CN102818395B - Mixed working medium cold convertor for profound hypothermia - Google Patents
Mixed working medium cold convertor for profound hypothermia Download PDFInfo
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- CN102818395B CN102818395B CN201210255406.5A CN201210255406A CN102818395B CN 102818395 B CN102818395 B CN 102818395B CN 201210255406 A CN201210255406 A CN 201210255406A CN 102818395 B CN102818395 B CN 102818395B
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- 230000002631 hypothermal effect Effects 0.000 title claims abstract description 28
- 239000006096 absorbing agent Substances 0.000 claims abstract description 23
- 230000006835 compression Effects 0.000 claims abstract description 17
- 238000007906 compression Methods 0.000 claims abstract description 17
- 239000003507 refrigerant Substances 0.000 claims description 192
- 239000012530 fluid Substances 0.000 claims description 83
- 238000005482 strain hardening Methods 0.000 claims description 54
- 238000009835 boiling Methods 0.000 claims description 43
- 238000010521 absorption reaction Methods 0.000 claims description 27
- 238000009833 condensation Methods 0.000 claims description 10
- 230000005494 condensation Effects 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 9
- 238000004804 winding Methods 0.000 claims description 4
- 239000002440 industrial waste Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 239000012595 freezing medium Substances 0.000 abstract 9
- 239000002609 medium Substances 0.000 abstract 4
- 230000008014 freezing Effects 0.000 abstract 2
- 238000007710 freezing Methods 0.000 abstract 2
- 230000005611 electricity Effects 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 abstract 1
- 239000000203 mixture Substances 0.000 description 39
- 238000005057 refrigeration Methods 0.000 description 25
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 13
- 230000002745 absorbent Effects 0.000 description 8
- 239000002250 absorbent Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 4
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- -1 carbon hydrocarbon compound Chemical class 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- RWRIWBAIICGTTQ-UHFFFAOYSA-N difluoromethane Chemical compound FCF RWRIWBAIICGTTQ-UHFFFAOYSA-N 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N dimethylmethane Natural products CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation 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
- 230000008020 evaporation Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000002608 ionic liquid Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 201000009240 nasopharyngitis Diseases 0.000 description 1
- 229910052754 neon Inorganic materials 0.000 description 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 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
- 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]
- Y02B30/70—Efficient control or regulation technologies, e.g. for control of refrigerant flow, motor or heating
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- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention discloses a mixed working medium cold convertor for profound hypothermia. The mixed working medium cold convertor comprises a generator, a first condenser, an absorber, a solution heat exchanger, a first freezing medium heat exchanger, a fifth freezing medium throttling device, a solution throttling device, a solution pump, a first component separating device, a third freezing medium throttling device, a third freezing medium heat exchanger, a fourth freezing medium heat exchanger, a fourth freezing medium throttling device, an evaporator, a compressor and a second condenser; and two pipelines between the first freezing medium heat exchanger and the fifth freezing medium throttling device carry out heat exchange by the fourth freezing medium heat exchanger. According to the mixed working medium cold convertor for profound hypothermia, a certain proportion of low grade cold quantity obtained in an absorbing type freezing manner can be exchanged into high grade cold quantity for profound hypothermia in a temperature zone at a temperature of less than minus 70 DEG C, so that the utilization rate of solar energy, floor heating and industrial waste heat as well as the efficiency of the compression freezing module are improved greatly, electricity consumption is reduced, and scientific grade utilization of energy is implemented, therefore, the mixed working medium cold convertor is good in energy-saving and emission-reducing effect and bright in application prospect.
Description
Technical field
The invention belongs to cryogenic refrigeration field, be specifically related to a kind of mixed working fluid cold convertor for profound hypothermia.
Background technology
The energy is the material base that maintains human society stable operation.But along with industrial development, the mankind sharply rise to the consumption of the energy, have caused energy starved situation.International Energy Agency (IEA) prediction, from 2006 to the year two thousand thirty, world's primary energy demand will rise to 170.1 hundred million tons of oil equivalents from 117.3 hundred million tons of oil equivalents.And the situation of China also allows of no optimist, although government pays much attention to energy problem, it is predicted that maximum power breach in 2011 reaches 30,000,000 kilowatts.And consume in a large number the fossil energy such as coal, oil and also caused serious environmental problem.As can be seen here, utilizing efficiently clean energy resource in refrigerating field promotion is the emphasis of future development.
At present, absorption refrigeration can effectively utilize a large amount of low-grade heats in the whole world, and such as solar heat, industrial waste heat, underground heat etc. reaches the object of energy-saving and emission-reduction.But traditional Absorption Refrigerator adopts H conventionally
2o/LiBr, NH
3/ H
2o etc. are as working medium, and cryogenic temperature is higher or have certain toxicity, has limited their scope of application.And the Absorption Refrigerator being driven by low-grade heat is subject to the impact of evaporating temperature, in the time that cryogenic temperature is lower, efficiency is very low even can not work.Restriction absorption refrigeration is at present not yet to find to absorb well the absorbent of the low-temperature refrigerants such as methane, ethane, nitrogen for the main cause of low temperature warm area, cannot be with these low-temperature refrigerant composition working medium to being applied to the absorption refrigeration of low temperature warm area.
For obtaining lower cryogenic temperature, publication number is that the patent documentation of CN11436990A discloses a kind of absorbing low-temperature refrigerator, the outlet of this Cryo Refrigerator generating unit refrigerant vapour is joined through main condenser and overlapping unit refrigerant inlet voluntarily, and liquid phase refrigerant outlet in overlapping unit is joined through regenerator high-pressure channel, the first decompressor, evaporimeter, regenerator low-pressure channel and absorptive unit the first refrigerant inlet voluntarily; Vapor phase refrigerant outlet in overlapping unit is joined with absorptive unit second refrigerant entrance voluntarily; Absorptive unit taphole joins through solution pump and solution heat exchanger concentrated solution passage and generating unit solution entrance, and generating unit taphole joins through solution heat exchanger weak solution passage and absorptive unit solution entrance.The advantage of this refrigeration machine is under not high low grade heat energy drives, just to reach the conventional absorption refrigeration deep-frozen below-40 DEG C that is beyond one's reach, and cryogenic temperature wide ranges, efficiency are high, stable and reliable for performance, compact conformation.Although above-mentioned refrigeration machine adopts the runback stack structure of mix refrigerant, lowest refrigerating temperature is also difficult to lower than-50 DEG C, be used for lower warm area and hardly may.For obtaining lower cryogenic temperature, publication number is that the patent documentation of CN1380525 discloses a kind of refrigeration equipment with cryogenic refrigeration absorbent, this device adopts the outlet of generator refrigerant vapour to join through condenser and component separation module, and outlet and the absorber of component separation module join; Another outlet of component separation module is joined through regenerator high-pressure channel, the first expansion gear, evaporimeter, regenerator low-pressure channel and absorber; Absorber liquid-phase outlet joins through solution pump, solution heat exchanger and generator solution entrance, and generator taphole joins through solution heat exchanger, the second expansion gear and absorber solution entrance.This device cold-producing medium used is binary or mix refrigerant more than binary, and absorbent is the organic solvent that can absorb these cold-producing mediums.Can realize the deep refrigerating that just can realize lower temperature with heat-driven by this device.This device performance is reliable, efficiency is high, applied widely, can be used for the occasion that existing thermal source needs again cryogenic refrigeration.But the electric energy that utilizes this device to consume is more, refrigeration cost is higher, and also cannot reach-70 DEG C of following cryogenic temperatures.
Summary of the invention
The present invention proposes a kind of mixed working fluid cold convertor for profound hypothermia, this converter is composited by absorption refrigeration subcycle and compression refrigeration subcycle, with low grade residual heat driving absorption refrigeration subcycle, the refrigerating capacity of its generation is for the condenser/evaporator of cooled compressed refrigeration subcycle, can increase the refrigerating capacity of compression refrigeration subcycle, improve the efficiency of compression refrigeration subcycle, can reduce cryogenic temperature, reduce the consumption of electric energy, can efficiently utilize solar energy simultaneously, industrial waste heat and waste heat, the low-grade heats such as underground heat, can realize the deep refrigerating of-80 DEG C of following warm areas.
For a mixed working fluid cold convertor for profound hypothermia, comprise absorption from overlapping unit and compression from overlapping unit,
Described absorption generator, the first condenser, absorber, solution heat exchanger, the first refrigerant heat exchanger, the 5th cold-producing medium throttling arrangement, solution throttling arrangement and the solution pump of comprising from overlapping unit; The cold working medium pipeline that the refrigerant outlet of described generator passes through hot working fluid pipeline, the 5th cold-producing medium throttling arrangement and first refrigerant heat exchanger of the first condenser, the first refrigerant heat exchanger is successively communicated with the refrigerant inlet of absorber; The taphole of described generator is communicated with the solution entrance of absorber by hot working fluid pipeline and the solution throttling arrangement of solution heat exchanger successively, and the taphole of absorber is communicated with the solution entrance of generator by the cold working medium pipeline of solution pump and solution heat exchanger successively;
Described compression comprises the first component separating device, the 3rd cold-producing medium throttling arrangement, the 3rd refrigerant heat exchanger and the 4th refrigerant heat exchanger, the 4th cold-producing medium throttling arrangement, evaporimeter, compressor and the second condenser from overlapping unit; The low boiling component outlet of the first described component separating device is communicated with evaporator inlet by the first hot working fluid pipeline of the 4th refrigerant heat exchanger, hot working fluid pipeline and the 4th cold-producing medium throttling arrangement of the 3rd refrigerant heat exchanger successively, evaporator outlet is communicated with the entrance of compressor by the cold working medium pipeline of the 3rd refrigerant heat exchanger, the first cold working medium pipeline of the 4th refrigerant heat exchanger successively, and the outlet of compressor is communicated with the entrance of the first component separating device by the second condenser; The high boiling component outlet of the first described component separating device is communicated with the first cold working medium entrance of the 4th refrigerant heat exchanger by the 3rd cold-producing medium throttling arrangement;
Between the hot working fluid pipe outlet of the first described refrigerant heat exchanger and the 5th cold-producing medium throttling arrangement entrance, form the first pipeline, between the 5th described cold-producing medium throttling arrangement outlet and the cold working medium entrance of the first refrigerant heat exchanger, form the second pipeline, the first described pipeline and the second pipeline carry out heat exchange by the 4th described refrigerant heat exchanger.
The 4th described refrigerant heat exchanger is four-way heat exchanger, is respectively equipped with two hot working fluid pipelines and two cold working medium pipelines in it, is respectively the first hot working fluid pipeline, the second hot working fluid pipeline, the first cold working medium pipeline and the second cold working medium pipeline.The high-grade cold that utilizes the 4th refrigerant heat exchanger to realize the low-grade cold being obtained by absorption refrigeration to be transformed to low temperature warm area, has improved energy utilization rate.
The solution of discharging from compressor outlet, carry more heat, for making full use of this part heat, a kind of preferred technical scheme is: between the cold working medium entrance of described solution delivery side of pump and solution heat exchanger, form the 3rd pipeline; Between described compressor outlet and the second condenser inlet, form the 4th pipeline; Described the 3rd pipeline and the 4th pipeline carry out heat exchange by cold-producing medium-solution heat exchanger.The setting of cold-producing medium-solution heat exchanger, the concentrated solution that makes this part heat can be used for the cold working medium pipe outlet of solution heat exchanger to discharge is carried out further preheating, further reduce the energy consumption of generator, the HTHP mix refrigerant that compressor is discharged is pulled away part heat through cold-producing medium-solution heat exchanger simultaneously, has improved capacity usage ratio.
The gas-liquid separator that the first described component separating device can select one or more series winding to arrange; Also can select rectifier unit.When concrete selection, the cryogenic temperature that need to reach as required determines, when the cryogenic temperature obtaining when needs is not very low, for example, during higher than-60 DEG C, generally can select to utilize one or more gas-liquid separator to carry out the separation of one or many component.And obtain the occasion of lower cryogenic temperature for needs, for example, during less than or equal to-60 DEG C, for the lubricating oil of avoiding carrying in low boiling component solidifies rear obstruction the 4th cold-producing medium throttling arrangement, cause refrigeration machine normally to move, now described component separating device is rectifier unit.Certainly, also can adopt rectifier unit to replace one or more gas-liquid separator at cryogenic temperature higher than-60 DEG C in the situation that.Utilize rectifier unit to replace many gas-liquid separators, in improving separative efficiency and ensureing the stability of refrigerator operation, also reduced pipeline installation difficulty.
In the time that the first component separating device is selected rectifier unit, further preferred technical scheme is: the first cold working medium pipe outlet of the 4th described refrigerant heat exchanger is first communicated with the entrance of compressor through the condensation channel of rectifier unit tower top again.Adopt this technical scheme, in realizing Cold Reuse, also saved the cooling energy consumption of rectifier unit tower top, further reduced refrigeration cost.
For further reducing refrigerating capacity, in another kind of preferred technical scheme, also comprise second refrigerant heat exchanger; The high boiling component outlet of the first described component separating device is first communicated with described the 3rd cold-producing medium throttling arrangement through the first hot working fluid pipeline of second refrigerant heat exchanger again; The hot working fluid pipe outlet of the first described refrigerant heat exchanger is communicated with by the cold working medium pipeline of the second hot working fluid entrance, the first cold-producing medium throttling arrangement and second refrigerant heat exchanger and the cold working medium entrance of the first refrigerant heat exchanger of second refrigerant heat exchanger successively.The setting of second refrigerant heat exchanger, make, in the time that the absorption cold from the output of overlapping unit is more, this part cold to be divided into two parts according to actual needs: the low boiling point refrigerant that a part of cold is discharged for the low boiling component outlet to the first component separating device carries out precooling; The higher boiling cold-producing medium that another part cold is discharged for the high boiling component outlet to the first component separating device carries out further precooling, further improve the cryogenic temperature of evaporimeter, improved the utilization ratio of the absorption cold carrying from overlapping unit simultaneously.
When absorption adopt polynary cold-producing medium in overlapping unit time, for further improving refrigerating capacity, a kind of preferred technical scheme is: between the outlet of the first described condenser and the hot working fluid entrance of the first refrigerant heat exchanger, be provided with second component separator; The entrance of described second component separator is communicated with the outlet of the first condenser, the high boiling component outlet of second component separator is communicated with the cold working medium entrance of the first refrigerant heat exchanger by second refrigerant throttling arrangement, and the low boiling component outlet of second component separator is communicated with the hot working fluid entrance of the first refrigerant heat exchanger.The gas-liquid separator that described second component separator can select one or more series winding to arrange.
For further improving versatility of the present invention, further preferred technical scheme is: the pipeline between the outlet of the first described condenser and the entrance of second component separator is provided with the first stop valve; Pipeline between low boiling component outlet and the hot working fluid entrance of the first refrigerant heat exchanger of described second component separator is provided with the 3rd stop valve; Between the outlet of the first described condenser and the hot working fluid entrance of the first refrigerant heat exchanger, be provided with the pipeline with the second stop valve.The making of the first stop valve, the second stop valve and the 3rd stop valve absorptionly can adopt polynary cold-producing medium from overlapping unit, also can adopt one-component refrigerant; In the time adopting one-component refrigerant, only need open the second stop valve, close the first stop valve and the 3rd stop valve simultaneously; In the time adopting the cold-producing medium of multicomponent mixture, for improving refrigerating efficiency, can adopt and close the second stop valve, then open the first stop valve and the 3rd stop valve.
Mixed working fluid cold convertor for profound hypothermia of the present invention:
Described is absorption in overlapping unit, cold-producing medium used can be selected carbon hydrocarbon compound, hydrogen fluorohydrocarbon compounds, and the binary being formed by carbon hydrocarbon compound or hydrogen fluorohydrocarbon compounds or mixed non-azeotropic refrigerant more than binary, absorbent is one or more in salt, alcohols, ethers, ketone, amine, aldehydes or ionic liquid.When actual use, all can select according to actual needs, be prior art.Described compression is in overlapping unit, and described cold-producing medium can be selected binary or mixed non-azeotropic refrigerant more than binary.Common cold-producing medium comprises carbon hydrocarbon compound, hydrogen fluorohydrocarbon compounds, ethene, methane, argon gas, xenon, neon and nitrogen.
Described the first condenser, solution heat exchanger, the first refrigerant heat exchanger, second refrigerant heat exchanger, the 3rd refrigerant heat exchanger, the 4th refrigerant heat exchanger, the second condenser, cold-producing medium-solution heat exchanger can be selected immersion, fountain, shell and tube, bushing type or plate type heat exchanger.
Described solution throttling arrangement, the first cold-producing medium throttling arrangement, second refrigerant throttling arrangement, the 3rd cold-producing medium throttling arrangement, the 4th cold-producing medium throttling arrangement and the 5th cold-producing medium throttling arrangement can be selected capillary, automatic or manual choke valve.
Described rectifier unit is filling extract rectification device or board-like rectifier unit.
Compared with prior art, the present invention has following useful technique effect:
(1) a certain proportion of low-grade cold being obtained by absorption refrigeration can be transformed to the high-grade cold of low temperature warm area, greatly improve the utilization rate of solar energy, underground heat and industrial waste heat.
(2) realized the scientific and reasonable management of energy, low-grade energy is used for producing low-grade cold, high-grade energy is used for producing high-grade cold, will greatly improve from its electrical efficiency of cascade refrigeration than existing mix refrigerant compression, has good effects of energy saving and emission reduction and application prospect.
(3) greatly expand the application warm area of absorption refrigeration, realized the application of absorption refrigeration low temperature warm area below-70 DEG C.
Brief description of the drawings
Fig. 1 is the structural representation of a kind of embodiment of the mixed working fluid cold convertor for profound hypothermia of the present invention.
Fig. 2 is the structural representation of the another kind of embodiment of the mixed working fluid cold convertor for profound hypothermia of the present invention.
Fig. 3 is the structural representation of the third embodiment of the mixed working fluid cold convertor for profound hypothermia of the present invention.
Fig. 4 is the structural representation of the 4th kind of embodiment of the mixed working fluid cold convertor for profound hypothermia of the present invention.
Fig. 5 is the structural representation of the 5th kind of embodiment of the mixed working fluid cold convertor for profound hypothermia of the present invention.
Fig. 6 is the structural representation of the 6th kind of embodiment of the mixed working fluid cold convertor for profound hypothermia of the present invention.
Detailed description of the invention
As shown in Figure 1, a kind of mixed working fluid cold convertor for profound hypothermia, comprise: absorption from overlapping unit and compression from overlapping unit, absorption generator 1, the first condenser 2, absorber 3, solution heat exchanger 4, solution throttling arrangement 5, solution pump 6, the first refrigerant heat exchanger 16 and the 5th cold-producing medium throttling arrangement 24 of comprising from overlapping unit.Compression comprises the first component separating device 7, the 3rd cold-producing medium throttling arrangement 8, the 3rd refrigerant heat exchanger 9, the 4th refrigerant heat exchanger 10, the 4th cold-producing medium throttling arrangement 11, evaporimeter 12, compressor 13 and the second condenser 14 from overlapping unit.Wherein, in the 4th refrigerant heat exchanger 10, be provided with four passages, be respectively the first hot working fluid pipeline, the second hot working fluid pipeline, the first cold working medium pipeline and the second cold working medium pipeline.
Annexation between above-mentioned each parts is:
The taphole 1a of generator 1 is communicated with the hot working fluid entrance 4a of solution heat exchanger 4, the hot working fluid pipe outlet 4b of solution heat exchanger 4 is communicated with the entrance 5a of solution throttling arrangement 5, and the outlet 5b of solution throttling arrangement 5 is communicated with the solution entrance 3b of absorber 3, the refrigerant outlet 1b of generator 1 is communicated with the entrance 2a of the first condenser 2, the outlet 2b of the first condenser 2 is communicated with the hot working fluid entrance 16a of the first refrigerant heat exchanger 16, the hot working fluid pipe outlet 16b of the first refrigerant heat exchanger 16 is communicated with the entrance 10e of the second hot working fluid pipeline of the 4th refrigerant heat exchanger 10, the outlet 10f of the second hot working fluid pipeline of the 4th refrigerant heat exchanger 10 is communicated with the entrance 24a of the 5th cold-producing medium throttling arrangement 24, the outlet 24b of the 5th cold-producing medium throttling arrangement 24 is communicated with the second cold working medium pipeline 10g entrance of the 4th refrigerant heat exchanger 10, the outlet 10h of the second cold working medium pipeline of the 4th refrigerant heat exchanger 10 is communicated with the cold working medium entrance 16c of the first refrigerant heat exchanger 16, the cold working medium pipe outlet 16d of the first refrigerant heat exchanger 16 is communicated with the refrigerant inlet 3c of absorber 3.The taphole 3a of absorber 3 is communicated with the entrance 6a of solution pump 6, and the outlet 6b of solution pump 6 is communicated with the cold working medium entrance 4c of solution heat exchanger 4, and the cold working medium pipe outlet 4d of solution heat exchanger 4 is communicated with the solution entrance 1c of generator 1.
The low boiling component outlet 7c of the first component separating device 7 is communicated with the first hot working fluid entrance 10a of the 4th refrigerant heat exchanger 10, the first hot working fluid pipe outlet 10b of the 4th refrigerant heat exchanger 10 is communicated with the hot working fluid entrance 9a of the 3rd refrigerant heat exchanger 9, the hot working fluid pipe outlet 9b of the 3rd refrigerant heat exchanger 9 is communicated with the entrance 11a of the 4th cold-producing medium throttling arrangement 11, the outlet 11b of the 4th cold-producing medium throttling arrangement 11 is communicated with the entrance 12a of evaporimeter 12, the outlet 12b of evaporimeter 12 is communicated with the cold working medium entrance 9c of the 3rd refrigerant heat exchanger 9, the cold working medium pipe outlet 9d of the 3rd refrigerant heat exchanger 9 is communicated with the first cold working medium entrance 10c of the 4th refrigerant heat exchanger 10, the first cold working medium pipe outlet 10d of the 4th refrigerant heat exchanger 10 is communicated with the entrance 13a of compressor 13, the outlet 13b of compressor 13 is communicated with the entrance 14a of the second condenser 14, the outlet 14b of the second condenser 14 is communicated with the entrance 7a of the first component separating device 7, the high boiling component outlet 7b of the first component separating device 7 is communicated with the entrance 8a of the 3rd cold-producing medium throttling arrangement 8, and the outlet 8b of the 3rd cold-producing medium throttling arrangement 8 is communicated with the first cold working medium entrance 10c of the 4th refrigerant heat exchanger 10.
Taking absorption HFC-134a (R134a) and the difluoromethane (R32) of adopting from overlapping unit as mix refrigerant, adopting dimethyl formamide (DMF) is absorbent, it is mix refrigerant that compression adopts R134a and R23 from overlapping unit, and the detailed operation flow process of the above-mentioned mixed working fluid cold convertor for profound hypothermia is described:
The mix refrigerant (R134a and R32) of the HTHP that generator 1 produces enters the first condenser 2 condensation heat releases, then enter and in the first refrigerant heat exchanger 16, after precooling, enter precooling in the 4th refrigerant heat exchanger 10, then after the 5th cold-producing medium throttling arrangement 24 throttlings, enter and in the 4th refrigerant heat exchanger 10, other mix refrigerant is carried out coolingly, then be back to after the first refrigerant heat exchanger 16 absorbs a part of heat and enter absorber 3.The high temperature weak solution being flowed out by generator 1, after solution heat exchanger 4 is by precooling, enters absorber 3 through solution throttling arrangement 5, after the mix refrigerant of absorption from the first refrigerant heat exchanger 16, becomes concentrated solution.Concentrated solution outlet by absorber 3 is preheated through solution heat exchanger 4 after solution pump 6 pressurizes, and enters subsequently generator 1, completes the circulation of solution loop.
The HTHP mix refrigerant (R134a and R23) that compressor 13 is discharged enters the first component separating device 7 after the second condenser 14 condensation heat releases, outlet taking R134a as main higher boiling mix refrigerant from the first component separating device 7 bottoms is flowed out, after the 3rd cold-producing medium throttling arrangement 8, temperature reduces, and with reflux mixes the low boiling mix refrigerant in precooling the 4th refrigerant heat exchanger 10 afterwards taking R23 as main low boiling mix refrigerant.The low boiling mix refrigerant of the top enrichment of the first component separating device 7 in the 4th refrigerant heat exchanger 10 by precooling, then entering the 3rd refrigerant heat exchanger 9 is further cooled, after the 4th cold-producing medium throttling arrangement 11, temperature reduces afterwards, enters evaporimeter 12 evaporation endothermics.From evaporimeter 12 low boiling mix refrigerant out through after the 3rd refrigerant heat exchanger 9, after mixing with from the higher boiling mix refrigerant of the 3rd cold-producing medium throttling arrangement 8, enter the 4th refrigerant heat exchanger 10, precooling low boiling mix refrigerant wherein, finally this strand of cold-producing medium got back to compressor 13, completes compression runback and fold the circulation of cold loop.
In this embodiment, the first component separating device 7 is selected gas-liquid separator.Utilize the mixed working fluid cold convertor for profound hypothermia of present embodiment, can obtain by regulation and control the cryogenic temperature of-30 DEG C～-60 DEG C.
As shown in Figure 2, difference from Example 1 is, between 6 outlets of solution pump and the cold working medium entrance of solution heat exchanger 4 pipeline (being defined as the first pipeline) and compressor 13 exports and the second condenser 14 entrances between pipeline (being defined as the second pipeline) carry out heat exchange by cold-producing medium-solution heat exchanger 20.Wherein, the hot working fluid entrance 20a of cold-producing medium-solution heat exchanger 20 exports 13b with compressor 13 and is communicated with, and the hot working fluid pipe outlet 20b of cold-producing medium-solution heat exchanger 20 is communicated with the entrance 14a of the second condenser 14; Cold working medium entrance 20c and the solution pump 6 of cold-producing medium-solution heat exchanger 20 exports 6b and is communicated with the cold working medium entrance 20c of cold-producing medium-solution heat exchanger 20, the cold working medium pipe outlet 20d of cold-producing medium-solution heat exchanger 20 is communicated with the cold working medium entrance 4c of solution heat exchanger 4, and the cold working medium pipe outlet 4d of solution heat exchanger 4 is communicated with the solution entrance 1c of generator 1.Other parts annexation is with embodiment 1.
Present embodiment adopts cold-producing medium and the absorbent identical with embodiment 1, be from embodiment 2, workflow is different: concentrated solution (R134a, R32 and DMF) by the taphole 3a of absorber 3 after solution pump 6 pressurizes through cold-producing medium-solution heat exchanger 20 by preliminary preheating after, then enter solution heat exchanger 4 by further preheating, enter subsequently generator 1, complete the circulation of solution loop.The HTHP mix refrigerant (R134a and R23) that compressor 13 is discharged is pulled away part heat through cold-producing medium-solution heat exchanger 20 and then enters the second condenser 14 condensations, and other workflow is with embodiment 1.Utilize this embodiment, realized the recycling of compressor 13 being discharged to the heat carrying in material, improved the refrigeration performance of the present invention for the mixed working fluid cold convertor of profound hypothermia, power consumption is lower.
As shown in Figure 3, difference from Example 2 is, in this embodiment, the first component separating device 7 is rectifier unit, and rectifier unit can be selected stuffing rectification column or plate distillation column.The first cold working medium pipe outlet 10d of the 4th refrigerant heat exchanger 10 is first communicated with the entrance 13a of compressor 13 through the condensation channel of the first component separating device 7 tower tops again, utilizes the cold carrying in the 4th refrigerant heat exchanger 10 low boiling point refrigerant out to carry out cooling to the material of the first component separating device 7 tower tops.
In this embodiment, absorption is mix refrigerant from overlapping unit employing HFC-134a (R134a) and difluoromethane (R32), adopting dimethyl formamide (DMF) is absorbent, and compression adopts the mixture of HFC-134a (R134a), fluoroform (R23), ethene and methane composition from overlapping unit be cold-producing medium.
In the present embodiment, the annexation of each parts is as follows: the first cold working medium pipe outlet 10d of the 4th refrigerant heat exchanger 10 is first communicated with the condensation channel entrance 7d of rectifier unit tower top, and the condensation channel outlet 7e of rectifier unit tower top is communicated with the entrance 13a of compressor 13 again.The annexation of other parts is with embodiment 2.
Be from embodiment 2, workflow is different, from the lower low boiling mix refrigerant of evaporimeter 12 temperature out (taking ethene and methane as main) successively through the 3rd refrigerant heat exchanger 9, the 4th refrigerant heat exchanger 10 precoolings hot fluid wherein, then enter the condensation channel of rectifier unit, provide rectifying required cold, then enter compressor 13.Other related work flow process is with embodiment 2.
While utilizing the cold-producing medium of the present embodiment to freeze, evaporimeter can obtain the cryogenic temperature of-60 DEG C～-150 DEG C; In meeting evaporimeter cryogenic temperature, provide cold to carry out rectifying without the external world, save energy.
Embodiment 4
As shown in Figure 4, be with the difference of embodiment 3, also comprise second refrigerant heat exchanger 21 and the first cold-producing medium throttling arrangement 18; The high boiling component outlet of the first component separating device 7 is first communicated with the 3rd cold-producing medium throttling arrangement 8 through the first hot working fluid pipeline of second refrigerant heat exchanger 21 again, and the hot working fluid pipe outlet of the first refrigerant heat exchanger 16 is communicated with by the cold working medium pipeline of the second hot working fluid entrance, the first cold-producing medium throttling arrangement 18 and second refrigerant heat exchanger 21 and the cold working medium entrance of the first refrigerant heat exchanger 16 of second refrigerant heat exchanger 21 successively.Concrete annexation is: the second hot working fluid entrance 21a of second refrigerant heat exchanger 21 is communicated with the hot working fluid pipe outlet 16b of the first refrigerant heat exchanger 16, the second hot working fluid pipe outlet 21b of second refrigerant heat exchanger 21 is communicated with the entrance 18a of the first cold-producing medium throttling arrangement 18, the outlet 18b of the first cold-producing medium throttling arrangement 18 is communicated with the cold working medium entrance 21c of second refrigerant heat exchanger 21, and the cold working medium pipe outlet 21d of second refrigerant heat exchanger 21 is communicated with the cold working medium entrance 16c of the first refrigerant heat exchanger 16.Other parts annexation is with embodiment 3; The high boiling component outlet 7b of the first component separating device 7 is communicated with the first hot working fluid entrance 21e of second refrigerant heat exchanger 21, and the first hot working fluid pipe outlet 21f of second refrigerant heat exchanger 21 is communicated with the entrance 18a of the first cold-producing medium throttling arrangement 18.The annexation of other parts is with embodiment 3.
Be from embodiment 3, workflow is different: be divided into two parts in the first refrigerant heat exchanger 16 by the mix refrigerant of precooling (R134a and R32), a part enters into the 4th refrigerant heat exchanger 10, and low boiling mix refrigerant wherein of precooling (taking ethene and methane as main) is got back in absorber 3 by the first refrigerant heat exchanger 16; Another part mix refrigerant enters into second refrigerant heat exchanger 21 to carry out after cooling being mixed together entering in absorber 3 after the cold-producing medium precooling in the first refrigerant heat exchanger 16 with the 4th refrigerant heat exchanger 10 cold-producing medium out to higher boiling mix refrigerant (R134a and R23 are main) wherein.Other related work flow process is with embodiment 3.
While utilizing the cold-producing medium of the present embodiment to freeze, evaporimeter can obtain the cryogenic temperature of-60 DEG C～-150 DEG C, can utilize low-grade heat to obtain more low temperature position refrigerating capacity simultaneously.
As shown in Figure 5, difference from Example 4 is: between the outlet of the first condenser 2 and the hot working fluid entrance of the first refrigerant heat exchanger 16, be provided with second component separator 15; The entrance of second component separator 15 is communicated with the outlet of the first condenser 2, the high boiling component outlet of second component separator 15 is communicated with the hot working fluid pipe outlet of the first refrigerant heat exchanger 16 by second refrigerant throttling arrangement 19, and the low boiling component outlet of second component separator 15 is communicated with the hot working fluid entrance of the first refrigerant heat exchanger 16.Concrete annexation is: second component separator 15 is gas-liquid separator, its entrance 15c is communicated with the outlet 2b of the first condenser 2, the high boiling component outlet 15a of second component separator 15 is communicated with the entrance 19a of second refrigerant throttling arrangement 19, and the outlet 19b of second refrigerant throttling arrangement 19 is communicated with the cold working medium entrance 16c of the first refrigerant heat exchanger 16; The low boiling component outlet 15b of second component separator 15 is communicated with the hot working fluid entrance 16a of the first refrigerant heat exchanger 16.Other parts annexation is with embodiment 4.
In this embodiment, absorption is mix refrigerant from overlapping unit employing HFC-134a (R134a) and fluoroform (R23), adopting dimethyl formamide (DMF) is absorbent, and compression adopts the mixture of iso-butane (R600a), propane alkane (R290), ethene (R1150), methane (R50) and nitrogen (R728) composition from overlapping unit be cold-producing medium.
Be from embodiment 4, workflow is different: the mix refrigerant (R134a and R23) of the HTHP that generator 1 produces enters the first condenser 2 condensation heat releases, then enter second component separator 15, in second component separator 15, higher boiling mix refrigerant (R134a is main) is enriched in the liquid phase of bottom, flow out from the higher boiling outlet of bottom, after second refrigerant throttling arrangement 19, become the relatively low mix refrigerant of temperature and mix the low boiling mix refrigerant in rear precooling the first refrigerant heat exchanger 16 with the low boiling mix refrigerant (R23 is main) of backflow, in the enrichment of the top of second component separator 15 low boiling mix refrigerant, this part cold-producing medium in the first refrigerant heat exchanger 16 by precooling, then share split enters cooling mix refrigerant wherein in the 4th refrigerant heat exchanger 10 and second refrigerant heat exchanger 21, and other workflow is with embodiment 4.
In present embodiment, due to adding of second component separator 15, the absorption cryogenic temperature from overlapping unit is minimized, refrigerating efficiency is improved, thereby compression can obtain-180 DEG C and lower cryogenic temperature from overlapping unit, or obtain more refrigerating capacity, improved the degree that low-grade heat utilizes.
Embodiment 6
As shown in Figure 6, difference from Example 5 is, the pipeline of the entrance 15c of the outlet of the first condenser 2 and second component separator 15 is provided with the first stop valve 17; Pipeline between low boiling component outlet and the hot working fluid entrance of the first refrigerant heat exchanger 16 of second component separator 15 is provided with the 3rd stop valve 23; Between the hot working fluid entrance of the outlet of the first condenser 2 and the first refrigerant heat exchanger 16, be provided with the pipeline with the second stop valve 22.Concrete annexation is: the entrance 17a of the first stop valve 17 is communicated with the outlet 2b of the first condenser 2, and outlet 17b is communicated with the entrance 15c of second component separator 15; The entrance 22a of the second stop valve 22 is communicated with the outlet 2b of the second condenser 2, and outlet is communicated with the hot working fluid entrance 16a of the first refrigerant heat exchanger 16; The entrance 23a of the 3rd stop valve 23 is communicated with the low boiling component of second component separator 15 outlet 15b, and outlet 23b is communicated with the hot working fluid entrance 16a of the first refrigerant heat exchanger 16.Other parts annexation is with embodiment 5.In the time adopting polynary cold-producing medium, for improving refrigerating efficiency, need to use second component separator 15, now only need close the second stop valve 22, open the first stop valve 17 and the 3rd stop valve 23; In the time not needing to use second component separator 15, close the first stop valve 17, the 3rd stop valve 23 and second refrigerant throttling arrangement 19, then open the second stop valve 22.
In above-mentioned embodiment,
The first condenser, solution heat exchanger, the first refrigerant heat exchanger, second refrigerant heat exchanger, the 3rd refrigerant heat exchanger, the 4th refrigerant heat exchanger, the second condenser, cold-producing medium-solution heat exchanger can be selected immersion, fountain, shell and tube, bushing type or plate type heat exchanger, concrete which kind of heat exchanger of selecting need to be determined according to actual needs, is prior art.
Solution throttling arrangement, the first cold-producing medium throttling arrangement, second refrigerant throttling arrangement, the 3rd cold-producing medium throttling arrangement, the 4th cold-producing medium throttling arrangement and the 5th cold-producing medium throttling arrangement can be selected capillary, automatic or manual choke valve, concrete which kind of throttling arrangement of selecting need to be determined according to actual needs, is prior art.
Rectifier unit can be selected filling extract rectification device or board-like rectifier unit, all can select according to actual needs, is prior art.
Claims (9)
1. for a mixed working fluid cold convertor for profound hypothermia, comprise absorption from overlapping unit and compression from overlapping unit,
Described absorption generator (1), the first condenser (2), absorber (3), solution heat exchanger (4), the first refrigerant heat exchanger (16), the 5th cold-producing medium throttling arrangement (24), solution throttling arrangement (5) and the solution pump (6) of comprising from overlapping unit; The cold working medium pipeline that the refrigerant outlet of described generator (1) passes through hot working fluid pipeline, the 5th cold-producing medium throttling arrangement (24) and first refrigerant heat exchanger (16) of the first condenser (2), the first refrigerant heat exchanger (16) is successively communicated with the refrigerant inlet of absorber (3); The taphole of described generator (1) is communicated with the solution entrance of absorber (3) by hot working fluid pipeline and the solution throttling arrangement (5) of solution heat exchanger (4) successively; The taphole of described absorber (3) is communicated with the solution entrance of generator (1) by the cold working medium pipeline of solution pump (6) and solution heat exchanger (4) successively;
Described compression comprises the first component separating device (7), the 3rd cold-producing medium throttling arrangement (8), the 3rd refrigerant heat exchanger (9) and the 4th refrigerant heat exchanger (10), the 4th cold-producing medium throttling arrangement (11), evaporimeter (12), compressor (13) and the second condenser (14) from overlapping unit, the low boiling component outlet of described the first component separating device (7) is successively by the first hot working fluid pipeline of the 4th refrigerant heat exchanger (10), the hot working fluid pipeline of the 3rd refrigerant heat exchanger (9) and the 4th cold-producing medium throttling arrangement (11) are communicated with evaporimeter (12) entrance, evaporimeter (12) outlet is successively by the cold working medium pipeline of the 3rd refrigerant heat exchanger (9), the first cold working medium pipeline of the 4th refrigerant heat exchanger (10) is communicated with the entrance of compressor (13), the outlet of compressor (13) is communicated with the entrance of the first component separating device (7) by the second condenser (14), the high boiling component outlet of described the first component separating device (7) is communicated with the first cold working medium entrance of the 4th refrigerant heat exchanger (10) by the 3rd cold-producing medium throttling arrangement (8),
It is characterized in that: between the hot working fluid pipe outlet of described the first refrigerant heat exchanger (16) and the 5th cold-producing medium throttling arrangement (24) entrance, form the first pipeline, between the 5th described cold-producing medium throttling arrangement (24) outlet and the cold working medium entrance of the first refrigerant heat exchanger (16), form the second pipeline, the first described pipeline and the second pipeline carry out heat exchange by the second hot working fluid pipeline and the second cold working medium pipeline that arrange in the 4th described refrigerant heat exchanger (10).
2. the mixed working fluid cold convertor for profound hypothermia according to claim 1, is characterized in that, between the outlet of described solution pump (6) and the cold working medium entrance of solution heat exchanger (4), forms the 3rd pipeline; Between described compressor (13) outlet and the second condenser (14) entrance, form the 4th pipeline; Described the 3rd pipeline and the 4th pipeline carry out heat exchange by cold-producing medium-solution heat exchanger (20).
3. the mixed working fluid cold convertor for profound hypothermia according to claim 1, is characterized in that, the gas-liquid separator that described the first component separating device (7) arranges for one or more series winding.
4. the mixed working fluid cold convertor for profound hypothermia according to claim 1, is characterized in that, described the first component separating device (7) is rectifier unit.
5. the mixed working fluid cold convertor for profound hypothermia according to claim 4, it is characterized in that, the condensation channel that the first cold working medium pipe outlet of the 4th described refrigerant heat exchanger (10) first passes through rectifier unit tower top is communicated with the entrance of compressor (13) again.
6. the mixed working fluid cold convertor for profound hypothermia according to claim 1, is characterized in that, also comprises second refrigerant heat exchanger (21);
The first hot working fluid pipeline that second refrigerant heat exchanger (21) is first passed through in the high boiling component outlet of described the first component separating device (7) is communicated with described the 3rd cold-producing medium throttling arrangement (8) again; The hot working fluid pipe outlet of described the first refrigerant heat exchanger (16) is communicated with by the second hot working fluid entrance, the first cold-producing medium throttling arrangement (18) and the cold working medium pipeline of second refrigerant heat exchanger (21) and the cold working medium entrance of the first refrigerant heat exchanger (16) of second refrigerant heat exchanger (21) successively.
7. the mixed working fluid cold convertor for profound hypothermia according to claim 1, it is characterized in that, between the outlet of described the first condenser (2) and the hot working fluid entrance of the first refrigerant heat exchanger (16), be provided with second component separator (15); The entrance of described second component separator (15) is communicated with the outlet of the first condenser (2), the high boiling component outlet of second component separator (15) is communicated with the cold working medium entrance of the first refrigerant heat exchanger (16) by second refrigerant throttling arrangement (19), and the low boiling component outlet of second component separator (15) is communicated with the hot working fluid entrance of the first refrigerant heat exchanger (16).
8. the mixed working fluid cold convertor for profound hypothermia according to claim 7, it is characterized in that, the pipeline between the outlet of described the first condenser (2) and second component separator (15) entrance is provided with the first stop valve (17); Pipeline between low boiling component outlet and the hot working fluid entrance of the first refrigerant heat exchanger (16) of described second component separator (15) is provided with the 3rd stop valve (23); Between the outlet of described the first condenser (2) and the hot working fluid entrance of the first refrigerant heat exchanger (16), be provided with the pipeline with the second stop valve (22).
9. according to the mixed working fluid cold convertor for profound hypothermia described in claim 7 or 8, it is characterized in that the gas-liquid separator that described second component separator (15) arranges for one or more series winding.
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| CN1363815A (en) * | 2002-01-25 | 2002-08-14 | 浙江大学 | Deep refrigerating method and equipment |
| CN1380525A (en) * | 2002-02-28 | 2002-11-20 | 浙江大学 | Refrigeration equipment with cryogenic refrigeration absorbent |
| DE10133905A1 (en) * | 2001-07-12 | 2003-01-23 | Inst Luft Kaeltetech Gem Gmbh | Method for acheiving very low refrigeration temperatures has a combination of compression and absorption processes using limited energy |
| US20050193758A1 (en) * | 2003-10-27 | 2005-09-08 | Wells David N. | System and method for selective heating and cooling |
| CN102141323A (en) * | 2011-03-11 | 2011-08-03 | 北京天际旭能太阳能制冷技术有限公司 | System combining compressor refrigerating and thermal refrigerating |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000274875A (en) * | 1999-03-26 | 2000-10-06 | Tokyo Gas Co Ltd | Composite cooling system and method for compositely cooling |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10133905A1 (en) * | 2001-07-12 | 2003-01-23 | Inst Luft Kaeltetech Gem Gmbh | Method for acheiving very low refrigeration temperatures has a combination of compression and absorption processes using limited energy |
| CN1363815A (en) * | 2002-01-25 | 2002-08-14 | 浙江大学 | Deep refrigerating method and equipment |
| CN1380525A (en) * | 2002-02-28 | 2002-11-20 | 浙江大学 | Refrigeration equipment with cryogenic refrigeration absorbent |
| US20050193758A1 (en) * | 2003-10-27 | 2005-09-08 | Wells David N. | System and method for selective heating and cooling |
| CN102141323A (en) * | 2011-03-11 | 2011-08-03 | 北京天际旭能太阳能制冷技术有限公司 | System combining compressor refrigerating and thermal refrigerating |
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| Title |
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| JP特开2000-274875A 2000.10.06 |
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