CN116123749B - Pump-driven jet boosting diffusion absorption type heat converter - Google Patents
Pump-driven jet boosting diffusion absorption type heat converter Download PDFInfo
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- CN116123749B CN116123749B CN202211644698.1A CN202211644698A CN116123749B CN 116123749 B CN116123749 B CN 116123749B CN 202211644698 A CN202211644698 A CN 202211644698A CN 116123749 B CN116123749 B CN 116123749B
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- 238000009792 diffusion process Methods 0.000 title claims abstract description 62
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 119
- 239000003507 refrigerant Substances 0.000 claims abstract description 116
- 239000000243 solution Substances 0.000 claims abstract description 95
- 239000006096 absorbing agent Substances 0.000 claims abstract description 38
- 238000002347 injection Methods 0.000 claims abstract description 16
- 239000007924 injection Substances 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 230000002745 absorbent Effects 0.000 claims description 19
- 239000002250 absorbent Substances 0.000 claims description 19
- 229910001868 water Inorganic materials 0.000 claims description 16
- 230000005484 gravity Effects 0.000 claims description 11
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 150000001298 alcohols Chemical class 0.000 claims description 6
- 150000002170 ethers Chemical class 0.000 claims description 6
- -1 hydrocarbon halides Chemical class 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 4
- 150000001299 aldehydes Chemical class 0.000 claims description 3
- 150000001412 amines Chemical class 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 3
- 239000002608 ionic liquid Substances 0.000 claims description 3
- 150000002576 ketones Chemical class 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims 1
- 238000005260 corrosion Methods 0.000 abstract description 4
- 230000007797 corrosion Effects 0.000 abstract description 4
- 238000005086 pumping Methods 0.000 abstract description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Inorganic materials [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 29
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 12
- 229910052734 helium Inorganic materials 0.000 description 12
- 239000001307 helium Substances 0.000 description 12
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 239000002270 dispersing agent Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000002440 industrial waste Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
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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
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption 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
- F25B33/00—Boilers; Analysers; Rectifiers
-
- 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
- F25B37/00—Absorbers; Adsorbers
-
- 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
- F25B39/00—Evaporators; Condensers
-
- 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
- F25B41/20—Disposition of valves, e.g. of on-off valves or flow control valves
-
- 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
- F25B41/40—Fluid line arrangements
-
- 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
- F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
- F25B43/006—Accumulators
-
- 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
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/08—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point using ejectors
-
- 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]
- Y02B30/62—Absorption based systems
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Power Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention provides an injection boosting diffusion absorption type heat converter without electric pump driving, which comprises a working vapor generator, an injector, a working vapor condenser, a buffer separator, a first stop valve, a second stop valve, a buffer liquid storage device, a third stop valve and a fourth stop valve; the refrigerant generating and absorbing module comprises a refrigerant generator, a riser, a solution separator, a refrigerant condenser, a refrigerant separator, an evaporator, an absorber, a liquid reservoir and a solution heat exchanger; the ejector is adopted to eject the diffusion gas, so that the problem that the traditional absorption type heat converter needs to input extremely high-grade electric energy is solved, full-heat driving is realized, a heat driving pump is used for pumping and separating the refrigerant and the solution, the corrosion problem can be avoided, and the system circulation structure is simplified.
Description
Technical Field
The invention relates to the technical field of absorption type heat converters, in particular to a jet boosting diffusion absorption type heat converter without pump driving.
Background
The absorption type heat converter is characterized in that solar energy, geothermal energy, industrial waste heat and other heat sources at medium temperature are input into a generator and an evaporator, and part of low temperature is released into the environment through a condenser, so that part of high temperature is obtained in the absorber, and the obtained high temperature is about occupied by the obtained high temperature50% of the heat input. The absorption type heat converter can be driven by a low-grade heat source, can effectively utilize low-grade heat sources such as industrial waste heat, geothermal heat, solar energy and the like, and realizes energy conservation, emission reduction and consumption reduction; and mostly adopt H 2 The natural working media such as O-LiBr solution and the like are environment-friendly, so the method has important significance for energy conservation and environmental protection. However, although the conventional absorption heat converter can realize the utilization of low-grade heat, power consumption still exists, and the solution pump also faces the problem of high-temperature corrosion, especially for a system using lithium bromide aqueous solution as a working medium.
To achieve zero electrical input, diffusion absorption thermal converter technology has been developed. Operation of the system under near isobaric conditions is achieved by adding and separating the diffusion gas, which makes possible the use of bubble pumps. The diffusion absorption type heat converter combines the principle of diffusion absorption and a bubble pump with the traditional absorption type heat converter, comprises a diffusion gas generation module and a refrigerant generation absorption module, replaces the pressure difference of the refrigerant in the traditional absorption type heat converter with the chemical potential difference of the refrigerant in the system, adopts a thermally driven bubble pump to replace an original solution pump, a refrigerant pump and other electrically driven pumps, realizes the simultaneous pumping and separation of the absorbent solution and the refrigerant, does not consume any electric energy, does not have any mechanical moving parts, avoids the problem of high-temperature corrosion of the electrically driven pump, and is more free in the selection of working media.
Many diffusion absorption type heat converters in the form of a double bubble pump are currently being studied. However, the theoretical analysis of the bubble pump is not perfect, the actual performance of the bubble pump is influenced by various factors, the use of two bubble pumps aggravates and amplifies the operation uncertainty of the diffusion absorption type heat exchanger, the heating performance of the system is greatly limited by the performance of the bubble pump, the performance analysis accuracy of the diffusion absorption type heat exchanger is poor, the experimental effect is limited by various operation parameters, and the heating capacity of the diffusion absorption type heat exchanger cannot be fully exerted.
Disclosure of Invention
According to the technical problems, the injection pressurizing diffusion absorption type heat exchanger without pump driving is provided.
The invention adopts the following technical means:
an injection pressurizing diffusion absorption type heat converter without electric pump driving, wherein the heat converter comprises a diffusion gas injection pressurizing module and a refrigerant generation absorbing module;
the diffusion gas injection pressurizing module comprises a working vapor generator, an ejector, a working vapor condenser, a buffer separator and a buffer liquid storage;
a liquid outlet of the buffer liquid storage device is connected with a liquid inlet of a working vapor generator of the working vapor generator through a third stop valve; the vapor outlet of the working vapor generator is connected with the ejector air inlet of the ejector, and the vapor outlet of the working vapor generator is connected with the buffer liquid storage device liquid inlet of the buffer liquid storage device through a fourth stop valve; the jet orifice of the ejector is connected with the working vapor condenser inlet of the working vapor condenser, the buffer reservoir exhaust port of the buffer reservoir is connected with the working vapor condenser inlet through a second stop valve, and the working vapor condenser outlet of the working vapor condenser is connected with the buffer separator inlet of the buffer separator; a buffer separator liquid outlet of the buffer separator is connected with a buffer liquid reservoir liquid inlet of the buffer liquid reservoir through a first stop valve;
the refrigerant generating and absorbing module comprises a refrigerant generator, a riser, a solution separator, a refrigerant condenser, a refrigerant separator, an evaporator, an absorber, a liquid reservoir and a solution heat exchanger;
the liquid storage outlet of the liquid storage device is connected with the first inlet of the solution heat exchanger, the first outlet of the solution heat exchanger is connected with the liquid inlet of the refrigerant generator, the air inlet of the refrigerant generator is connected with the air outlet of the buffer separator, the air outlet of the refrigerant generator is connected with the bottom end of the lifting pipe, the top end of the lifting pipe is connected with the inlet of the solution separator, the solution separator air outlet of the solution separator is connected with the condensation inlet of the refrigerant condenser, the condensation outlet of the refrigerant condenser is connected with the refrigerant separator inlet of the refrigerant separator, the refrigerant separator air outlet of the refrigerant separator is connected with the injection port of the ejector, the refrigerant separator liquid outlet of the refrigerant separator is connected with the evaporation inlet of the evaporator, the evaporation outlet of the evaporator is connected with the absorber first inlet of the absorber, and the absorber outlet of the absorber is connected with the reservoir inlet of the reservoir; the liquid outlet of the solution separator is connected with the first inlet of the solution heat exchanger, and the second outlet of the solution heat exchanger is connected with the second inlet of the absorber.
The dilute solution stored in the liquid storage device enters the refrigerant generator after being precooled by the solution heat exchanger under the action of gravity, the dilute solution comprises a refrigerant and an absorbent, the refrigerant is heated in the refrigerant generator and diffuses and evaporates into diffusion gas to form mixed gas, the mixed gas carrying part of the dilute solution is lifted in the lifting pipe and enters the solution separator for separation, the separated mixed gas enters the refrigerant separator after being condensed in the refrigerant condenser, the refrigerant is separated from the diffusion gas which is still in a gaseous state, and the refrigerant which is in a liquid state is evaporated from the evaporator by gravity and is changed into a gaseous state again, and then enters the absorbent;
the liquid separated by the solution separator is a concentrated solution with the refrigerant and the absorbent, the concentrated solution enters the solution heat exchanger by gravity to exchange heat and preheat, then enters the absorber to absorb the refrigerant which becomes gas state and release heat, the concentrated solution is changed into a dilute solution again, the dilute solution flows into the liquid storage device, and the liquid in the liquid storage device flows into the solution heat exchanger to exchange heat and cool and then enters the refrigerant generator again;
working vapor generated by the working vapor generator enters the ejector from a vapor outlet of the working vapor generator to be used as working fluid of the ejector, the ejector ejects the diffusion gas from the refrigerant separator, the ejector ejects the working vapor and the diffusion gas from a working vapor condenser inlet of the working vapor condenser into the working vapor condenser to be condensed, the condensed working vapor enters the buffer separator to be separated, and the diffusion gas reenters the refrigerant generator from the buffer separator;
the working vapor entering the buffer separator is changed into liquid, and a buffer separator liquid outlet at the bottom of the buffer separator is connected with a buffer liquid storage inlet of the buffer liquid storage through a first stop valve; the bottom outlet of the buffer liquid reservoir is connected with the liquid inlet of the working vapor generator through a third stop valve, and the vapor outlet is connected with the liquid inlet of the buffer liquid reservoir through a fourth stop valve. And a buffer reservoir exhaust port at the top of the buffer reservoir is connected with a working vapor condenser inlet of the working vapor condenser through a second stop valve.
The diffusion gas injection pressurizing module has two working modes:
liquid storage mode: the first stop valve and the second stop valve are opened, and the third stop valve and the fourth stop valve are closed;
liquid return mode: and the third stop valve and the fourth stop valve are opened, and the first stop valve and the second stop valve are closed.
Preferably, the refrigerant condenser is located at the highest position of the heat exchanger, the refrigerant separator is lower than the refrigerant condenser, the evaporator is lower than the refrigerant separator, the absorber is lower than the evaporator, the liquid storage is lower than the absorber, the solution heat exchanger is lower than the liquid storage, the solution separator is lower than the refrigerant condenser, the riser is lower than the solution separator, the refrigerant generator is lower than the riser, and the solution separator outlet of the solution separator is higher than the absorber second inlet of the absorber; the buffer separator is lower than the working vapor condenser, the buffer reservoir is lower than the buffer separator, and lower than the ejector; the working vapor generator is lower than the buffer reservoir.
Preferably, the refrigerant used in the heat exchanger is one or more of water, hydrocarbons, hydrocarbon halides, alcohols or ethers.
Preferably, the absorbent adopted in the heat exchanger is one or more of salts, alcohols or ethers, ketones, amines, aldehydes or ionic liquids.
Preferably, the molecules of the diffuser gas should be as small as possible, have a boiling point well below that of the refrigerant, and be insoluble in the refrigerant, the absorbent, and the liquid working vapor. The dispersing agent adopted in the heat converter is hydrogen, inert gas, hydrocarbons, hydrocarbon halides or carbon dioxide.
Preferably, the working vapor should have proper saturated vapor pressure at corresponding temperature, and the diffusion gas meeting the requirements of conveying capacity and pressure can be ejected in the ejector, and meanwhile, the diffusion gas together with the diffusion gas should be reduced to the greatest extent so as not to influence the generation process of the refrigerant.
Compared with the prior art, the invention has the following advantages:
1. the heat driven bubble pump is adopted to pump the absorbent and the refrigerant simultaneously, so that electric energy can not be consumed at all.
2. The solution pump has no moving parts, solves the problem of corrosion of the solution pump at high temperature, and improves the reliability of system operation.
3. Introducing the injector pressurizes the diffusion gas injection, avoiding the use of multiple bubble pumps from having an uncertainty impact and performance limitations on system performance.
For the reasons, the invention can be widely popularized in the fields of diffusion absorption type heat converters and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic diagram of a pump-driven jet boost diffusion absorption type heat converter according to an embodiment of the present invention.
Fig. 2 is a schematic view of an ejector structure according to an embodiment of the present invention.
Detailed Description
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other. The invention will be described in detail below with reference to the drawings in connection with embodiments.
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. The following description of at least one exemplary embodiment is merely exemplary in nature and is in no way intended to limit the invention, its application, or uses. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present invention. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
The relative arrangement of the components and steps, numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless it is specifically stated otherwise. Meanwhile, it should be clear that the dimensions of the respective parts shown in the drawings are not drawn in actual scale for convenience of description. Techniques, methods, and apparatus known to one of ordinary skill in the relevant art may not be discussed in detail, but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any specific values should be construed as merely illustrative, and not a limitation. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further discussion thereof is necessary in subsequent figures.
In the description of the present invention, it should be understood that the azimuth or positional relationships indicated by the azimuth terms such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal", and "top, bottom", etc., are generally based on the azimuth or positional relationships shown in the drawings, merely to facilitate description of the present invention and simplify the description, and these azimuth terms do not indicate and imply that the apparatus or elements referred to must have a specific azimuth or be constructed and operated in a specific azimuth, and thus should not be construed as limiting the scope of protection of the present invention: the orientation word "inner and outer" refers to inner and outer relative to the contour of the respective component itself.
Spatially relative terms, such as "above … …," "above … …," "upper surface at … …," "above," and the like, may be used herein for ease of description to describe one device or feature's spatial location relative to another device or feature as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations in use or operation in addition to the orientation depicted in the figures. For example, if the device in the figures is turned over, elements described as "above" or "over" other devices or structures would then be oriented "below" or "beneath" the other devices or structures. Thus, the exemplary term "above … …" may include both orientations of "above … …" and "below … …". The device may also be positioned in other different ways (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
In addition, the terms "first", "second", etc. are used to define the components, and are only for convenience of distinguishing the corresponding components, and the terms have no special meaning unless otherwise stated, and therefore should not be construed as limiting the scope of the present invention.
As shown in fig. 1-2, an injection pressurizing diffusion absorption type heat converter driven by an electroless pump comprises a diffusion gas injection pressurizing module and a refrigerant generation absorbing module;
the diffusion gas injection pressurizing module comprises a working vapor generator 1, an injector 2, a working vapor condenser 3, a buffer separator 4, a first stop valve 5, a second stop valve 6, a buffer liquid storage 7, a third stop valve 8 and a fourth stop valve 9; the refrigerant generating and absorbing module comprises a refrigerant generator 10, a lifting pipe 11, a solution separator 12, a refrigerant condenser 13, a refrigerant separator 14, an evaporator 15, an absorber 16, a liquid storage 17 and a solution heat exchanger 18;
the pipeline connection mode is as follows:
a buffer liquid outlet 7c of the buffer liquid reservoir 7 is connected with a working vapor generator liquid inlet 1b of the working vapor generator 1 through a third stop valve 8; the vapor outlet 1a of the working vapor generator 1 is connected with the ejector air inlet 2a of the ejector 2, and the vapor outlet 1a of the working vapor generator 1 is connected with the buffer liquid inlet 7a of the buffer liquid reservoir 7 through a fourth stop valve 9; the injection port 2c of the injector 2 is connected with the working vapor condenser inlet 3a of the working vapor condenser 3, the buffer reservoir exhaust port 7b of the buffer reservoir 7 is connected with the working vapor condenser inlet 3a through the second stop valve 6, and the working vapor condenser outlet 3b of the working vapor condenser 3 is connected with the buffer separator inlet 4a of the buffer separator 4; the buffer separator liquid outlet 4c of the buffer separator 4 is connected with the buffer liquid inlet 7a of the buffer liquid reservoir 7 through a first stop valve 5;
the liquid storage outlet 17b of the liquid storage 17 is connected with the first inlet 18a of the liquid heat exchanger 18, the first outlet 18b of the liquid heat exchanger 18 is connected with the liquid inlet 10c of the liquid generator 10, the liquid inlet 10a of the liquid generator 10 is connected with the buffer separator outlet 4b of the buffer separator 4, the liquid generator outlet 10b of the liquid generator 10 is connected with the bottom end of the lifting pipe 11, the top end of the lifting pipe 11 is connected with the liquid separator inlet 12a of the liquid separator 12, the liquid separator outlet 12b of the liquid separator 12 is connected with the condensation inlet 13a of the liquid condenser 13, the condensation outlet 13b of the liquid condenser 13 is connected with the liquid separator inlet 14a of the liquid separator 14, the liquid separator 14c of the liquid separator 14 is connected with the liquid storage outlet 2b of the ejector 2, the liquid separator 14b of the liquid separator 14 is connected with the liquid evaporator inlet 16a of the liquid absorber 16a, and the liquid absorber outlet 16b of the liquid absorber 16a is connected with the liquid absorber inlet 16a of the liquid absorber 16 a; the solution separator outlet 12c of the solution separator 12 is connected to the first inlet 18c of the solution heat exchanger 18, and the second outlet 18d of the solution heat exchanger 18 is connected to the absorber second inlet 16b of the absorber 16.
The upper and lower position relationship is as follows:
the refrigerant condenser 13 is positioned at the highest position of the heat exchanger, the refrigerant separator 14 is positioned below the refrigerant condenser 13, the evaporator 15 is positioned below the refrigerant separator 14, the absorber 16 is positioned below the evaporator 15, the liquid storage 17 is positioned below the absorber 16, the solution heat exchanger 18 is positioned below the liquid storage 17, the solution separator 12 is positioned below the refrigerant condenser 13, the riser pipe 11 is positioned below the solution separator 12, the refrigerant generator 10 is positioned below the riser pipe 11, and the solution separator liquid outlet 12c of the solution separator 12 is positioned above the absorber second inlet 16b of the absorber 16; the buffer separator 4 is below the working vapour condenser 3, the buffer reservoir 7 is below the buffer separator 4 and below the ejector 2; the working vapour generator 1 is below the buffer reservoir 7.
The medium adopted by the heat converter is as follows:
the refrigerant adopted in the heat converter is one or more of water, hydrocarbons, hydrocarbon halides, alcohols or ethers. The absorbent is one or more of salts, alcohols or ethers, ketones, amines, aldehydes or ionic liquid. The dispersing agent is hydrogen, inert gas, hydrocarbon halide or carbon dioxide. The molecules of the diffusant gas should be as small as possible, have a boiling point well below that of the refrigerant, and are insoluble in the refrigerant, the absorbent and the liquid working vapor.
The component structure of the heat converter is described as follows:
the lifting pipe 11 mainly plays roles of lifting solution and driving solution circulation, and can be a common metal pipe or a pressure-resistant hose; the buffer separator 4, the solution separator 12 and the refrigerant separator 14 function to balance and separate the two-phase mixture entering the buffer separator, the gas phase flows out from the top, and the liquid phase flows out from the bottom. The vapor generator 1, the working vapor condenser 3, the refrigerant generator 10, the refrigerant condenser 13, the evaporator 15, the absorber 16 and the solution heat exchanger 18 are all heat exchangers, and can be spray type or immersion type, sleeve type or other forms, and the heat exchange tubes can be common tubes or reinforced tubes.
The heat exchanger can be divided into a low-temperature heat source (environment, about 30 ℃), a medium-temperature heat source (i.e. an input heat source of the refrigerant generator 10 and the evaporator 15, about 90 ℃), and a high-temperature heat source (i.e. high temperature discharged from the absorber 16, about 120 ℃), wherein the system is driven by heat energy, and the heat energy grade is improved without consuming any electric energy or mechanical energy. Has good application prospect in recycling low-temperature heat resources and improving the energy utilization rate.
In the specific embodiment, water is used as a refrigerant, lithium bromide is used as an absorbent, helium is used as a diffusion gas, and cyclopentane is used as working vapor.
The flow directions of water, lithium bromide and helium in the refrigerant generating absorption module are as follows:
the diluted lithium bromide solution stored in the liquid storage 17 is cooled by the solution heat exchanger 18 under the action of gravity and then enters the refrigerant generator 10, meanwhile helium from the buffer separator 4 also enters the refrigerant generator 10, and the gas phase composition in the refrigerant generator 10 is changed, so that the chemical potential of refrigerant water in the aqueous lithium bromide solution is greater than the chemical potential of the refrigerant water in the gas phase, the refrigerant water in the aqueous lithium bromide solution diffuses and evaporates into the helium of the diffusion gas, the concentration of the aqueous lithium bromide solution is increased, the water is generated and mixed into the helium of the diffusion gas to form a mixed gas, and meanwhile, the external world inputs a certain medium-temperature heat to the refrigerant generator 10 to supply energy required by water evaporation and energy required by the temperature rise of the diffusion gas, so that the diffusion generating process of the refrigerant is completed.
The mixed gas formed by the water vapor and the helium gas carries part of lithium bromide concentrated solution in the refrigerant generator 10 into the riser 11, the mixed gas carries the lithium bromide concentrated solution into the solution separator 12 for separation according to the thermosiphon effect of a bubble pump, the separated mixed gas enters the refrigerant condenser 13 for condensation, the water vapor is condensed into liquid water and emits low-temperature condensation heat to the environment, the helium gas still keeps in a gaseous state, then enters the refrigerant separator 14 for separation, the liquid water evaporates from flowing into the evaporator 15 by gravity, is heated and evaporated by an external medium-temperature heat source to form water vapor, and then enters the absorber 16;
the concentrated lithium bromide solution separated by the solution separator 12 enters the solution heat exchanger 18 by gravity to exchange heat and then enters the absorber 16, and in the absorber 16, the concentrated lithium bromide solution meets gaseous water, but unlike the environment that the concentrated lithium bromide solution exists in the refrigerant generator 10, the existence of diffusion gas helium does not exist in the absorber 16 any more, almost all water vapor in the gas phase has extremely high chemical potential, the chemical potential of the water in the concentrated lithium bromide solution is smaller than that of the gaseous water from the evaporator 15, the water absorbing capacity of the concentrated lithium bromide solution which is restrained by the diffusion gas helium before being recovered, the water vapor from the evaporator 15 is absorbed, and a large amount of high temperature is available, which is represented by the most important temperature raising function of the system. The absorbent absorbed with the refrigerant flows into the liquid storage tank 17, and the liquid in the liquid storage tank 17 flows into the solution heat exchanger 18 to exchange heat and cool, and then reenters the refrigerant generator 10; it should be noted that the heat exchange of the solution heat exchanger 18 refers to the heat exchange between the high-temperature absorbent flowing out of the reservoir 17 and the low-temperature absorbent flowing out of the solution separator 12.
The flow direction of cyclopentane and helium in the diffusion gas injection pressurizing module is as follows:
the diffusion gas injection pressurizing module has two working modes:
liquid storage mode: the first stop valve 5 and the second stop valve 6 are opened, and the third stop valve 8 and the fourth stop valve 9 are closed; the working vapor generator 1 is input with a medium-temperature heat source to generate high-pressure working vapor, the high-pressure working vapor enters the ejector 2 and then ejects low-temperature low-pressure diffusion gas from the refrigerant separator 14, mixed gas with medium temperature and medium pressure is formed after the low-temperature low-pressure diffusion gas is mixed, the mixed gas enters the working vapor condenser 3 and then the working vapor is condensed into low-temperature medium-pressure liquid which enters the buffer separator 4 and then enters the liquid storage 7; the low temperature, low pressure, diffused gas reenters the refrigerant generator 10.
Liquid return mode: the third stop valve 8 and the fourth stop valve 9 are opened, and the first stop valve 5 and the second stop valve 6 are closed. In order to realize that the medium-pressure cyclopentane liquid enters the high-pressure working vapor generator 1, part of the high-pressure working vapor is released to enter the buffer liquid reservoir 7 to balance the pressure in the working vapor, and the liquid in the buffer liquid reservoir 7 flows into the vapor generator 1 under the action of gravity. At the same time, the generated cyclopentane gas still ejects helium as working fluid, helium is supplied as diffusion gas to the refrigerant generator without being affected, and the cyclopentane liquid condensed in the working vapor condenser 3 is temporarily stored in the buffer separator 4. After the cyclopentane liquid in the buffer reservoir 4 has all flowed into the vapor generator, it returns to the liquid storage mode.
The invention provides a jet pressurizing diffusion absorption type heat converter without electric pump driving, wherein diffusion gas is pressurized by an ejector 2 adopting gravity liquid supply, and the flow of a refrigerant and a solution thereof utilizes the thermosiphon principle of a bubble pump, so that the innovation improvement of the diffusion absorption type heat converter is realized. By changing the phase equilibrium relationship of the mixture of the absorbent, the refrigerant and the diffusion gas at different temperatures and concentrations, different chemical potential differences of the refrigerant in the absorbent solution and the gas phase are created under near-isobaric conditions, so that the temperature of the absorption process is higher than the temperature of the occurrence process, and finally the high-temperature heat is prepared. The whole system organically combines the ejector 2, the bubble pump and the absorption system, is driven by heat energy, realizes the improvement of heat energy grade under the condition of not consuming any electric energy or mechanical energy, and improves the operation reliability. Has good application prospect in recycling low-temperature heat resources and improving the energy utilization rate.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (5)
1. The jet boosting diffusion absorption type heat converter without pump driving is characterized by comprising a diffusion gas jet boosting module and a refrigerant generation absorption module;
the refrigerant generation and absorption module comprises a refrigerant generator (10), a riser (11), a solution separator (12), a refrigerant condenser (13), a refrigerant separator (14), an evaporator (15), an absorber (16), a liquid reservoir (17) and a solution heat exchanger (18);
the dilute solution stored in the liquid storage device (17) enters the refrigerant generator (10) after being precooled by the solution heat exchanger (18) under the action of gravity, the dilute solution comprises a refrigerant and an absorbent, the refrigerant is heated in the refrigerant generator (10) and diffuses and evaporates into a diffusion gas to form a mixed gas, the absorbent is lifted in the lifting pipe (11) and enters the solution separator (12) for separation, the separated mixed gas enters the refrigerant condenser (13) and then enters the refrigerant separator (14), the refrigerant is separated from the diffusion gas which is still in a gaseous state, and the refrigerant which is in the liquid state evaporates and is again in the gaseous state from the diffusion gas flowing into the evaporator (15) by gravity and then enters the absorber (16);
the liquid separated by the solution separator (12) is a concentrated solution with the refrigerant and the absorbent, the concentrated solution enters the solution heat exchanger (18) by gravity for heat exchange and preheating, then enters the absorber (16) to absorb the refrigerant which is changed into a gaseous state and release heat, the concentrated solution absorbed with the refrigerant is changed into a dilute solution again, the dilute solution flows into the liquid storage device (17), and the liquid in the liquid storage device (17) flows into the solution heat exchanger (18) for heat exchange and cooling and then reenters the refrigerant generator (10);
the diffusion gas injection pressurizing module comprises a working vapor generator (1), an injector (2), a working vapor condenser (3), a buffer separator (4) and a buffer reservoir (7);
working vapor generated by the working vapor generator (1) enters the ejector (2) from a vapor outlet (1 a) of the working vapor generator (1) to be used as working fluid of the ejector (2), the ejector (2) ejects the diffusion gas from the refrigerant separator (14), the ejector (2) ejects the working vapor and the diffusion gas from a working vapor condenser inlet (3 a) of the working vapor condenser (3) into the working vapor condenser (3) to be condensed, and enters the buffer separator (4) to be separated after condensation, and the diffusion gas re-enters the refrigerant generator (10) from the buffer separator (4);
the working vapor entering the buffer separator (4) is changed into liquid, and a buffer separator liquid outlet (4 c) at the bottom of the buffer separator (4) is connected with a buffer liquid inlet (7 a) of the buffer liquid reservoir (7) through a first stop valve (5); the bottom outlet of the buffer liquid reservoir (7) is connected with a working vapor generator liquid inlet (1 b) of the working vapor generator (1) through a third stop valve (8), the vapor outlet (1 a) is connected with a buffer liquid reservoir liquid inlet (7 a) of the buffer liquid reservoir (7) through a fourth stop valve (9), and a buffer liquid reservoir exhaust port (7 b) at the top of the buffer liquid reservoir (7) is connected with a working vapor condenser inlet (3 a) of the working vapor condenser (3) through a second stop valve (6);
the diffusion gas injection pressurizing module has two working modes:
liquid storage mode: the first stop valve (5) and the second stop valve (6) are opened, and the third stop valve (8) and the fourth stop valve (9) are closed;
liquid return mode: the third stop valve (8) and the fourth stop valve (9) are opened, and the first stop valve (5) and the second stop valve (6) are closed.
2. A pump-driven ejector-boost diffusion-absorption heat converter according to claim 1, characterized in that the refrigerant condenser (13) is located at the highest position of the heat converter, the refrigerant separator (14) is located below the refrigerant condenser (13), the evaporator (15) is located below the refrigerant separator (14), the absorber (16) is located below the evaporator (15), the reservoir (17) is located below the absorber (16), the solution heat exchanger (18) is located below the reservoir (17), the solution separator (12) is located below the refrigerant condenser (13), the riser (11) is located below the solution separator (12), the refrigerant generator (10) is located below the riser (11), and the solution separator outlet (12 c) of the solution separator (12) is located above the absorber second inlet (16 b) of the absorber (16); -said buffer separator (4) is lower than said working vapour condenser (3), said buffer reservoir (7) is lower than said buffer separator (4) and lower than said ejector (2); the working vapour generator (1) is lower than the buffer reservoir (7).
3. The pump-less ejector-booster diffusion-absorbing heat exchanger of claim 1, wherein the refrigerant is one or more of water, hydrocarbons, hydrocarbon halides, alcohols, or ethers.
4. The pump-driven jet boost diffusion absorption heat converter of claim 1, wherein the absorbent is one or more of salts, alcohols or ethers, ketones, amines, aldehydes or ionic liquids.
5. A pump-driven jet boost diffusion absorption thermal converter according to claim 1 wherein the diffusion gas is hydrogen, an inert gas, hydrocarbons, hydrocarbon halides or carbon dioxide.
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| GB390181A (en) * | 1930-07-28 | 1933-03-27 | Axel Uno Saernmark | Improvements in absorption refrigerating machines |
| JP2003014332A (en) * | 2001-04-26 | 2003-01-15 | Sekisui Chem Co Ltd | Absorption heat pump |
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| CN107915309A (en) * | 2017-11-30 | 2018-04-17 | 安徽工业大学 | A kind of method that fine catalyst efficiently separates simultaneously automatic cycle during catalytic oxidation treatment sewage |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB390181A (en) * | 1930-07-28 | 1933-03-27 | Axel Uno Saernmark | Improvements in absorption refrigerating machines |
| JP2003014332A (en) * | 2001-04-26 | 2003-01-15 | Sekisui Chem Co Ltd | Absorption heat pump |
| CN102121761A (en) * | 2011-02-28 | 2011-07-13 | 浙江大学 | Diffusion absorption type thermal converter without moving parts |
| CN102213501A (en) * | 2011-03-31 | 2011-10-12 | 浙江大学 | Mechanical work drive-free absorption type thermal converter |
| CN105485959A (en) * | 2015-12-04 | 2016-04-13 | 内蒙古科技大学 | Low-grade thermally driven vortex tube-ejector absorption refrigeration system |
| CN107915309A (en) * | 2017-11-30 | 2018-04-17 | 安徽工业大学 | A kind of method that fine catalyst efficiently separates simultaneously automatic cycle during catalytic oxidation treatment sewage |
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