2013 " lithium bromide adsorption water chilling unit energy efficiency market and efficiency grade " Standard determining, the COP of double-effect lithium bromide absorption type unit is 1.12~1.4, and double-effect lithium bromide refrigeration machine Input heat source stream be 150 DEG C of even more high-temperatures, and the ammonia-water cold COP of absorption unit processed only 0.3~ 0.4.Relevant disclosed patent documentation: ZL011426144 " band in terms of improving absorption type refrigerating unit Energy Efficiency Ratio Steam compressed three-effect absorption-type refrigerator in parallel " in propose reduce previous stage generator temperature reach fall The efficiency of the corrosion simultaneity factor of low equipment slightly improves, CN101520250 " efficient double-lift absorption refrigeration Device " propose one more conveniently route and slightly improve efficiency.Have due to steam mechanical compressing hot pump in the recent period There is the sensible heat that can promote low temperature exhaust heat steam by the least mechanical power, become high-temperature steam with regard to its latent heat recyclable, Utilize as high temperature heat source, therefore come into one's own in heat energy system, at Chinese patent CN201010198705.0 " by pump for extracting power plant waste heat heating condensate water system ";Chinese patent CN20101063699.5 " thermoelectricity Coproduction coupling heat pump feasible region cold-hot combined supply system and method ";Chinese patent CN200910223748.7 is " low Temperature cogeneration system exhaust steam condensation process self-coupling cold source heat pump circulating device ";Chinese patent CN201010163688.7 " central heating system of coupling circulating water heat pump of power plant with cogeneration and method " is Relate to utilize low-temperature heat source, including water and steam, improved the generating of whole cogeneration of heat and power by source pump The Energy Efficiency Ratio of heating system;But all it is not involved with utilizing steam mechanical compressing hot pump to be applied to refrigeration, air-conditioning Problem in circulation, to improve the Energy Efficiency Ratio problem of refrigeration unit itself.
Low underlying reason is that of Energy Efficiency Ratio of absorption-type refrigerating method carries out weak solution concentration at high tension generator Time the refrigerant vapour that generates of heat absorption need to absorb substantial amounts of vaporization heat energy, and contained by the refrigerant vapour of high temperature Heat in condensation process, discharge the heat of transformation be all discharged into outside system, do not recycle;With The heat of condensation that the refrigerant vapour of sample low temperature is discharged when being changed into liquid phase by vapour phase in entering low-pressure absorber Heat is also discharged into outside refrigeration system, is not the most recycled utilization.The disclosedest patent documentation All there is no water as refrigerant steam phase transforming recuperation of heat and the report for self refrigeration system.? CN201020188184.6 " dual-effect type-II lithium bromide absorption heat pump unit " simply develops a kind of confession The source pump of heat, does not solve to discharge in above-mentioned circulation the reuse of heat.At CN200820115165.3 " The single-effect type third-kind absorption heat pump that kind of cold and hot two-way simultaneous utilizes ", make use of the discharge heat of a part for Heat supply, can simultaneously cooling and heat supply, COP is up to 2.2~2.6.But because be not again be back to be System is used for reducing driving refrigeration system energy input, so the reuse problem of discharge heat can not fundamentally be solved. The problem the most not solving low-energy-efficiency ratio, therefore refrigeration and the Energy Efficiency Ratio of heating, the lowest.
Absorption refrigeration, the major reason that Air-conditioning Cycle cost is high are to use pipe shell type heat exchange traditionally more Equipment and spray mass transfer method, heat transfer, mass tranfer coefficient low, heat exchange area is big, in addition it is also necessary to circulating pump, repeatedly Spray-absorption solution and cold-producing medium, and in the Chinese patent CN200480010361.9 " absorption of band external circuit Device and heat exchanger and include this absorber or the heat pump of heat exchanger and air conditioning system " change with board-like Hot device is as absorber or condenser, to improve heat exchange efficiency, including United States Patent (USP) US6176101 B1 “FLAT-PLATE ABSORBERS AND EVAPORATORS FOR ABSORPTION COOLERS " then condenser and absorber are assembled in a plate type heat exchanger, this equipment is cold for reclaiming Solidifying heat provides possibility, but this patent is not for solving the Energy Efficiency Ratio raising of absorption-type refrigerating method and reducing system System cost proposes solution.ZL201510465086X " a kind of Multi-effect plate type rising film counter flow evaporation plant and Method " propose board-like multiple-effect device liquid-gas phase transition process application mode, the most energy-efficient open spy Levy and application process, but have not yet to see for absorption system.
Absorption refrigeration, all using thermal source as driving energy, starts and runs refrigeration system work, consumption Being heat energy, output is cold, obviously can not use such device, the scope of application in the area not having thermal source It is restricted, there is presently no the input of a kind of full electric power and go to meet driving and the lithium bromide refrigerating system of normal work System, the method and apparatus that simultaneously be also satisfied high Energy Efficiency Ratio.
[summary of the invention]
The purpose of this utility model is the agent vapour latent heat system of being greatly improved discharged by recovery The Energy Efficiency Ratio of cold, hot and partially recycled cold by all reclaiming the water as refrigerant discharge when high temperature evaporation condenses The mode of the low-temperature evaporation discharge heat of agent water is achieved.In order to expand the application of Absorption Refrigerator originally Utility model proposes the high energy efficiency ratio Absorption Refrigerator that can also drive in the occasion without thermal source supply.For Realize above-mentioned purpose, the absorption type refrigerating unit of utility model a kind of full electric power reuse discharge heat, including:
Solution heat exchanger H5, cold side-entrance connects low-pressure absorber DX by pipeline, and cold side outlet port passes through Pipeline is connected to the cold side-entrance of coupling phase-change heat-exchanger H3 in the 3rd, and hot side-entrance connects first by pipeline The concentrated solution outlet of flash separation tank S1 bottom, hot side outlet enters with absorber DX via solution heat exchanger H5 Mouth connects,
First board-like interior coupling phase-change heat-exchanger H1, cold side-entrance is molten with the second flash separation tank S2 bottom Liquid pipeline connects, and connecting line series solution circulating pump E2, cold side outlet port connects the first flash distillation by pipeline and divides From tank S1, the compressed vapour that hot side-entrance connects Mechanical Vapor Compression M1 by steam tank H0 exports,
Second board-like interior coupling phase-change heat-exchange H2, pipeline and the first flash separation tank S1 are passed through in hot side-entrance The outlet of top indirect steam connect, the hot side-entrance connection of hot side outlet and the first water as refrigerant cooler H6, Cold side-entrance is connected with the 3rd flash separation tank S3 bottom solution line, connecting line series solution circulating pump E3, cold side outlet port connects the second flash separation tank S2 by pipeline,
Coupling phase-change heat-exchanger H3 in three-plate type, pipeline and the second flash separation tank are passed through in hot side-entrance The top indirect steam outlet of S2 connects, and the hot side-entrance of hot side outlet and the second water as refrigerant cooler H7 is even Connecing, cold side-entrance is connected with the weak solution outlet conduit of solution heat exchanger H5, and cold side outlet port is connected by pipeline 3rd flash separation tank S3,
4th board-like interior coupling phase-change heat-exchanger H4, pipeline and the 3rd flash separation tank are passed through in hot side-entrance The top indirect steam outlet of S3 connects, and the hot side-entrance of hot side outlet and the 3rd water as refrigerant cooler H8 is even Connecing, cold side-entrance is with the hot side lower part steam condensate (SC) outlet conduit coupling phase-change heat-exchanger H1 in first even Connecing, condensate water circulatory pump of connecting in pipeline, cold side outlet port connects the 4th flash separation tank S4 by pipeline,
4th flash separation tank S4 upper outlet is connected with the import of steam mechanical compressor M1, middle part Having two imports, the cold side outlet port of one and the 4th board-like interior coupling phase-change heat-exchanger H4 connects, another and plate The cold side outlet port of formula evaporative phase-change device H1 connects, lower part outlet and the cold side-entrance of plate evaporation phase transformation device H9 Pipeline is connected,
Mechanical vapor-compression pump M1, has inlet and outlet, its import and the vapour phase of flash separator S4 Outlet is connected by pipeline, and outlet is connected by pipeline with the hot side-entrance of steam tank HO,
Three the most corresponding respective board-like interior coupling phase inversion at different levels of water as refrigerant cooler (H6, H7, H8) Hot device (H2, H3, H4), hot side-entrance is connected by pipeline with the board-like interior hot side outlet of phase-change heat-exchanger that couples Connecing, outlet is connected with the intake header of low pressure evaporator DZ, cold side-entrance and the cooling of low-pressure absorber DX Water out connects, and cold side outlet port enters with generator FSQ, the low-temperature heat source of vaporizer ZF1 of absorption heat pump Mouth connects, generator FSQ, the low-temperature heat source water out of vaporizer ZF1 and the cooling of low-pressure absorber DX Water inlet connects,
Plate evaporation phase transformation device H9, cold side outlet port and the 4th flash separation tank S4 import are connected by pipeline, Cold side-entrance is connected by pipeline with the 4th flash separation tank S4 outlet, hot side outlet and import the second absorber Coupling into and out of pipeline of XS2 heat medium water,
Generator FSQ, top has agent steam outlet and is connected with condenser LNQ, and bottom has dense molten Liquid outlet is connected with absorber XS2 through solution heat exchanger (H11, H10) by circulating pump E8, occurs There is heat exchange coil, the outlet of the cooling water pipe of the import of heat exchange coil and low-pressure absorber DX in device FSQ Connecting, the outlet of heat exchange coil is connected with the import of the cooling water pipe of low-pressure absorber DX,
Condenser LNQ, top has agent water vapour import and is connected with FSQ, and bottom has agent water out It is connected with vaporizer ZF1 and vaporizer ZF2 by circulating pump E9, in condenser LNQ, there is heat exchange coil, Heat exchange coil turnover/mouth goes out with low pressure evaporator DZ chilled water/and inlet pipe road is connected,
First absorber XS1, top has concentrated solution import side outlet hot with solution heat exchanger H10 and is connected, Bottom has taphole to be connected with the survey import of solution heat exchanger H11 heat, the hot side outlet of H11 and generator FSQ Overhead reflux mouth is connected by pipeline, and absorber XS1 top has agent water vapour import to be connected with vaporizer ZF1, Having heat exchange coil in absorber XS1, the outlet of heat exchange coil is entered hot side with the heat exchange coil of vaporizer ZF2 Mouth connects, and import is connected with the outlet of vaporizer ZF2 heat exchange coil by circulating pump E11,
First vaporizer ZF1, top has agent water sprayer tube import mediating recipe steam outlet, agent water vapour Outlet is connected with absorber XS1, and shower import is by agent water bottom circulating pump E9 and condenser LNQ Outlet connects, and has the cooling water pipe of its import/export of heat exchange coil and low-pressure absorber DX in vaporizer ZF1 Go out/import connect,
Second absorber XS2, top has agent water vapour import and solution inlet port, and taphole is arranged at bottom, Having heat exchange coil and solution spraying pipe in second absorber XS2, solution spraying pipe is cold with solution heat exchanger H10 Side outlet connects, and bottom solution exports side-entrance hot with solution heat exchanger H10 and is connected, the agent of absorber overhead Water vapour import is connected with vaporizer ZF2, heat exchange coil outlet/import respectively with the heat of plate-type evaporator H9 Side-entrance/outlet connects.
Second vaporizer ZF2, top has agent water sprayer tube import mediating recipe steam outlet, the second evaporation Having heat exchange coil in device ZF2, shower import is connected with condenser LNQ by circulating pump E9, and second Heat exchange coil in vaporizer ZF and the heat exchange coil in the first absorber XS1 are connected and composed by pipeline and close Formula recycle loop pump E11 connects wherein, the agent steam outlet at top and the agent of the second absorber XS2 Water vapour import is connected by pipeline.
Described board-like interior coupling phase-change heat-exchanger be plate type heat exchanger, plate-type evaporator, plate-type condenser, Shell-and-tube heat exchanger.
Described water as refrigerant cooler is plank frame, the board-like interior coupling phase-change heat-exchange of corresponding each position Water as refrigerant chilling temperature needed for device realizes controlling by the automatic control components and parts configured.
This utility model also includes the absorption-type refrigerating method of a kind of full electric power reuse discharge heat, uses above-mentioned Full electric power reuse discharge heat absorption type refrigerating unit,
Weak solution evaporation and concentration is by the board-like interior coupling phase-change heat-exchanger (H1, H2, H3) of the first to the third level The evaporation separative element combined with flash separation tank (S1, S2, S3) undertakes, and the cryogen that previous stage generates steams Vapour is used for the heat energy needed for heat dilute solution by next stage,
Regeneration steam is to reclaim previous stage water as refrigerant steam by the 4th board-like interior coupling phase-change heat-exchanger H4 Heat energy is also generated by the 4th flash separation tank S4,
Mechanical vapor-compression pump M1 absorbs the low-order bit regeneration steam warp from the 4th flash separation tank S4 Power-actuated mechanical power makes regeneration steam supercharging input H0 steaming after heating the regeneration steam generating higher order position The hot side of the first board-like interior coupling phase-change heat-exchanger H1 is entered after vapour blending tank H0,
Inhaled from low pressure by reclaiming by the double effect absorption type heat pump of second-kind absorption-type heat pump principle design The cryogenic energy receiving device DX cooling circulating water mean temperature 36.7 degree generates 100 through bipolar absorption heat pump Degree high-temperature-hot-water supplements the not enough energy needed for system,
Driving heat source needed for the FSQ generator of absorption heat pump and ZF1 the first vaporizer is by low Obtaining in the cooling circulating water of pressure absorber DX, the low-temperature receiver of condenser LNQ is by low pressure evaporator DZ Chilled water obtain.
The utility model proposes a kind of superposition lithium bromide refrigerating and heating so that suction-type lithium bromide Refrigeration system has all reclaimed the water as refrigerant discharge heat when high temperature evaporation condenses in addition complete when refrigerating operaton Portion is back to this refrigerator system, and suction-type lithium bromide heating reuse is discharged by low-pressure absorber DX Part cryogenic temperature condensation heat and produce high-temperature-hot-water and be back to this refrigeration system as supplementary heat energy, thus significantly Degree improves the Energy Efficiency Ratio of lithium bromide water absorption refrigerating plant, due to the discharged at lower temperature by having reclaimed refrigeration system Heat further improves usefulness needed for meeting the even running of system as supplementary heat energy simultaneously.This project Also proposed the lithium bromide refrigerating method that the input of full electric power drives, during usual absorption cold work processed, need heat energy Input.Owing to have employed full electric power input pattern, expand the range of such device.This utility model The trapped energy theory (or COP) of the method and apparatus of example can reach 18, this than lithium bromide refrigerator COP=0.7~ 1.4 to exceed about more than 10 times.It is calculated as follows with this utility model example: obtain the cold Q produced cold =3489kw/h, inputs electricity total amount Q input=190kw/h, wherein: 1, MVR steam mechanical compressor 125kw/h, 2, all kinds of circulating pump 70kw/h.COP=Q is cold/Q input=3489kw/190kw=18.
[accompanying drawing explanation]
Fig. 1 is the main apparatus structure flow chart of embodiment;
In figure in the first order in the coupling phase-change heat-exchanger H1 first order flash separation tank S1 second level Coupling phase-change heat-exchanger H3 the in the coupling phase-change heat-exchanger H2 second level flash separation tank S2 third level In the three stages of flashing knockout drum S3 fourth stage, coupling phase-change heat-exchanger H4 fourth stage steam dodges and divides tank S4 molten Liquid heat exchanger H5 plate evaporation phase transformation device H9 mechanical vapor-compression pump M1 first order water as refrigerant cooler H6 second level water as refrigerant cooler H7 third level water as refrigerant cooler H8 generator FSQ condenser LNQ first absorbs XS1 the second absorber XS2 the first vaporizer ZF1 the second vaporizer ZF2 Intermediate solution heat exchanger H10 solution heat exchanger level circulating pump H11 low pressure cryogen water evaporimeter DZ low pressure Absorber DX
[detailed description of the invention]
Hereinafter, with accompanying drawing, this utility model is described further, embodiment and accompanying drawing in conjunction with the embodiments It is only used for illustrating rather than limiting protection domain of the present utility model.As it is shown in figure 1, the present embodiment Middle main device is as follows:
Steam mechanical compressor M1: can be centrifugal, roots-type, shuttle version is full The supercharging purposes of foot steam.
Interior coupling phase-change heat-exchanger: select board-like version, it is also possible to for shell-tube type.Including: structure Form, imports and exports and connects, and weak solution side Process flow is for rising film Forced Mixing pattern, and thermal source and low-temperature receiver are inverse Stream mode.Water as refrigerant is cooled in interior coupling phase-change heat-exchanger and water as refrigerant cooler being carried out continuously, and Cold side is carried out by two media segmentation, dodges and divides a tank vacuum, water as refrigerant chilling temperature automatically to lock control.
By FSQ generator, LNQ condenser, XS1 the first absorber, XS2 the second absorber, ZF1 Hydrothermal solution heat exchanger, H11 solution heat exchanger and circulating pump in the middle of first vaporizer, ZF2 the second vaporizer, H10 The twin-stage absorption type heat pump system of composition absorbs the energy in the low-temperature water heating of DX and absorbs the low temperature cold source of DZ And the method producing high-temperature-hot-water, including importing and exporting and connected mode.
Plate evaporation phase transformation device vaporizer therein uses plank frame form, including import, exports, cold The pump of side forced circulation configuration, circulating ratio automatically controls according to design.
First solution heat exchanger H1, cold side-entrance connects low-pressure absorber DX, cold side outlet port by pipeline Being connected to the cold side-entrance of coupling phase-change heat-exchanger H3 in the 3rd by pipeline, hot side-entrance is connected by pipeline First flash separation tank S1 bottom concentrated solution outlet, hot side outlet is via the first solution heat exchanger H5 and absorption Device XD import connects,
First board-like interior coupling phase-change heat-exchanger H1, cold side-entrance is molten with the second flash separation tank S2 bottom Liquid pipeline connects, and connecting line series solution circulating pump E2, cold side outlet port connects the first flash distillation by pipeline and divides From tank S1, the compressed vapour that hot side-entrance connects Mechanical Vapor Compression M1 by steam tank H0 exports.
Second board-like interior coupling phase-change heat-exchange H2, pipeline and the first flash separation tank S1 are passed through in hot side-entrance The outlet of top indirect steam connect, the hot side-entrance connection of hot side outlet and the first water as refrigerant cooler H6, Cold side-entrance is connected with the 3rd flash separation tank S3 bottom solution line, connecting line series solution circulating pump E3, cold side outlet port connects the second flash separation tank S2 by pipeline.
Coupling phase-change heat-exchanger H3 in three-plate type, pipeline and the second flash separation tank are passed through in hot side-entrance The top indirect steam outlet of S2 connects, and the hot side-entrance of hot side outlet and the second water as refrigerant cooler H7 is even Connecing, cold side-entrance is connected with the weak solution outlet conduit of solution heat exchanger H5, and cold side outlet port is connected by pipeline 3rd flash separation tank S3.
4th board-like interior coupling phase-change heat-exchanger H4, pipeline and the 3rd flash separation tank are passed through in hot side-entrance The top indirect steam outlet of S3 connects, and the hot side-entrance of hot side outlet and the 3rd water as refrigerant cooler H8 is even Connecing, cold side-entrance is with the hot side lower part steam condensate (SC) outlet conduit coupling phase-change heat-exchanger H1 in first even Connecing, connect in pipeline condensate water circulatory pump E1, and cold side outlet port connects the 4th flash separation tank S4 by pipeline.
4th flash separation tank S4 upper outlet is connected with the import of steam mechanical compressor M1, middle part Having two imports, the cold side outlet port of one and the 4th board-like interior coupling phase-change heat-exchanger H4 connects, another and plate The cold side outlet port of formula evaporative phase-change device H9 connects, lower part outlet and the cold side-entrance of plate evaporation phase transformation device H9 Pipeline is connected.
Mechanical vapor-compression pump M1, has inlet and outlet, its import and the vapour phase of flash separation tank S4 Outlet is connected by pipeline, and outlet is connected by pipeline with the hot side-entrance of steam tank.
Three the most corresponding respective board-like interior coupling phase inversion at different levels of water as refrigerant cooler (H6, H7, H8) Hot device (H2, H3, H4), hot side-entrance is connected by pipeline with the board-like interior hot side outlet of coupling phase-change heat-exchanger, Outlet is connected with the intake header road of low pressure evaporator DZ, cold side-entrance and the cooling water of low-pressure absorber DX Outlet connects, cold side outlet port and the generator FSQ of absorption heat pump, the low-temperature heat source import of vaporizer ZF1 Connect, generator FSQ, the low-temperature heat source water out of vaporizer ZF1 and the cooling water of low-pressure absorber DX Import connects.
Plate evaporation phase transformation device H9, cold side outlet port and the 4th flash separation tank S4 import are connected by pipeline, Cold side-entrance is connected by pipeline with the 4th flash separation tank S4 outlet, hot side outlet and import the second absorber Coupling into and out of pipeline of XS2 heat medium water.
Generator FSQ, top has agent steam outlet and weak solution refluxing opening, and bottom has concentrated solution Outlet, occurs.There is heat exchange coil, the import of heat exchange coil and the cooling of low-pressure absorber DX in FQS The outlet of water pipe connects, and the outlet of heat exchange coil is connected with the import of the cooling water pipe of low-pressure absorber DX,
Condenser LNQ, top has agent water vapour refluxing opening, and bottom has agent water out, condenser There is in LNQ the agent steam outlet at heat exchange coil, top agent water vapour refluxing opening and generator FSQ top Being connected by pipeline, agent water out in bottom is evaporated with the first vaporizer ZF1 and second respectively by circulating pump E9 The agent water sprayer tube link of device ZF2, heat exchange coil import/export chilled water with deferred vaporizer respectively goes out/import Connect,
First absorber XS1, top has agent water vapour import and intermediate concentration solution refluxing opening, bottom Having weak solution outlet, have heat exchange coil in the first absorber XS1, weak solution outlet in bottom is changed with solution The hot side-entrance of hot device H11 connects, the hot side outlet of solution heat exchanger E11 and generator FSQ top weak solution Refluxing opening is connected by pipeline, and the concentrated solution bottom the cold side-entrance of E11 and generator FSQ exports via circulation Pump E8 is connected by pipeline, and crown center strength solution import side outlet hot with solution heat exchanger H10 is connected, The going out of the heat exchange coil of heat exchange coil import/export and the second vaporizer ZF2/import is connected formation closed cycle, follows Circulating pump E11 it is in series with on endless tube road,
First vaporizer ZF1, top has agent water sprayer tube import mediating recipe steam outlet, the first evaporation Having heat exchange coil and shower in device ZF1, shower import is at the bottom of via circulating pump E9 and condenser LNQ Agent water out in portion's connects, and the import of heat exchange coil is connected with the outlet of the cooling water pipe of low-pressure absorber DX, The outlet of heat exchange coil is connected with the import of the cooling water pipe of low-pressure absorber DX, and the agent water vapour at top goes out Mouth is connected by pipeline with the agent water vapour refluxing opening at the first absorber XS1 top,
Second absorber XS2, top has agent water vapour import and the concentrated solution spray mouth of pipe, and bottom has Intermediate concentration taphole, has heat exchange coil and a shower in the second absorber XS2, shower import with The cold side outlet port of solution heat exchanger connects, the intermediate concentration taphole bottom absorber XS2 and solution heat exchange The hot side-entrance of device H10 connects, and the cold side-entrance of solution heat exchanger H10 goes out with the cold side of solution heat exchanger H11 Mouthful being connected by pipeline, heat exchange coil import/export goes out with the hot side of plate evaporation phase transformation device H9/and import is connected, Formed, on closed circuit loop, circulating pump will be installed,
Second vaporizer ZF2, top has agent water sprayer tube import mediating recipe steam outlet, the second evaporation Having heat exchange coil and shower in device ZF2, shower pipe import is via circulating pump E9 and condenser LNQ Connecting, the heat exchange coil import/export in the second vaporizer ZF2 goes out/import with the heat exchange coil in the first absorber Connect and compose closed circuit by pipeline, loop be in series with circulating pump E11, the agent steam outlet at top with The agent water vapour import mouth at the second absorber XS2 top connects.
Low-pressure absorber DX is for the absorption of water as refrigerant steam, and it also includes coolant outlet and import, Cooling water output point three tunnel configuration: (1) is respectively used to water as refrigerant cooler (H6, H7, H8) to cryogen Water cools down, and (2) are input to generator FSQ and the first vaporizer device of source pump as low-temperature heat source ZF1 drive train works, and (3) return low-pressure absorber as recirculated cooling water after going air cooling compressor cooling In the cooling water coil group of DX.
First, second, third flash separator (S1, S2, S3), has import, outlet, top Gaseous phase outlet is connected with the coupling hot side-entrance of phase-change heat-exchanger in rear stage by pipeline.Bottom liquid phases exports, Liquid-phase outlet is connected with the cold side-entrance of coupling phase-change heat-exchanger in previous stage by pipeline and pipeline force (forcing) pump, The import at middle part is then connected with the interior coupling phase-change heat-exchanger cold side outlet port of this grade by pipeline.
Driving energy in the present embodiment is mechanical power, therefore properly functioning consumed energy is only electric energy, and it is main It is: the secondary cycle steam of (1) low-order bit and supplementary steam are the mechanical vapor-compression done work by electric power Pump mechanical power is converted into the process of heat energy.(2) various circulating pump work process consume electric energy.
Level Four evaporation element is by board-like interior coupling phase-change heat-exchanger (H1, H2, H3, H4) and flash distillation Vapor-liquid separation tank (S1, S2, S3, S4) forms, and system work is in airtight vacuum state, for keeping vacuum Degree and maintain high heat exchanger efficiency system to be configured with vacuum pump group and its UNICOM, vacuum pump extraction on-condensible gas and Preset system vacuum state;Individual unit group has different vacuum level requirements respectively, thus often organize all have the most right The absolute pressure value answered ensures.
[principle and process description]
Lithium bromide weak solution concentration cycles process: heat source stream enters first after entering steam tank H0 The weak solution that cold side is entered by the hot side of board-like interior coupling phase-change heat-exchanger H1 heats, and weak solution absorbs and is subject to After heat, increasing enthalpy heats up to go out from the first cold side of board-like interior coupling phase-change heat-exchanger H1 in vapour-liquid mixed phase and then enters Flash separation tank S1, in S1, shwoot is separated into vehicle repair major, and vapour phase is that agent water vapour goes out S1 as rear stage Thermal source, and the steam advancing into the hot side of H1 be cooled to condensed water by the solution of cold side when going out H1, cold Solidifying water enters the cold side joint heat side of the 4th board-like interior coupling phase-change heat-exchanger H4 by condensate circulating pump E1 The heating of agent water vapour, be the simple agent water vapour thermal source as rear stage from the isolated steam of S1, The weak solution that cold side is entered by the hot side of the second board-like interior coupling phase-change heat-exchanger H2 entered heats, dilute The solution increasing enthalpy that is heated heats up to go out the cold side of H2 in vapour-liquid mixed phase and enter flash separation tank S2, and in S2, shwoot separates For vehicle repair major, vapour phase is that agent water vapour goes out the S2 thermal source as rear stage, and enters the agent water of the hot side of H2 Being cooled to agent water-setting by the solution of cold side when steam goes out H2 bear water, agent water will be by agent water cooler H6 quilt The recirculated cooling water from low-pressure absorber DX of cold side is inhaled into low pressure after indirectly cooling down under the effect of negative pressure In vaporizer DZ, same process is in the heat of the three, the 4th board-like interior coupling phase-change heat-exchangers (H3, H4) Agent water vapour in side is carried out to the path of agent water, go out the agent water of H3, H4 via agent water cooler (H7, H8) after Entering DZ, the agent water vapour going out S2 enters the hot side of rear stage three-plate type interior coupling phase-change heat-exchanger H3 to cold The weak solution that side enters heats, and the weak solution increasing enthalpy that is heated heats up to go out the cold side of H3 in vapour-liquid mixed phase and enter and dodge Steaming knockout drum S3, in S3, shwoot is separated into vehicle repair major, and vapour phase is that agent water vapour goes out S3 and enters rear stage the The condensed water that cold side is entered by the hot side of four board-like interior coupling phase-change heat-exchanger H4 heats, and condensed water is heated Increasing enthalpy intensification and go out entrance flash separation tank S4 in H4 cold side in vapour-liquid mixed phase, in S4, shwoot is separated into vapour-liquid two Phase, vapour phase is that regeneration steam goes out S4 entrance steam mechanical compressor M1, after the regeneration steam in M1 is compressed Temperature, pressure and heat content are all improved and meet the MI to be obtained of heat source stream parameter and return to steam Tank H0,
Lithium bromide weak solution (60%) goes out low-pressure absorber DX and exports via circulating pump E7, via solution The cold side of heat exchanger H5 couples phase-change heat-exchange with via in entering three-plate type after the high temperature concentrated solution heat exchange of hot side The isolated liquid phase of S3 (61.33%) is entered from S3 after the heating of the cold side joint heat side agent water vapour of device H3 Bottom goes out the cold side joint heat side steam entering the second board-like interior coupling phase-change heat-exchanger H2 via circulating pump E3 Heating after enter the isolated liquid phase of S2 (62.67%) go out bottom S2 via circulating pump E2 enter first The isolated liquid phase of S1 is entered after the heating of the cold side joint heat side steam of board-like interior coupling phase-change heat-exchanger H1 (64%) be the concentrated solution of end of a period concentration go out bottom S1 via solution heat exchanger H5 cold side is entered dilute molten Liquid goes out H5 and enters low-pressure absorber DX after carrying out heat exchange,
The agent water of entrance low pressure evaporator DZ extremely low absolute draft evaporating temperature in device is 5 DEG C, wink Between vaporize, during vaporization, in absorber, the circulating refrigerant hydro-thermal amount in heat exchange coil causes the chilled water output temperature to be 7 DEG C, during return, chilled water temperature is 12, DEG C low pressure evaporator DZ generate agent water vapour by with low pressure Absorber DX connecting line enters low-pressure absorber DX, and agent water vapour is entered in device in low-pressure absorber DX Dense lithium-bromide solution absorbed, also become liquid phase from vapour phase at this process agent water vapour and discharge condensation simultaneously Heat, the heat of condensation taken out of by the cooling circulating water in the coil exchanger in DX device,
[process description]
1, initial start-up needs the raw steam outside input, gives birth to steam and from the first order to fourth stage flash distillation The indirect steam flow process that knockout drum generates is as follows: it is board-like interior that outside raw steam enters steam tank H0-the first Coupling phase-change heat-exchanger H1-flash separator S1 (generation indirect steam) the-second board-like interior coupling phase inversion Coupling phase-change heat-exchanger H3-flash separation tank S3-the in hot device H2-flash separator S2-the three-plate type Four board-like interior coupling phase-change heat-exchanger H4-flash separation tank S4-Mechanical Vapor Compression M1-steam Tank H0.
2, enter normality to run: regeneration steam substitutes outside raw steam, steam flow: mechanical vapour pressure The board-like interior coupling phase-change heat-exchanger H1-flash separator S1 of contracting machine M1-steam tank H0-the first is (raw Become indirect steam) coupling in-second board-like interior coupling phase-change heat-exchanger H2-flash separator S2-the three-plate type Close the board-like interior coupling phase-change heat-exchanger H4-flash separation of phase-change heat-exchanger H3-flash separation tank S3-the 4th Tank S4-Mechanical Vapor Compression M1
3, weak solution concentration flow path: coupling in low-pressure absorber DX-solution heat exchanger H5-the three-plate type Close the board-like interior coupling phase-change heat-exchanger H2-flash separation of phase-change heat-exchanger H3-flash separator S3-the second The board-like interior coupling phase-change heat-exchanger H1-flash separator S1-solution heat exchanger H5-low pressure of device S2-the first Absorber DX.
4, water as refrigerant flow process: weak solution is separated into water as refrigerant at flash separator (S1~S3) shwoot and steams Gas-enter board-like interior coupling phase-change heat-exchanger (H2~H4)-water as refrigerant cooler (H6~H8)-low pressure Vaporizer DZ.
5, also need the heat energy steam of 4% to supplement when properly functioning according to heat Balance Calculation, supplement heat energy Generation process and method are as follows: by generator FSQ, solidifying cooler LNQ, the first absorber XS1, the first steaming Send out device ZF1, the second absorber XS2, the second vaporizer ZF2, solution heat exchanger H10, solution heat exchanger H11, circulating pump (E8, E9, E11) composition Equations of The Second Kind bipolar lithium bromide absorption type heat pump system, unit leads to Cross the low temperature heat energy absorbing the cooling circulating water discharge from refrigeration system as driving energy through this heat pump machine The operation of group is made steam again and is added to the regeneration steam pipeline of refrigeration system.This example source pump drives Heat source water be from refrigeration system discharge heat its mean temperature of recirculated cooling water 36.7 DEG C, heat source water respectively with 1:1.25 ratio enters the internal heat coil pipe of generator FSQ and the first vaporizer ZF1 and has gone heat exchange, Go out generator FSQ and the first vaporizer ZF1 the most respectively by the cooling water backwater with low-pressure absorber DX Pipeline connects and returns.The temperature of the low-temperature receiver water turnover needed for solidifying cooler LNQ is 7 DEG C and 12 DEG C, and low-temperature receiver water comes From the chilled water outlet pipeline of low pressure evaporator DZ, after completing heat exchange in solidifying cooler LNQ, return low pressure Vaporizer DZ.In this example, the lithium-bromide solution initial concentration in generator FSQ is X=0.5, in device definitely Under the conditions of pressure 2.3Kpa, 36.7 DEG C of hot water in heated coil pipe heat indirectly, and now the agent water in solution is steamed Sending out and go out the solidifying cooler LNQ of generator FSQ entrance for agent water vapour, solution concentration also rises the dense of most X=0.54 Solution, temperature rises most 49 DEG C, and concentrated solution goes out generator FSQ via circulating pump E8 approach solution heat exchanger (H10, H11) inputs the second absorber XS2.Enter the agent water vapour of solidifying cooler LNQ in absolute pressure 2.3Kpa Device in indirectly cooled down by the cooling water in heat exchange coil and to be condensed into agent water, agent water goes out device and divides via circulating pump E9 Not inputting the first vaporizer ZF1 and the second vaporizer ZF2, in agent water entrance device, absolute pressure is 12Kpa's First vaporizer ZF1, agent water absorbs 36.7 DEG C of heat source waters in heat exchange coil by indirect heat exchange in ZF1 Energy after instant vaporization generate agent water vapour, then agent water vapour enter identical absolute pressure the first absorber XS1 is absorbed by the solution of intermediate concentration X=0.52 in device, and in the first absorber XS1, the end of a period of solution is dense Degree is X=0.5, and solution temperature is 75 DEG C, and the latent heat that agent water recovery is released is by the first absorber XS1 Heat exchange coil in recirculated water take out of, recirculated water output time temperature 70 C enter changing of the second vaporizer ZF2 After hot coil heats the agent water in the second vaporizer ZF2, warp is returned by circulating pump E11, the second vaporizer ZF2 Absolute pressure 31Kpa in device, after agent water enters, vapourizing temperature is 70 DEG C, absorbs in heat exchange coil and follow during vaporization Ring hot water heat energy, agent water vapour go out second vaporizer ZF2 enter uniform pressure the second absorber XS2, The while that in XS2, the concentrated solution of concentration X=0.54 that agent water vapour is entered in device absorbing, solution is diluted, device Interior solution end of a period concentration X=0.52, temperature 103 DEG C, the heat of condensation that the condensation of agent water vapour discharges is by heat exchange dish Pipe heated the recirculated water in pipe, makes circulating water temperature be increased to 100 degree and inputs board-like evaporative phase-change device H9's Hot side is gone to heat the condensed water that H9 opposite side enters, and after condensed water heat exchange, temperature rises to 95 degree and enters the 4th sudden strain of a muscle Steaming knockout drum S4 shwoot is regeneration steam, and the concentration in the second absorber XS2 now is X=0.52's Intermediate solution is via entering the first absorber XS1 after solution heat exchanger H10, and in XS1, solution absorbent water steams The weak solution being diluted to concentration X=0.5 after vapour enters generator FSQ via solution heat exchanger H11.Owing to mending Fill the used heat for system discharge that the second-kind absorption-type heat pump of energy consumed therefore this portion of energy is not counted in reality Border energy consumption, this increase simultaneously can reduce again the discharge of thermal pollution further.
6, the regeneration steam recycled and supplementary steam (are now its pressure and temperature of low-order bit steam Relatively low and tool is less than the parameter of heat source stream) it is incorporated to the 4th flash separation tank S4 and is inhaled into steam mechanical compression Pump M1, low order steam compressed output intermittent fever break is raised, and supercharging, heats and reach technological design Parameter, to steam tank H0 and the first order, couple phase-change heat-exchanger H1 via airtight pipeline output, Enter the hot side of H1 to be heated to the lithium bromide weak solution of cold side setting evaporating temperature entrance first order flash distillation Separator S1, the separation of vapour-liquid moment, the water as refrigerant steam occupying tank top couples via in the pipeline entrance second level The hot side of phase-change heat-exchanger H2, heats, to weak solution temperature the weak solution of another cold side in device as thermal source It is increased to evaporating temperature, enters the process one of flash separation tank S1 with coupling phase-change heat-exchanger H1 in the first order Sample.Water as refrigerant condenses water by the road in the hot side of the second board-like coupling phase-change heat-exchanger H2 through lowering the temperature, becoming mutually Output after to water as refrigerant cooler H6, cooling water brief introduction through opposite side is cooled to design temperature again water as refrigerant enter Enter low pressure evaporator DZ.The third level, the fourth stage (regeneration steam level) weak solution heating evaporation and separation etc. are all As constituting with the front second level.The vacuum of every one-level is different, absolute pressure from high to low, the existing first order > The second level > third level > fourth stage, corresponding evaporating temperature is also arranged in order.
Weak solution couples phase-change heat-exchanger H3, enters and dodge in out being entered the third level by solution heat exchanger H5 The solution dividing tank S3 removing portion of water couples phase inversion in entering the second level further along via solution circulation pump A hot device H2 and sudden strain of a muscle point tank S2, the first order interior coupling phase-change heat-exchanger H1 and sudden strain of a muscle divide a tank S1, perform identical Step.
At condensate water circulatory pump E1 after in the first order, the condensed water of the coupling hot side of phase-change heat-exchanger H1 goes out device Promote and lower enter the cold side of coupling phase-change heat-exchanger H4 in the fourth stage, enter a 4th sudden strain of a muscle point tank after accumulation of energy of being heated The steam that S4 and plate evaporation phase transformation device H9 enters merges generation regeneration steam, enters and steam after going out to dodge point device S4 Vapour mechanical compressor M1.
Steam mechanical compressor M1 heats process by the sensor-based system configured, control system pair in supercharging Automatically carry out the operating procedures such as moisturizing, speed governing, pressure regulation after each parameter comparison, process, and then ensure output The saturation of regeneration steam, temperature, pressure, flow etc. are constant.
It is lost in normal course of operation Theoretical Calculation and actual motion and is both needed in time system be carried out a small amount of heat Can supplement, dynamic quantity processes collecting Centralized Controller after the data acquisition unit by individual point, by adjusting The parameter of Equations of The Second Kind absorption lithium bromide heat pump is to meet normal operation needs.
Low pressure evaporator DZ, low-pressure absorber DX use traditional contemporary devices, retain it original Control system, vacuum system, weak solution Sprayer Circulation system, water as refrigerant Sprayer Circulation system, therefore briefly chat State.Weak solution multistage evaporation concentration systems is configured with vacuum equipment, meets system vacuum duty, vacuum Degree, fixed gas extract, system intialization vacuum.
Weak solution flow to and heat source stream flow in adverse current, in interior coupling phase-change heat-exchanger also in adverse current to.
In adverse current to.

Claims (4)

1. a superposition heat pump and the absorption cooling-water machine of kind of refrigeration cycle, it is characterised in that including:
First solution heat exchanger, cold side-entrance connects low-pressure absorber by pipeline, cold side outlet port is connected to the cold side-entrance of coupling phase-change heat-exchanger in the 3rd by pipeline, hot side-entrance connects the first flash separation tank bottom concentrated solution by pipeline and exports, hot side outlet is connected via with low-pressure absorber import
First board-like interior coupling phase-change heat-exchanger, cold side-entrance is connected with the second flash separation tank bottom solution line, connecting line series solution circulating pump, and cold side outlet port connects the first flash separation tank by pipeline, the compressed vapour that hot side-entrance connects Mechanical Vapor Compression by steam tank exports
Second board-like interior coupling phase-change heat-exchanger, hot side-entrance is connected by the top indirect steam outlet of pipeline and the first flash separation tank, the hot side-entrance of hot side outlet and the first water as refrigerant cooler connects, cold side-entrance is connected with the 3rd flash separation tank bottom solution line, connecting line series solution circulating pump, cold side outlet port connects the second flash separation tank by pipeline
Coupling phase-change heat-exchanger in three-plate type, hot side-entrance is connected by the top indirect steam outlet of pipeline and the second flash separation tank, the hot side-entrance of hot side outlet and the second water as refrigerant cooler connects, cold side-entrance is connected with the weak solution outlet conduit of the first solution heat exchanger, cold side outlet port connects the 3rd flash separation tank by pipeline
4th board-like interior coupling phase-change heat-exchanger, hot side-entrance is connected by the top indirect steam outlet of pipeline and the 3rd flash separation tank, the hot side-entrance of hot side outlet and the 3rd water as refrigerant cooler connects, cold side-entrance is connected with the hot side lower part steam condensate (SC) outlet conduit of coupling phase-change heat-exchanger in first, series connection condensate water circulatory pump in pipeline, cold side outlet port connects the 4th flash separation tank by pipeline
4th flash separation tank upper outlet is connected with the import of steam mechanical compressor, and there are two imports at middle part,
The cold side outlet port of one and the 4th board-like interior coupling phase-change heat-exchanger connects, and another is connected with the cold side outlet port of plate evaporation phase transformation device, and the cold side-entrance pipeline of lower part outlet and plate evaporation phase transformation device is connected,
Mechanical vapor-compression pump, has inlet and outlet, and its import is connected by pipeline with the vapor phase exit of the 4th flash separator, and outlet is connected by pipeline with the hot side-entrance of steam tank,
Three the most corresponding respective board-like interior coupling phase-change heat-exchangers at different levels of water as refrigerant cooler, hot side-entrance is connected by pipeline with the board-like interior hot side outlet of coupling phase-change heat-exchanger, outlet is connected with the import of low pressure evaporator, cold side-entrance is connected with the coolant outlet of low-pressure absorber, cold side outlet port is connected with the outlet conduit of the cooling water pipe of low-pressure absorber
Plate evaporation phase transformation device, cold side outlet port and the 4th flash separation tank import are connected by pipeline, and cold side-entrance is connected by pipeline with the 4th flash separation tank outlet, and hot side outlet and import absorption heat pump connect.
2. superposition heat pump as claimed in claim 1 and the absorption cooling-water machine of kind of refrigeration cycle, it is characterised in that described absorption heat pump includes:
Generator, top has outlet and refluxing opening, and bottom has outlet, has heat exchanger tube in generator, and the import of heat exchanger tube is connected with the outlet conduit of the cooling water pipe of low-pressure absorber, and the outlet of heat exchanger tube is connected with the import of the cooling water pipe of low-pressure absorber,
Condenser, top has refluxing opening, and bottom has outlet, has heat exchanger tube in condenser, and overhead reflux mouth is connected by pipeline with the outlet at generator top,
First absorber, top has import and refluxing opening, bottom has outlet, in first absorber, there is heat exchanger tube, outlet at bottom is connected with the hot side-entrance of solution heat exchanger level circulating pump, and hot side outlet is connected by pipeline with generator overhead reflux mouth, and cold side-entrance is connected by pipeline with the outlet bottom generator, top inlet is connected with middle hydrothermal solution heat exchanger cold side outlet port
First vaporizer, top has inlet and outlet, there is in first vaporizer heat exchanger tube and shower, shower is connected with import in the first vaporizer, the import of heat exchanger tube is connected with the outlet of the cooling water pipe of low-pressure absorber, and the outlet of heat exchanger tube is connected with the import of the cooling water pipe of low-pressure absorber, and import is connected by pipeline with the outlet bottom condenser, the outlet at top is connected by pipeline with the refluxing opening of the first absorber overhead
Second absorber, top has import and refluxing opening, bottom has outlet, there is in second absorber heat exchanger tube and shower, shower is connected with its import in the second absorber, the outlet of the second absorber bottom is connected with the middle cold side-entrance of hydrothermal solution heat exchanger, the import of the second absorber overhead is connected by pipeline with the cold side outlet port of middle hydrothermal solution heat exchanger, the middle cold side-entrance of hydrothermal solution heat exchanger is connected by pipeline with the cold side outlet port of solution heat exchanger level circulating pump, the inlet and outlet of heat exchanger tube hot side with plate evaporation phase transformation device respectively is entered, outlet is connected by pipeline,
Second vaporizer, top has inlet and outlet, there is in second vaporizer heat exchanger tube and shower, shower is connected with import in the second vaporizer, heat exchanger tube in second vaporizer and the heat exchanger tube in the first absorber connect and compose closed circuit by pipeline, the import at top is connected by pipeline with the outlet bottom condenser, and the outlet at top stays mouth to be connected with the meeting of the second absorber overhead.
3. superposition heat pump as claimed in claim 1 and the absorption cooling-water machine of kind of refrigeration cycle, it is characterised in that the board-like interior coupling phase-change heat-exchanger of described first, second, third and fourth is plate type heat exchanger, plate-type evaporator, plate-type condenser, shell-and-tube heat exchanger.
4. superposition heat pump as claimed in claim 1 and the absorption cooling-water machine of kind of refrigeration cycle, it is characterized in that first, second, and third described water as refrigerant cooler is plank frame, the water as refrigerant chilling temperature needed for the board-like interior coupling phase-change heat-exchanger of corresponding each position realizes controlling by the automatic control components and parts configured.
CN201620015304.XU 2016-01-08 2016-01-08 Stack heat pump and refrigeration cycle's absorption formula cold water machine Expired - Fee Related CN205536654U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201620015304.XU CN205536654U (en) 2016-01-08 2016-01-08 Stack heat pump and refrigeration cycle's absorption formula cold water machine

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201620015304.XU CN205536654U (en) 2016-01-08 2016-01-08 Stack heat pump and refrigeration cycle's absorption formula cold water machine

Publications (1)

Publication Number Publication Date
CN205536654U true CN205536654U (en) 2016-08-31

Family

ID=56763502

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201620015304.XU Expired - Fee Related CN205536654U (en) 2016-01-08 2016-01-08 Stack heat pump and refrigeration cycle's absorption formula cold water machine

Country Status (1)

Country Link
CN (1) CN205536654U (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113074403A (en) * 2021-04-28 2021-07-06 郑晓昱 Heating system based on absorption heat pump

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113074403A (en) * 2021-04-28 2021-07-06 郑晓昱 Heating system based on absorption heat pump

Similar Documents

Publication Publication Date Title
CN104964477B (en) A kind of multistage plate evaporation absorption type refrigerating unit and method
CN106895603B (en) Compression/absorption enclosed parallel connection composite fuel gas heat pump system operation method
CN102797524B (en) Medium-and-low-temperature waste-heat utilization cooling/power combination system
CN106369866A (en) Waste steam directly absorbed type double-effect lithium bromide heat pump system and working method thereof
CN103090593B (en) Heat pump circulating system and heat pump cycle method and vapo(u)rization system
CN104633981B (en) A kind of based on photovoltaic and photothermal and electrodialytic lithium bromide-water absorption refrigerating plant
CN107091542A (en) A kind of coupling circulation system and control method for solar energy thermal-power-generating
CN100390476C (en) Work-cold joint supplied cross still state straight and reverse coupling heating power circulation system and method
CN206352906U (en) A kind of exhaust steam direct-absorption type lithium bromide heat pump system
CN105066502B (en) A kind of direct-fired absorption refrigeration method and device for reclaiming the heat of transformation
CN1641292A (en) Absorption refrigerator
CN110469835A (en) Thermoelectricity decoupled system and operation method based on absorption heat pump and thermal storage equipment
CN204902309U (en) Multistage plate type evaporation absorbed refrigeration device
CN109350983A (en) A kind of two-stage compression heat pump double-effect evaporation concentration systems
CN205536654U (en) Stack heat pump and refrigeration cycle's absorption formula cold water machine
CN105650938B (en) A kind of absorption-type refrigerating method and device of full electric power reuse discharge heat
CN105485960B (en) A kind of dual vapor compressibility absorption-type refrigerating method and device
CN206056011U (en) High temperature heat pump system
CN206113419U (en) Absorption heat pump and generator thereof
CN101093118A (en) Single stage composite absorption type compressor
CN208108536U (en) A kind of low temperature exhaust heat reclaiming type lithium bromide absorption cold and hot water system
CN205300024U (en) Lithium bromide vapor compression formula air conditioner
CN106196726B (en) High temperature heat pump system and its round-robin method
CN205079495U (en) Retrieve direct combustion formula absorption refrigeration device of heat of transformation
CN202648240U (en) Parallel, steam type, dual-effect and lithium bromide-absorbing refrigeration optimization system

Legal Events

Date Code Title Description
GR01 Patent grant
C14 Grant of patent or utility model
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20160831

Termination date: 20170108

CF01 Termination of patent right due to non-payment of annual fee