CN116222020B - Phase change cold accumulation system based on transcritical carbon dioxide absorption refrigeration cycle - Google Patents
Phase change cold accumulation system based on transcritical carbon dioxide absorption refrigeration cycle Download PDFInfo
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 310
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 155
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 153
- 238000005057 refrigeration Methods 0.000 title claims abstract description 110
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 85
- 238000009825 accumulation Methods 0.000 title claims abstract description 46
- 230000008859 change Effects 0.000 title claims description 30
- 239000000243 solution Substances 0.000 claims description 91
- 239000006096 absorbing agent Substances 0.000 claims description 39
- 239000003507 refrigerant Substances 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 238000005338 heat storage Methods 0.000 claims description 26
- 239000012530 fluid Substances 0.000 claims description 20
- 239000012782 phase change material Substances 0.000 claims description 16
- 239000000498 cooling water Substances 0.000 claims description 15
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 claims description 10
- 239000011259 mixed solution Substances 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 4
- 230000005514 two-phase flow Effects 0.000 claims description 3
- 239000011810 insulating material Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 21
- 230000007613 environmental effect Effects 0.000 abstract description 9
- 230000009467 reduction Effects 0.000 abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 238000004134 energy conservation Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 53
- 238000001816 cooling Methods 0.000 description 15
- 239000002608 ionic liquid Substances 0.000 description 8
- 230000006872 improvement Effects 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- IPLONMMJNGTUAI-UHFFFAOYSA-M lithium;bromide;hydrate Chemical compound [Li+].O.[Br-] IPLONMMJNGTUAI-UHFFFAOYSA-M 0.000 description 5
- 238000011161 development Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 4
- 231100000956 nontoxicity Toxicity 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000005855 radiation Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 230000006378 damage Effects 0.000 description 3
- 238000004781 supercooling Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- IQQRAVYLUAZUGX-UHFFFAOYSA-N 1-butyl-3-methylimidazolium Chemical compound CCCCN1C=C[N+](C)=C1 IQQRAVYLUAZUGX-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 240000005373 Panax quinquefolius Species 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005482 strain hardening Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/002—Machines, plants or systems, using particular sources of energy using solar energy
- F25B27/007—Machines, plants or systems, using particular sources of energy using solar energy in sorption type systems
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24S—SOLAR HEAT COLLECTORS; SOLAR HEAT SYSTEMS
- F24S10/00—Solar heat collectors using working fluids
- F24S10/30—Solar heat collectors using working fluids with means for exchanging heat between two or more working fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24S—SOLAR HEAT COLLECTORS; SOLAR HEAT SYSTEMS
- F24S60/00—Arrangements for storing heat collected by solar heat collectors
- F24S60/10—Arrangements for storing heat collected by solar heat collectors using latent heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B40/00—Subcoolers, desuperheaters or superheaters
- F25B40/06—Superheaters
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention relates to a phase-change cold accumulation system based on transcritical carbon dioxide absorption refrigeration cycle, which comprises a solar heat collection system, an absorption refrigeration cycle system and a phase-change cold accumulation and discharge system; the solar heat collection system is connected with the absorption refrigeration cycle system and is used for providing solar energy for the absorption refrigeration cycle system, and the absorption refrigeration cycle system is connected with the phase-change cold accumulation and release system and is used for providing refrigeration for the phase-change cold accumulation and release system. The invention effectively combines the green carbon dioxide refrigeration technology with other energy-saving technologies, namely solar heat supply technology, through the generator. When solar natural resources are rich in daytime, the transcritical carbon dioxide absorption refrigeration system fully utilizes heat energy provided by the transcritical carbon dioxide absorption refrigeration system to generate cold and supply cold continuously and stably, so that the high-efficiency utilization of renewable energy sources is realized, the advantages of environmental friendliness, sustainability and the like are realized, and the transcritical carbon dioxide absorption refrigeration system has important significance for energy conservation and carbon reduction.
Description
Technical Field
The invention relates to the technical field of refrigeration and cold accumulation, in particular to a phase change cold accumulation system based on transcritical carbon dioxide absorption refrigeration cycle.
Background
Nowadays, along with continuous exhaustion of traditional fossil energy, a lot of environmental pollution, ecological destruction and other problems are brought at the same time, and realizing sustainable development of energy and solving environmental problems are now urgent problems to be solved. The solar energy is taken as renewable energy, has the advantages of cleanness, economy, safety and the like, promotes the development and diversified utilization of solar energy resources, and can be beneficial to relieving the energy shortage and environmental problems.
Compared with the existing refrigerants, the defects of ozone layer damage, high global warming potential and the like are harmful to the environment, and the traditional carbon dioxide refrigerant can well solve the environmental problem caused by the use of the refrigerant. The carbon dioxide has the advantages of no color, no smell, no toxicity, stable chemical property, low safety, easy realization of critical state, and the like, is an environment-friendly natural working medium, and therefore, the green carbon dioxide refrigeration technology has wide applicationDevelopment of application prospect. The absorption refrigeration is widely focused by utilizing the characteristic that a low-grade heat source can be utilized without a compressor to do work for circulation driving, is a common refrigeration technology, and has a better application prospect in refrigeration occasions with lack of electric energy. The traditional absorption refrigeration cycle mostly adopts lithium bromide-water and ammonia-water as working medium pairs, and the two working medium pairs have some defects, wherein a lithium bromide-water solution has strong corrosiveness, has high tightness to a system, ammonia has explosiveness and toxicity, and transcritical carbon dioxide and ionic liquid [ bmim ]]PF 6 The working substance pair has the advantages of no toxicity, good thermal stability, environmental friendliness and the like.
The phase change cold accumulation technology can break the time limit to realize the economic operation of the refrigerating system, can realize the high-efficiency utilization of energy, accords with the development trend of the future international society, and has considerable application prospect. The sodium sulfate decahydrate serving as an inorganic phase change material has the advantages of high energy storage density, low price, easy phase change temperature adjustment and the like, and is widely applied to the cold storage field.
At present, applications of supercritical carbon dioxide as working media are concentrated in the field of power generation, for example, yang Sheng et al (patent name: coupled lithium bromide absorption refrigeration transcritical carbon dioxide cycle waste heat power generation system; application number: 201910829358.8) propose that a refrigeration system is coupled with a carbon dioxide cycle power generation system, and gradient utilization waste heat is adopted as a heat source, and the patent not only considers the problem of medium-low temperature waste heat utilization, but also provides a new thought for a power generation mode. Shen Jiang et al propose a thermally driven pump-less absorption-assisted subcooled transcritical CO2 refrigeration system (application number: 201811568330.5) that couples an absorption refrigeration cycle with lithium bromide-water as a working substance pair to a transcritical carbon dioxide refrigeration cycle through a heat exchanger and a generator to solve the problem of heat utilization of compressor discharge from the heat recovery level, but does not consider sustainable development and multiple utilization of energy from the energy saving technology level.
The patent with the name of solar energy driven refrigerator and carbon dioxide heat pump (application number: 201110072622.1) proposes a system combining a refrigerator driven by solar energy and a heat pump with carbon dioxide as a medium, which can switch different operation modes, wherein in the refrigeration mode, the lithium bromide refrigerator and the carbon dioxide heat pump are mainly adopted for refrigeration, a conventional heat pump system is adopted, the work of a compressor is not separated from the heat pump to provide power for circulation, and the system has certain dependence on electric energy. The patent considers the special working state of the carbon dioxide working medium in the heat pump system and designs the carbon dioxide working medium, but the adopted absorption refrigerator still takes the traditional lithium bromide-water solution as the working medium pair, and does not carry out related design for carbon dioxide absorption refrigeration. In the period of poor solar radiation such as night or cloudy days, when the heat collected by solar energy can not meet the requirements of a refrigerator, refrigeration can only be independently born by a carbon dioxide heat pump, and the refrigerator has certain dependence on primary energy.
The invention discloses a solar energy absorption injection composite transcritical CO2 refrigerating system (application number: 202010069090.5), which is mainly used for optimizing and designing the working efficiency of a transcritical carbon dioxide working medium in a heat pump system, and introduces a solar energy absorption injection supercooling cycle (namely an absorption refrigerating cycle taking lithium bromide-water or ammonia-water solution as a working medium pair), wherein the cycle reduces irreversible throttling loss by continuously cooling carbon dioxide twice in steps, improves the overall energy efficiency of the system, but does not consider the operation and energy efficiency problems of the transcritical carbon dioxide working medium from the aspect of the absorption refrigerating system.
At present, the global energy crisis and the environmental problem are prominent, and if the green carbon dioxide refrigeration technology can be effectively combined with other energy-saving technologies for use, the method has important significance in the aspects of energy conservation and carbon reduction. At present, no design is available for effectively and reasonably combining a transcritical carbon dioxide absorption refrigeration cycle technology with other energy-saving technologies and a phase-change cold accumulation and release technology and being used in the field of refrigeration and cold accumulation.
Disclosure of Invention
The invention mainly solves the technical problems of providing a phase change cold accumulation system based on transcritical carbon dioxide absorption refrigeration cycle, which combines transcritical carbon dioxide refrigeration technology, solar heat supply technology and phase change cold accumulation cold discharge technology, and the system supplies cold and stores cold when solar energy is sufficient in daytime, and the stored cold quantity can be cooled and supplied at night, thereby breaking the time and space limitation of cold utilization, realizing the high-efficiency utilization of energy, having the advantages of environmental friendliness, sustainability, compact structure and the like, having important significance for energy conservation and carbon reduction and having wide application prospect.
The technical scheme of the invention is as follows: the phase change cold accumulation system based on the transcritical carbon dioxide absorption refrigeration cycle comprises a solar heat collection system, an absorption refrigeration cycle system and a phase change cold accumulation cold release system;
the solar heat collection system is connected with the absorption refrigeration cycle system and is used for providing solar energy for the absorption refrigeration cycle system, and the absorption refrigeration cycle system is connected with the phase-change cold accumulation and release system and is used for providing refrigeration for the phase-change cold accumulation and release system.
As an improvement, the solar heat collection system comprises a solar heat collector, a first circulating pump and a heat storage tank; the outlet of the first circulating pump is communicated with the inlet of the solar heat collector, and the outlet of the solar heat collector is communicated with the inlet of the heat storage tank.
As an improvement, the absorption refrigeration cycle system comprises a generator, an absorber, a solution heat exchanger, a solution pump, a first throttle valve, a gas cooler, a regenerator, a second throttle valve and a heat exchanger; the first outlet of the generator is communicated with the inlet of the heat storage tank, the second circulating pump is communicated with the first inlet of the generator, the second outlet of the generator is communicated with the first inlet of the gas cooler, the first outlet of the gas cooler is communicated with the first inlet of the heat regenerator, the first outlet of the heat regenerator is communicated with the inlet of the second throttle valve, the outlet of the second throttle valve is communicated with the first inlet of the heat exchanger, the first outlet of the heat exchanger is communicated with the second inlet of the heat regenerator, the second outlet of the heat regenerator is communicated with the first inlet of the absorber, the first outlet of the absorber is communicated with the inlet of the solution pump, the outlet of the solution pump is communicated with the first inlet of the solution heat exchanger, the first outlet of the solution heat exchanger is communicated with the second inlet of the generator, the third outlet of the generator is communicated with the inlet of the solution heat exchanger, the second outlet of the solution heat exchanger is communicated with the inlet of the first throttle valve, and the outlet of the first throttle valve is communicated with the second inlet of the absorber.
As an improvement, the phase-change cold accumulation and release system comprises a heat exchanger and a water-gas heat exchanger; an inlet and an outlet are arranged on the heat exchanger, and an inlet, an outlet, a third inflow pipeline and a third outflow pipeline are arranged on the water-gas heat exchanger; the inlet and the outlet on the heat exchanger are respectively connected with the outlet and the inlet of the water-gas heat exchanger.
As an improvement, the carbon dioxide of the refrigerant in the absorption refrigeration cycle system is in a transcritical state, wherein the transcritical state refers to that when the pressure of the refrigerant separated out from the generator is higher than the critical pressure of the carbon dioxide, then high-temperature high-pressure supercritical carbon dioxide flows into the gas cooler to release heat, the temperature of the supercritical carbon dioxide fluid is slightly higher than the ambient temperature, then the temperature of the carbon dioxide fluid is reduced after heat exchange with low-temperature low-pressure carbon dioxide vapor in the regenerator, then the carbon dioxide fluid enters the second throttling valve to be throttled and then becomes a low-temperature low-pressure gas-liquid two-phase flow, finally heat is absorbed in the heat exchanger to store heat, and the carbon dioxide of the refrigerant is in the transcritical state in the whole cycle.
According to the solar heat collection system, working medium heat conduction oil in the solar heat collection system flows out of an outlet of a heat storage tank, enters the solar heat collector through the first circulating pump, after heat is obtained in the solar heat collector, the high-temperature heat conduction oil flows from the outlet of the solar heat collector to the heat storage tank to form a circulating loop, the high-temperature heat conduction oil flows to the generator through a first inlet of the generator through the second circulating pump, and after being heated in the generator, returns to the heat storage tank through the first outlet of the generator to form circulation.
As an improvement, the refrigerant carbon dioxide in the absorption refrigeration cycle system is separated out from the concentrated solution in the generator after being heated by the high-temperature heat conduction oil in the generator, the concentrated solution in the generator is changed into a dilute solution after being heated, the separated high-temperature high-pressure carbon dioxide flows to the gas cooler from the second outlet of the generator, the pressure of the high-temperature high-pressure carbon dioxide refrigerant is higher than the critical pressure of the carbon dioxide, the high-temperature high-pressure supercritical carbon dioxide is changed into high-pressure room-temperature supercritical carbon dioxide after being heat exchanged with the outdoor normal-temperature cooling water in the gas cooler, the temperature of the high-pressure room-temperature supercritical carbon dioxide is slightly higher than the ambient temperature after being heat exchanged with the outdoor normal-temperature cooling water, the high-pressure room-temperature supercritical carbon dioxide refrigerant enters the regenerator, the low-temperature low-pressure carbon dioxide vapor flowing out of the heat exchanger and entering the heat regenerator exchanges heat in the heat regenerator, flows out of the heat regenerator to the second throttle valve, enters the heat exchanger after being throttled in the second throttle valve, flows into the heat regenerator after absorbing heat and evaporating in the heat exchanger, flows into the heat regenerator after being heated in the heat regenerator, flows into the absorber after being mixed with the dilute solution flowing out of the second outlet of the solution heat exchanger and entering the absorber through the first throttle valve, becomes a low-pressure concentrated solution, the low-pressure concentrated solution in the absorber flows into the solution pump through the first outlet of the absorber, heat generated by reaction in the absorber is taken away by outdoor normal-temperature cooling water, the mixed low-pressure concentrated solution flows into the solution heat exchanger from the solution pump, and after heat exchange is carried out on the solution heat exchanger and the dilute solution flowing out from the generator and flowing into the solution heat exchanger, the dilute solution flows out from the first outlet of the solution heat exchanger and returns to the generator through the second inlet of the generator, so that a refrigeration closed circulation loop is formed. The refrigerant carbon dioxide flows into the absorber through the first inlet of the absorber, and is mixed with the dilute solution flowing out of the solution heat exchanger through the first throttle valve and then flowing into the absorber to become low-pressure concentrated solution.
As an improvement, the heat exchanger comprises a shell, a cavity, a working medium water heat exchange channel and a working medium carbon dioxide heat exchange channel; the heat-insulating material is wrapped around the shell, the phase-change material is placed in the cavity, the phase-change material adopts sodium sulfate decahydrate, four working medium water heat exchange channels are arranged and are uniformly arranged in the cavity in an annular mode, and one working medium carbon dioxide heat exchange channel is arranged and is arranged in the middle of the cavity.
The invention relates to a phase change cold accumulation system based on a transcritical carbon dioxide absorption refrigeration cycle, which comprises a solar heat collection system, a generator, a refrigerating agent and an ionic liquid [ bm im ] which are taken as transcritical carbon dioxide, wherein the generator is used for generating the refrigerating agent and the ionic liquid [ bm im ] which are taken as transcritical carbon dioxide]PF 6 The invention has the following advantages and beneficial effects that the absorption refrigeration cycle system serving as an absorbent is combined together, and the absorption refrigeration cycle system is combined with the phase-change cold accumulation and release system taking sodium sulfate decahydrate as a phase-change material through the heat exchanger:
(1) The green carbon dioxide refrigeration technology is effectively combined with other energy-saving technologies, namely, solar heat supply technology through the generator. When solar natural resources are rich in daytime, the transcritical carbon dioxide absorption refrigeration system fully utilizes heat energy provided by the transcritical carbon dioxide absorption refrigeration system to generate cold and supply cold continuously and stably, so that the high-efficiency utilization of renewable energy sources is realized, the advantages of environmental friendliness, sustainability and the like are realized, and the transcritical carbon dioxide absorption refrigeration system has important significance for energy conservation and carbon reduction.
(2) The refrigerant of the transcritical carbon dioxide absorption refrigeration system adopts carbon dioxide, has the advantages of no toxicity, no harm, no color, no smell, no toxicity, stable chemical property, low safety, easy realization of critical state and the like, and is an environment-friendly natural working medium.
(3) The heat regenerator is arranged in the transcritical carbon dioxide absorption refrigeration system, so that the temperature of the carbon dioxide fluid is reduced, the supercooling degree of the carbon dioxide fluid is increased, and the energy efficiency of the system is improved.
(4) And a phase change cold accumulation and release system is introduced. The system supplies and stores cold when the solar energy is sufficient in daytime, the stored cold energy can be cooled at night, the refrigeration and cold storage are integrated, the time and space limitation of the refrigeration is broken, and the system has wide application prospect.
(5) The invention designs and describes the application of the transcritical carbon dioxide working medium in the absorption refrigeration system in detail, adopts the carbon dioxide and ionic liquid working medium pair, is safe, nontoxic and environment-friendly, and is additionally provided with a heat regenerator, thereby reducing the temperature of the carbon dioxide working medium, increasing the supercooling degree and improving the refrigeration efficiency of the refrigeration system; meanwhile, a phase change cold accumulation and cold accumulation system is introduced, refrigeration, cold supply and cold accumulation are integrated, and in the daytime, sufficient solar energy can be used for accumulating cold while supplying cold, so that uninterrupted cold supply in the evening is realized. Compared with a heat pump which does not need a compressor to do work to provide power, the transcritical carbon dioxide absorption refrigeration system provided by the invention utilizes the heat energy recovered by the solar heat collector to drive the system to circularly refrigerate, thereby saving electric energy resources and improving the utilization rate of renewable energy sources.
Drawings
FIG. 1 is a schematic diagram of a phase change cold storage system based on a transcritical carbon dioxide absorption refrigeration cycle of the present invention;
FIG. 2 is a schematic diagram of a portion of a phase change cold storage system based on a transcritical carbon dioxide absorption refrigeration cycle of the present invention;
FIG. 3 is a schematic diagram of a portion of a phase change cold storage system based on a transcritical carbon dioxide absorption refrigeration cycle of the present invention;
fig. 4 is a schematic structural diagram of a heat exchanger in a phase change cold storage system based on a transcritical carbon dioxide absorption refrigeration cycle according to the present invention.
1-solar heat collector, 2-first circulating pump, 3-heat storage tank, 4-second circulating pump, 5-generator, 6-absorber, 7-solution heat exchanger, 8-solution pump, 9-first throttle valve, 10-gas cooler, 11-regenerator, 12-second throttle valve, 13-heat exchanger, 14-water-gas heat exchanger, 15-shell, 16-cavity, 17-working medium water heat exchange channel, 18-working medium CO 2 Heat exchange channels, 19-generator first outlet, 20-generator first inlet, 21-generator second outlet, 22-gas cooler first inlet, 23-gas cooler first outlet, 24-first inflow conduit, 25-first outflow conduit, 26-regenerator first inlet, 27-regenerator first outlet, 28-heat exchanger first inlet, 29-heat exchanger first outlet, 30-regenerator second inlet, 31-regenerator second outlet, 32-absorber first inlet, 33-second outflow conduit, 34-second inflow conduit, 35-absorber first outlet, 36-absorber second inlet, 37-solution heat exchangerA first inlet, a 38-solution heat exchanger second outlet, a 39-solution heat exchanger first outlet, a 40-solution heat exchanger second inlet, a 41-generator second inlet, a 42-generator third outlet, a 43-heat exchanger second inlet, a 44-heat exchanger third inlet, a 45-heat exchanger second outlet, a 46-heat exchanger third outlet, a 47-water-gas heat exchanger first outlet, a 48-water-gas heat exchanger first inlet, a 49-water-gas heat exchanger second outlet, a 50-water-gas heat exchanger second inlet, a 51-third inflow conduit, a 52-third outflow conduit, a 53-first shut-off valve, a 54-second shut-off valve, a 55-first water supply valve, a 56-second water supply valve, a 57-third water supply valve, and a 58-fourth water supply valve.
Detailed Description
The following will make additional description on the technical solution in the embodiment of the present invention with reference to the drawings in the embodiment of the present invention. The phase change cold storage system based on the transcritical carbon dioxide absorption refrigeration cycle of the present invention, as shown in fig. 1 and 2 and fig. 3 and 4, has the preferred embodiments that:
as shown in fig. 1, a phase change cold storage system based on transcritical carbon dioxide absorption refrigeration cycle comprises a solar heat collection system, an absorption refrigeration cycle system and a phase change cold storage and release system; the solar energy system is connected with the absorption refrigeration cycle system and is used for providing solar energy for the absorption refrigeration cycle system, and the absorption refrigeration cycle system is connected with the phase-change cold accumulation and release system and is used for providing refrigeration for the phase-change cold accumulation and release system.
As shown in fig. 1, the solar heat collection system comprises a solar heat collector 1, a first circulating pump 2, a second circulating pump 4 and a heat storage tank 3; the outlet of the first circulating pump 2 is communicated with the inlet of the solar heat collector 1, and the outlet of the solar heat collector 1 is communicated with the inlet of the heat storage tank 3; the fluid absorbs solar energy in the solar heat collector 1, then transfers heat to the heat storage tank 3, exchanges heat in the heat storage tank 3, and circulates back to the solar heat collector 1 through the first circulating pump 2.
As shown in fig. 1, the absorption refrigeration cycle system includes a generator 5, an absorber 6, a solution heat exchanger 7, a solution pump 8, a first throttle valve 9, a gas cooler 10, a regenerator 11, a second throttle valve 12, and a heat exchanger 13; the generator 5 is provided with a first outlet 19, a first inlet 20, a second outlet 21, a second inlet 41 and a third outlet 42, the gas cooler 10 is provided with a first inlet 22, a first outlet 23, a first inflow pipeline 24 and a first outflow pipeline 25, the regenerator 11 is provided with a first inlet 26, a first outlet 27, a second inlet 30 and a second outlet 31, the heat exchanger 13 is provided with a first inlet 28, a first outlet 29, a second inlet 43, a third inlet 44, a second outlet 45 and a third outlet 46, the absorber 6 is provided with a first inlet 32, a first outlet 35, a second inlet 36, a second outflow pipeline 33 and a second inflow pipeline 34, and the solution heat exchanger 7 is provided with a first inlet 37, a second outlet 38, a first outlet 39 and a second inlet 40; the first generator outlet 19 is communicated with the inlet of the heat storage tank 3, the second circulating pump 4 is communicated with the first generator inlet 20, the second generator outlet 21 is communicated with the first gas cooler inlet 22, the first gas cooler outlet 23 is communicated with the first regenerator inlet 26, the first regenerator outlet 27 is communicated with the inlet of the second throttle valve 12, the outlet of the second throttle valve 12 is communicated with the first heat exchanger inlet 28, the first heat exchanger outlet 29 is communicated with the second regenerator inlet 30, the second regenerator outlet 31 is communicated with the first absorber inlet 32, the first absorber outlet 35 is communicated with the inlet of the solution pump 8, the outlet of the solution pump 8 is communicated with the first solution heat exchanger inlet 37, the first solution heat exchanger outlet 39 is communicated with the second generator inlet 41, the third generator outlet 42 is communicated with the second solution heat exchanger inlet 40, the second solution heat exchanger outlet 38 is communicated with the first throttle valve 9, and the second absorber outlet 9 is communicated with the first absorber inlet 36.
The solution in the generator 5 is a mixed solution of carbon dioxide and ionic liquid, after the mixed solution in the generator 5 absorbs heat of working medium heat conduction oil from a first inlet 20 of the generator, carbon dioxide is separated out from the mixed solution, so that the mixed solution is changed from a concentrated solution into a dilute solution, the separated high-temperature high-pressure carbon dioxide fluid flows out from a second inlet 36 of the generator through a first inlet 22 of the gas cooler into the gas cooler 10, the high-temperature high-pressure carbon dioxide fluid releases heat in the gas cooler 10, the released heat is taken away by room-temperature circulating cooling water, the high-temperature high-pressure carbon dioxide fluid is changed into a normal-temperature carbon dioxide supercritical liquid after being released and cooled, the rest dilute solution in the generator 5 flows into the solution heat exchanger 7 through a third outlet 42 of the generator, after being subjected to heat exchange and temperature reduction through the solution heat exchanger 7, the rest dilute solution is throttled and depressurized through a first throttle valve 9, and flows into the absorber 6 from the second inlet 36 of the absorber, the dilute solution absorbs the low-temperature low-pressure carbon dioxide fluid from the first inlet 32 of the absorber and releases a large amount of heat, the heat is taken away by the room-temperature circulating cooling water, the low-pressure carbon dioxide fluid is taken away by the room-temperature circulating cooling water, the released heat is changed into a low-temperature circulating cooling water, the mixed solution is cooled down from the low-pressure circulating cooling water, the concentrated solution 5 is continuously returns to the heat pump 5 through the first heat exchanger 5, and is heated by the heat pump, and the concentrated solution is discharged by the heat pump through the first heat exchanger 5, and the heat pump 5, and the concentrated solution is heated by the heat pump through the heat pump, and the heat pump is heated through the heat pump, and the heat is cooled through the heat pump, and the heat is heated. The solution heat exchanger realizes heat exchange between the low-pressure mixed concentrated solution and the dilute solution, and effectively improves the temperature of the concentrated solution before entering the generator.
As shown in fig. 1, the phase-change cold accumulation and discharge system consists of the heat exchanger 13 and a water-gas heat exchanger 14; the heat exchanger 13 is provided with a first inlet 28, a second inlet 43, a first outlet 29, a second outlet 45, a third inlet 44 and a third outlet 46, and the water-gas heat exchanger 14 is provided with a first outlet 47, a first inlet 48, a second outlet 49, a second inlet 50, a third inflow pipe 51 and a third outflow pipe 52; the second outlet 45 of the heat exchanger is communicated with the second inlet 50 of the water-gas heat exchanger, the second outlet 49 of the water-gas heat exchanger is communicated with the second inlet 43 of the heat exchanger, the third outlet 46 of the heat exchanger is communicated with the first inlet 48 of the water-gas heat exchanger, and the first outlet 47 of the water-gas heat exchanger is communicated with the third inlet 44 of the heat exchanger.
Preferably, the transcritical absorption refrigeration system has a pressure in the range of from 4MPa to 10MPa, wherein the heat rejection process in the gas cooler occurs at a supercritical region pressure greater than 7.18MPa and a temperature in the range of from about 5 ℃ to 100 ℃.
The phase change cold accumulation system based on the transcritical carbon dioxide absorption refrigeration cycle is provided with a solar heat collection system, an absorption refrigeration cycle system and a phase change cold accumulation and discharge system, wherein the solar heat collection system is combined with the absorption refrigeration cycle system through the generator 5, and the absorption refrigeration cycle system is combined with the phase change cold accumulation and discharge system through the heat exchanger 13; working medium conduction oil in the solar heat collection system flows out from an outlet of the heat storage tank 3, enters the solar heat collector 1 through the first circulating pump 2, after heat is obtained in the solar heat collector 1, high-temperature conduction oil flows from the outlet of the solar heat collector 1 to the heat storage tank 3 to form a circulating loop, high-temperature conduction oil flows to the generator 5 through the first generator inlet 20 through the second circulating pump 4, and after being heated in the generator 5, returns to the heat storage tank 3 through the first generator outlet 19 to form circulation.
Wherein the refrigerant used in the absorption refrigeration cycle system is transcritical carbon dioxide, and the absorbent is ionic liquid [ bm im ]]PF 6 。
The carbon dioxide refrigerant in the absorption refrigeration cycle system is in a transcritical state, wherein the transcritical state refers to that after the refrigerant is heated and separated from the generator 5, the high-temperature and high-pressure carbon dioxide is in a supercritical state, then the high-temperature and high-pressure supercritical carbon dioxide flows into the gas cooler 10 to perform constant-pressure heat release, the constant-pressure heat release process is located in a carbon dioxide supercritical region, at this time, the temperature of the carbon dioxide supercritical fluid is slightly higher than the temperature of the cooling medium (preferably 2-3 ℃ higher than the temperature of the cooling medium), and in the refrigeration cycle flow process, the temperature of the carbon dioxide at the outlet of the gas cooler is optimal to be closer to the inlet temperature of the cooling medium. And the temperature of the carbon dioxide fluid is reduced after heat exchange with low-temperature low-pressure carbon dioxide vapor in the heat regenerator 11, the carbon dioxide fluid enters the second throttling valve 12 to be throttled and then is changed into a low-temperature low-pressure gas-liquid two-phase flow, finally, the heat is absorbed by internal pressure in the heat exchanger 13 to store cold, the constant-pressure heat absorption process is carried out in a carbon dioxide subcritical region, and the carbon dioxide refrigerant is in a transcritical state in the circulation of the whole system. The supercritical carbon dioxide flowing out of the gas cooler in the heat regenerator exchanges heat with low-temperature steam from the heat exchanger, and the supercritical carbon dioxide with higher temperature is cooled, so that the throttling loss of the system is reduced, and the system performance and the refrigerating capacity are effectively improved.
The outdoor normal temperature cooling water flows into the gas cooler 10 through the first inflow pipe 24, and flows out 25 of the gas cooler 10 through the first outflow pipe.
Wherein the outdoor normal temperature cooling water flows into the absorber 6 through the second inflow pipe 34 and then flows out of the absorber 6 through the second outflow pipe 33.
The phase change cold storage system based on the transcritical carbon dioxide absorption refrigeration cycle according to the embodiment of the invention, wherein the refrigerant used in the absorption refrigeration cycle is transcritical carbon dioxide, and the absorbent is ionic liquid [ bm im ]]PF 6 The method comprises the steps of carrying out a first treatment on the surface of the The refrigerant carbon dioxide in the absorption refrigeration cycle system is separated out from the concentrated solution in the generator 5 after being heated by the high-temperature heat conduction oil in the generator 5, the concentrated solution in the generator 5 is heated and becomes a dilute solution, the separated high-temperature high-pressure carbon dioxide flows from the generator second outlet 21 to the gas cooler 10 through the gas cooler first inlet 22, the pressure of the high-temperature high-pressure carbon dioxide refrigerant is higher than the critical pressure of the carbon dioxide, the high-temperature high-pressure supercritical carbon dioxide is changed into high-pressure room-temperature supercritical carbon dioxide after being heat exchanged with the outdoor normal-temperature cooling water in the gas cooler 10, the temperature of the high-pressure room-temperature supercritical carbon dioxide is slightly higher than the ambient temperature after being heat exchanged with the outdoor normal-temperature cooling water, the high-pressure room-temperature supercritical carbon dioxide refrigerant flows from the gas cooler first outlet 23 to the heat regenerator 11 through the heat regenerator first inlet 26, flows from the heat exchanger first outlet 29 to the low-pressure carbon dioxide 11 through the heat regenerator second inlet 30, the high-pressure supercritical carbon dioxide flows from the heat regenerator 11 to the low-pressure throttle valve 12 after being heat exchanged with the low-pressure supercritical carbon dioxide in the heat regenerator 11, and the low-pressure supercritical carbon dioxide flows from the heat regenerator first outlet 27 to the low-pressure throttle valve 12 after being heat exchanged with the outdoor normal-temperature cooling waterAfter throttling, the mixed solution enters the heat exchanger 13 through the first inlet 28 of the heat exchanger, after endothermic evaporation in the heat exchanger 13, the mixed solution flows out from the first outlet 29 of the heat exchanger to the regenerator 11 through the second inlet 30 of the regenerator, after heating in the regenerator 11, flows out from the second outlet 31 of the regenerator, flows out from the first inlet 32 of the absorber to the absorber 6, after mixing with the diluted solution flowing out from the second outlet 38 of the solution heat exchanger to the absorber 6 through the second inlet 36 of the absorber through the first throttle valve 9 in the absorber 6, the concentrated solution flows out from the first outlet 35 of the absorber 6 to the solution pump 8, the heat generated by the reaction in the absorber 6 is taken away by the outdoor normal temperature cooling water, the mixed low-pressure concentrated solution flows out from the solution pump 8 to the solution heat exchanger 7 through the first inlet 37 of the solution heat exchanger, flows out from the third outlet 42 of the solution exchanger to the second inlet 39 of the heat exchanger 7, and the mixed solution flows out from the second outlet 40 of the second heat exchanger to the second inlet 41 of the heat exchanger. The supercritical carbon dioxide from the gas cooler 10 and the low-temperature steam from the heat exchanger 13 in the heat regenerator 11 exchange heat, and the supercritical carbon dioxide with higher temperature is cooled by the low-temperature steam, so that the throttling loss of the system is reduced, and the system performance and the refrigerating capacity are effectively improved.
The phase-change cold accumulation and release system also comprises a structural design of the heat exchanger, and the heat exchanger 13 is composed of a shell 15, a cavity 16, a working medium water heat exchange channel 17 and a working medium carbon dioxide 18 heat exchange channel; the heat insulation material is wrapped around the shell 15, the phase change material is placed in the cavity 16, the phase change material is sodium sulfate decahydrate, four working medium water heat exchange channels 17 are arranged inside the cavity in an annular and uniform manner, and one working medium carbon dioxide heat exchange channel 18 is arranged in the middle of the cavity. Compared with the prior commonly used cold storage type heat exchanger, the heat exchanger is provided with only one fluid channel, and cold storage and heat storage can be realized by sequentially flowing through the same flow channel by using two cold working mediums, and the heat exchanger is internally provided with four working medium water heat exchange channels and one carbon dioxide heat exchange channel which are annularly arranged.
Wherein indoor (to be cooled) air flows into the water-gas heat exchanger 14 through the third inflow pipe 51 and then flows out of the water-gas heat exchanger 14 through the third outflow pipe 52.
Wherein, through the circulation flow of the working medium water between the phase change material and the water-gas heat exchanger 14, the cooling is realized, and the air at room temperature (to be cooled) is cooled and supplied into the room.
According to the phase-change cold accumulation system based on the transcritical carbon dioxide absorption refrigeration cycle, which is disclosed by the embodiment of the invention, the sodium sulfate decahydrate is used as a phase-change material, and the heat exchanger 13 is designed to be composed of a shell 15, a cavity 16, a working medium water heat exchange channel 17 and a working medium carbon dioxide heat exchange channel 18; the carbon dioxide refrigerant flows from the first inlet 28 of the heat exchanger to the working medium carbon dioxide heat exchange channel 18, absorbs heat and evaporates in the working medium carbon dioxide heat exchange channel 18, and flows out from the first outlet 29 of the heat exchanger to realize refrigeration and reciprocating circulation, so as to realize continuous cold accumulation of the phase change material sodium sulfate decahydrate; the heat exchanger 13 and the water-gas heat exchanger 14 are respectively provided with four working medium water heat exchange channels 17 and are uniformly arranged in a ring shape, the working medium water flows out from the first outlet 47 of the water-gas heat exchanger and the second outlet 49 of the water-gas heat exchanger, flows into the heat exchanger 13 through the third inlet 44 of the heat exchanger and the second inlet 43 of the heat exchanger, is changed into cold water after heat exchange with sodium sulfate decahydrate in the heat exchanger 13, realizes cooling release, the cold water flows out from the third outlet 46 of the heat exchanger and the second outlet 45 of the heat exchanger, flows into the water-gas heat exchanger 14 through the first inlet 48 of the water-gas heat exchanger and the second inlet 50 of the water-gas heat exchanger, and the indoor (to-be-cooled) air flows into the water-gas heat exchanger 14 from the third inflow pipeline 51, is changed into cold air after heat exchange with the cold water in the water-gas heat exchanger 14, flows out from the third outflow pipeline 52 and then flows into the indoor.
The system has three working modes, including: a refrigeration and cold supply mode, a refrigeration and cold accumulation mode and a cold accumulation and discharge mode.
Before the device is used, the precooling stage is started, the first stop valve 53 and the second stop valve 54 are opened, the solar heat collecting system works, and the first water supply valve 55, the second water supply valve 56, the third water supply valve 57 and the fourth water supply valve 58 are closed, so that no domestic cooling is provided. The heat collecting plate 1 in the solar heat collecting system circularly heats the heat conducting oil working medium in the system by recovering solar radiation, and stores heat in the heat storage tank 3, high-temperature heat conducting oil in the heat storage tank 3 is supplied to the generator 5, so that the absorption refrigeration cycle system is refrigerated, the generated cold is stored in the phase change material of the heat exchanger 13, when the temperature of sodium sulfate decahydrate in the phase change cold storage and releasing system is lower than about 6 ℃, the pre-cooling stage is started to be regarded as completed, and the system enters a working mode.
In the cooling and refrigerating mode, the first and second shut-off valves 53 and 54 are opened, the solar heat collecting system is operated, and the first, second, third and fourth water supply valves 55, 56, 57 and 58 are opened to provide domestic cooling. When the temperature of the heat conduction oil measured in the heat storage tank 3 is higher than 80 ℃, the stored heat conduction oil is supplied to the generator 5 through the second circulating pump 4, so that the absorption refrigeration system circularly refrigerates, the generated cold is transferred to the heat exchanger 13, the heat exchanger 13 transfers the cold to working medium water in a loop, the working medium water exchanges heat with air flowing in through the third inflow pipeline 51 under the action of the water-air heat exchanger, and the cold air is sent to the indoor end through the third outflow pipeline 52.
In the cooling/cold storage mode, when the solar radiation amount is sufficient in the daytime, but the cooling demand is not provided or the generated cooling amount is greater than the demand, the first, second, third and fourth water supply valves 55, 56, 57 and 58 are closed in the cooling/cold supply mode described above, and no domestic cooling is provided. The cold energy generated by the absorption refrigeration cycle system is stored in the phase change material of the heat exchanger 13, and the amount of the stored cold energy is related to the structural size of the heat exchanger and the selection of the phase change material.
In the cold accumulation and release mode, in order to prevent heat stored in the heat storage tank 3 from being radiated and lost through the heat collector 1 during other periods of poor solar energy radiation such as night or cloudy days, the first stop valve 53 and the second stop valve 54 are closed, and the solar heat collection system is closed on the basis of the refrigerating and cooling mode described above. The cold stored in the phase change material in the heat exchanger 13 is transferred to the water-gas heat exchanger through the working fluid water in the loop, in which the working fluid water transfers the cold to the air flowing in through the third inflow pipe 51, and the cold air is fed into the indoor end through the third outflow pipe 52.
The phase change cold accumulation system based on the transcritical carbon dioxide absorption refrigeration cycle disclosed by the embodiment of the invention is provided with a solar heat collection system, an absorption refrigeration cycle system and a phase change cold accumulation cold release system, wherein the absorption refrigeration cycle system takes the transcritical carbon dioxide as a refrigerant and the ionic liquid [ bm im ]]PF 6 The phase-change cold accumulation and release system takes the sodium sulfate decahydrate as a phase-change material, and the heat regenerator 11 can effectively reduce the temperature of the refrigerant entering the second throttle valve 12 and reduce the throttle loss; the solar heat collection system is combined with the absorption refrigeration cycle system through the generator, the absorption refrigeration cycle system is combined with the phase-change cold accumulation and release system through the heat exchanger, and the transcritical carbon dioxide refrigeration technology, the solar heat supply technology and the phase-change cold accumulation technology are combined, so that the efficient utilization of energy sources is realized, the refrigeration and cold accumulation are integrated, the time and space limitation of cooling is broken, the advantages of environmental friendliness, sustainability, compact structure and the like are achieved, the energy conservation and carbon reduction are achieved, and the application prospect is wide.
The above embodiments are provided to illustrate the technical concept and features of the present invention and are intended to enable those skilled in the art to understand the content of the present invention and implement the same, and are not intended to limit the scope of the present invention. All equivalent changes or modifications made according to the spirit of the present invention should be construed to be included in the scope of the present invention.
Claims (5)
1. The phase change cold accumulation system based on the transcritical carbon dioxide absorption refrigeration cycle comprises a solar heat collection system, an absorption refrigeration cycle system and a phase change cold accumulation cold release system;
the solar heat collection system is connected with the absorption refrigeration cycle system and is used for providing solar energy for the absorption refrigeration cycle system, and the absorption refrigeration cycle system is connected with the phase-change cold accumulation and release system and is used for providing refrigeration for the phase-change cold accumulation and release system;
the solar heat collection system comprises a solar heat collector, a first circulating pump and a heat storage tank; the outlet of the first circulating pump is communicated with the inlet of the solar heat collector, and the outlet of the solar heat collector is communicated with the inlet of the heat storage tank;
the absorption refrigeration cycle system comprises a generator, an absorber, a solution heat exchanger, a solution pump, a first throttle valve, a gas cooler, a heat regenerator, a second throttle valve and a heat exchanger; the first outlet of the generator is communicated with the inlet of the heat storage tank, the second circulating pump is communicated with the first inlet of the generator, the second outlet of the generator is communicated with the inlet of the gas cooler, the first outlet of the gas cooler is communicated with the first inlet of the heat regenerator, the first outlet of the heat regenerator is communicated with the inlet of the second throttle valve, the outlet of the second throttle valve is communicated with the first inlet of the heat exchanger, the first outlet of the heat exchanger is communicated with the second inlet of the heat regenerator, the second outlet of the heat regenerator is communicated with the first inlet of the absorber, the first outlet of the absorber is communicated with the inlet of the solution pump, the outlet of the solution pump is communicated with the first inlet of the solution heat exchanger, the first outlet of the solution heat exchanger is communicated with the second inlet of the generator, the third outlet of the generator is communicated with the second inlet of the solution heat exchanger, the second outlet of the solution heat exchanger is communicated with the inlet of the first throttle valve, and the outlet of the first throttle valve is communicated with the second inlet of the absorber; the carbon dioxide of the refrigerant in the absorption refrigeration cycle system is in a transcritical state, wherein the transcritical state refers to that when the pressure of the refrigerant separated out from the generator is higher than the critical pressure of the carbon dioxide, then high-temperature high-pressure supercritical carbon dioxide flows into the gas cooler to release heat, the temperature of the supercritical carbon dioxide fluid is cooled to be close to the ambient temperature, then the temperature of the carbon dioxide fluid is reduced after heat exchange with low-temperature low-pressure carbon dioxide vapor in the heat regenerator, then the carbon dioxide fluid enters the second throttling valve to be throttled and then becomes a low-temperature low-pressure gas-liquid two-phase flow, finally heat is absorbed in the heat exchanger to store heat, and the carbon dioxide of the refrigerant is in the transcritical state in the whole cycle.
2. The phase-change cold storage system based on a transcritical carbon dioxide absorption refrigeration cycle according to claim 1, wherein the phase-change cold storage and release system comprises a heat exchanger and a water-gas heat exchanger; an inlet and an outlet are arranged on the heat exchanger, and an inlet, an outlet, a third inflow pipeline and a third outflow pipeline are arranged on the water-gas heat exchanger; the inlet and the outlet on the heat exchanger are respectively connected with the outlet and the inlet of the water-gas heat exchanger.
3. The phase change cold storage system based on transcritical carbon dioxide absorption refrigeration cycle as set forth in claim 1, wherein working medium conduction oil in the solar heat collection system flows out from an outlet of a heat storage tank, enters the solar heat collector through the first circulating pump, after heat is obtained in the solar heat collector, high temperature conduction oil flows from the outlet of the solar heat collector to the heat storage tank to form a circulating loop, the high temperature conduction oil flows to the generator through a first inlet of the generator through the second circulating pump, and returns to the heat storage tank through a first outlet of the generator to form a circulation after being heated in the generator.
4. The phase-change cold storage system based on transcritical carbon dioxide absorption refrigeration cycle as set forth in claim 1, wherein carbon dioxide as refrigerant in said absorption refrigeration cycle system is separated out from concentrated solution in said generator after being heated by high temperature conduction oil in said generator, said concentrated solution in said generator is changed into a dilute solution after being heated, said separated high temperature and high pressure carbon dioxide flows out from said generator second outlet to said gas cooler, pressure of said high temperature and high pressure carbon dioxide refrigerant is higher than critical pressure of carbon dioxide, said high temperature and high pressure supercritical carbon dioxide becomes high pressure room temperature supercritical carbon dioxide after being heat exchanged with outdoor normal temperature cooling water in said gas cooler, said high pressure room temperature supercritical carbon dioxide becomes high pressure room temperature supercritical carbon dioxide after being heat exchanged with said outdoor normal temperature cooling water, said high pressure room temperature supercritical carbon dioxide refrigerant enters said regenerator, after being heat exchanged with low temperature low pressure carbon dioxide vapor flowing out from said heat exchanger into said regenerator, said second outlet to said gas cooler, said high pressure supercritical carbon dioxide refrigerant enters said regenerator after being heat exchanged with said outdoor temperature conduction oil, said low pressure supercritical carbon dioxide refrigerant enters said regenerator after being heat exchanged with said outdoor temperature heat conduction oil, said low pressure supercritical carbon dioxide refrigerant enters said regenerator, said dilute carbon dioxide refrigerant enters said regenerator after being mixed solution after flowing out from said heat exchanger, said low pressure supercritical carbon dioxide refrigerant enters said heat absorber after being absorbed in said heat exchanger, and the solution flows from the solution pump to the solution heat exchanger, exchanges heat with the dilute solution flowing from the generator to the solution heat exchanger in the solution heat exchanger, flows out of the first outlet of the solution heat exchanger, and returns to the generator through the second inlet of the generator to form a refrigeration closed circulation loop.
5. The phase change cold storage system based on transcritical carbon dioxide absorption refrigeration cycle as set forth in claim 1, wherein said heat exchanger comprises a housing, a cavity, a working medium water heat exchange channel and a working medium carbon dioxide heat exchange channel; the heat-insulating material is wrapped around the shell, the phase-change material is placed in the cavity, the phase-change material adopts sodium sulfate decahydrate, four working medium water heat exchange channels are arranged and are uniformly arranged in the cavity in an annular mode, and one working medium carbon dioxide heat exchange channel is arranged and is arranged in the middle of the cavity.
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