CN108050571B - Single-stage balanced ammonia-water reabsorption heat pump circulation equipment and heating method - Google Patents
Single-stage balanced ammonia-water reabsorption heat pump circulation equipment and heating methodDownload PDFInfo
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- CN108050571B CN108050571BCN201711230635.0ACN201711230635ACN108050571BCN 108050571 BCN108050571 BCN 108050571BCN 201711230635 ACN201711230635 ACN 201711230635ACN 108050571 BCN108050571 BCN 108050571B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D3/00—Hot-water central heating systems
- F24D3/18—Hot-water central heating systems using heat pumps
- 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
- F25B15/04—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being ammonia evaporated from aqueous solution
- 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
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
- 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
- F25B35/02—Boiler-absorbers, i.e. boilers usable for absorption or adsorption using a liquid as sorbent, e.g. brine
- 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
- 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]
- Y02B30/12—Hot water central heating systems using heat pumps
- 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
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- Mechanical Engineering (AREA)
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- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
Translated fromChinese
Description
Technical Field
The invention relates to the field of solar heat utilization and heat pump air conditioning, in particular to single-stage balanced ammonia-water re-absorption heat pump circulating equipment and a heat supply method.
Background
China is the first energy consuming country and CO of the world2The countries with the largest discharge amount face a severe pressure of energy conservation and emission reduction. The rapid development of renewable energy sources such as solar energy and the like is an important direction for coping with climate change, promoting energy conservation and emission reduction and relieving environmental pollution.
At present, the development and utilization modes of solar energy are single, and most of the solar energy is low-temperature hot water. Solar heating, refrigeration, industrial heating and solar thermal power generation have been applied, but are far from reaching the scale. In various implementation modes of solar heating, the heat pump driven by the heat energy generated by the solar heat collector under given conditions has better heat supply efficiency, and theoretically 80% of solar radiation energy can be converted into heat supply capacity.
Through the published literature search of the prior art, the problems that the heating of the current solar heat pump is still unstable and inefficient are found. The solar energy density is low, and the solar radiation is intermittent and unstable due to day and night and weather changes. But the heating requirement is stable and reliable; the low ambient temperature in winter, the sunshine time is short, can cause solar energy system heat waste to increase, and the thermal-arrest temperature is not high, but the efficiency reduction can lead to can not satisfying the heating load requirement. Theoretically, a conventional absorption and adsorption heat pump driven by heat energy can be used for heating in combination with a solar heat collector, but the traditional absorption or adsorption heat pump cycle using water as a working medium cannot meet the requirement of a low-temperature refrigeration environment, a heat pump system using low-boiling point working media such as ammonia and the like requires high driving heat source temperature (generally higher than 120 ℃), and the driving working time is short or the starting is difficult completely depending on the driving of the solar heat collector.
The invention replaces the evaporator and the condenser in the traditional absorption heat pump cycle with the low pressure generator and the high pressure absorber, gets rid of the limitation of the cycle working pressure difference of the absorption heat pump by the condensing pressure and the evaporating pressure of the refrigerant, greatly reduces the working pressure and the high and low pressure difference of the system, and enhances the adaptability to the temperature change of the driving heat source. Meanwhile, compared with the traditional ammonia-water absorption cycle, the method reduces the rectification link and has simpler and more compact system structure.
Disclosure of Invention
Due to the technical defects of solar heat pump heating, the invention aims to provide single-stage balanced ammonia-water reabsorption heat pump circulation equipment which can be driven by solar energy for a long time and can work in a lower-temperature environment and is driven by low-temperature solar heat (70-100 ℃), and a method for applying the circulation equipment to indoor heat supply.
The invention provides single-stage balanced ammonia-water re-absorption heat pump circulating equipment which comprises a solution loop, a refrigerant steam pipeline, a water supply and return pipeline and a driving heat source. The solution loop comprises a high-pressure generator (generator with highest pressure), a high-pressure absorber (absorber with highest pressure), a low-temperature solution heat exchanger, a low-pressure generator (generator with lowest pressure), a low-pressure absorber (absorber with lowest pressure) and a high-temperature solution heat exchanger, wherein a solution separation tank is connected between the high-pressure generator and the high-pressure absorber, a first throttle valve is connected between the low-temperature solution heat exchanger and the low-pressure generator, a second throttle valve is connected between the high-temperature solution heat exchanger and the low-pressure absorber, a solution mixing tank is connected between the low-pressure generator and the low-pressure absorber, and a solution circulating pump is connected between the solution separation tank and the high-temperature solution heat exchanger; the refrigerant vapor lines include a high pressure refrigerant vapor line (the highest pressure refrigerant vapor line) and a low pressure refrigerant vapor line (the lowest pressure refrigerant vapor line); the water supply and return pipeline comprises a water supply pipeline and a water return pipeline; the driving heat sources are classified into a high-temperature driving heat source (a heat source driving a high-temperature generator) and a low-temperature driving heat source (a heat source driving a low-temperature generator).
The working medium for the solution loop operation of the single-stage balanced ammonia-water re-absorption heat pump circulating equipment is ammonia solution; the working medium for the operation of the refrigerant steam pipeline is ammonia steam; the working medium running in the water supply and return pipeline is water. Specifically, the single-stage balanced ammonia-water re-absorption heat pump circulating equipment has 10 working media which run simultaneously and comprises 2 ammonia steam, 7 ammonia solution and 1 water (namely, water supply and return). The 2 strands of ammonia steam comprise high-temperature high-pressure ammonia steam HV generated by a high-pressure generator and low-temperature low-pressure ammonia steam LV generated by a low-pressure generator; the 7 strands of solutions comprise a dilute solution A generated by a high-pressure generator, a concentrated solution B generated by a low-pressure absorber, a concentrated solution C generated by a high-pressure absorber, a dilute solution D generated by the low-pressure generator, a solution E generated by mixing the dilute solution B and the solution D, and solutions F and G which respectively enter the high-pressure generator and the high-pressure absorber after passing through a solution separation tank; 1 share of water is the supply water SW and the return water RW.
The refrigerant vapor pipeline is connected in a way that an inlet and an outlet of the high-pressure ammonia vapor pipeline are respectively connected with the high-pressure generator and the high-pressure absorber; the inlet and outlet of the low-pressure ammonia vapor pipeline are respectively connected with the low-pressure generator and the low-pressure absorber.
The connection mode of the water supply and return pipeline is as follows: the water return pipeline is connected with an outlet at the indoor heat exchange end and penetrates through the low-pressure absorber to be connected with the high-pressure absorber, an inlet of the water supply pipeline is connected with the high-pressure absorber, and an inlet of the water supply pipeline is connected with an inlet at the indoor heat exchange end.
The high-temperature driving heat source in the invention is solar heat of 70-100 ℃ generated by CPC (Compound Parabolic Collector)/ETC (Evacuated Tube Collector), and the heat of a gas furnace is used as a standby high-temperature driving heat source; the low-temperature driving heat source is ambient heat or waste heat at the temperature of not less than-10 ℃, and the standby low-temperature driving heat source is solar heat at the temperature of 10-35 ℃. The working mode can be switched according to the ambient temperature, when the ambient temperature is not lower than-10 ℃, the CPC/ETC is used as a high-temperature driving heat source, namely, the CPC/ETC works in the high-temperature driving mode, heat generated by the high-temperature driving heat source exchanges heat with ammonia solution in a high-temperature generator, and the low-temperature generator provides heat by a low-temperature driving heat source, namely ambient air heat or waste heat; when the ambient temperature is lower than-10 ℃, the CPC/ETC is used as a low-temperature driving heat source, namely, the low-temperature driving mode is switched, the heat generated by the low-temperature driving heat source exchanges heat with ammonia solution in the low-temperature generator, and the high-temperature generator supplies heat by a standby high-temperature driving heat source, namely, a gas furnace.
The method for supplying heat by using the single-stage balanced ammonia-water re-absorption heat pump circulating equipment comprises the working operation process of an ammonia solution loop, an ammonia steam pipeline, a water supply and return pipeline and a driving heat source.
The working operation process of the solution loop and the ammonia vapor pipeline is that the ammonia solution at the inlet of the high-pressure generator exchanges heat with a driving heat source in the high-pressure generator, the temperature rises, high-temperature high-pressure ammonia vapor HV is separated out, and the ammonia solution becomes dilute solution A; the dilute solution A from the high-pressure generator flows through the high-temperature solution heat exchanger to exchange heat with the solution E and reduce the temperature, and then the pressure is reduced through the throttle valve and enters the low-pressure absorber; the concentrated solution C from the high-pressure absorber flows through the low-temperature solution heat exchanger to exchange heat with the solution E and reduce the temperature, then flows through the throttle valve to reduce the pressure, and enters the low-pressure generator; and after the low-pressure generator inlet solution exchanges heat with the low-temperature driving heat source in the low-pressure generator, the temperature rises to become a dilute solution D, and low-temperature low-pressure ammonia vapor LV is separated out. Fully mixing the dilute solution D at the outlet of the low-pressure generator with the concentrated solution B at the outlet of the low-pressure absorber in a solution mixing tank to generate a solution E; the solution E flows through the low-temperature solution heat exchanger to exchange heat with the solution C, then flows through the high-temperature solution heat exchanger to exchange heat with the solution A, and is sent into the solution separation tank by the solution circulating pump; the solution at the outlet of the solution separation tank is divided into two paths, the solution F flows into the high-pressure generator, and the solution G flows into the high-pressure absorber. The process of absorbing ammonia vapor in the high-pressure absorber and the low-pressure absorber is a non-isothermal process, heat exchange exists, the temperature of the concentrated solution C at the outlet of the high-pressure absorber can be lower than the temperature of water supply flowing out of the high-pressure absorber, and the temperature of the concentrated solution C at the outlet of the low-pressure absorber can be lower than the temperature of return water flowing out of the low-pressure absorber.
The working operation process of the water supply and return pipeline is as follows: a water supply process: the ammonia solution G of the high-pressure absorber absorbs the heat released by the high-temperature high-pressure ammonia steam HV from the high-pressure generator, and the heat is exchanged with the water supply pipeline to generate water supply; indoor heat supply process: the water supply from the high-pressure absorber exchanges heat with the indoor heat exchange tail end; a water return process: the temperature of the supplied water is reduced to return water after passing through the indoor heat exchange terminal, the return water enters the low-pressure absorber, the dilute ammonia solution A of the low-pressure absorber absorbs the heat released by the low-temperature low-pressure ammonia steam from the low-pressure generator, the heat is exchanged with a return water pipeline, and the return water continues to enter the high-pressure absorber to complete a cycle heat supply process.
Compared with the prior art, the invention has the following beneficial effects: the low-pressure generator and the high-pressure absorber respectively replace an evaporator and a condenser in the traditional absorption heat pump cycle, and the limitation that the cycle working pressure difference of the absorption heat pump is limited by the condensing pressure and the evaporating pressure of a refrigerant is eliminated; the ammonia-water working medium is adopted, and the established cycle is suitable for heating in a low-temperature environment in winter; the condition limitation of saturated vapor pressure at the evaporation and condensation temperature of a single pure working medium is eliminated, and the working pressure difference is small; the temperature range of the working heat source is wider by controlling the concentration difference to operate; a rectifying device is not needed, only one solution circulating pump is needed, and the system has simple and compact structure, simple manufacturing process and low investment cost.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, the features and the effects of the present invention.
Drawings
FIG. 1 is a schematic diagram of a single stage balanced ammonia-water re-absorption heat pump cycle plant of the present invention operating in a mode where solar energy is used as the high temperature driving heat source;
FIG. 2 is a schematic diagram of a single stage balanced ammonia-water re-absorption heat pump cycle apparatus of the present invention operating in a solar low temperature driven heat source mode;
FIG. 3a is a schematic diagram of the operation of the refrigerant line of the single-stage balanced ammonia-water re-absorption heat pump cycle device of the present invention with high-temperature and high-pressure ammonia vapor HV;
FIG. 3b is a schematic diagram of the operation of the refrigerant line low temperature and low pressure ammonia vapor LV of the single stage balanced ammonia-water re-absorption heat pump cycle device of the present invention;
FIG. 4 is a schematic diagram of the solution loop operation of the single stage balanced ammonia-water re-absorption heat pump circulating device of the present invention;
FIG. 5 is a schematic diagram illustrating the operation of the single-stage balanced ammonia-water re-absorption heat pump circulating equipment of the present invention with supply and return water;
Detailed Description
The structural schematic diagram of the single-stage balanced ammonia-water re-absorption heat pump circulating equipment provided by the invention is shown in fig. 1 or fig. 2, and the single-stage balanced ammonia-water re-absorption heat pump circulating equipment comprises a solution loop, a refrigerant steam pipeline, a water supply and return pipeline and a driving heat source.
The working medium for the solution loop operation of the single-stage balanced ammonia-water re-absorption heat pump circulating equipment is ammonia solution; the working medium for the operation of the refrigerant steam pipeline is ammonia steam; the working medium running in the water supply and return pipeline is water. Specifically, the single-stage balanced ammonia-water re-absorption heat pump circulating equipment has 10 working media which run simultaneously and comprises 2 ammonia steam, 7 ammonia solution and 1 water (namely, water supply and return). The 2 strands of ammonia steam comprise high-temperature high-pressure ammonia steam HV generated by a high-pressure generator and low-temperature low-pressure ammonia steam LV generated by a low-pressure generator; the 7 strands of solutions comprise a dilute solution A generated by a high-pressure generator, a concentrated solution B generated by a low-pressure absorber, a concentrated solution C generated by a high-pressure absorber, a dilute solution D generated by the low-pressure generator, a solution E generated by mixing the dilute solution B and the solution D, and solutions F and G which respectively enter the high-pressure generator and the high-pressure absorber after passing through a solution separation tank; 1 share of water is the supply water SW and the return water RW.
The refrigerant vapor pipeline is connected in a way that an inlet and an outlet of the high-pressure ammonia vapor pipeline are respectively connected with the high-pressure generator and the high-pressure absorber; the inlet and outlet of the low-pressure ammonia vapor pipeline are respectively connected with the low-pressure generator and the low-pressure absorber.
The connection mode of the water supply and return pipeline is as follows: the water return pipeline is connected with an outlet at the indoor heat exchange end and penetrates through the low-pressure absorber to be connected with the high-pressure absorber, an inlet of the water supply pipeline is connected with the high-pressure absorber, and an outlet of the water supply pipeline is connected with an inlet at the indoor heat exchange end.
The solution loop comprises a high-pressure generator 1, a high-pressure absorber 2, a low-temperaturesolution heat exchanger 11, a low-pressure generator 3, a low-pressure absorber 4 and a high-temperaturesolution heat exchanger 10 which are sequentially connected, wherein asolution separation tank 8 is connected between the high-pressure generator 1 and the high-pressure absorber 2, afirst throttle valve 5 is connected between the low-temperaturesolution heat exchanger 11 and the low-pressure generator 3, asecond throttle valve 6 is connected between the high-temperaturesolution heat exchanger 10 and the low-pressure absorber 4, asolution mixing tank 7 is connected between the low-pressure generator 3 and the low-pressure absorber 4, and asolution circulating pump 9 is connected between the solution separation tank; the ammonia vapor line comprises a high pressure ammoniavapor HV line 12 and a low pressure ammoniavapor LV line 13; thewater supply pipeline 14 and thewater return pipeline 15 form a water supply and return pipeline; the driving heat source is divided into a high-temperature driving heat source and a low-temperature driving heat source.
The heat supply method by using the single-stage balanced ammonia-water re-absorption heat pump circulating equipment provided by the invention comprises the working operation processes of a solution loop, an ammonia steam pipeline, a water supply and return pipeline and a driving heat source. The ammonia vapor line operation is divided into two parts, as shown in fig. 3a, the high-temperature and high-pressure ammonia vapor HV is generated by the high-pressure generator 1 and flows into the high-pressure absorber 2 via the high-pressureammonia vapor line 12 to be absorbed, and as shown in fig. 3b, the low-temperature and low-pressure ammonia vapor LV is generated by the low-pressure generator 3 and flows into the low-pressure absorber 4 via the low-pressureammonia vapor line 13 to be absorbed.
The operation of the solution loop is shown in fig. 4, and the ammonia solution flows out of thehigh pressure generator 1 and the high pressure absorber 2, respectively, then flows through the high temperaturesolution heat exchanger 10, thethrottle valve 6, the low temperaturesolution heat exchanger 11, thethrottle valve 5, respectively, and enters the low pressure absorber 4 and thelow pressure generator 3, respectively. The solution flowing out of thelow pressure generator 3 and the low pressure absorber 4 is mixed in the solution mixingtank 7, then flows through the low temperaturesolution heat exchanger 11 and the high temperaturesolution heat exchanger 10 in sequence, is finally sent into thesolution separation tank 8 by thesolution circulating pump 9, and then is divided into two paths according to a certain flow ratio to enter thehigh pressure generator 1 and the high pressure absorber 2, so that a complete solution circulation process is formed.
The operation of the water supply and return line is shown in fig. 5. The water supply SW flows into the indoor heatexchange tail end 17 through thewater supply pipeline 14 to release heat and then generates return water RW, and the return water RW flows into the high-pressure absorber 2 through the low-pressure absorber 4 through thereturn pipeline 15 to absorb heat, so that a complete heat supply circulation process is formed.
In order to achieve efficient and continuous heat supply effects, the single-stage balanced ammonia-water re-absorption heat pump circulation equipment and the heat supply method have two operation modes, namely the operation modes in which solar energy is respectively used as a high-temperature driving heat source and a low-temperature driving heat source, and the two operation modes are switched according to the ambient temperature. As shown in fig. 1 and 2, the thick arrows indicate the heat transfer direction of the components, the arrows on the solid lines indicate the flow direction of the solution, the supply water, the return water or the heat collecting working medium, the arrows in the long dashed lines indicate the flow direction of the ammonia vapor in the heat pump system, and the short dashed lines indicate the pipelines which are not used in the operation mode.
As shown in fig. 1, when the environmental temperature is not lower than-10 ℃, the single-stage balanced ammonia-water re-absorption heat pump circulation equipment of the invention operates in the high-temperature driving heat source operation mode, the operation process of the solution, ammonia vapor and water supply and return water is as described above, the CPC/ETC solar heat collection temperature reaches 70-100 ℃, the heat collection working medium flows into the high-pressure generator 1, the heat is transferred to the ammonia solution in the high-pressure generator 1 through the heat exchange pipeline for heating, and the high-pressure generation process is completed. The low pressure generation process is driven by the low-temperature heat energy of the environment.
As shown in fig. 2, when the environmental temperature is lower than-10 ℃, the flow conditions of the ammonia solution, the ammonia vapor and the water supply and return are the same as those in the first operation mode under the low-temperature driving heat source operation mode of the single-stage balanced ammonia-water re-absorption heat pump circulation equipment of the invention, the solar heat collection temperature is lower (10-35 ℃), the heat collection working medium flows into the low-pressure generator 3, the heat is transferred to the ammonia solution in the low-pressure generator 3 through the heat exchange pipeline for heating, the low-pressure generation process is completed, and the high-pressure generation process is assisted to be driven by thegas furnace 16.
The foregoing detailed description of the preferred embodiments of the invention has been presented. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the present teachings without departing from the inventive concepts. Therefore, the technical solutions available to those skilled in the art through logic analysis, reasoning and limited experiments based on the prior art according to the concept of the present invention should be within the scope of protection defined by the claims.
Claims (8)
1. The single-stage balanced ammonia-water re-absorption heat pump circulating equipment is characterized by comprising a solution loop, a refrigerant steam pipeline, a water supply and return pipeline and a driving heat source;
the solution loop comprises a high-pressure generator (1), a high-pressure absorber (2), a low-temperature solution heat exchanger (11), a low-pressure generator (3), a low-pressure absorber (4) and a high-temperature solution heat exchanger (10), wherein a solution separation tank (8) is connected between the high-pressure generator (1) and the high-pressure absorber (2), a first throttling valve (5) is connected between the low-temperature solution heat exchanger (11) and the low-pressure generator (3), a second throttling valve (6) is connected between the high-temperature solution heat exchanger (10) and the low-pressure absorber (4), a solution mixing tank (7) is connected between the low-pressure generator (3) and the low-pressure absorber (4), and a solution circulating pump (9) is connected between the solution separation tank (8) and the high-temperature solution heat exchanger (10);
the refrigerant vapor lines include a high pressure refrigerant vapor line (12) and a low pressure refrigerant vapor line (13); the water supply and return pipeline comprises a water supply pipeline (14) and a water return pipeline (15); the driving heat source comprises a high-temperature driving heat source and a low-temperature driving heat source; the two ends of the high-pressure refrigerant steam pipeline (12) are respectively connected with the high-pressure generator (1) and the high-pressure absorber (2), and a rectifying device is not contained; both ends of the low-pressure refrigerant steam pipeline (13) are respectively connected with the low-pressure generator (3) and the low-pressure absorber (4), and a rectifying device is not contained; the both ends of water supply line (14) are connected respectively high pressure absorber (2) and indoor heat transfer are terminal (17), the both ends of return water pipeline (15) are connected respectively indoor heat transfer are terminal (17) with low pressure absorber (4), low pressure absorber (4) with high pressure absorber (2) link to each other.
2. The single-stage balanced ammonia-water re-absorption heat pump cycle equipment as claimed in claim 1, wherein the working medium of the solution loop is ammonia solution; the working medium of the refrigerant steam pipeline is ammonia water steam; the working medium in the water supply and return pipeline is water.
3. The single-stage balanced ammonia-water reabsorption heat pump cycle apparatus according to claim 1, wherein said high-temperature driving heat source is 70-100 ℃ solar heat generated by CPC/ETC (18), and said low-temperature driving heat source is low-temperature ambient heat or waste heat of not less than-10 ℃.
4. The single-stage balanced ammonia-water re-absorption heat pump cycle equipment as claimed in claim 1, wherein the gas furnace (16) is a backup high-temperature driving heat source, and the solar heat at 10-35 ℃ generated by the CPC/ETC (18) is a backup low-temperature driving heat source.
5. The single-stage balanced ammonia-water re-absorption heat pump cycle equipment as claimed in claim 4, wherein when the ambient temperature is not lower than-10 ℃, the mode is a high temperature driving heat source and a low temperature driving heat source; when the ambient temperature is lower than-10 ℃, the mode is switched to the working mode of a standby high-temperature driving heat source and a standby low-temperature driving heat source.
6. The method for supplying heat by using the single-stage balanced ammonia-water re-absorption heat pump cycle device as claimed in claim 2, wherein the operation process of the water supply and return pipeline is as follows:
a water supply process: the ammonia solution G of the high-pressure absorber (2) absorbs the heat released by the high-temperature high-pressure ammonia water steam from the high-pressure generator (1) and exchanges heat with the water return pipeline (15) to generate water supply SW;
indoor heat supply process: the water supply SW from the high pressure absorber (2) exchanges heat with the indoor heat exchange terminal (17);
a water return process: the temperature of the supplied water is reduced after passing through the indoor heat exchange tail end (17) to generate return water RW, the return water RW enters the low-pressure absorber (4) through the return water pipeline (15), the dilute ammonia solution A of the low-pressure absorber (4) absorbs the low-temperature low-pressure ammonia water steam from the low-pressure generator (3) to release heat, the heat exchange is carried out between the dilute ammonia solution A and the return water pipeline (15), and then the return water RW flows into the high-pressure absorber (2);
the above process is operated circularly.
7. The method of claim 6 wherein the solution loop is operated as follows:
the generation process of the high-voltage generator comprises the following steps: the ammonia solution F of the high-pressure generator (1) absorbs heat, the temperature is increased, ammonia water vapor is separated out, and an ammonia dilute solution A is generated;
the generation process of the low-pressure absorber comprises the following steps: the dilute ammonia solution A of the low-pressure absorber (4) absorbs ammonia water vapor and releases heat to generate a concentrated ammonia solution B;
the high-pressure absorber is generated by the following steps: the ammonia solution G of the high-pressure absorber (2) absorbs ammonia water vapor and releases heat to generate a concentrated ammonia solution C;
the generation process of the low-voltage generator comprises the following steps: the concentrated ammonia solution C of the low-pressure generator (3) absorbs heat, the temperature is increased, ammonia water vapor is separated out, and a dilute ammonia solution D is generated;
solution mixing process: the concentrated ammonia solution B and the dilute ammonia solution D are mixed by the solution mixing tank (7) to generate an ammonia solution E;
a solution separation process, wherein the ammonia solution E is separated by the solution separation tank (8) to generate an ammonia solution F and an ammonia solution G which respectively enter the high-pressure generator (1) and the high-pressure absorber (2);
the above process is operated circularly.
8. The method of claim 6 wherein the refrigerant vapor line is operated as follows:
the high-temperature high-pressure ammonia water steam HV generation process comprises the following steps: the ammonia solution F of the high-pressure generator (1) absorbs heat, the temperature is increased, and ammonia water vapor is separated out;
high-temperature high-pressure ammonia water vapor HV absorption process: the ammonia solution G of the high-pressure absorber (2) absorbs ammonia water vapor and releases heat;
the low-temperature low-pressure ammonia water steam LV generation process: the strong ammonia water solution C of the low-pressure generator (3) absorbs heat and ammonia water vapor is separated out;
low-temperature low-pressure ammonia water vapor LV absorption process: and the dilute ammonia water solution A of the low-pressure absorber (4) absorbs ammonia water vapor and releases heat.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711230635.0ACN108050571B (en) | 2017-11-29 | 2017-11-29 | Single-stage balanced ammonia-water reabsorption heat pump circulation equipment and heating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711230635.0ACN108050571B (en) | 2017-11-29 | 2017-11-29 | Single-stage balanced ammonia-water reabsorption heat pump circulation equipment and heating method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108050571A CN108050571A (en) | 2018-05-18 |
| CN108050571Btrue CN108050571B (en) | 2020-04-03 |
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| CN109579105B (en)* | 2018-10-30 | 2020-10-27 | 中国科学院理化技术研究所 | A gas absorption heat pump system |
| CN110081636A (en)* | 2019-04-19 | 2019-08-02 | 东南大学 | A kind of solution chiasma type ammonium hydroxide absorbs, reabsorbs formula heat pump system |
| CN110173919B (en)* | 2019-04-30 | 2020-10-16 | 东南大学 | Device for improving performance of gas type ammonia water bromine heat pump based on electrically driven membrane separation technology |
| CN112078834B (en)* | 2020-08-24 | 2022-04-19 | 航天科工空间工程发展有限公司 | Spacecraft heat dissipation system and method |
| CN113203112B (en)* | 2021-05-20 | 2024-11-15 | 江苏河海新能源技术发展有限公司 | Absorption double effect heat pump |
| CN115013998B (en)* | 2022-06-27 | 2023-05-12 | 张丽红 | Ammonia water absorption heat pump and control method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPH09243198A (en)* | 1996-03-04 | 1997-09-16 | Matsushita Electric Ind Co Ltd | Absorption heat pump |
| CN1220014C (en)* | 2003-07-07 | 2005-09-21 | 佛山市大东南电器有限公司 | Absorption refrigeration device with biabsorption |
| CN101059290A (en)* | 2007-05-25 | 2007-10-24 | 东南大学 | Ammonia absorption type refrigeration and hot pump dual-purpose system and cool and heat supply method |
| CN101093118B (en)* | 2007-07-08 | 2010-07-14 | 李华玉 | Single stage composite absorption type compressor |
| CN100578116C (en)* | 2008-05-09 | 2010-01-06 | 武汉云鹤定宇制冷科技有限公司 | A refrigeration and air conditioner using hot water from solar vacuum glass tube collectors as energy |
| CN101458006B (en)* | 2009-01-01 | 2011-11-16 | 李华玉 | Method for enhancing heat pump heat supply temperature and high temperature first kind absorption heat pump |
| CN101520250B (en)* | 2009-03-26 | 2011-03-16 | 浙江大学 | Efficient two-stage absorption refrigerating device |
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