CN102213501A - Mechanical work drive-free absorption type thermal converter - Google Patents
Mechanical work drive-free absorption type thermal converter Download PDFInfo
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- CN102213501A CN102213501A CN2011100797068A CN201110079706A CN102213501A CN 102213501 A CN102213501 A CN 102213501A CN 2011100797068 A CN2011100797068 A CN 2011100797068A CN 201110079706 A CN201110079706 A CN 201110079706A CN 102213501 A CN102213501 A CN 102213501A
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 110
- 239000006096 absorbing agent Substances 0.000 claims abstract description 81
- 230000002745 absorbent Effects 0.000 claims description 75
- 239000002250 absorbent Substances 0.000 claims description 75
- 239000007789 gas Substances 0.000 claims description 38
- 239000012530 fluid Substances 0.000 claims description 24
- 238000005482 strain hardening Methods 0.000 claims description 16
- 238000007599 discharging Methods 0.000 claims description 14
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 238000007789 sealing Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 claims description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 3
- 150000001299 aldehydes Chemical class 0.000 claims description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- -1 alkane halide Chemical class 0.000 claims description 3
- 150000001412 amines Chemical class 0.000 claims description 3
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 claims description 3
- 150000004820 halides Chemical class 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
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 238000007670 refining Methods 0.000 claims 1
- 238000009835 boiling Methods 0.000 abstract description 29
- 239000003507 refrigerant Substances 0.000 abstract description 25
- 239000000203 mixture Substances 0.000 description 12
- 230000000694 effects Effects 0.000 description 10
- 230000005484 gravity Effects 0.000 description 9
- 239000001648 tannin Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000007654 immersion Methods 0.000 description 4
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 4
- ZUHZGEOKBKGPSW-UHFFFAOYSA-N tetraglyme Chemical group COCCOCCOCCOCCOC ZUHZGEOKBKGPSW-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000009792 diffusion process Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 208000002925 dental caries Diseases 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000011900 installation process Methods 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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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
-
- 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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- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention discloses a mechanical work drive-free absorption type thermal converter which comprises a generator, a lifting pipe, a first gas-liquid separator, a condenser, a second gas-liquid separator, an evaporator, a first absorber, a first heat return device and a second absorber that are sequentially connected, wherein the lifting pipe and the first gas-liquid separator are arranged between the generator and the condenser; the second gas-liquid separator is arranged between the condenser and the evaporator; and the first heat return device is arranged between the first gas-liquid separator and the first absorber. The absorption type thermal converter is basically isotonic and ensures that an absorbing agent solution and a large-boiling range mixing refrigerant are simultaneously pumped by adopting a thermally-driven bubble pump without using a mechanical solution pump and a refrigerant pump, thus electric energy is not completely consumed, and operation reliability is improved. The invention is especially suitable for occasions having abundant medium-low temperature thermal resource and power shortage and needing high-temperature heat, and has a better application prospect.
Description
Technical field
The invention belongs to absorption heat pump and low-grade energy utilizes the field, relate in particular to a kind of absorption type heat converter that mechanical power drives that do not have.
Background technology
The absorption type heat converter also claims absorption warming heat pump, can make full use of a large amount of industrial low-temperature used heat that produce in energy consumption of industry such as petrochemical industry, metallurgy, power, makes it directly to be utilized by production process institute again after the grade rising.Can effectively utilize low-grade energies such as industrial exhaust heat, underground heat, solar energy.In addition, the absorption type heat converter can avoid using the refrigeration working medium that atmospheric ozone layer is had destruction, so energy-conservation and environmental protection are all had great importance.Dropped into commercial traditional absorption type heat converter of using mainly with H
2O/LiBr is a working medium, because the temperature of mechanical type solution pump operation is higher and sealing requirements is higher, H
2The severe corrosive of O/LiBr solution has a strong impact on the reliability of solution system, has limited the extensive use of traditional absorption type heat converter.
Diffusion absorption refrigerating machine is to spread in diffusion gas by cold-producing medium to obtain cool effect, internal system does not have pressure reduction basically, flow in system so the airlift pump that utilizes heat to drive just can promote absorbent and cold-producing medium, need not the pyrosol pump and the refrigerated medium pump that use mechanical power to drive.
Summary of the invention
The invention provides a kind of absorption type heat converter that mechanical power drives that do not have, this thermal converter need not to use mechanical type pyrosol pump and the refrigerated medium pump in traditional absorption type heat converter, not only can avoid the electric energy work of consume valuable, and improve reliability of operation; The low temperature thermal resource is abundant in being specially adapted to, power tense, and the while needs to use the occasion of elevated temperature heat again, and good prospects for application is arranged.
A kind of absorption type heat converter that does not have the mechanical power driving comprises generator, condenser, evaporimeter, first absorber and second absorber, is provided with the riser and first gas-liquid separator between described generator and the condenser; Be provided with second gas-liquid separator between described condenser and the evaporimeter; Be provided with first regenerator between described first gas-liquid separator and first absorber;
The port of export of described condenser is higher than the charging aperture in second gas-liquid separator; The liquid level of liquid segment is higher than the entrance point of evaporimeter in described second gas-liquid separator; The absorbent entrance point of described first absorber is lower than the liquid level of liquid segment in first gas-liquid separator, and the absorbent liquid level of first absorber is higher than the absorbent entrance point of second absorber; The absorbent liquid level of described second absorber is higher than the discharging opening on generator top;
Described riser bottom feed mouth is communicated with the discharging opening on generator top, and the top is passed and exceeded first gas-liquid separator bottom and be communicated with the top exterior walls and the first gas-liquid separator bottom inlet end margin sealing and fixing with its inner chamber; Described condenser inlet end is communicated with the gas outlet of gas section in first gas-liquid separator, and the port of export is communicated with the charging aperture of second gas-liquid separator; The liquid outlet of liquid segment is communicated with cold working medium pipe head in first regenerator in described first gas-liquid separator; The gas outlet of gas section is communicated with the air inlet of second absorber in described second gas-liquid separator, and the liquid outlet of liquid segment is communicated with the entrance point of evaporimeter; The gas outlet of described first absorber is communicated with the entrance point of condenser, air inlet is communicated with the port of export of evaporimeter, the absorbent entrance point is communicated with cold working medium pipe outlet in first regenerator, and the absorbent port of export is communicated with hot working fluid pipe head in first regenerator; The absorbent entrance point of described second absorber is communicated with hot working fluid pipe outlet in first regenerator, and the absorbent port of export is communicated with generator bottom feed mouth; The described cold-producing medium mix refrigerant that two or more component is formed of serving as reasons.
The setting of difference in height between condenser, second gas-liquid separator, evaporimeter, first gas-liquid separator and the generator, realized the automatic circulation under the gravity effect of system's inner absorbent and cold-producing medium, basically keep isobaric in the system, guaranteed the stability of heat exchanger operation, avoid use mechanical energy simultaneously, reduced energy consumption and cost.The setting of first regenerator has further improved the heating capacity of heat exchanger and has heated temperature, can satisfy the needs of different occasions.
A spot of absorbent that can carry in the gas that comes out by first gas-liquid separator separates, for the absorbent of avoiding carrying enters in the evaporimeter after condenser condenses, influence absorbs thermal discharge, in the optimized technical scheme, a rectifier unit that is used to remove a small amount of absorbent can be set between described first gas-liquid separator and condenser; The gas that obtains for ease of first gas-liquid separator separates enters in the rectifier unit smoothly, can select the height of rectifier unit setting is higher than the height of first gas-liquid separator, at this moment, the charging aperture of rectifier unit is communicated with the gas outlet of gas section in first gas-liquid separator, and discharging opening links to each other with the entrance point of condenser.
Heat exchanger can be selected fountain, immersion or double pipe heat exchanger for use, and its heat exchanger tube can be that common tube also can be an enhanced tube.
For guaranteeing the stability in the whole thermal converter running, need to guarantee certain amount of liquid in first absorber and second absorber; As further preferred, one first reservoir can be set between described first absorber and first regenerator, the first reservoir entrance point is communicated with the absorbent port of export of first absorber, the port of export links to each other with hot working fluid pipe head in first regenerator, the liquid level of first reservoir is higher than the absorbent entrance point of second absorber, flow into smoothly in second absorber under the gravity effect to satisfy the liquid of collecting in first reservoir.Equally, also can between described second absorber and generator, second reservoir be set, the entrance point of second reservoir is communicated with the absorbent port of export of second absorber, the port of export is communicated with the charging aperture of generator bottom, the liquid level of second reservoir is higher than generator top discharging opening, be back to smoothly in the generator under the gravity effect with the liquid of realizing collecting in second reservoir, satisfy the needs of work operation.The setting of first reservoir and second reservoir has further guaranteed to absorb the absorbent finished and has been back in the generator with flow velocity stably.
For further improving the assimilation effect of second absorber, guarantee that whole low boiling point refrigerants is absorbed agent and absorbs, in the optimized technical scheme, second regenerator can be set between second absorber and generator; At this moment, cold working medium pipe head is communicated with the absorbent port of export of second absorber in second regenerator, cold working medium pipe outlet is communicated with the charging aperture of generator bottom, the hot working fluid pipe head is communicated with hot working fluid pipe outlet in first regenerator, and the hot working fluid pipe outlet is communicated with the absorbent entrance point of second absorber.Lower by separating the gas temperature that obtains in second gas-liquid separator, the absorbent temperature that is absorbed after agent absorbs is also lower, the setting of second regenerator, absorbent preheating to discharging on the one hand from second absorber, reduced the evaporation energy consumption of generator, also reduced the temperature of the absorbent that enters second absorber on the other hand, more helped the absorption of absorbent low boiling point refrigerant.When using second reservoir, in the optimized technical scheme, second regenerator can be set between second reservoir and generator, at this moment, cold working medium pipe head is communicated with the second reservoir port of export in second regenerator, cold working medium pipe outlet is communicated with the charging aperture of generator bottom, and the hot working fluid pipe head is communicated with hot working fluid pipe outlet in first regenerator, and the hot working fluid pipe outlet is communicated with the absorbent entrance point of second absorber.
Described generator, condenser, evaporimeter, first absorber, second absorber, first regenerator and second regenerator all are heat exchangers, can adopt fountain or immersion, also can be bushing type, its heat exchanger tube can be that common tube also can be an enhanced tube.
Need certain boiling range between low boiling component during two or more component in the cold-producing medium is formed and the high boiling component, to guarantee generation and separating effect preferably.According to actual heat exchange needs, take all factors into consideration heat exchange efficiency simultaneously and reduce cost, in the optimized technical scheme, available cold-producing medium is made up of component A and B component, wherein component A normal temperature and pressure (20 ℃, 1 standard atmospheric pressure) is gaseous material down, and the B component normal temperature and pressure is liquid down.The boiling range of component A and B component is bigger, realizes both separation easily, has reduced energy consumption.Further preferred ingredients A comprises one or more in hydrogen, inert gas, oxygen, carbon dioxide, nitrogen, propane, ethane, HFC-134a, methane, halide and the ethene, wherein uses to be fluoroform (being cold-producing medium R23) comparatively widely; B component comprises one or more in water, alkane, alkane halide, the pure and mild ether.Wherein water is present modal higher boiling cold-producing medium because of its pollution-free and nonhazardous.The absorbent of often selecting for use comprises one or more in inorganic salts, alcohol, ether, ketone, amine, aldehyde and the ionic liquid.The most common absorbent is tetraethylene glycol dimethyl ether (E181).
The present invention has different absorbabilities according to absorbent solution to the big boiling range mix refrigerant gas of variable concentrations, proposing a kind of internal system is isobaric absorption type heat converter basically, use for reference the airlift pump principle of diffusion absorption refrigerating machine, adopt heat to drive the simultaneous pumping that airlift pump is realized absorbent solution and cold-producing medium.The present invention compares with traditional absorption type heat converter, does not re-use high-temperature machinery formula solution pump and refrigerated medium pump, has following beneficial effect:
(1) the present invention adopts heat to drive airlift pump simultaneous pumping absorbent solution and big boiling range mix refrigerant, can be fully the electric energy of consume valuable not.
(2) heat-exchange system of the present invention is simple in structure, does not have moving component, has thoroughly solved a mechanical type solution pump corrosion and a sealing difficult problem at high temperature, has greatly improved reliability of operation.
Description of drawings
Fig. 1 is the structural representation of first kind of embodiment of the absorption type heat converter that drives of no mechanical power of the present invention;
Fig. 2 is that the structural representation of second kind of enforcement side of the absorption type heat converter that drives of no mechanical power of the present invention is graphic;
Fig. 3 is the structural representation of the third embodiment of the absorption type heat converter that drives of no mechanical power of the present invention;
Fig. 4 is the structural representation of the 4th kind of embodiment of the absorption type heat converter that drives of no mechanical power of the present invention.
The specific embodiment
As shown in Figure 1, a kind of absorption type heat converter that does not have the mechanical power driving comprises: generator 1, riser 2, first gas-liquid separator 3, condenser 5, second gas-liquid separator 6, evaporimeter 7, first absorber 8, first regenerator 10 and second absorber 12.
Wherein, the charging aperture 1a of generator 1 bottom links to each other with the absorbent port of export 12c of second absorber 12, and the discharging opening 1b on generator 1 top links to each other with the charging aperture of riser 2 bottoms.The discharging opening on riser 2 tops is in the entrance point 3a of the bottom of first gas-liquid separator 3 inserts first gas-liquid separator, 3 cavitys, insert height more than or equal to 1/2 of inner chamber height overall, the edge sealing and fixing of the entrance point 3a of the sidewall at the top of riser 2 and first gas-liquid separator, 3 bottoms.The liquid segment liquid outlet 3b of first gas-liquid separator 3 links to each other with the cold working medium pipe head 10c of first regenerator 10, and the gas outlet 3c of the gas section of first gas-liquid separator 3 links to each other with the entrance point 5a of condenser 5.The port of export 5b of condenser 5 links to each other with the charging aperture 6a of second gas-liquid separator 6.The gas outlet 6b of the gas section of second gas-liquid separator 6 links to each other with the air inlet 12a on second absorber, 12 tops, and the liquid outlet 6c of the liquid segment of second gas-liquid separator 6 links to each other with the entrance point 7a of evaporimeter 7.The port of export 7b of evaporimeter 7 links to each other with the air inlet 8a on first absorber, 8 tops.The gas outlet 8b on first absorber, 8 tops links to each other with the entrance point 5a of condenser 5, the absorbent entrance point 8c of first absorber, 8 one sides links to each other with the port of export 10d of cold working medium pipeline in first regenerator 10, and the absorbent port of export 8d of first absorber, 8 bottoms links to each other with the entrance point 10a of hot working fluid pipeline in first regenerator 10.The port of export 10b of hot working fluid pipeline links to each other with the absorbent entrance point 12b of second absorber, 12 1 sides in first regenerator 10.The absorbent port of export 12c of the bottom of second absorber 12 links to each other with the charging aperture 1a of generator 1 bottom.
During actual installation, it is poor to satisfy certain height, to realize the circulation automatically under the gravity effect of cold-producing medium and absorbent.Wherein condenser 5 will be positioned at the extreme higher position of thermal converter, and the height of the charging aperture 6a of second gas-liquid separator 6 is lower than the height of the port of export 5b of condenser 5; The height of the entrance point 7a of evaporimeter 7 is lower than the height of liquid outlet 6c of the liquid segment of second gas-liquid separator 6; The height of the air inlet 8a on the top of first absorber 8 is lower than the height of the port of export 7b of evaporimeter 7, the liquid level of the absorbent liquid of accumulative total is higher than the height of the absorbent entrance point of second absorber 12 in first absorber 8, and the height of the absorbent entrance point 8c of first absorber 8 is lower than the height of liquid level of the liquid segment of first gas-liquid separator 3; The liquid level of the absorbent of second absorber 12 is higher than the height of the discharging opening 1b on generator 1 top.
Generator in the above-mentioned embodiment, condenser, evaporimeter, first absorber, second absorber, first regenerator are heat exchanger, can adopt fountain or immersion, also can be bushing types, and its heat exchanger tube can be that common tube also can be an enhanced tube.
Used cold-producing medium is a mixture refrigerant in the above-mentioned embodiment, mix refrigerant by a kind of by one or more the component A that form in hydrogen, inert gas, oxygen, carbon dioxide, nitrogen, propane, ethane, HFC-134a, methane, halide and the ethene etc. with by one or more B component formed in water, alkane, alkane halide, the pure and mild ether; Absorbent can be selected one or more in salt, alcohols, ethers, ketone, amine, aldehydes or the ionic liquid.
Riser 2 mainly plays the effect that promotes solution and drive the solution circulation in the above-mentioned embodiment, can be the common metal pipe, also can be pressure hose.The effect of first gas-liquid separator 3, second gas-liquid separator 6 is the two-phase mixture equilibrium separation that will enter wherein in the above-mentioned embodiment, and gas phase flows out from its top, and liquid phase flows out from its bottom.Connection between above-mentioned said each parts adopts metal tubes to connect high temperature conduit outer wrapping insulation material.
Below to adopt higher boiling cold-producing medium H
2O and low boiling point refrigerant R23 form big boiling range mix refrigerant, tetraethylene glycol dimethyl ether (E181) is that example is described concrete running for absorbent:
Be rich in higher boiling cold-producing medium H
2The absorbent E181 concentrated solution of O and low boiling point refrigerant R23 is warm heating in the quilt in generator 1, mix refrigerant H
2O/R23 gas comes out from solution.Because buoyancy, the bubble of mix refrigerant rises in riser 2, promotes simultaneously in part absorbent E181 weak solution to the first gas-liquid separator 3.Mix refrigerant gas separates the back from first gas-liquid separator 3 to be continued to rise, and rises to then in the condenser 5, emits cryogenic condensation heat after the part condensation therein to environment, flows to subsequently in second gas-liquid separator 6.Because low boiling point refrigerant R23 and higher boiling cold-producing medium H
2The boiling-point difference of O is very big, and the liquid phase in second gas-liquid separator 6 is pure higher boiling cold-producing medium H basically
2O, and gas phase is pure low boiling point refrigerant R23 gas.Liquid pure higher boiling cold-producing medium H
2O flow to evaporimeter 7 downwards by gravity, warm heating and gasifying in the quilt, and pure low boiling point refrigerant R23 gas then enters second absorber 12.
Absorbent E181 weak solution flows out from first gas-liquid separator 3, to dirty, flows to first absorber 8 after being heated by gravity in first regenerator 10, absorbs the pure higher boiling cold-producing medium H of flash-pot 7
2O gas produces a large amount of elevated temperature heat in the absorption process.Having a spot of low boiling point refrigerant R23 gas in the absorption process diffuses out from absorbent E181 solution, need by the balance pipe between absorber 8 tops and condenser 5 imports, be back to the import of condenser 5, with mix refrigerant H from first gas-liquid separator 3
2O/R23 gas mixes.And absorb to end be rich in higher boiling cold-producing medium H
2The absorbent E181 concentrated solution of O then flows back to first regenerator 10 by gravity, flows into second absorber 12 after the heat release, absorbs the pure low boiling point refrigerant R23 gas from second gas-liquid separator 6.What absorb to end is rich in low boiling point refrigerant R23 and higher boiling cold-producing medium H
2The absorbent E181 concentrated solution of O then is admitted in the generator 1 once more by gravity.
Structure is identical with embodiment 1, and difference is to be provided with a rectifier unit between first gas-liquid separator 3 and condenser 5, is used for further removing a spot of absorbent that carries from first gas-liquid separator, 3 gas separated.
The absorbent of collecting in rectifier unit 4 is back in first gas-liquid separator 3 the mix refrigerant H after the purification along the pipeline between first gas-liquid separator 3 and the rectifier unit 4
2O/R23 gas enters into condenser 5 condensations, and all the other processes are with embodiment 1.
All the other structures are identical with embodiment 2, difference is, between first absorber 8 and first regenerator 10, be provided with one first reservoir 9, between second absorber 12 and generator, be provided with one second reservoir 13, with the stability of further increase system operation.
The absorbent that the absorbent port of export 8d of first absorber 8 discharges at first enters into the absorbent of collecting in first reservoir, 9, the first reservoirs 9 and enters into the absorption that second absorber 12 carries out low boiling point refrigerant with constant speed through first regenerator 10; Absorbent is finished absorption in second absorber 12 after, enter in second reservoir 13, get back to once more stably then and carry out next working cycles in the generator 1, all the other processes are identical with embodiment 2.
All the other structures are identical with embodiment 3, and difference is, is provided with one second regenerator 11 between second reservoir 13 and the generator 1, to improve heat recovery and utilization and the reinforcement absorption to low boiling point refrigerant.
The absorbent that first reservoir 9 is collected enters in second absorber 12 after through first regenerator 10 and 11 heat releases of second regenerator, the absorbent that absorption is finished enters in second reservoir 13, get back to once more after 11 heating of second regenerator then and carry out next circulation in the generator 1, all the other processes are with embodiment 3.
Claims (10)
1. one kind is not had the absorption type heat converter that mechanical power drives, comprise generator (1), condenser (5), evaporimeter (7), first absorber (8) and second absorber (12), it is characterized in that, be provided with riser (2) and first gas-liquid separator (3) between described generator (1) and the condenser (5); Be provided with second gas-liquid separator (6) between described condenser (5) and the evaporimeter (7); Be provided with first regenerator (10) between described first gas-liquid separator (3) and first absorber (8);
The port of export of described condenser (5) is higher than the charging aperture of second gas-liquid separator (6); The liquid level of the interior liquid segment of described second gas-liquid separator (6) is higher than the entrance point of evaporimeter (7); The absorbent entrance point of described first absorber (8) is lower than the liquid level of the interior liquid segment of first gas-liquid separator (3), and the absorbent liquid level of first absorber (8) is higher than the absorbent entrance point of second absorber (12); The absorbent liquid level of described second absorber (12) is higher than the discharging opening on generator (1) top;
The charging aperture of described riser (2) bottom is communicated with the discharging opening on generator (1) top, the top is passed and is exceeded first gas-liquid separator (3) bottom and be communicated with top exterior walls and first gas-liquid separator (3) bottom inlet end margin sealing and fixing with its inner chamber;
Described condenser (5) entrance point is communicated with the gas outlet of the interior gas section of first gas-liquid separator (3), and the port of export is communicated with the charging aperture of second gas-liquid separator (6); The liquid outlet of the interior liquid segment of described first gas-liquid separator (3) is communicated with cold working medium pipe head in first regenerator (10);
The gas outlet of the interior gas section of described second gas-liquid separator (6) is communicated with the air inlet of second absorber (12), and the liquid outlet of liquid segment is communicated with the entrance point of evaporimeter (7);
The gas outlet of described first absorber (8) is communicated with the entrance point of condenser (5), air inlet is communicated with the port of export of evaporimeter (7), the absorbent entrance point is communicated with cold working medium pipe outlet in first regenerator (10), and the absorbent port of export is communicated with the interior hot working fluid pipe head of first regenerator (10);
The absorbent entrance point of described second absorber (12) is communicated with the interior hot working fluid pipe outlet of first regenerator (10), and the absorbent port of export is communicated with the charging aperture of generator (1) bottom.
2. the absorption type heat converter that no mechanical power according to claim 1 drives is characterized in that be provided with refining plant (4) between described first gas-liquid separator (3) and the condenser (5), rectifier unit (4) is higher than first gas-liquid separator (3); The charging aperture of rectifier unit (4) is communicated with the gas outlet of the interior gas section of first gas-liquid separator (3), and discharging opening links to each other with the entrance point of condenser (5).
3. the absorption type heat converter that no mechanical power according to claim 1 drives is characterized in that, is provided with first reservoir (9) between described first absorber (8) and first regenerator (10); The entrance point of first reservoir (9) is communicated with the absorbent port of export of first absorber (8), and the port of export is communicated with the interior hot working fluid pipe head of first regenerator (10); The liquid level of described first reservoir (9) is higher than the absorbent entrance point of second absorber (12).
4. the absorption type heat converter that no mechanical power according to claim 1 drives is characterized in that, is provided with second reservoir (13) between described second absorber (12) and the generator (1); The entrance point of second reservoir (13) is communicated with the absorbent port of export of second absorber (12), and the port of export is communicated with the charging aperture of generator (1) bottom; The liquid level of described second reservoir (13) is higher than the discharging opening on generator (1) top.
5. the absorption type heat converter that no mechanical power according to claim 4 drives is characterized in that, is provided with second regenerator (11) between described second reservoir (13) and the generator (1); Cold working medium pipe head is communicated with the port of export of second reservoir (13) in second regenerator (11), cold working medium pipe outlet is communicated with the charging aperture of generator (1) bottom, the hot working fluid pipe head is communicated with the interior hot working fluid pipe outlet of first regenerator (10), and the hot working fluid pipe outlet is communicated with the absorbent entrance point of second absorber (12).
6. the absorption type heat converter that no mechanical power according to claim 1 drives is characterized in that, is provided with second regenerator (11) between described second absorber (12) and the generator (1); Cold working medium pipe head is communicated with the absorbent port of export of second absorber (12) in second regenerator (11), cold working medium pipe outlet is communicated with the charging aperture of generator (1) bottom, the hot working fluid pipe head is communicated with the interior hot working fluid pipe outlet of first regenerator (10), and the hot working fluid pipe outlet is communicated with the absorbent entrance point of second absorber (12).
7. the absorption type heat converter that no mechanical power according to claim 1 drives, it is characterized in that, the cold-producing medium of circulation is made up of component A and B component in the described absorption type heat converter, and wherein component A normal temperature and pressure is gaseous material down, and the B component normal temperature and pressure is liquid down.
8. the absorption type heat converter that no mechanical power according to claim 7 drives, it is characterized in that described component A comprises one or more in hydrogen, inert gas, oxygen, carbon dioxide, nitrogen, propane, ethane, HFC-134a, methane, halide and the ethene.
9. according to the absorption type heat converter of claim 7 or 8 described no mechanical powers drivings, it is characterized in that described B component comprises one or more in water, alkane, alkane halide, the pure and mild ether.
10. the absorption type heat converter that drives according to the described no mechanical power of the arbitrary claim of claim 1～8, it is characterized in that the absorbent of circulation comprises one or more in inorganic salts, alcohol, ether, ketone, amine, aldehyde and the ionic liquid in the described absorption type heat converter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100797068A CN102213501B (en) | 2011-03-31 | 2011-03-31 | Mechanical work drive-free absorption type thermal converter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100797068A CN102213501B (en) | 2011-03-31 | 2011-03-31 | Mechanical work drive-free absorption type thermal converter |
Publications (2)
| Publication Number | Publication Date |
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| CN102213501A true CN102213501A (en) | 2011-10-12 |
| CN102213501B CN102213501B (en) | 2012-07-25 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011100797068A Expired - Fee Related CN102213501B (en) | 2011-03-31 | 2011-03-31 | Mechanical work drive-free absorption type thermal converter |
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| CN (1) | CN102213501B (en) |
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| CN107060926A (en) * | 2017-01-25 | 2017-08-18 | 天津大学 | A kind of middle low temperature heat energy combined generating system of utilization two-phase pipe airlift pump |
| CN107192163A (en) * | 2017-07-06 | 2017-09-22 | 华南理工大学 | A kind of semiconductor absorber propagation property refrigerating plant |
| CN114322354A (en) * | 2021-12-20 | 2022-04-12 | 安徽普泛能源技术有限公司 | Absorption type circulating refrigeration system and process thereof |
| CN116123749A (en) * | 2022-12-20 | 2023-05-16 | 大连海事大学 | Pump-driven jet boosting diffusion absorption type heat converter |
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| CN202066245U (en) * | 2011-03-31 | 2011-12-07 | 浙江大学 | Absorption type thermal converter without mechanical power driving |
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| CN114322354A (en) * | 2021-12-20 | 2022-04-12 | 安徽普泛能源技术有限公司 | Absorption type circulating refrigeration system and process thereof |
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| CN116123749A (en) * | 2022-12-20 | 2023-05-16 | 大连海事大学 | Pump-driven jet boosting diffusion absorption type heat converter |
| CN116123749B (en) * | 2022-12-20 | 2024-04-09 | 大连海事大学 | Pump-driven jet boosting diffusion absorption type heat converter |
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| CN102213501B (en) | 2012-07-25 |
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