CN110906582A - Refrigerating system and method based on secondary condensation pressurization absorption and supercooling compression - Google Patents
Refrigerating system and method based on secondary condensation pressurization absorption and supercooling compression Download PDFInfo
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- CN110906582A CN110906582A CN201911156542.7A CN201911156542A CN110906582A CN 110906582 A CN110906582 A CN 110906582A CN 201911156542 A CN201911156542 A CN 201911156542A CN 110906582 A CN110906582 A CN 110906582A
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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
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
- F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
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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
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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
- F25B35/00—Boiler-absorbers, i.e. boilers usable for absorption or adsorption
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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
- F25B41/00—Fluid-circulation arrangements
- F25B41/30—Expansion means; Dispositions thereof
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- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
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- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
Abstract
The invention discloses a refrigerating system and method based on secondary condensation, pressure boost absorption and supercooling compression; the heat collector is connected with the first hot water pump and the heat storage box in sequence; the heat storage tank is connected with the second hot water pump and the generator in sequence; the generator is connected with the absorption cycle condenser, the absorption cycle throttle valve, the absorption cycle evaporator, the secondary condenser, the booster pump, the absorber, the solution pump, the solution heat exchanger and the solution throttle valve in sequence; the main-stage circulating compressor is sequentially connected with the condenser, the subcooler, the main-stage throttling valve and the main-stage evaporator; the secondary circulating compressor is connected with the condenser, the subcooler, the secondary throttle valve and the secondary evaporator in sequence; the cold storage box is connected with an absorption cycle chilled water pump and an absorption cycle evaporator in sequence; the cold storage tank is connected with the supercooling pump and the subcooler in sequence. The system combines secondary condensation and a booster pump to replace a large-scale water vapor compressor to realize booster absorption, widens the working condition range of a heat source and obviously improves the working condition performance of the low-temperature heat source of the system.
Description
Technical Field
The invention relates to a refrigeration system, in particular to a refrigeration system and a method based on secondary condensation, pressurization and absorption and supercooling compression.
Background
At present, the total amount of energy consumption is on a rapid rise. Therefore, the conversion from the fossil energy system to the low-carbon energy system is realized, and the direction of global energy transformation is provided.
The distributed photovoltaic system has the advantages of huge resource amount, convenient installation of photovoltaic power generation equipment, low power transmission and distribution loss, high reliability and the like, so that the distributed photovoltaic system has the attention.
Although the distributed photovoltaic system has excellent development potential, the popularization has certain restriction due to higher power generation cost. Therefore, the energy utilization efficiency of the distributed photovoltaic system is improved to increase the economic benefit of the distributed photovoltaic system, and the distributed photovoltaic system has obvious effects of promoting the construction of a modern energy system and promoting energy conservation and emission reduction.
At present, the maximum power generation efficiency of a crystalline silicon battery widely used in a distributed photovoltaic system under a Standard Test Condition (STC) is about 0.16. The data indicates that nearly 85% of the solar energy is not fully utilized in the photovoltaic power generation process, but is discharged directly to the environment, primarily as low-grade thermal energy. Therefore, the photovoltaic waste heat is utilized to drive the absorption refrigeration system, and the combined use of the photovoltaic heat collector and the photo-thermal integrated heat collector realizes cold electricity or combined cold, heat and power generation, so that the energy-saving economic benefit of the distributed photovoltaic system can be greatly improved.
Currently, absorption-supercooling compression type composite refrigeration cycles are widely used in the above-described cogeneration systems. Because the energy-saving benefit is obviously influenced by the photovoltaic efficiency, and the photovoltaic efficiency and the temperature of the photovoltaic cell and hot water are in a negative correlation rule, the driving temperature of the absorption refrigeration cycle heat source is reduced, and the energy-saving benefit of the system is improved. As the temperature of the heat source decreases, the bleed range of the absorption refrigeration cycle gradually decays until the refrigeration capacity is completely lost, for which a supercharged absorption refrigeration cycle can be used, i.e. a water vapor compressor is coupled between the evaporator and the absorber to increase the bleed range. However, in engineering applications, the water vapor compressor has the disadvantages of large size, high price and the like, so that the supercharged absorption refrigeration system has no economic feasibility.
Disclosure of Invention
The invention overcomes the defects and shortcomings of large size, high price and the like of a vapor compressor in the existing composite refrigeration system, and provides a refrigeration system and a method based on secondary condensation, pressurization and absorption and supercooling compression. Not only technically has widened the heat source operating mode scope and is showing the low temperature heat source operating mode performance that promotes, makes the system can retrieve the photovoltaic waste heat better and carry out the cooling utilization, moreover greatly reduced economic cost.
The invention is realized by the following technical scheme:
the utility model provides a refrigerating system based on secondary condensation pressure boost is absorbed and subcooling compression, includes following adapting unit, connects between each part including the tube coupling: the heat collector comprises a heat collector 1, a first hot water pump 2, a heat storage tank 3 and a second hot water pump 4; a generator 5, an absorption cycle condenser 6, an absorption cycle throttle valve 7, an absorption cycle evaporator 8, a secondary condenser 9, a booster pump 10, an absorber 11, a solution pump 12, a solution heat exchanger 13, and a solution throttle valve 14; a condenser 15, a subcooler 16, a secondary throttle valve 17, a secondary evaporator 18, a secondary circulating compressor 19, a main throttle valve 20, a main evaporator 21, a main circulating compressor 22, a cold storage tank 23, an absorption circulating chilled water pump 24, a subcooling pump 25 and a secondary condensing pump 26;
an outlet of the heat collector 1 is connected with an inlet at the A end of the heat storage tank 3 through a first hot water pump 2; an outlet at the A end of the heat storage box 3 is connected with an inlet of the heat collector 1;
an outlet at the B end of the heat storage tank 3 is connected with a hot water side inlet of a generator 5 through a second hot water pump 4, and a hot water side outlet of the generator 5 is connected with an inlet at the B end of the heat storage tank 3;
a water vapor outlet of the generator 5 connected to a refrigerant-side inlet of the absorption cycle condenser 6; a refrigerant side outlet of the absorption cycle condenser 6 is connected with a refrigerant side inlet of the absorption cycle evaporator 8 through an absorption cycle throttle valve 7; the refrigerant side outlet of the absorption cycle evaporator 8 is connected with the refrigerant side inlet of the secondary condenser 9; the refrigerant side outlet of the secondary condenser 9 is connected with the liquid water inlet of the absorber 11 through a booster pump 10;
the solution outlet of the absorber 11 is connected with the low-temperature side inlet of the solution heat exchanger 13 through a solution pump 12, and the low-temperature side outlet of the solution heat exchanger 13 is connected with the solution inlet of the generator 5; the solution outlet of the generator 5 is connected with the high-temperature side inlet of the solution heat exchanger 13; the high-temperature side outlet of the solution heat exchanger 13 is connected with the solution inlet of the absorber 11 through a solution throttle valve 14;
a refrigerant side outlet of the condenser 15 is connected to a refrigerant side inlet of the subcooler 16; the refrigerant side outlet of the subcooler 16 is divided into two branches: one branch is connected with a refrigerant side inlet of a secondary evaporator 18 through a secondary throttle valve 17, and a refrigerant side outlet of the secondary evaporator 18 is connected with a refrigerant side inlet of a condenser 15 through a secondary circulation compressor 19; one branch is connected with a refrigerant side inlet of a main-stage evaporator 21 through a main-stage throttle valve 20, and a refrigerant side outlet of the main-stage evaporator 21 is connected with a refrigerant side inlet of a condenser 15 through a main-stage circulating compressor 22;
the secondary condenser 9 is communicated with the chilled water side of the secondary evaporator 18, and a secondary condensing pump 26 is arranged on an inlet pipeline on the chilled water side of the secondary condenser 9;
the chilled water side of the absorption cycle evaporator 8 is connected with a first port 231 of the cold storage box 23, and an absorption cycle chilled water pump 24 is arranged on an inlet pipeline at the chilled water side of the absorption cycle evaporator 8;
the second port 232 of the cold storage tank 23 is connected to the chilled water side of the subcooler 16, and the supercooling pump 25 is provided on the inlet pipe of the chilled water side of the subcooler 16.
The lithium bromide solution in the generator 5 and the absorber 11 is circulated among the generator 5, the solution heat exchanger 13 and the absorber 11 by a solution pump 12; the water vapor evaporated by the lithium bromide solution in the generator 5 enters the absorption circulating condenser 6 to be condensed into liquid water and then is sent to the absorption circulating evaporator 8, the liquid water is evaporated into water vapor by the absorption circulating evaporator 8 and then is sent to the secondary condenser 9, the water vapor is condensed into liquid water by the secondary condenser 9, and finally the liquid water is sent to the absorber 11 through the booster pump 10.
The heat collector 1 is a solar photovoltaic photo-thermal integrated component.
The secondary circulation compressor 19 and the primary circulation compressor 22 are inverter compressors.
The booster pump 10 is a liquid water booster pump.
The operation method of a refrigerating system, it includes supplying power valley time operation step and supplying power peak section and flat time operation step; in the two operation steps, the main stage throttle valve 20, the main stage evaporator 21 and the main stage circulation compressor 22 in the vapor compression cycle are all in an opening and working state;
firstly, operating step of power supply valley period
A vapor compression cycle operation step:
the secondary throttle valve 17 and the secondary cycle compressor 19 are opened to make the primary and secondary vapor compression cycles in working condition and the corresponding condensation heat is discharged to the environment in the condenser 15;
in the main-stage steam compression cycle, the main-stage evaporator 21 generates 3-5 ℃ low-temperature refrigerating capacity for meeting the cold load required by the building; in the secondary steam compression cycle, the secondary evaporator 18 generates medium-temperature refrigerating capacity at 14-16 ℃, and the secondary condenser 9 is cooled by a secondary condensing pump 26, so that the water vapor generated in the absorption cycle evaporator 8 is condensed into liquid water in the secondary condenser 9; when the absorption cycle stops operating, synchronously closing the secondary cycle compressor 19, the secondary throttle valve 17 and the secondary condensate pump 26;
an absorption cycle operation step:
starting the second hot water pump 4, the absorption cycle throttle valve 7, the booster pump 10, the solution pump 12, the solution throttle valve 14, the absorption cycle chilled water pump 24 and the secondary condensation pump 26 to enable the absorption cycle to be in a working state;
the second hot water pump 4 sends 68-73 ℃ hot water stored in the heat storage box 3 into the generator 5 for heat supply, a lithium bromide solution in the generator 5 is heated, water in the lithium bromide solution is converted into water vapor to enter the absorption cycle condenser 6, the water vapor is condensed into liquid water at 40 ℃ under the cooling of external cooling water, the liquid water is throttled by the absorption cycle throttle valve 7 and then evaporated and absorbed heat at 22-24 ℃ on the refrigerant side of the absorption cycle evaporator 8, the first port 231 outlet of the cold storage box 23 enters 31-33 ℃ water on the chilled water side of the absorption cycle evaporator 8, the water is cooled to 24-26 ℃ and then sent back to the first port 231 inlet, and the valley section is supplied with cold through the cold storage box 23;
the water vapor generated by evaporation in the absorption circulating evaporator 8 enters a secondary condenser 9 to be condensed into liquid water at 24 ℃, the liquid water enters an absorber 11 after being pressurized by a booster pump 10 for 1.8-2 kPa and is mixed with the lithium bromide solution in the absorber 11, and the mass concentration of the solution in the absorber 11 is reduced to 30-31.5% from 42-45.1% of the conventional non-pressurized absorption circulation due to the secondary condensation and pressurization;
the dilute solution in the absorber 11 enters the solution heat exchanger 13 under the driving of the solution pump 12, the dilute solution at the low-temperature side is heated to 46-47.2 ℃ by the concentrated solution at the high-temperature side, then enters the generator 5, is heated to generate water vapor, the temperature is raised to 59-60 ℃, the concentration is increased to 45-46.8%, then the dilute solution enters the high-temperature side of the solution heat exchanger 13 through the concentrated solution outlet and is cooled by the dilute solution at the low-temperature side, and the dilute solution is throttled by the solution throttle valve 14 and then cooled to 44-45.4 ℃ and returns to the absorber 11 to be mixed with the lithium bromide solution therein;
when the temperature of the top layer of the heat storage tank 3 is low and the absorption cycle can not work any more, closing the second hot water pump 4, the absorption cycle throttling valve 7, the booster pump 10, the solution pump 12, the solution throttling valve 14, the absorption cycle chilled water pump 24 and the secondary condensation pump 26 to stop the absorption cycle, and synchronously closing the secondary throttling valve 17 and the secondary cycle compressor 19;
second, operation steps in peak period and flat period of power supply
A vapor compression cycle operation step:
the secondary recycle compressor 19, secondary throttle 17 and secondary condensate pump 26 are closed;
the main-stage throttle valve 20 and the main-stage circulating compressor 22 keep working states, and meanwhile, the supercooling pump 25 is started to enable cold water at the temperature of 24-26 ℃ in the cold storage tank 23 to enter the chilled water side of the subcooler 16 through the outlet of the second port 232, so that the refrigerant at the temperature of 40 ℃ at the refrigerant side outlet of the condenser 15 is subcooled to be 28-30.2 ℃ in the subcooler 16, and further the purpose of saving energy consumption of a power supply peak section by utilizing medium-temperature cold energy prepared by solar heat and electric energy of a power supply valley section is achieved; when the cold storage box 23 finishes the cold release, the supercooling pump 25 is closed;
the operation of the heat collector:
when the solar radiation is higher than the starting condition of the heat collector 1, the first hot water pump 2 is started to send the water in the heat storage tank 3 into the heat collector 1, and the solar heat is collected.
Compared with the prior art, the invention has the following advantages and effects:
in the traditional absorption-supercooling compression type composite refrigeration system, a steam compressor with large size and high price is ingeniously replaced by a mode of combining secondary condensation and a booster pump, so that the booster absorption refrigeration with technical and economic feasibility is realized, the working condition range of a heat source is widened, the working condition performance of a low-temperature heat source is obviously improved, and the system can better recover photovoltaic waste heat for cooling utilization.
In addition, the heat and mass transfer process in the traditional non-supercharged absorption refrigeration cycle absorber is changed into a condensation and liquid mixing process, and the booster pump only improves the pressure of the working medium and avoids the temperature of the working medium from being greatly increased, so that the heat exchange area is effectively reduced and the system is more compact. Therefore, due to the pressurization of the booster pump, the air bleeding range of the supercharged absorption refrigeration cycle is increased by about 0.136 compared with the conventional non-supercharged cycle, and the relative increase rate is about 800%, so that the working condition range of the absorption cycle heat source is effectively widened, and the working condition performance of the low-temperature heat source is remarkably improved.
On the other hand, the energy consumption required by secondary condensation comes from valley section electric energy, and the refrigeration gain brought by the energy consumption is used for saving peak section electric energy, so that the energy-saving economic benefit of the system is greatly increased.
Drawings
Fig. 1 is a schematic structural diagram of a refrigeration system based on secondary condensation, pressure boost absorption and supercooling compression.
Detailed Description
The present invention will be described in further detail with reference to specific examples.
As shown in fig. 1. The invention discloses a refrigerating system based on secondary condensation, pressurization and absorption and supercooling compression.
The refrigeration system comprises the following connecting parts, wherein the connecting parts comprise pipeline connections: the heat collector comprises a heat collector 1, a first hot water pump 2, a heat storage tank 3 and a second hot water pump 4; a generator 5, an absorption cycle condenser 6, an absorption cycle throttle valve 7, an absorption cycle evaporator 8, a secondary condenser 9, a booster pump 10, an absorber 11, a solution pump 12, a solution heat exchanger 13, and a solution throttle valve 14; a condenser 15, a subcooler 16, a secondary throttle valve 17, a secondary evaporator 18, a secondary circulating compressor 19, a main throttle valve 20, a main evaporator 21, a main circulating compressor 22, a cold storage tank 23, an absorption circulating chilled water pump 24, a subcooling pump 25 and a secondary condensing pump 26;
an outlet of the heat collector 1 is connected with an inlet at the A end of the heat storage tank 3 through a first hot water pump 2; an outlet at the A end of the heat storage box 3 is connected with an inlet of the heat collector 1;
an outlet at the B end of the heat storage tank 3 is connected with a hot water side inlet of a generator 5 through a second hot water pump 4, and a hot water side outlet of the generator 5 is connected with an inlet at the B end of the heat storage tank 3;
a water vapor outlet of the generator 5 connected to a refrigerant-side inlet of the absorption cycle condenser 6; a refrigerant side outlet of the absorption cycle condenser 6 is connected with a refrigerant side inlet of the absorption cycle evaporator 8 through an absorption cycle throttle valve 7; the refrigerant side outlet of the absorption cycle evaporator 8 is connected with the refrigerant side inlet of the secondary condenser 9; the refrigerant side outlet of the secondary condenser 9 is connected with the liquid water inlet of the absorber 11 through a booster pump 10;
the solution outlet of the absorber 11 is connected with the low-temperature side inlet of the solution heat exchanger 13 through a solution pump 12, and the low-temperature side outlet of the solution heat exchanger 13 is connected with the solution inlet of the generator 5; the solution outlet of the generator 5 is connected with the high-temperature side inlet of the solution heat exchanger 13; the high-temperature side outlet of the solution heat exchanger 13 is connected with the solution inlet of the absorber 11 through a solution throttle valve 14;
a refrigerant side outlet of the condenser 15 is connected to a refrigerant side inlet of the subcooler 16;
the refrigerant side outlet of the subcooler 16 is divided into two branches: one branch is connected with a refrigerant side inlet of a secondary evaporator 18 through a secondary throttle valve 17, and a refrigerant side outlet of the secondary evaporator 18 is connected with a refrigerant side inlet of a condenser 15 through a secondary circulation compressor 19; one branch is connected with a refrigerant side inlet of a main-stage evaporator 21 through a main-stage throttle valve 20, and a refrigerant side outlet of the main-stage evaporator 21 is connected with a refrigerant side inlet of a condenser 15 through a main-stage circulating compressor 22;
the secondary condenser 9 is communicated with the chilled water side of the secondary evaporator 18, and a secondary condensing pump 26 is arranged on an inlet pipeline on the chilled water side of the secondary condenser 9;
the chilled water side of the absorption cycle evaporator 8 is connected with a first port 231 of the cold storage box 23, and an absorption cycle chilled water pump 24 is arranged on an inlet pipeline at the chilled water side of the absorption cycle evaporator 8;
the second port 232 connected with the cold storage tank 23 is connected with the chilled water side of the subcooler 16, and the supercooling pump 25 is arranged on the inlet pipeline of the chilled water side of the subcooler 16.
The lithium bromide solution in the generator 5 and the absorber 11 is circulated among the generator 5, the solution heat exchanger 13 and the absorber 11 by a solution pump 12; the water vapor evaporated by the lithium bromide solution in the generator 5 enters the absorption circulating condenser 6 to be condensed into liquid water and then is sent to the absorption circulating evaporator 8, the liquid water is evaporated into water vapor by the absorption circulating evaporator 8 and then is sent to the secondary condenser 9, the water vapor is condensed into liquid water by the secondary condenser 9, and finally the liquid water is sent to the absorber 11 through the booster pump 10. The secondary condenser 9 is a heat exchanger which condenses and absorbs the water vapor generated by the circulating evaporator 8 by using the medium-temperature cold energy.
The heat collector 1 is a solar photovoltaic photo-thermal integrated component.
The secondary circulation compressor 19 and the primary circulation compressor 22 are inverter compressors.
The booster pump 10 is a liquid water booster pump.
The operation method of a refrigerating system, it includes supplying power valley time operation step and supplying power peak section and flat time operation step; in the two operation steps, the main stage throttle valve 20, the main stage evaporator 21 and the main stage circulation compressor 22 in the vapor compression cycle are all in an opening and working state;
firstly, operating step of power supply valley period
A vapor compression cycle operation step:
the secondary throttle valve 17 and the secondary cycle compressor 19 are opened to make the primary and secondary vapor compression cycles in working condition and the corresponding condensation heat is discharged to the environment in the condenser 15;
in the main-stage steam compression cycle, the main-stage evaporator 21 generates 3-5 ℃ low-temperature refrigerating capacity for meeting the cold load required by the building; in the secondary steam compression cycle, the secondary evaporator 18 generates medium-temperature refrigerating capacity at 14-16 ℃, and the secondary condenser 9 is cooled by a secondary condensing pump 26, so that the water vapor generated in the absorption cycle evaporator 8 is condensed into liquid water in the secondary condenser 9; when the absorption cycle stops operating, synchronously closing the secondary cycle compressor 19, the secondary throttle valve 17 and the secondary condensate pump 26;
an absorption cycle operation step:
starting the second hot water pump 4, the absorption cycle throttle valve 7, the booster pump 10, the solution pump 12, the solution throttle valve 14, the absorption cycle chilled water pump 24 and the secondary condensation pump 26 to enable the absorption cycle to be in a working state;
the second hot water pump 4 sends 68-73 ℃ hot water stored in the heat storage box 3 into the generator 5 for heat supply, a lithium bromide solution in the generator 5 is heated, water in the lithium bromide solution is converted into water vapor to enter the absorption cycle condenser 6, the water vapor is condensed into liquid water at 40 ℃ under the cooling of external cooling water, the liquid water is throttled by the absorption cycle throttle valve 7 and then evaporated and absorbed heat at 22-24 ℃ on the refrigerant side of the absorption cycle evaporator 8, the first port 231 outlet of the cold storage box 23 enters 31-33 ℃ water on the chilled water side of the absorption cycle evaporator 8, the water is cooled to 24-26 ℃ and then sent back to the first port 231 inlet, and the valley section is supplied with cold through the cold storage box 23;
the water vapor generated by evaporation in the absorption circulating evaporator 8 enters a secondary condenser 9 to be condensed into liquid water at 24 ℃, the liquid water enters an absorber 11 after being pressurized by a booster pump 10 for 1.8-2 kPa and is mixed with the lithium bromide solution in the absorber 11, and the mass concentration of the solution in the absorber 11 is reduced to 30-31.5% from 42-45.1% of the conventional non-pressurized absorption circulation due to the secondary condensation and pressurization; due to the pressurization of the booster pump 10, the deflation range of the supercharged absorption refrigeration cycle is increased by 0.136 compared with the conventional non-supercharged cycle, and the relative increase rate is about 800%, so that the working condition range of the absorption cycle heat source is effectively widened, and the working condition performance of the low-temperature heat source is obviously improved.
The dilute solution in the absorber 11 enters the solution heat exchanger 13 under the driving of the solution pump 12, the dilute solution at the low-temperature side is heated to 46-47.2 ℃ by the concentrated solution at the high-temperature side, then enters the generator 5, is heated to generate water vapor, the temperature is raised to 59-60 ℃, the concentration is increased to 45-46.8%, then the dilute solution enters the high-temperature side of the solution heat exchanger 13 through the concentrated solution outlet and is cooled by the dilute solution at the low-temperature side, and the dilute solution is throttled by the solution throttle valve 14 and then cooled to 44-45.4 ℃ and returns to the absorber 11 to be mixed with the lithium bromide solution therein;
when the temperature of the top layer of the heat storage tank 3 is low and the absorption cycle can not work any more, closing the second hot water pump 4, the absorption cycle throttling valve 7, the booster pump 10, the solution pump 12, the solution throttling valve 14, the absorption cycle chilled water pump 24 and the secondary condensation pump 26 to stop the absorption cycle, and synchronously closing the secondary throttling valve 17 and the secondary cycle compressor 19;
second, operation steps in peak period and flat period of power supply
A vapor compression cycle operation step:
the secondary recycle compressor 19, secondary throttle 17 and secondary condensate pump 26 are closed;
the main-stage throttle valve 20 and the main-stage circulating compressor 22 keep working states, and meanwhile, the supercooling pump 25 is started to enable cold water at the temperature of 24-26 ℃ in the cold storage tank 23 to enter the chilled water side of the subcooler 16 through the outlet of the second port 232, so that the refrigerant at the temperature of 40 ℃ at the refrigerant side outlet of the condenser 15 is subcooled to be 28-30.2 ℃ in the subcooler 16, and further the purpose of saving energy consumption of a power supply peak section by utilizing medium-temperature cold energy prepared by solar heat and electric energy of a power supply valley section is achieved; when the cold storage box 23 finishes the cold release, the supercooling pump 25 is closed;
the operation of the heat collector:
when the solar radiation is higher than the starting condition of the heat collector 1, the first hot water pump 2 is started to send the water in the heat storage tank 3 into the heat collector 1, and the solar heat is collected.
As described above, the present invention can be preferably realized.
The embodiments of the present invention are not limited to the above-described embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be construed as equivalents thereof, and they are included in the scope of the present invention.
Claims (6)
1. The utility model provides a refrigerating system based on secondary condensation pressure boost is absorbed and subcooling compression which characterized in that includes following adapting unit, connects including the tube coupling between each part: the heat collector (1), the first hot water pump (2), the heat storage tank (3) and the second hot water pump (4); a generator (5), an absorption cycle condenser (6), an absorption cycle throttle valve (7), an absorption cycle evaporator (8), a secondary condenser (9), a booster pump (10), an absorber (11), a solution pump (12), a solution heat exchanger (13) and a solution throttle valve (14); the system comprises a condenser (15), a subcooler (16), a secondary throttle valve (17), a secondary evaporator (18), a secondary circulating compressor (19), a primary throttle valve (20), a primary evaporator (21), a primary circulating compressor (22), a cold storage tank (23), an absorption circulating chilled water pump (24), an supercooling pump (25) and a secondary condensing pump (26);
an outlet of the heat collector (1) is connected with an inlet at the A end of the heat storage tank (3) through a first hot water pump (2); an outlet at the A end of the heat storage box (3) is connected with an inlet of the heat collector (1);
an outlet at the B end of the heat storage tank (3) is connected with an inlet at the hot water side of the generator (5) through a second hot water pump (4), and an outlet at the hot water side of the generator (5) is connected with an inlet at the B end of the heat storage tank (3);
a water vapor outlet of the generator (5) is connected with a refrigerant side inlet of the absorption cycle condenser (6); a refrigerant side outlet of the absorption cycle condenser (6) is connected with a refrigerant side inlet of an absorption cycle evaporator (8) through an absorption cycle throttle valve (7); a refrigerant side outlet of the absorption cycle evaporator (8) is connected with a refrigerant side inlet of the secondary condenser (9); a refrigerant side outlet of the secondary condenser (9) is connected with a liquid water inlet of an absorber (11) through a booster pump (10);
a solution outlet of the absorber (11) is connected with a low-temperature side inlet of the solution heat exchanger (13) through a solution pump (12), and a low-temperature side outlet of the solution heat exchanger (13) is connected with a solution inlet of the generator (5); the solution outlet of the generator (5) is connected with the high-temperature side inlet of the solution heat exchanger (13); the high-temperature side outlet of the solution heat exchanger (13) is connected with the solution inlet of the absorber (11) through a solution throttle valve (14);
a refrigerant side outlet of the condenser (15) is connected with a refrigerant side inlet of the subcooler (16);
the refrigerant side outlet of the subcooler (16) is divided into two branches: one branch is connected with a refrigerant side inlet of a secondary evaporator (18) through a secondary throttling valve (17), and a refrigerant side outlet of the secondary evaporator (18) is connected with a refrigerant side inlet of a condenser (15) through a secondary circulation compressor (19); one branch is connected with a refrigerant side inlet of a main-stage evaporator (21) through a main-stage throttle valve (20), and a refrigerant side outlet of the main-stage evaporator (21) is connected with a refrigerant side inlet of a condenser (15) through a main-stage circulating compressor (22);
the secondary condenser (9) is communicated with the chilled water side of the secondary evaporator (18), and a secondary condensing pump (26) is arranged on an inlet pipeline on the chilled water side of the secondary condenser (9);
the freezing water side of the absorption cycle evaporator (8) is connected with a first port (231) of the cold storage box (23), and an absorption cycle freezing water pump (24) is arranged on an inlet pipeline of the freezing water side of the absorption cycle evaporator (8);
the second port (232) of the cold storage tank (23) is connected with the chilled water side of the subcooler (16), and an inlet pipeline at the chilled water side of the subcooler (16) is provided with a supercooling pump (25).
2. A refrigeration system based on secondary condensation pressure-increasing absorption and subcooling compression as described in claim 1, wherein: the lithium bromide solution in the generator (5) and the absorber (11) is circulated among the generator (5), the solution heat exchanger (13) and the absorber (11) through a solution pump (12); the water vapor evaporated by the lithium bromide solution in the generator (5) enters the absorption circulating condenser (6) to be condensed into liquid water, and then the liquid water is sent to the absorption circulating evaporator (8), the liquid water is evaporated into the water vapor by the absorption circulating evaporator (8) and then sent to the secondary condenser (9), the water vapor is condensed into the liquid water by the secondary condenser (9), and finally the liquid water is sent back to the absorber (11) through the booster pump (10).
3. A refrigeration system based on secondary condensation pressure-increasing absorption and subcooling compression as described in claim 2, wherein: the heat collector (1) is a solar photovoltaic photo-thermal integrated component.
4. A refrigeration system based on secondary condensation pressure-increasing absorption and subcooling compression as described in claim 3, wherein: the secondary circulation compressor (19) and the main circulation compressor (22) are frequency conversion compressors.
5. A refrigeration system based on secondary condensation pressure-increasing absorption and subcooling compression as described in claim 4, wherein: the booster pump (10) is a liquid water booster pump.
6. A method for operating a refrigeration system, which is characterized by being implemented by the refrigeration system based on secondary condensation pressure boost absorption and supercooling compression as claimed in claim 3, and comprising a power supply valley period operation step and a power supply peak period and flat period operation step; in the two operation steps, a main stage throttle valve (20), a main stage evaporator (21) and a main stage cycle compressor (22) in the vapor compression cycle are all in an opening and working state;
firstly, operating step of power supply valley period
A vapor compression cycle operation step:
opening a secondary throttle valve (17) and a secondary cycle compressor (19) to enable the primary and secondary vapor compression cycles to be in working condition, and discharging corresponding condensation heat to the environment at a condenser (15);
in the main-stage steam compression cycle, the main-stage evaporator (21) generates low-temperature refrigerating capacity of 3-5 ℃ for meeting the cold load required by the building; in the secondary steam compression cycle, a secondary evaporator (18) generates medium-temperature refrigerating capacity at 14-16 ℃, and a secondary condenser (9) is cooled by a secondary condensing pump (26), so that water vapor generated in an absorption cycle evaporator (8) is condensed into liquid water in the secondary condenser (9); synchronously closing the secondary circulation compressor (19), the secondary throttle valve (17) and the secondary condensation pump (26) when the absorption circulation stops working;
an absorption cycle operation step:
starting a second hot water pump (4), an absorption cycle throttling valve (7), a booster pump (10), a solution pump (12), a solution throttling valve (14), an absorption cycle chilled water pump (24) and a secondary condensation pump (26) to enable an absorption cycle to be in a working state;
the second hot water pump (4) sends hot water at 68-73 ℃ stored in the heat storage box (3) into the generator (5) for heating, a lithium bromide solution in the generator (5) is heated, water in the lithium bromide solution is converted into water vapor to enter the absorption cycle condenser (6), the water vapor is condensed into liquid water at 40 ℃ under the cooling of external cooling water, the liquid water is throttled by the absorption cycle throttle valve (7) and then evaporated and absorbed at 22-24 ℃ on the refrigerant side of the absorption cycle evaporator (8), the outlet of the first port (231) of the cold storage box (23) enters 31-33 ℃ water on the frozen water side of the absorption cycle evaporator (8) and is cooled to 24-26 ℃ and then is sent back to the inlet of the first port (231), and the cold storage of a valley section through the cold storage box (23) is realized;
the water vapor generated by evaporation in the absorption circulating evaporator (8) enters a secondary condenser (9) to be condensed into liquid water at 24 ℃, the liquid water enters an absorber (11) after being pressurized by a booster pump (10) for 1.8-2 kPa and is mixed with the lithium bromide solution in the absorber (11), and the mass concentration of the solution in the absorber (11) is reduced to 30-31.5% from 42-45.1% of the conventional non-pressurized absorption circulation due to secondary condensation and pressurization;
the dilute solution in the absorber (11) enters a solution heat exchanger (13) under the drive of a solution pump (12), the dilute solution at the low-temperature side is heated to 46-47.2 ℃ by the concentrated solution at the high-temperature side and then enters a generator (5), water vapor is generated after the dilute solution is heated, the temperature is raised to 59-60 ℃, the concentration is increased to 45-46.8%, then the dilute solution enters the high-temperature side of the solution heat exchanger (13) through a concentrated solution outlet and is cooled by the dilute solution at the low-temperature side, and the dilute solution is throttled by a solution throttle valve (14) and then cooled to 44-45.4 ℃ and returns to the absorber (11) to be mixed with the lithium bromide solution;
when the temperature of the top layer of the heat storage box (3) is low and the absorption cycle can not work any more, closing the second hot water pump (4), the absorption cycle throttling valve (7), the booster pump (10), the solution pump (12), the solution throttling valve (14), the absorption cycle chilled water pump (24) and the secondary condensation pump (26) to enable the absorption cycle to be in a stop working state, and synchronously closing the secondary throttling valve (17) and the secondary cycle compressor (19);
second, operation steps in peak period and flat period of power supply
A vapor compression cycle operation step:
the secondary circulation compressor (19), the secondary throttle valve (17) and the secondary condensate pump (26) are closed;
the main-stage throttle valve (20) and the main-stage circulating compressor (22) keep working states, and meanwhile, the supercooling pump (25) is started to enable 24-26 ℃ cold water in the cold storage tank (23) to enter the freezing water side of the subcooler (16) through the outlet of the second port (232), so that the 40 ℃ refrigerant at the refrigerant side outlet of the condenser (15) is subcooled to 28-30.2 ℃ in the subcooler (16), and further the purpose of saving energy consumption of a power supply peak section by utilizing the medium-temperature cold energy prepared by solar heat and power supply valley section electric energy is achieved; when the cold storage box (23) finishes cold release, the supercooling pump (25) is closed;
the operation of the heat collector:
when the solar radiation is higher than the starting condition of the heat collector (1), the first hot water pump (2) is started to send the water in the heat storage tank (3) into the heat collector (1) to collect solar heat.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112629067A (en) * | 2020-10-28 | 2021-04-09 | 华南理工大学 | Two-stage compression composite refrigeration system with parallel thermal compression and mechanical compression and method thereof |
| CN113587471A (en) * | 2021-06-21 | 2021-11-02 | 东南大学 | Cold and hot confession system that allies oneself with of doublestage compression and absorption formula high temperature heat pump complex |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004190886A (en) * | 2002-12-09 | 2004-07-08 | Ebara Corp | Absorption refrigerating machine and absorption refrigerating system |
| CN102230686A (en) * | 2011-06-12 | 2011-11-02 | 浙江理工大学 | Lithium bromide absorption-compression type series boosting refrigeration/heating pump system |
| CN108106050A (en) * | 2018-01-15 | 2018-06-01 | 江苏乐科节能科技股份有限公司 | The refrigeration system and method for chilled water are produced using low-grade exhaust heat |
| CN109883079A (en) * | 2019-03-18 | 2019-06-14 | 华南理工大学 | A kind of absorption compression interactive cold type composite refrigeration system and method again |
| US10337771B2 (en) * | 2015-12-30 | 2019-07-02 | King Fahd University Of Petroleum And Minerals | Closed loop solar refrigeration system |
| CN110056936A (en) * | 2019-04-24 | 2019-07-26 | 东北大学 | A kind of low ebb electric heat storage cascade type heat pump heating system and mode |
-
2019
- 2019-11-22 CN CN201911156542.7A patent/CN110906582B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004190886A (en) * | 2002-12-09 | 2004-07-08 | Ebara Corp | Absorption refrigerating machine and absorption refrigerating system |
| CN102230686A (en) * | 2011-06-12 | 2011-11-02 | 浙江理工大学 | Lithium bromide absorption-compression type series boosting refrigeration/heating pump system |
| US10337771B2 (en) * | 2015-12-30 | 2019-07-02 | King Fahd University Of Petroleum And Minerals | Closed loop solar refrigeration system |
| CN108106050A (en) * | 2018-01-15 | 2018-06-01 | 江苏乐科节能科技股份有限公司 | The refrigeration system and method for chilled water are produced using low-grade exhaust heat |
| CN109883079A (en) * | 2019-03-18 | 2019-06-14 | 华南理工大学 | A kind of absorption compression interactive cold type composite refrigeration system and method again |
| CN110056936A (en) * | 2019-04-24 | 2019-07-26 | 东北大学 | A kind of low ebb electric heat storage cascade type heat pump heating system and mode |
Non-Patent Citations (3)
| Title |
|---|
| LIMING LIU等: "Energetic, economic and environmental study of cooling capacity for", 《ENERGY CONVERSION AND MANAGEMENT》 * |
| 吴业正: "《制冷原理及设备（第4版）》", 31 December 2015 * |
| 谢国珍: "溴化锂吸收式制冷机亚稳平衡增压吸收试验和机理", 《化工学报》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112629067A (en) * | 2020-10-28 | 2021-04-09 | 华南理工大学 | Two-stage compression composite refrigeration system with parallel thermal compression and mechanical compression and method thereof |
| CN113587471A (en) * | 2021-06-21 | 2021-11-02 | 东南大学 | Cold and hot confession system that allies oneself with of doublestage compression and absorption formula high temperature heat pump complex |
| CN113587471B (en) * | 2021-06-21 | 2022-06-28 | 东南大学 | Double-stage compression and absorption type high-temperature heat pump combined cold and heat combined supply system |
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