CN107407510A - Use the Absorption Cooling System of LGWP refrigerants - Google Patents
Use the Absorption Cooling System of LGWP refrigerants Download PDFInfo
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- CN107407510A CN107407510A CN201680014576.0A CN201680014576A CN107407510A CN 107407510 A CN107407510 A CN 107407510A CN 201680014576 A CN201680014576 A CN 201680014576A CN 107407510 A CN107407510 A CN 107407510A
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K5/00—Heat-transfer, heat-exchange or heat-storage materials, e.g. refrigerants; Materials for the production of heat or cold by chemical reactions other than by combustion
- C09K5/02—Materials undergoing a change of physical state when used
- C09K5/04—Materials undergoing a change of physical state when used the change of state being from liquid to vapour or vice versa
- C09K5/047—Materials undergoing a change of physical state when used the change of state being from liquid to vapour or vice versa for absorption-type refrigeration systems
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/002—Machines, plants or systems, using particular sources of energy using solar energy
- F25B27/007—Machines, plants or systems, using particular sources of energy using solar energy in sorption type systems
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
- F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
- F25B2400/12—Inflammable refrigerants
- F25B2400/121—Inflammable refrigerants using R1234
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Engineering & Computer Science (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Sustainable Energy (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Lubricants (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
Absorption-type refrigerating method and system, it includes the refrigerant containing one or more HF hydrocarbons and/or hydro-chloro fluoroolefin and the solvent or absorbent selected from PAG oil, poly-a-olefin oil, mineral oil and/or polyalcohol ester oil.
Description
The cross reference of related application
The priority for the U.S. Provisional Application 62/101,718 submitted this application claims on January 9th, 2015, it is incorporated by through this
Herein.
Invention field
The present invention relates to use to have low global warming up trend（GWP）Potentiality is consumed with low-ozone（ODP）Refrigerant
Absorption system.
Background of invention
Used heat or other inexpensive thermals source can obtained（Such as solar energy heating）When, absorption refrigeration is to compression-type refrigeration
More economical replacement.Absorption Refrigerator and vapor compression refrigerator, which all use, has extremely lower boiling refrigerant.This two
In type, when this refrigerant evaporates or seethes with excitement, some heat all are taken away with it, to provide cooling effect.It is but absorption
The difference of refrigeration and steam compression type refrigerating is that refrigerant becomes liquid again so that the circulation repeats from gas.Steam compression type
Refrigeration machine using motor compressor improve gas pressure, then by with cooling agent（Typically air）Heat exchange and will heat it is high
Body of calming the anger condenses back liquid.Absorption Refrigerator is using only needing low-power pump or optionally only need the distinct methods of heat by gas
Become liquid again, thus eliminate the needs to movable part.
One importance of most of Absorption Cooling Systems is the refrigerant/absorbent pair for operating whole system.
It is that liquid and refrigerant are usually to use absorbent absorption refrigeration agent under conditions of gas in absorbent.Then this can be freezed
Pump pressurizes agent/absorber blend in liquid form（pumped）To higher pressure, thus avoid the need for using compressor.Should
Highly pressurised liquid mixture then separates to produce charging to the high pressure steam refrigerant of condenser and follow again at elevated pressures and temperatures
Loopback is gone to absorb the absorbent of the liquid form of more refrigerants.
Two kinds of most common absorption refrigerations are to being NH3- Shui Heshui-LiBr.NH3- water uses NH3As refrigerant and water
As absorbent.NH3Serve as refrigerant well in numerous applications.But NH3Toxicity limit it in public space
Use.In addition, ammonia is high corrosiveness and and copper（Common used material in cooling system）It is incompatible.
Water-LiBr is another conventional refrigerant pair in absorption system.Water has two shortcomings：Water freezes less than 0 DEG C, and
And due to low vapour density, it is necessary to big equipment size so that the solution it is limited in space position it is impracticable.
This conventional systems another problem is that evaporator and absorber are generally run at sub-atmospheric pressure, this is carried
The cost of high such system, because must be specifically designed the equipment safely to run under low pressure.
Therefore, there is still a need for the safer and environment-friendly refrigerant for absorption system.
General introduction
In certain non-limiting embodiments, the present invention relates to the refrigerant for absorption system and absorbent pair
It was found that.Some HF hydrocarbons and/or hydro-chloro fluoroolefins, refrigerant those are particularly suitable as, is at least partially soluble in oil,
Such as PAG（PAG）Oil, poly-a-olefin oil, mineral oil and polyol ester（POE）Oil.It has been found that refrigerant and oil
Some pairings can realize absorption system, and such system that including but not limited to thermal source includes solar thermal collector goes out
Color performance.The many of these refrigerants is with low GWP（I.e. relative to CO2For<1000, preferably<100）, it is low or without notable
ODP is characterized and nontoxic and non-combustible.
Correspondingly, one aspect of the present invention is related to the method for providing refrigeration, and it includes：(a) evaporation is included selected from one kind
Or the first liquid phase refrigerant logistics of the refrigerant of a variety of HF hydrocarbons, one or more hydro-chloro fluoroolefins and its blend is to produce
Raw low-pressure vapor phase refrigerant stream, wherein described evaporate from system heat of transfer to be cooled；(b) low-pressure vapor phase is made to freeze
Agent logistics and the comprising the solvent selected from PAG oil, poly-a-olefin oil, mineral oil, polyalcohol ester oil and combinations thereof
Substantially all refrigerants of the vapor phase refrigerant logistics are effectively being dissolved into the first liquid phase solvent by one liquid phase solvent logistics
Contacted in the solvent of logistics with producing under conditions of refrigerant-solvent solution logistics；(c) by from solar thermal collector to system
Cryogen-solvent solution heat transfer improves the pressure and temperature of the refrigerant-solvent solution logistics；(d) by the refrigerant-molten
Agent solution logistics thermodynamics is separated into high pressure vapor refrigerant stream and second liquid phase solvent stream；(e) by the second liquid phase
Solvent stream is recycled to step (b) to produce the first liquid phase solvent logistics；(f) the high pressure vapor refrigerant is condensed
Logistics is to produce second liquid phase refrigerant stream；(g) by the second liquid phase refrigerant stream be recycled to step (a) with
Produce the first liquid phase refrigerant logistics.
In certain embodiments of the invention, the absorption process is with economic benefits and social benefits（double effect）Or triple effect is characterized.
Correspondingly, absorption system is provided in another aspect of the present invention, and it is included：(a) one or more hydrogen fluorine alkene are selected from
The refrigerant of hydrocarbon, one or more hydro-chloro fluoroolefins and its blend；(b) selected from PAG oil, poly-a-olefin oil, ore deposit
The solvent of thing oil, polyalcohol ester oil and combinations thereof；(c) it is applied to evaporate the evaporator of the refrigerant；(d) it is applied to condensation
The condenser of the refrigerant；(e) suitable for the solution thermodynamics comprising the refrigerant being dissolved in the solvent is divided
From the separator into vapor refrigerant component and liquid flux component；At least one gas dissolving subsystem, it include (f)
Suitable for the refrigerant is mixed with the solvent blender, suitable at least a portion refrigerant is dissolved into institute
State to produce the absorber of solution, pump and heat exchanger in solvent, wherein the blender is fluidly connected to the absorber, institute
State absorber and be fluidly connected to the pump, and the pump is fluidly connected to the heat exchanger；Wherein described gas dissolving subsystem
System is in fluid communication with Unit at least two selected from the evaporator, the separator and another gas dissolving subsystem,
Condition is that at least one subsystem is in fluid communication with the evaporator and at least one subsystem is in fluid communication with the separator.
Term " low-pressure vapor phase refrigerant " used herein and " high pressure vapor refrigerant " be relative to each other for.Also
It is to say, the pressure of low-pressure vapor phase refrigerant is higher than 0 psia but less than the pressure of high pressure vapor refrigerant.Similarly, high pressure vapor
Critical point of the pressure of refrigerant less than said composition but the pressure higher than low-pressure vapor phase refrigerant.
On composition, term " substantially all " used herein refers to the gross weight based on said composition at least about
90 weight %.
On the other hand, the present invention provides absorption system, and it is included：(a) selected from one or more HF hydrocarbons,
The refrigerant of one or more hydro-chloro fluoroolefins and its blend；(b) selected from PAG oil, poly-a-olefin oil, mineral
The solvent of oil, polyalcohol ester oil and combinations thereof；(c) it is applied to evaporate the evaporator of the refrigerant；(d) it is applied to by described in
The blender that refrigerant mixes with the solvent, wherein the blender is fluidly connected to the evaporator；(e) being applied to will
The refrigerant is dissolved into produce the absorber of solution in the solvent at least partially, wherein the absorber fluidly connects
To the blender；(f) it is fluidly connected to the pump of the absorber；(g) heat exchanger of the pump is fluidly connected to, wherein
The heat exchanger absorbs heat from solar thermal collector in certain embodiments；(h) it is applied to the solution thermodynamics point
From the separator into vapor refrigerant component and liquid flux component, wherein the separator is fluidly connected to the heat exchange
Device；(i) the oil return pipeline of the separator and the blender is fluidly connected to, and (j) is applied to condense the steam system
The condenser of refrigerant components, wherein the condenser fluid is connected to the separator and the evaporator.
In preferred aspect, the present invention provides environment-friendly, economic refrigerating method.Technical staff is based on provided herein
Disclosure be readily seen other embodiments and advantage.
Brief description
Fig. 1 is the trans-1,3,3,3-tetrafluoropropene such as determined according to embodiment 2（1234ze(E)）In PAG coolant compressors
The figure of solubility in oil.
Fig. 2 is the trans-1,3,3,3-tetrafluoropropene such as determined according to embodiment 5（1234ze(E)）It is molten in POE oil
Xie Du figure.
Fig. 3 is the anti-form-1-chloro- 3,3,3- trifluoro propenes such as determined according to embodiment 8（1233zd(E)）In mineral oil
Solubility figure.
Fig. 4 is the rough schematic view of single-effective absorption kind of refrigeration cycle.
Fig. 5 is the rough schematic view of double effect absorption kind of refrigeration cycle.
It is described in detail
In certain non-limiting embodiments, the present invention relates to low-grade heat source, particularly as waste heat source, from solar energy
Thermal source, the thermal source from underground heat and these combination etc the low-grade heat source refrigerant that is used in combination and absorbent pair
It was found that.House and commercial building are the large users of the electric energy of demand fluctuation.The most high-efficiency appliance run by nearly singular integral generates electricity.
But in order to meet peak requirements, using compared with Low Performance Equipment, generally with natural gas or oil for fuel.Gas Prices are unstable,
And the dependence of oil is weakened（dilute）The safety in the U.S..But peak requirements cause added burden to power network.Work as peak
When demand flattens out, the reliability improvement of electric service.It is low-grade peak requirements are turned to, preferably renewable U.S.'s resource（Too
Positive energy or underground heat）Or power supply control is reduced or eliminated while waste heat source（brown-outs）Or during power failure, America's economy
Safety improves.
As confirmed herein, the combination of refrigerant and absorbent provided herein is for such low-grade heat and excellent
Renewable origin is selected, when being such as derived from solar energy and/or heat from underground heat, year power consumption can be significantly reduced, be averaged for the U.S.
Value reduces about 10% and reduces by 30% for hot climate.Can be with further such that CO2Discharge reduces high for U.S.'s average value
30% is reduced up to 11% and for hot climate.Especially in hot climate, it is cold that this absorption system provides peak in peak requirements
But.In other application, in heat pump, it was observed that being similarly modified.
Include the certain preferred embodiments of solar thermal collector according to the thermal source, it preferably comprises light-focusing type
（concentrated）And/or non-concentrating type solar thermal collection system.Focus solar collector is usually using mirror and instead
Penetrate etc. from the cross section more much bigger than absorber cross section and assemble the energy from the sun.High stream can be produced using such system
Temperature（Up to 400 DEG C, even more high in some cases）.These arrays also need to keep the machine with the best orientation of the sun
System and periodic monitoring and preventive maintenance are to keep required output.
Non-concentrating type array typically only absorbs the self-cleaning fixed structure for the sunshine for being emitted directly toward heat absorbing coating.It is non-poly-
Light type solar collector, which usually can produce, to be up to about 140 DEG C under vacuum tube design and leads under advanced slab design
Often it is up to about 90 DEG C of temperature.
The present invention may include any or both combination of these designs.In certain non-limiting embodiments, its
Including vacuum tube specification to produce the solar air regulating system for the maximum temperature for reaching 120 DEG C.
Type regardless of array used, the heat collected from solar thermal collector serve as the " hot pressing of the refrigeration system
Contracting machine ".That is, it promotes the heating of refrigerant and absorbent so that both can separate under the conditions of high temp/high pressure.Due to
Few mechanical part, it is simplicity, reliability and long durability the advantages of absorption system.Unique movable part of absorption system
It is liquid pump.Absorption system has the shortcomings that working fluid is limited.So far, due to no safe refrigerant/absorbent fluid
Right, absorption refrigeration is confined to commercial Application.
In a preferred embodiment of the invention, HF hydrocarbon and/or hydro-chloro fluoroolefin refrigerant are as working fluid, i.e.,
It is used for absorption system from gas to liquid or from liquid to the fluid of gas and changing state via thermodynamic cycle.Pass through
Vapor phase refrigerant is dissolved in oil solvent to form solution and promotes this phase transformation.It is preferred that had respectively using pump and heat exchanger
Effect improves the pressure and temperature of the solution.Then the solution of the pressurization and heating is flashed and steamed with the refrigerant produced under high pressure
Gas.Then make this high pressure steam by condenser and evaporator with from system heat of transfer to be cooled.
Preferred but non-limiting refrigerant for the present invention includes formula CwHxFyClzHF hydrocarbon and hydro-chloro fluoroolefin,
Wherein w is 3 to 5 integer, and x is 1 to 3 integer, and z is 0 to 1 integer, and wherein y=(2w)-x-z.Particularly preferably
Refrigerant include hydrogen halogen propylene（hydrohalopropene）, more preferably four halogen propylene, even more preferably tetrafluoropropene and single-
Chloro- trifluoro propene, even more preferably there is-CF3Four halogen propylene of group.In certain preferred embodiments, the refrigerant bag
Containing 2,3,3,3- tetrafluoropropenes, 1,3,3,3- tetrafluoropropenes or 1- chloro-3,3,3 ,-trifluoropropenes, including their all solids are different
Structure body, such asTrans-1,3,3,3- tetrafluoropropenes,Cis-1,3,3,3- tetrafluoropropenes,Trans-The chloro- 3,3,3- trifluoro propenes of 1-,Cis-One of the chloro- 3,3,3- trifluoro propenes of 1- and 3,3,3- trifluoro propenes or combination.Some available refrigerants also include two kinds
Or more kind HF hydrocarbon, the mixture and HF hydrocarbon and the mixture of hydro-chloro fluoroolefin of hydro-chloro fluoroolefin.
Solvent or absorbent available for the present invention are preferably selected from PAG oil, poly-a-olefin oil, mineral oil and more
First polyol ester oil.The selected usual thermostabilization of oil, there is extremely low vapour pressure, and nontoxic and non-aggressive.Meet these standards and can
It is polyethylene glycol oil, polyalcohol ester oil, based on polypropylene glycol dimethyl ether with the preferred oil that above-mentioned various alkene are used together
Oil and mineral oil.
In preferable non-limiting embodiments, the refrigerant is or comprising 2,3,3,3- tetrafluoropropene（HFO-
1234yf）And the solvent（Or absorbent）Selected from PAG oil, poly-a-olefin oil, mineral oil and polyalcohol ester oil.Entering
In one step embodiment, the refrigerant is or comprising 2,3,3,3- tetrafluoropropene（HFO-1234yf）And the solvent（Or absorbent）
Selected from PAG oil and/or polyalcohol ester oil.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% 2,3,3,3- tetrafluoropropenes are even more preferably included in a not limiting embodiment（HFO-
1234yf）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %, even more preferably
In a not limiting embodiment PAG oil, poly-a-olefin oil, mineral oil and polyalcohol are selected from comprising about 100%
The solvent of ester oil.In further embodiment, the refrigerant is or comprising 2,3,3,3- tetrafluoropropene（HFO-1234yf）And
The solvent（Or absorbent）Selected from PAG oil and/or polyalcohol ester oil.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% 2,3,3,3- tetrafluoropropenes are even more preferably included in a not limiting embodiment（HFO-
1234yf）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %, even more preferably
In a not limiting embodiment comprising about 100% PAG oil.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% 2,3,3,3- tetrafluoropropenes are even more preferably included in a not limiting embodiment（HFO-
1234yf）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %, even more preferably
About 100% polyalcohol ester oil is included in a not limiting embodiment.
In certain non-limiting embodiments, the refrigerant is or comprising 1,3,3,3- tetrafluoropropene（HFO-1234ze）
And the solvent（Or absorbent）Selected from PAG oil, poly-a-olefin oil, mineral oil and polyalcohol ester oil.Further real
Apply in scheme, the refrigerant is or comprising 1,3,3,3- tetrafluoropropene（HFO-1234ze）And the solvent（Or absorbent）Selected from poly-
Aklylene glycol oil and/or polyalcohol ester oil.In above-mentioned some aspects, 1,3,3,3- tetrafluoropropene include transisomer,
Substantially formed by or by transisomer.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, even more preferably include in a not limiting embodiment about 100% trans 1,3,3,3- tetrafluoropropenes（HFO-
1234ze(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %, even more
It is preferred that about 100% polyalcohol ester oil is included in a not limiting embodiment.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, even more preferably include in a not limiting embodiment about 100% trans 1,3,3,3- tetrafluoropropenes（HFO-
1234ze(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %, even more
It is preferred that in a not limiting embodiment comprising about 100% PAG oil.
In certain non-limiting embodiments, the refrigerant is or comprising 1- chloro-3,3,3 ,-trifluoropropene（HCFO-
1233zd）And the solvent（Or absorbent）Selected from PAG oil, poly-a-olefin oil, mineral oil and polyalcohol ester oil.Entering
In one step embodiment, the refrigerant is or comprising 1- chloro-3,3,3 ,-trifluoropropene（HCFO-1233zd）And the solvent（Or inhale
Receive agent）Selected from PAG oil, polyalcohol ester oil and/or mineral oil.In above-mentioned some aspects, 1- chloro- 3,3,3- tri-
Fluoropropene（HCFO-1233zd）Comprising transisomer, substantially formed by or by transisomer.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% trans 1- chloro-3,3,3 ,-trifluoropropenes are even more preferably included in a not limiting embodiment
（HCFO-1233zd(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %,
About 100% polyalcohol ester oil is even more preferably included in a not limiting embodiment.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% trans 1- chloro-3,3,3 ,-trifluoropropenes are even more preferably included in a not limiting embodiment
（HCFO-1233zd(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %,
Even more preferably in a not limiting embodiment comprising about 100% PAG oil.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% trans 1- chloro-3,3,3 ,-trifluoropropenes are even more preferably included in a not limiting embodiment
（HCFO-1233zd(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %,
About 100% mineral oil is even more preferably included in a not limiting embodiment.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% trans 1- chloro-3,3,3 ,-trifluoropropenes are even more preferably included in a not limiting embodiment
（HCFO-1233zd(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %,
About 100% alkylbenzene oil is even more preferably included in a not limiting embodiment.
In preferable non-limiting embodiments, the refrigerant includes at least about 50 weight %, more preferably at least about
75 weight %, about 100% trans 1- chloro-3,3,3 ,-trifluoropropenes are even more preferably included in a not limiting embodiment
（HCFO-1233zd(E)）And the solvent（Or absorbent）Comprising at least about 50 weight %, more preferably at least about 75 weight %,
About 100% silicone oil is even more preferably included in a not limiting embodiment.
Preferably, it is refrigerant and solvent is proportional and be effectively formed solution（Wherein refrigerant dissolves in a solvent）'s
Under the conditions of mix.The mixture of refrigerant and solvent is preferably proportional, wherein the signal portion of the refrigerant mixed with solvent, more
It is preferred that substantially all be dissolved in the solvent.Exist that is, the amount for the refrigerant for treating to mix with solvent is preferably shorter than the solvent
Saturation point under the running temperature and pressure of the refrigerant system.Refrigerant concentration is kept below saturation point reduces steam system
Cryogen reaches pump（It may cause cavitation herein）Possibility.
In certain embodiments, blender mix refrigerant and solvent can be passed through.Preferable blender includes static mixed
Clutch and aspirator（That is venturi pump）.In certain embodiments, the blender is two feed-lines（Such as pipeline, pipe,
Flexible pipe etc.）Easy engagement, its turbulization, such as T joints.
Low-pressure vapor phase refrigerant is preferably at about -10 DEG C to about 30 DEG C, preferably approximately 0 DEG C to about 30 DEG C, preferably greatly
It is dissolved under about 0 DEG C to about 10 DEG C of refrigerant temperature in oil solvent.
Refrigerant is preferably at least most of to be dissolved in a solvent in absorber.The absorber can be adapted to refrigerant
Gas is dissolved into any types in the solvent based on oil.The example of absorber includes heat exchanger, cooling medium by itself or
Around its circulation.
Solution comprising refrigerant and solvent is resisted into drag devices（means of resistance）Pump pressurizes to improve
The pressure of the solution.The paramount operating pressure of liquid solution pump pressurization is usually required than using compressor compresses vaporous cryogen
Substantially few energy.In addition to less energy is consumed, pump is cheaper than compressor generally in installation and maintenance.This energy and cost
Saving is remarkable advantage of the present invention compared with traditional compression type refrigeration system.
Also the solution is heated, preferably heated after the pressurizing.It is preferred that heat exchanger is used, such as shell and tube heat exchanger and plate
Formula heat exchanger or destilling tower realize heating.In preferred embodiments, the solution is heated to be related to from low-grade heat source, used heat time
Receive unit（WHRU）, geothermal source, the heat of transfer such as thermal source from solar energy.WHRU may include, for example, coming from hot gas or liquid
Logistics（Waste gas of the Tathagata from the exhaust of gas turbine or from power plant or refinery）Heat.Working media for thermal source can be with
Respectively become the characteristics of application, but be preferably water in numerous applications（It is pure or containing triethylene glycol（TEG））, deep fat or other contribute to
The medium of heat transfer.In other embodiments, heat the solution to be related to by fuel, as the burning of propane directly heats, such as herein
The be derived from solar energy and/or the heat of geothermal source discussed are highly preferred embodiments.
After the solution is heated and pressurizeed, thermodynamics partition method is imposed to it to produce vaporous cryogen fraction and liquid
Solvent fraction.The example of such thermodynamics partition method includes column distillation and flash distillation.Because both fractions are in different phases, they
It can be easily separated.
It is preferred that liquid flux is mutually recirculated back into blender, while the gas phase comprising refrigerant is transferred to condenser,
This at least a portion, preferably substantially all refrigerant is from its gas phase conversion into liquid phase.
Type available for the condenser of the present invention is not particularly limited, as long as they are applied to condensation HF hydrocarbon or hydrogen
Chlorine fluoroolefins refrigerant.The example of condenser includes horizontal or vertical shell inner condenser and horizontal or vertical tube inner condenser.
It is preferred that make liquid phase refrigerant by expansion valve to reduce the pressure of refrigerant and correspondingly cool down the refrigerant.Cooling
Throttling（throttled）Refrigerant can be liquid phase, gas phase or mixed phase.
Then the refrigerant is made to pass through evaporator, wherein cold from treating using cooling capacity of the refrigerant in evaporation process
But heat is extracted in system（Freeze）.Preferably, the material to be cooled in the system is water, with or without heat transfer additive,
Such as PEG, the cold water for the air processor being for example recycled in the distribution system of air adjustment can be used.It is but to be cooled
Material can also be the air for being directly used in air adjustment.In addition, exterior material can also be need cool down it is any flowable
Material, and if water or air, the material through cooling can be used for non-air regulation purposes（Such as frozen food or other productions
Product）.
The type of evaporator for evaporating liquid phase refrigerant is not particularly limited, as long as it is applied to evaporation HF hydrocarbon
Or hydro-chloro fluoroolefin refrigerant.The example of available evaporator include forced-circulation evaporator, natural-circulation evaporator, long tube and
Calandria evaporator, falling film evaporator, horizontal tube evaporator and plate-type evaporator.
After refrigerant evaporation, it becomes preferably have about 30 DEG C to about 60 DEG C, and more preferably from about 40 DEG C to about
The low-pressure vapor phase refrigerant of 50 DEG C of temperature.It is preferred that the low-pressure vapor phase refrigerant is recirculated back to blender.
The method of the present invention is preferably closed-loop system, and wherein refrigerant and solvent all recycles.According to the absorption of the present invention
Formula refrigeration system is preferably directed to single-action, economic benefits and social benefits or three-effect absorption-type refrigerating method.Single-action is described in following embodiments and accompanying drawing
With economic benefits and social benefits method.
Embodiment
Embodiment 1
Exploitation uses the steady-state system model of ideal composition to investigate and the lubricant as absorbent（Such as PAG
Or polyol ester）It is used together low GWP refrigerants HFO-1234yf.As QCooling/(Qin+Wp) calculate Absorption heat-transformer efficiency
Or the coefficient of performance（COP）.Although QinIt is considered as used heat in numerous applications and is " free " energy in application of solar energy, but
This is the best mode of more potential refrigerant pair.The modeling primarily looks at NH3The concurrent present 5 DEG C steaming of-water absorption type circulation
Send out and run under device temperature and 40 DEG C of environment temperature with about 0.6 COP.For preferable HFO-1234yf/ lubricants model,
It was found that under identical operational factor, i.e., COP is about 0.6 when being run under 2 DEG C of evaporator temperature and 40 DEG C of environment temperature.
Using this system model, the system proposed with bin analysis and evaluations and the performance relative to current techniques.Will be
Conventional roof air adjustment unit is used during 1 year（RTU）Cool down the electric power of typical larger retail industry building consumption with it is same
The solar powered absorption auxiliary RTU of size compares.This analysis considers the average weather data in 29 cities in the whole America
（Air Conditioning, Heating and Refrigeration Institute Standard for chillers
（AHRI Std 550））And dry hot climate Phoenix, Arizona.Summary is assessed to provide in table 1 below.
Table 1:Use conventional roof unit and the typical megastore for absorbing auxiliary roof unit（100,000 ft2）'s
The comparison of annual energy consumption and peak power demands（Assuming that 450 tons of total coolings（total cooling））
In order to further study the benefit using this technology, point that the integrated environment of these cooling technologies influences is carried out
Analysis.Due in the most of by fossil fuel of energy caused by the U.S.（That is coal, natural gas, oil）Burning produce, set at this
The electric energy of standby middle consumption can cause CO2Discharge, therefore contribute to global warming.In addition to this " indirect contribution ", also exist and come from
The global warming gases release of refrigerant leakage in RTU directly affects.Main flow R410A refrigerants in RTU, which have, to be exceeded
2100 GWP.2100 times more severe than the refrigerant mixture proposed of the leakage of this refrigerant.Lifetime climate performance
（LCCP）Analysis takes in these sources into account together with the influence of the generation process of global warming gases.The summary of LCCP analyses
It is given in Table 2 below.
Table 2:Using conventional roof unit compared with the LCCP for the typical megastore for absorbing auxiliary roof unit
This innovation is related to uses solar thermal collector under the output of rational high temperature, and it causes vacuum pipe solar thermal-arrest
Device（Commercially available prod）It is suitable for this application.For the absorption cooling under 0.6 cooling COP, the peace needed for cooling per ton
Area is filled for 800 W/m2Solar day is about 18 m2Or more precisely, the roof area accounted in above-mentioned analysis about 1/
3 array.This also can make market avoid peak power demands expense simultaneously by providing " free " cooling during peak requirements
It is final to reduce peak network load.
Embodiment 2
Trans-1,3,3,3-tetrafluoropropene is measured by microbalance（1234ze(E)）In Ford Motor craft oil（Meet
Ford specification No. WSH-M1C231-B PAG refrigerant compression machine oil）In solubility.The solubility that measures with using it is non-with
Machine biliquid（Non-Random Two Liquid）（“NRTL”）Activity Coefficient Models（Renon H., Prausnitz J.
M., "Local Compositions in Thermodynamic Excess Functions for Liquid
Mixtures," AIChE J., 14(1), S.135-144, 1968））The data of association are shown in Fig. 1 together.By these
Data find out that Ford Motor Craft oil has almost negligible vapour pressure and the NRTL models can accurate generation
The table data.
Embodiment 3
Circulated using the data mining single-effective absorption from embodiment 2.Use the absorption system as disclosed in Fig. 4.
By the oil based on Ford Motorcraft polypropylene glycol dimethyl ethers in closed mixer（It can be connection two or more
Simple " T " joint of multiple pipelines）In mixed with liquid 1234ze (E) refrigerant.The mixture is sent to absorber, herein
Gaseous state 1234ze (E) is dissolved into the oil in shown degree in fig. 2.The liquid mixture is sent to pump, it mixes this
Compound pressurizes and the mixture is sent into heat exchanger/boiler.In the boiler, with the mixture exchanged heat.The thermal source can be with
The heat of the solar thermal collector come outside automatic heat-exchanger.The temperature of the mixture, which is brought up to, can make 1234ze (E) refrigerant
The temperature separated with oil.Heated mixture is taken out from heat exchanger and introduces separator, thus refrigerant is substantially with gas
State separates with the basic oil for keeping liquid.Then send the oil back to through fuel tap, reduce its pressure herein to match initial pressure.From this
Valve sends oil back to blender, and it is mixed with refrigerant to repeat the process again herein.
Condenser is sent to be liquefied from separator by refrigerant vapour.The liquid is sent to expansion valve, by this
Liquid refrigerant throttles to cool down the refrigerant.According to the selection of operating personnel, the throttling refrigerant of the cooling can be liquid,
Steam or its combination.The refrigerant of cooling is passed through evaporator, thus utilize the cooling capacity cooling of the refrigerant and evaporator
In the material of heat exchange relationship（Water or air）.Then the refrigerant is sent back to blender from evaporator, it is mixed with oil again herein
Close to repeat the process.
The single-effective absorption circulation input parameter be：
1) evaporator temperature-refrigerant side: 2℃
2) condenser temperature-refrigerant side: 40℃
3) to the kJ/hr of boiler supplying 3000
4) saturated liquid leaves absorber
5) overheat of evaporator is left: 3℃
6) it is 90 weight % oil and 10 weight % refrigerants into the composition of the logistics of separator.
Using these parameters and using used heat and/or the heat from solar energy and/or from underground heat, use 1234ze (E)
With the calculating coefficient of performance of Ford motor craft oil（“COP”）For 4.56.
Embodiment 4
Circulated using the data mining double effect absorption from embodiment 2.Ford Motorcraft polypropylene glycol diformazans will be based on
The oil of base ether mixes in closed mixer with liquid 1234ze (E) refrigerant.The mixture is sent to the first absorber,
It is dissolved into this gaseous state 1234ze (E) in oil.Then the mixture is sent to the first pump, the mixture is pressurizeed and should by it
Mixture is sent to first heat exchanger/boiler.In the boiler, with the mixture exchanged heat.The thermal source can carry out self-heating friendship
The heat of solar thermal collector outside parallel operation.Improve the temperature of the mixture.Heated mixture is taken out from heat exchanger simultaneously
The second blender is introduced, it is mixed with oil herein.Then the mixture from the second blender is introduced into the second absorber with true
All 1234ze (E) are protected to be dissolved in oil.From the second absorber by the mixture draw to（drawn to）Second pump, it should
Mixture is pumped to the second boiler, and bringing up to the temperature of the mixture can make what 1234ze (E) refrigerants separated with oil herein
Temperature.Still thermal source is provided for boiler to realize this point, the thermal source can be derived from the thermal source of solar thermal collector.
The mixture is fetched into separator from the second boiler, thus refrigerant is substantially with gaseous state and basic holding liquid
Oil separation.Then send the oil back to threeway, shunt it herein, a part of oil is delivered into the second blender through the second fuel tap and incited somebody to action
The oil of remainder delivers to the first fuel tap, reduces pressure herein to match initial pressure.The oil is then sent to the first mixing
Device, herein its mixed again with refrigerant to repeat the process.
Condenser is sent to be liquefied from separator by refrigerant vapour.The liquid is set to pass through expansion valve, by the liquid
Cryogen throttles to cool down the refrigerant.According to the selection of operating personnel, the throttling refrigerant of the cooling can be liquid, steam
Gas or its combination.The refrigerant of cooling is passed through evaporator, be thus cooled in using the cooling capacity of the refrigerant outside evaporator
Material（Water or air）.Then the refrigerant is sent back to first blender from evaporator, it is mixed to weigh again with oil again herein
The multiple process.
The double effect absorption circulation input parameter be：
1) evaporator temperature-refrigerant side: 2℃
2) condenser temperature-refrigerant side: 40℃
3) pressure for leaving pump is
4) to generator（generator）The kJ/hr of boiler supplying 1500
5) leave the two absorbers is all saturated liquid
6) overheat of evaporator is left: 3℃
7) threeway branches to intergrade absorber by the 30% of the logistics and branched to 70% rudimentary（low stage）Absorber
8) it is 90 weight % oil and 10 weight % refrigerants into the total composition of the logistics of separator.
Using these parameters and using used heat and/or the heat from solar energy and/or from underground heat, use 1234ze (E)
Calculating COP with Ford motor craft oil is 5.04.
Embodiment 5
Trans-1,3,3,3-tetrafluoropropene is measured by microbalance（1234ze(E)）It is molten in POE oil-Ultra 22CC
Xie Du.Measure solubility and use NRTL Activity Coefficient Models（Renon H., Prausnitz J. M., "Local
Compositions in Thermodynamic Excess Functions for Liquid Mixtures," AIChE
J., 14(1), S.135-144, 1968））Associated data, its result are shown in fig. 2.Found out by this data, POE oil
With almost negligible vapour pressure and the NRTL Activity Coefficient Models（It is still derived by the data obtained）Can be accurate
Represent the data.
Embodiment 6
Circulated using the dissolubility data development model single-effective absorption in embodiment 5.More specifically, in the model system,
By POE oil in closed mixer（It can be simple " T " joint for connecting two or more pipelines）In with liquid
1234ze (E) refrigerant mixes.The mixture is sent to absorber, is dissolved into this gaseous state 1234ze (E) in oil.By the liquid
Body mixture is sent to pump, and the mixture is pressurizeed and the mixture is sent into heat exchanger/boiler by it.In the boiler, with
The mixture exchanged heat.The heat for the solar thermal collector that the thermal source can come outside automatic heat-exchanger.By the temperature of the mixture
Bring up to the temperature that 1234ze (E) refrigerants can be made to be separated with oil.Then heated mixture is taken out from heat exchanger simultaneously
Separator is introduced, thus refrigerant is separated with gaseous state with the basic oil for keeping liquid substantially.Then the oil is sent back to through fuel tap, herein
Its pressure is reduced to match initial pressure.Blender is sent back to from the valve by oil, and it is mixed with refrigerant to repeat the mistake again herein
Journey.
Condenser is sent to be liquefied from separator by refrigerant vapour.The liquid is set to pass through expansion valve, by the liquid
Cryogen throttles to cool down the refrigerant.According to the selection of operating personnel, the throttling refrigerant of the cooling can be liquid, steam
Gas or its combination.The refrigerant of cooling is passed through evaporator, be thus in evaporator using the cooling capacity cooling of the refrigerant
The material of heat exchange relationship（Water or air）.Then the refrigerant is sent back to blender from evaporator, it is mixed with oil again herein
To repeat the process.
The single-effective absorption circulation input parameter be：
1) evaporator temperature-refrigerant side: 2℃
2) condenser temperature-refrigerant side: 40℃
3) to the kJ/hr of generator boiler supplying 3000
4) leave the two absorbers is all saturated liquid
5) overheat of evaporator is left: 3℃
6) it is 90 weight % oil and 10 weight % refrigerants into the composition of the logistics of separator.
Using these parameters and using used heat and/or the heat from solar energy and/or from underground heat, use 1234ze (E)
With the calculating coefficient of performance of POE oil（“COP”）For 4.96.
Embodiment 7
Circulated using the dissolubility data development model double effect absorption in embodiment 5.More specifically, in the model system,
Mineral oil is mixed in closed mixer with liquid 1234ze (E) refrigerant.The mixture is sent to the first absorber,
It is dissolved into this gaseous state 1234ze (E) in oil.Then the mixture is sent to the first pump, the mixture is pressurizeed and should by it
Mixture is sent to first heat exchanger/boiler.In the boiler, with the mixture exchanged heat.The thermal source can carry out self-heating friendship
The heat of solar thermal collector outside parallel operation.Improve the temperature of the mixture.Heated mixture is taken out from heat exchanger simultaneously
The second blender is introduced, it is mixed with oil herein.Mixture from the second blender is introduced into the second absorber to ensure
There is 1234ze (E) to be dissolved in oil.Drawn from the second absorber by the mixture to the second pump, the mixture is pumped to by it
Two boilers, the temperature of the mixture is brought up to the temperature that 1234ze (E) refrigerants can be made to be separated with oil herein.For the second boiler
Thermal source is provided to realize this point, it can be the heat from solar thermal collector.
The mixture is fetched into separator from the second boiler, thus refrigerant is substantially with gaseous state and basic holding liquid
Oil separation.Then send the oil back to threeway, shunt it herein.Part transmission by the second fuel tap and is delivered into the second mixing
Device.The first fuel tap is passed through into remainder transmission, reduces pressure herein to match initial pressure.The oil is then sent to first
Blender, herein its mixed again with refrigerant to repeat the process.
Condenser is sent to be liquefied from separator by refrigerant vapour.The liquid is set to pass through expansion valve, by the liquid
Cryogen throttles to cool down the refrigerant.According to the selection of operating personnel, the throttling refrigerant of the cooling can be liquid, steam
Gas or its combination.The refrigerant of cooling is passed through evaporator, be thus cooled in using the cooling capacity of the refrigerant outside evaporator
Material（Water or air）.Then the refrigerant is sent back to first blender from evaporator, it is mixed to weigh again with oil again herein
The multiple process.
This double effect absorption circulation parameter be：
1) evaporator temperature-refrigerant side: 2℃
2) condenser temperature-refrigerant side: 40℃
3) pressure for leaving pump is
4) to the kJ/hr of generator boiler supplying 1500
5) leave the two absorbers is all saturated liquid
6) overheat of evaporator is left: 3℃
7) threeway branches to intergrade absorber by the 30% of the logistics and branches to rudimentary absorber by 70%
8) it is 90 weight % oil and 10 weight % refrigerants into the total composition of the logistics of separator.
Using these parameters, the calculating COP using 1234ze (E) and POE is 5.35.
Embodiment 8
Anti-form-1-chloro- 3,3,3- trifluoro propenes are measured by microbalance（1233zd(E)）Mineral oil-C-3 refrigeration oil-
In solubility.The solubility and use NRTL Activity Coefficient Models measured（Renon H., Prausnitz J. M., "
Local Compositions in Thermodynamic Excess Functions for Liquid Mixtures,"
AIChE J., 14(1), S.135-144, 1968））The data of association are shown in figure 3.Found out by this data, the mineral
Oil has almost negligible vapour pressure and the NRTL Activity Coefficient Models（It is still derived by the data obtained）Can be accurate
Really represent the data.
Embodiment 9
Circulated using the dissolubility data development model single-effective absorption in embodiment 8.More specifically, in the model system,
By mineral oil in closed mixer（It can be simple " T " joint for connecting two or more pipelines）In with liquid
1233zd (E) refrigerant mixes.The mixture is sent to absorber, is dissolved into this gaseous state 1233zd (E) in oil.By the liquid
Body mixture is sent to pump, and the mixture is pressurizeed and the mixture is sent into heat exchanger/boiler by it.In the boiler, with
The mixture exchanged heat.The heat for the solar thermal collector that the thermal source can come outside automatic heat-exchanger.By the temperature of the mixture
Bring up to the temperature that 1233zd (E) refrigerants can be made to be separated with oil.Heated mixture and introducing are taken out from heat exchanger
Separator, thus refrigerant separated substantially with gaseous state with the basic oil for keeping liquid.Then the oil is returned into fuel tap, dropped herein
Its low pressure is to match initial pressure.Blender is sent back to from the valve by oil, and it is mixed with refrigerant to repeat the process again herein.
Condenser is sent to be liquefied from separator by refrigerant vapour.The liquid is set to pass through expansion valve, by the liquid
Cryogen throttles to cool down the refrigerant.According to the selection of operating personnel, the throttling refrigerant of the cooling can be liquid, steam
Gas or its combination.The refrigerant of cooling is passed through evaporator, be thus in evaporator using the cooling capacity cooling of the refrigerant
The material of heat exchange relationship（Water or air）.Then the refrigerant is sent back to blender from evaporator, it is mixed with oil again herein
To repeat the process.
The single-effective absorption circulation input parameter be：
1) evaporator temperature-refrigerant side: 2℃
2) condenser temperature-refrigerant side: 40℃
3) to the kJ/hr of generator boiler supplying 3000
4) leave the two absorbers is all saturated liquid
5) overheat of evaporator is left: 3℃
6) it is 90 weight % oil and 10 weight % refrigerants into the composition of the logistics of separator.
Using these parameters and assume to utilize used heat, use 1233zd (E) and the calculating coefficient of performance of mineral oil（“COP”）
For 21.61.
Embodiment 10
Circulated using the dissolubility data development model double effect absorption from embodiment 8.More specifically, in the model system
In, mineral oil is mixed in closed mixer with liquid 1233zd (E) refrigerant.The mixture is sent to the first absorption
Device, it is dissolved into this gaseous state 1233zd (E) in oil.Then the mixture is sent to the first pump, it pressurizes the mixture simultaneously
It is sent to first heat exchanger/boiler.In the boiler, with the mixture exchanged heat.The thermal source can come from heat exchange
The heat of solar thermal collector outside device.Improve the temperature of the mixture.Then heated mixture is taken out from heat exchanger
And the second blender is introduced, it is mixed with oil herein.Then by from the second blender mixture introduce the second absorber with
Ensure that all 1233zd (E) are dissolved in oil.Drawn from the second absorber by the mixture to the second pump, it is by the mixture pump
The second boiler is delivered to, the temperature of the mixture is brought up to the temperature that 1233zd (E) refrigerants can be made to be separated with oil herein.For pot
Stove provides thermal source to realize this point, and the thermal source can be the above-mentioned type（That is solar thermal collector）.
The mixture is fetched into separator from the second boiler, thus refrigerant is substantially with gaseous state and basic holding liquid
Oil separation.Then send the oil back to threeway, shunt it herein.A part of oil is delivered into the second fuel tap and delivers to the second mixing
Device.The oil of remainder is delivered into the first fuel tap, reduces pressure herein to match initial pressure.The oil is then sent to first
Blender, herein its mixed again with refrigerant to repeat the process.
Condenser is sent to be liquefied from separator by refrigerant vapour.Then the liquid is made to pass through expansion valve, will
The liquid refrigerant throttles to cool down the refrigerant.According to the selection of operating personnel, the throttling refrigerant of the cooling can be liquid
Body, steam or its combination.Then the refrigerant of cooling is passed through evaporator, be thus cooled in using the cooling capacity of the refrigerant
Material outside evaporator（Water or air）.Then the refrigerant is sent back to first blender from evaporator, it is mixed with oil again herein
Close to repeat the process.
This double effect absorption circulation input parameter be：
1) evaporator temperature-refrigerant side: 2℃
2) condenser temperature-refrigerant side: 40℃
3) pressure for leaving pump is
4) to the kJ/hr of generator boiler supplying 1500
5) leave the two absorbers is all saturated liquid
6) overheat of evaporator is left: 3℃
7) threeway branches to intergrade absorber by the 30% of the logistics and branches to rudimentary absorber by 70%
8) it is 90 weight % oil and 10 weight % refrigerants into the total composition of the logistics of separator.
Using these parameters and using used heat and/or the heat from solar energy and/or from underground heat, use 1233zd (E)
Calculating COP with mineral oil is 25.69.
Embodiment 11
It has been confirmed that solubility of the refrigerant in absorber to the present invention kind of refrigeration cycle many important embodiments it is whole
Body performance is important.More specifically, absorb refrigerant higher concentration tend to by reduce the mixture boiling point and
Reducing the heat aspect reached needed for the boiling point reduces boiler/generator load and improves circulation COP.In addition, pressure is to determine
Determine the important parameter of absorber solubility and evaporator temperature, therefore higher solubility is tended to reduce required low pressure side pressure
Power, so that evaporator service condition is more flexible.In the temperature and pressure important to many Absorption Cooling Systems according to the present invention
The dissolubility data of HFO-1234ze (E) and HFO-1234yf in different grades of POE oil is determined under power, reports this below
Data.
Although both refrigerants are all substantially dissolved in POE oil, observe 1234ze (E) in about 30C to about
There is obvious solubility advantage at a temperature of 50C compared with 1234yf.On average, POE oil is transported in Absorption Cooling System
Especially interesting temperature range internal absorptance 1234yf more 23% 1234ze (E) in row.It has also been found that with the oily viscosity
Reduce（Relatively low ISO grades）Reduced with absorber temperatures, refrigerant solubility improves.Therefore, the Absorption heat-transformer is unrestricted
Property preferred embodiment oily, the 1234ze (E) more preferably under the absorber temperatures less than 50 DEG C that includes 1234ze (E) and POE
With the POE of ISO 10 oil.
Embodiment 12
Use the absorption system as disclosed in Fig. 4.By ISO 10 POE oil in closed mixer with liquid
1234ze (E) refrigerant is mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption system
It is cold.
Embodiment 13
Use the absorption system as disclosed in Fig. 4.By ISO 32 POE oil in closed mixer with liquid
1234ze (E) refrigerant is mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption system
It is cold.
Embodiment 14
Use the absorption system as disclosed in Fig. 4.By ISO 68 POE oil in closed mixer with liquid
1234ze (E) refrigerant is mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption system
It is cold.
Embodiment 15
Use the absorption system as disclosed in Fig. 4.By ISO 10 POE oil in closed mixer with liquid
1234yf refrigerants are mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption refrigeration.
Embodiment 16
Use the absorption system as disclosed in Fig. 4.By ISO 32 POE oil in closed mixer with liquid
1234yf refrigerants are mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption refrigeration.
Embodiment 17
Use the absorption system as disclosed in Fig. 4.By ISO 68 POE oil in closed mixer with liquid
1234yf refrigerants are mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption refrigeration.
Embodiment 18
Use the multistage absorption refrigerating system as disclosed in Fig. 5.By ISO 10 POE oil in closed mixer with liquid
1234ze (E) refrigerant is mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption system
It is cold.
Embodiment 19
Use the multistage absorption refrigerating system as disclosed in Fig. 5.By ISO 32 POE oil in closed mixer with liquid
1234ze (E) refrigerant is mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption system
It is cold.
Embodiment 20
Use the multistage absorption refrigerating system as disclosed in Fig. 5.By ISO 68 POE oil in closed mixer with liquid
1234ze (E) refrigerant is mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption system
It is cold.
Embodiment 21
Use the multistage absorption refrigerating system as disclosed in Fig. 5.By ISO 10 POE oil in closed mixer with liquid
1234yf refrigerants are mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption refrigeration.
Embodiment 22
Use the multistage absorption refrigerating system as disclosed in Fig. 5.By ISO 32 POE oil in closed mixer with liquid
1234yf refrigerants are mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption refrigeration.
Embodiment 23
Use the absorption system as disclosed in Fig. 5.By ISO 68 POE oil in closed mixer with liquid
1234yf refrigerants are mixed and used according to the condition described in embodiment 2 and operational factor.Realize effective absorption refrigeration.
Embodiment 24
Trans HCFO-1233zd is determined under the temperature and pressure important to many Absorption Cooling Systems according to the present invention to exist
Dissolubility data in three kinds of refrigeration lubricants, reports these data below.
It was observed that trans 1233zd is significantly dissolved in each alkylbenzene oil, silicone oil and mineral oil, alkylbenzene oil is especially connecing
There is solubility advantage at a temperature of nearly 30 DEG C.Therefore, the non-limiting preferred embodiment of Absorption heat-transformer includes trans
1233zd and in any of alkylbenzene oil, silicone oil or mineral oil, more preferably trans 1233zd and alkylbenzene oil, it is small
Under 50 DEG C of absorber temperatures, preferably at a temperature of about 0 DEG C to about 30 DEG C, preferably at about 10 DEG C to about 30 DEG C
At a temperature of.
Embodiment 25
Use the absorption system as disclosed in Fig. 4.By alkylbenzene oil in closed mixer with liquid 1233zd (E)
Refrigerant is mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption refrigeration.
Embodiment 26
Use the absorption system as disclosed in Fig. 4.Silicone oil is freezed in closed mixer with liquid 1233zd (E)
Agent is mixed and used according to the condition described in embodiment 3 and operational factor.Realize effective absorption refrigeration.
Embodiment 27
Use the multistage absorption refrigerating system as disclosed in Fig. 5.By alkylbenzene oil in closed mixer with liquid
1233zd (E) refrigerant is mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption system
It is cold.
Embodiment 28
Use the absorption system as disclosed in Fig. 5.Silicone oil is freezed in closed mixer with liquid 1233zd (E)
Agent is mixed and used according to the condition described in embodiment 6 and operational factor.Realize effective absorption refrigeration.
Claims (12)
1. providing the method for refrigeration, it includes：
A. evaporation includes the refrigerant containing about 95 weight % to about 100 weight % trans-1,3,3,3-tetrafluoropropene
First liquid phase refrigerant logistics is to produce low-pressure vapor phase refrigerant stream, wherein described evaporate from system heat of transfer to be cooled；
B. the low-pressure vapor phase refrigerant stream is made and comprising the polyol ester containing about 95 weight % to about 100 weight %
Substantially all refrigerants of the vapor phase refrigerant logistics are effectively being dissolved into by the first liquid phase solvent logistics of the solvent of oil
Contacted in the solvent of first liquid phase solvent logistics with producing under conditions of refrigerant-solvent solution logistics；
C. by from solar thermal collector to refrigerant-solvent solution heat transfer improves the pressure of the refrigerant-solvent solution logistics
Power and temperature；
D. the refrigerant-solvent solution logistics thermodynamics is separated into high pressure vapor refrigerant stream and second liquid phase solvent
Logistics；
E. the second liquid phase solvent stream is recycled to step (b) to produce the first liquid phase solvent logistics；
F. the high pressure vapor refrigerant stream is condensed to produce second liquid phase refrigerant stream；With
G. the second liquid phase refrigerant stream is recycled to step (a) to produce the first liquid phase refrigerant logistics.
2. the method for claim 1 wherein the solar energy source is non-light-focusing type system.
3. the method for claim 1 wherein the refrigerant includes 99 weight % to 100 weight % anti-form-1,3,3,3- tetrafluoros
Propylene and the solvent include the polynary of 99 weight % to the 100 weight % viscosity with about ISO 10 to about ISO 100
Polyol ester oil.
4. providing the method for refrigeration, it includes：
A. evaporation includes the refrigeration of anti-form-1-chloro- 3,3,3- trifluoro propenes containing about 95 weight % to about 100 weight %
First liquid phase refrigerant logistics of agent is to produce low-pressure vapor phase refrigerant stream, wherein the evaporation is shifted from system to be cooled
Heat；
B. the low-pressure vapor phase refrigerant stream is made and comprising mineral oil, the alkane containing about 95 weight % to about 100 weight %
First liquid phase solvent logistics of the solvent of base benzene oil and combinations thereof is effectively by the substantially all of the vapor phase refrigerant logistics
Refrigerant is dissolved into the solvent of the first liquid phase solvent logistics molten to generate less than refrigerant-solvent at a temperature of about 50 DEG C
Contacted under conditions of liquid logistics；
C. by from solar thermal collector to refrigerant-solvent solution heat transfer improves the pressure of the refrigerant-solvent solution logistics
Power and temperature；
D. the refrigerant-solvent solution logistics thermodynamics is separated into high pressure vapor refrigerant stream and second liquid phase solvent
Logistics；
E. the second liquid phase solvent stream is recycled to step (b) to produce the first liquid phase solvent logistics；
F. the high pressure vapor refrigerant stream is condensed to produce second liquid phase refrigerant stream；With
G. the second liquid phase refrigerant stream is recycled to step (a) to produce the first liquid phase refrigerant logistics.
5. the method for claim 4, wherein the solar energy source is non-light-focusing type system.
6. the method for claim 4, wherein the refrigerant includes 99 weight % to 100 weight % anti-form-1,3,3,3- tetrafluoros
Propylene and the solvent include 99 weight % to 100 weight % mineral oil.
7. the method for claim 4, wherein the refrigerant includes 99 weight % to 100 weight % anti-form-1-chloro- 3,3,3- tri-
Fluoropropene and the solvent include 99 weight % to 100 weight % alkylbenzene oil.
8. absorption system, it is included：
A. about 95 weight % to about 100 weight % trans-1,3,3,3-tetrafluoropropene refrigerant is included；
B. about 95 weight % to about 100 weight % polyalcohol ester oil solvent is included；
C. it is applied to evaporate the evaporator of the refrigerant；
D. it is applied to the blender that mixes the refrigerant with the solvent, wherein described in the blender is fluidly connected to
Evaporator；
E. suitable at least a portion refrigerant is dissolved into produce the absorber of solution the solvent, wherein institute
State absorber and be fluidly connected to the blender；
F. it is fluidly connected to the pump of the absorber；
G. the heat exchanger of the pump is fluidly connected to, wherein the heat exchanger is energized by solar thermal collector；
H. it is applied to the solution thermodynamics being separated into vapor refrigerant component and the separator of liquid flux component, wherein
The separator is fluidly connected to the heat exchanger；
I. the oil return pipeline of the separator and the blender is fluidly connected to, and
J. it is applied to condense the condenser of the vapor refrigerant component, wherein the condenser fluid is connected to the separation
Device and the evaporator.
9. the method for claim 8, wherein the refrigerant includes 99 weight % to 100 weight % anti-form-1,3,3,3- tetrafluoros
Propylene and the solvent include 99 weight % to 100 weight % polyalcohol ester oil.
10. absorption system, it is included：
A. the refrigerant of anti-form-1-chloro- 3,3,3- trifluoro propenes comprising about 95 weight % to about 100 weight %；
B. the solvent of the mineral oil comprising about 95 weight % to about 100 weight %, alkylbenzene oil and combinations thereof；
C. it is applied to evaporate the evaporator of the refrigerant；
D. it is applied to the blender that mixes the refrigerant with the solvent, wherein described in the blender is fluidly connected to
Evaporator；
E. suitable for substantially all refrigerants are dissolved into the solvent at a temperature of about 10 DEG C to about 30 DEG C
To produce the absorber of solution, wherein the absorber is fluidly connected to the blender；
F. it is fluidly connected to the pump of the absorber；
G. the heat exchanger of the pump is fluidly connected to, wherein the heat exchanger is energized by solar thermal collector；
H. it is applied to the solution thermodynamics being separated into vapor refrigerant component and the separator of liquid flux component, wherein
The separator is fluidly connected to the heat exchanger；
I. the oil return pipeline of the separator and the blender is fluidly connected to, and
J. it is applied to condense the condenser of the vapor refrigerant component, wherein the condenser fluid is connected to the separation
Device and the evaporator.
11. the method for claim 10, wherein the refrigerant includes 99 weight % to 100 weight % anti-form-1-chloro- 3,3,3-
Trifluoro propene and the solvent include 99 weight % to 100 weight % mineral oil.
12. the method for claim 10, wherein the refrigerant includes 99 weight % to 100 weight % anti-form-1-chloro- 3,3,3-
Trifluoro propene and the solvent include 99 weight % to 100 weight % alkylbenzene oil.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201562101718P | 2015-01-09 | 2015-01-09 | |
| US62/101718 | 2015-01-09 | ||
| US14/991,520 US20160123632A1 (en) | 2008-04-30 | 2016-01-08 | Absorption refrigeration cycles using a lgwp refrigerant |
| US14/991520 | 2016-01-08 | ||
| PCT/US2016/012763 WO2016112363A1 (en) | 2015-01-09 | 2016-01-09 | Absorption refrigeration cycles using a lgwp refrigerant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107407510A true CN107407510A (en) | 2017-11-28 |
Family
ID=56356517
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680014576.0A Pending CN107407510A (en) | 2015-01-09 | 2016-01-09 | Use the Absorption Cooling System of LGWP refrigerants |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP3243031A4 (en) |
| JP (1) | JP2018507381A (en) |
| KR (1) | KR20170106646A (en) |
| CN (1) | CN107407510A (en) |
| WO (1) | WO2016112363A1 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR3056222B1 (en) * | 2016-09-19 | 2020-01-10 | Arkema France | COMPOSITION BASED ON 1-CHLORO-3,3,3-TRIFLUOROPROPENE |
| CN109425256A (en) * | 2017-08-29 | 2019-03-05 | 上海泰禾国际贸易有限公司 | A kind of anhydrous thermal medium of novel biography and its application |
| FR3070982B1 (en) * | 2017-09-12 | 2019-08-30 | Arkema France | COMPOSITION BASED ON HYDROCHLOROFLUOROOLEFIN AND MINERAL OIL |
| US11635091B2 (en) | 2020-03-13 | 2023-04-25 | Honeywell International Inc. | Compressor with integrated accumulator |
| US11841031B2 (en) | 2020-03-13 | 2023-12-12 | Honeywell International Inc. | Compressor sensor mount |
| WO2022210007A1 (en) * | 2021-03-31 | 2022-10-06 | 大阪瓦斯株式会社 | Absorption refrigeration cycle and compression-absorption refrigeration cycle |
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| US5237839A (en) * | 1992-05-22 | 1993-08-24 | Gas Research Institute | Gas absorber and refrigeration system using same |
| US20080016902A1 (en) * | 2006-07-23 | 2008-01-24 | Totec Ltd. | Absorption cooling system |
| US20110041549A1 (en) * | 2007-07-23 | 2011-02-24 | Van Derschrick Bernard | Method for Cooling in Distillation and Polymerisation Process by Absorption Refrigeration |
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| CN102906515A (en) * | 2010-04-01 | 2013-01-30 | 霍尼韦尔国际公司 | Absorption refrigeration cycles using LGWP refrigerant |
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| US4285211A (en) * | 1978-03-16 | 1981-08-25 | Clark Silas W | Compressor-assisted absorption refrigeration system |
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| JP6213194B2 (en) * | 2013-11-29 | 2017-10-18 | セントラル硝子株式会社 | Method for converting thermal energy into mechanical energy, organic Rankine cycle device, and method for replacing working fluid |
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2016
- 2016-01-09 JP JP2017536303A patent/JP2018507381A/en active Pending
- 2016-01-09 KR KR1020177021089A patent/KR20170106646A/en unknown
- 2016-01-09 CN CN201680014576.0A patent/CN107407510A/en active Pending
- 2016-01-09 WO PCT/US2016/012763 patent/WO2016112363A1/en active Application Filing
- 2016-01-09 EP EP16735526.2A patent/EP3243031A4/en not_active Withdrawn
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4178989A (en) * | 1977-04-15 | 1979-12-18 | Matsushita Electric Industrial Co., Ltd. | Solar heating and cooling system |
| US5237839A (en) * | 1992-05-22 | 1993-08-24 | Gas Research Institute | Gas absorber and refrigeration system using same |
| US20080016902A1 (en) * | 2006-07-23 | 2008-01-24 | Totec Ltd. | Absorption cooling system |
| US20110041549A1 (en) * | 2007-07-23 | 2011-02-24 | Van Derschrick Bernard | Method for Cooling in Distillation and Polymerisation Process by Absorption Refrigeration |
| CN102016451A (en) * | 2008-04-30 | 2011-04-13 | 霍尼韦尔国际公司 | Absorption refrigeraton cycles using a LGWP refrigerant |
| CN102906515A (en) * | 2010-04-01 | 2013-01-30 | 霍尼韦尔国际公司 | Absorption refrigeration cycles using LGWP refrigerant |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2018507381A (en) | 2018-03-15 |
| EP3243031A1 (en) | 2017-11-15 |
| WO2016112363A1 (en) | 2016-07-14 |
| KR20170106646A (en) | 2017-09-21 |
| EP3243031A4 (en) | 2018-08-01 |
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