WO2000070289A1 - Transfert de chaleur en deux phases, sans degazage - Google Patents

Transfert de chaleur en deux phases, sans degazage Download PDF

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Publication number
WO2000070289A1
WO2000070289A1 PCT/US1999/029486 US9929486W WO0070289A1 WO 2000070289 A1 WO2000070289 A1 WO 2000070289A1 US 9929486 W US9929486 W US 9929486W WO 0070289 A1 WO0070289 A1 WO 0070289A1
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Prior art keywords
heat
condenser
expansion device
vapor
temperature
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PCT/US1999/029486
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English (en)
Inventor
Phillip E. Tuma
Lew A. Tousignant
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3M Innovative Properties Company
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Priority to AU23588/00A priority Critical patent/AU2358800A/en
Publication of WO2000070289A1 publication Critical patent/WO2000070289A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/0266—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with separate evaporating and condensing chambers connected by at least one conduit; Loop-type heat pipes; with multiple or common evaporating or condensing chambers
    • C—CHEMISTRY; METALLURGY
    • C23—COATING METALLIC MATERIAL; COATING MATERIAL WITH METALLIC MATERIAL; CHEMICAL SURFACE TREATMENT; DIFFUSION TREATMENT OF METALLIC MATERIAL; COATING BY VACUUM EVAPORATION, BY SPUTTERING, BY ION IMPLANTATION OR BY CHEMICAL VAPOUR DEPOSITION, IN GENERAL; INHIBITING CORROSION OF METALLIC MATERIAL OR INCRUSTATION IN GENERAL
    • C23C—COATING METALLIC MATERIAL; COATING MATERIAL WITH METALLIC MATERIAL; SURFACE TREATMENT OF METALLIC MATERIAL BY DIFFUSION INTO THE SURFACE, BY CHEMICAL CONVERSION OR SUBSTITUTION; COATING BY VACUUM EVAPORATION, BY SPUTTERING, BY ION IMPLANTATION OR BY CHEMICAL VAPOUR DEPOSITION, IN GENERAL
    • C23C30/00—Coating with metallic material characterised only by the composition of the metallic material, i.e. not characterised by the coating process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/06—Control arrangements therefor

Definitions

  • This invention relates to a two-phase heat-transfer apparatus and methods therefor.
  • this invention relates to an apparatus (and methods therefor) using volatile fluids for two-phase heat transfer without first de-gassing the fluid or having to maintain the apparatus in a de-gassed state.
  • Two-phase heat transfer can generally be described as a process wherein the heat- transfer fluid changes phase from a liquid to a vapor (or vice- versa) thus utilizing the latent heat of vaporization for the heat-transfer fluid to either cool or heat a surface.
  • Applications utilizing two-phase heat transfer include, but are not limited to, direct contact electronic cooling (for example, cooling of supercomputers, avionics, transformers, train- traction electronics, and power electronics), heat pipes/thermosyphons (that is, saturated devices designed to operate as thermal superconductor or as thermo diodes), cooling of fuel cells (that is, electrochemical cells which produce useable electrical energy from a chemical reaction utilizing an external chemical fuel source), electrochemical batteries (that is, similar to fuel cells except they contain their own fuel), and other applications.
  • direct contact electronic cooling for example, cooling of supercomputers, avionics, transformers, train- traction electronics, and power electronics
  • heat pipes/thermosyphons that is, saturated devices designed to operate as thermal superconductor or as thermo diodes
  • cooling of fuel cells that is, electrochemical cells which produce useable electrical energy from a chemical reaction utilizing an external chemical fuel source
  • electrochemical batteries that is, similar to fuel cells except they contain their own fuel
  • Fluids used in such applications are typically required to possess low or zero ozone depletion potential, low toxicity, be preferably non-flammable, be non-aqueous, be inert, be dielectric, etc.
  • Volatile halogenated organic compounds such as perfluorocarbons (PFCs), perfluoropolyethers (PFPEs), hydrofluorocarbons (HFCs), chlorofluorocarbons
  • CFCs hydrochlorofluorocarbons
  • HFEs hydrofluoroethers
  • HHFEs hydrohalofluoroethers
  • HCCs hydrochlorocarbons
  • HBCs hydrobromocarbons
  • PFIs perfluoroalkyl iodides
  • PFOs perfluoroolefins
  • fluorinated compounds containing at least one aromatic moiety, and combinations thereof can be used as two-phase heat-transfer fluids.
  • halogenated organic compounds are often used as heat-transfer fluids because many of them possess the requisite properties. These properties ensure, for example, that the heat-transfer fluids will not degrade sensitive components or allow electric discharge or parasitic current drains.
  • Fluorinated organic compounds are particularly suitable as heat-transfer fluids because of the combination of their physical properties and their safety of use.
  • Fluorinated organic compounds are chemically inert (defined herein as being non-reacting with sensitive components (for example, capacitors, diodes, transistors, process fluids, etc.)) and have excellent dielectric properties (defined herein as being non-conductive). Thus, fluorinated organic compounds will not degrade sensitive components or allow electric discharge or parasitic current drains.
  • a common practice when using such fluids in a two-phase mode is to first de-gas the fluid to remove any dissolved air or other non-condensable gases and further to use the fluid in a vacuum-tight system to ensure that such gases do not re-enter the system if it reaches a vacuum condition (that is, the internal pressure is less than the ambient pressure).
  • a vacuum condition that is, the internal pressure is less than the ambient pressure.
  • the presence of air in a system is commonly believed to adversely affect condenser performance by reducing the partial pressure of the fluid vapor and thus reducing the temperature required to condense the vapor.
  • C4F9OCH3 boils and condenses at about 61 °C at one atmosphere (absolute pressure). Assuming ideal gas behavior, the presence of 20 percent by volume air in the condenser lowers the partial pressure of the C4F9OCH3 vapor to approximately 0.8 atmosphere. Though the boiling temperature remains at about 61 °C, the temperature required to condense the vapor present in the resultant vapor/air mixture is now about 55 °C. The affect of air on required condenser temperature is shown in Fig. 1. Thus, with air present in the vapor, it is a common belief that vapor can be condensed only by lowering the condenser temperature or by increasing the condenser surface area. These alterations are undesirable because they increase the system cost, for example, by necessitating larger condenser surfaces, larger fans, and possibly even requiring mechanical refrigeration.
  • the present invention provides an apparatus for two-phase heat transfer where volatile fluids such as volatile halogenated organic compounds may be used without first de-gassing the volatile fluid or having to maintain the apparatus/system in a de-gassed state.
  • the apparatus of the present invention allows for self-modulating two-phase heat transfer and for evaporation temperatures which, once the system is operating, are stable to within a couple of °C regardless of the temperature of the heat sink (for example, the fluid cooling the condenser). Expensive condenser capacity modulation schemes are unnecessary when the apparatus of the present invention is employed.
  • the present invention provides an apparatus for two-phase heat transfer comprising a heat source comprising energy; an evaporator through which said energy is dissipated containing a heat-transfer fluid as a condensate and a vapor; a condenser comprising a first end and a second end, said condenser first end in fluid connection with said evaporator, said condenser being of a size such that said condensate is not entrained by said vapor; a heat sink for dissipating said energy from said condenser; and an expansion device in fluid connection with said condenser second end, said expansion device containing heat-transfer fluid vapor and non-condensable gas and being of a size to allow for expansion of said vapor and said gas into said expansion device while maintaining a substantially constant operating pressure by causing said vapor and said gas to flow into and out of said condenser second end to optimize dissipation of said energy; wherein said heat source is maintained at substantially constant temperature and said apparatus is maintained
  • the apparatus of the present invention may further comprise an adjuster device.
  • Another embodiment of the present invention is a method of two-phase heat transfer which comprises a method suitable for two-phase heat transfer comprising the steps of: (a) providing non-condensable gas; (b) causing energy to flow from a heat source to an evaporator which contains heat-transfer fluid as a condensate; (c) after step (b), said condensate absorbing energy from said evaporator and forming a vapor; (d) after step (c), causing a heat sink to come into contact with a condenser containing said vapor to form in-part condensate of said vapor and to remove energy; (e) after step (d), causing the condensate to return to said evaporator; (f) after step (c), causing some vapor to flow through to an expansion device where said expansion device adjusts to provide sufficient volume for said vapor; (g) causing some non-condensable gas to flow through to an expansion device where
  • Fig. 1 is a graph of condensation temperature versus volume percent of non- condensable gas in an ideal vapor/non-condensable gas mixture.
  • Fig. 2a is a graph of condenser operating temperature over time for varying cooling water temperatures.
  • Fig. 2b is a graph of condenser operating temperature over time in a saturated system (that is, air removed) for varying condenser water temperatures.
  • Fig. 2c is a graph of evaporator operating temperature over time using a similar configuration as the apparatus depicted in Fig. 5.
  • Fig. 3 is a schematic of an apparatus of the present invention comprising a heat source 30, evaporator 32, vertical pipe 34, condenser 36, heat sink 37, and an expansion device 38.
  • Fig. 4 is a schematic of an apparatus of the present invention comprising a heat source 40, evaporator 42, vapor line 44, liquid return line 45, condenser 46, heat sink 47, and an expansion device 48.
  • Fig. 5 is a schematic of an apparatus of the present invention comprising a heat source 50, an evaporator 52, a condenser 56, an expansion device 58, a vapor line 54, a liquid return line 55, and a heat sink 57.
  • Fig. 6 is a schematic of an apparatus of the present invention comprising a heat source 60, thermocouple 61, evaporator 62, condenser 66, thermocouple 65, cooling water in 67a, cooling water out 67b, and an expansion device 68.
  • the present invention provides an apparatus for two-phase heat transfer.
  • the apparatus of the present invention comprises a heat source, evaporator, condenser, heat sink, expansion device, and a heat-transfer fluid.
  • the evaporator and condenser may be one unit.
  • the condenser and expansion device may be one unit.
  • the apparatus may further comprise an adjuster device.
  • the apparatus of the present invention may be used with applications/systems requiring either heating or cooling, for example an application requiring a constant surface temperature which generates or absorbs heat during use.
  • the apparatus of the present invention provides for the evaporation or condensation temperature to be held substantially constant at the saturation temperature of the heat-transfer fluid at the pressure selected by the user and maintained by the expansion device.
  • no costly and complex heat-transfer fluid de-gassing is required.
  • no costly and complex measures are required to ensure that no air enters into the system. If the heat-transfer fluid is properly selected, the system, including the apparatus of the present invention, may run at zero to slight gage pressure and therefore, high pressure components may not be required. Therefore, less expensive, low pressure components such as thin-walled or plastic heat exchangers may be used.
  • an adjuster device which will increase the system pressure may be used if the use of a low boiling temperature fluid is desirable or if operating temperature modulation is desirable.
  • the present invention utilizes a heat-transfer fluid.
  • the particular heat-transfer fluid is largely chosen based on the application/system with which the apparatus is used.
  • the heat-transfer fluids are inert, dielectric, nonflammable, volatile, non-aqueous, and environmentally acceptable.
  • the heat-transfer fluids are preferably non-flammable, which is defined herein as having a flash point significantly greater (for example, 10 to 20 °C) than the operating temperature for the application/system.
  • the flash point is above about 60 °C and more preferably the flash point is above about 100 °C.
  • the heat-transfer fluids are volatile under the application conditions.
  • the boiling point will be less than about 120 °C at atmospheric pressure. More preferably, the boiling point of the heat-transfer fluids will range from about 50 °C to about 80 °C at the system pressure.
  • Suitable heat-transfer fluids for use in this invention include, but are not limited to, halogenated (that is, fluorine-, chlorine-, bromine and/or iodine-substituted) and non- halogenated organic compounds.
  • Classes of non-halogenated organic compounds which can be used include linear, branched and cyclic aliphatic hydrocarbons; aromatic hydrocarbons; alcohols; ethers; ketones; and esters.
  • non-halogenated organic compounds examples include n-heptane, n-octane, cyclohexane, toluene, ethanol, n- propanol, isopropanol, methyl ethyl ketone, ethyl acetate and diisopropyl ether.
  • these relatively low boiling non-halogenated organic compounds are flammable and toxic so are not desirable as heat-transfer fluids.
  • Halogenated organic compounds are preferred as heat-transfer fluids.
  • halogenated organic compounds include perfluorocarbons (PFCs), perfluoropolyethers (PFPEs), hydrofluorocarbons (HFCs), hydrofluoroethers (HFEs), hydrochlorofluorocarbons (HCFCs), hydrohalofluoroethers (HHFEs), chlorofluorocarbons (CFCs), hydrochlorocarbons (HCCs), hydrobromocarbons (HBCs), perfluoroiodides (PFIs), perfluoroolefins (PFOs), fluorinated compounds containing at least one aromatic moiety, or a combination thereof.
  • the halogenated organic compound(s) comprise a fluorinated organic compound.
  • flammable halogenated or flammable non-halogenated organic compounds can be incorporated in the heat-transfer fluid (for example, azeotropic or near-azeotropic compositions), provided that the resulting mixture is non-flammable and has a very narrow boiling point range.
  • liquid CFCs such as CFC-113 (CC1F 2 CC1 F) and CFC-11 (CC1 3 F) were considered ideal candidates for heat-transfer applications, exhibiting excellent performance, low cost, and no safety drawbacks.
  • CFC-113 CFC-113
  • CFC-11 CC1 3 F
  • HCFCs useful as heat-transfer fluids include CF3CHCI2, CH3CCI2F,
  • HCFCs may also be legislated out of production due to ozone layer degradation.
  • Useful PFCs include perfluorinated fluids that can be single compounds, but usually will be a mixture of such compounds.
  • the PFCs have molecular structures which can be straight-chained, branched-chained or cyclic, or a combination thereof, such as perfluoroalkylcycloaliphatic, are fluorinated to greater than at least 95 molar percent substitution of the carbon chain, and are preferably free of ethylenic unsaturation.
  • the skeletal chain of the molecular structure can contain catenary (that is, "in-chain") oxygen, trivalent nitrogen or hexavalent sulfur heteroatoms bonded only to carbon atoms, such heteroatoms providing stable linkages between fluorocarbon groups and not interfering with the inert character of the fluid.
  • the perfluorinated fluid will preferably have about 5 to about 9 carbon atoms, the maximum number being dictated by the desired boiling point.
  • Preferred PFCs typically contain about 60 to about 76 weight percent carbon-bonded fluorine.
  • Useful PFCs include perfluoro-4-methylmorpholine, perfluorotriethylamine, perfluoro-2-ethyltetrahydrofuran, perfluoro-2-butyltetrahydrofuran, perfluoropentane, perfluorohexane, perfluoro-4-methylmorpholine, perfluorodibutyl ether, perfluoroheptane, perfluorooctane, perfluorotripropylamine, perfluorononane, and mixtures thereof.
  • Preferred inert fluorochemical liquids include perfluorohexane, perfluoro-2- butyltetrahydrofuran, perfluoroheptane, perfluorooctane, and mixtures thereof, especially perfluoroheptane and perfluorooctane.
  • Commercially available PFCs useful in this invention include FLUORINERTTM liquids, for example, FC-72, FC-75, FC-77 and FC- 84, described in the 1990 product bulletin #98-0211-5347-7(101.5) NPI, and mixtures thereof.
  • FLUORINERTTM liquids FC-3284 and FC-6003. FLUORINERTTM liquids are available from Minnesota Mining and Manufacturing Company, St. Paul, Minnesota.
  • PFPEs Useful PFPEs are described in U.S. Patent Nos. 3,250,807 (Fritz et al.); 3,250,808 (Moore et al.); and 3,274,239 (Selman).
  • PFPEs derived by polymerization of perfluoropropylene oxide followed by stabilization, for example, with fluorinating agents are available as KRYTOXTM K fluorinated oils from E. I. du Pont de Nemours & Co., Wilmington, Delaware. Fluids derived from tetrafluoroethylene and hexafluoropropylene oxide are available as GALDENTM HT fluids from Ausimont Corp., Thorofare, New Jersey.
  • Useful HFCs include organic compounds having a 3- to 8-carbon saturated backbone substituted with both hydrogen and fluorine atoms, but essentially no other atoms, such as chlorine. HFCs having a 4- to 8-carbon backbone are preferred. The carbon backbone can be straight, branched, cyclic, or mixtures of these. Useful HFCs include compounds having more than approximately 5 molar percent fluorine substitution, or less than 95 molar percent fluorine substitution, based on the total number of hydrogen and fluorine atoms bonded to carbon, and specifically excludes PFCs, PFOs, PFPEs, CFCs, HCFCs, and HHFEs.
  • Useful HFCs can be selected from:
  • representative compounds of Formula I include CHF2(CF2)2CF2H, CF3CF2CH2CH2F, CF3CH2CF2CH2F, CH3CHFCF2CF3, CF3CH2CH2CF3, CH2FCF2CF2CH2F,
  • n ⁇ 6 representative compounds of Formula II include CF3CH2CHFCF2CF3, CF 3 CHFCH2CF 2 CF3 ? CF3CH2CF2CH2CF3, CF3CHFCHFCF2CF3, CF3CH2CH2CF2CF3, CH3CHFCF2CF2CF3, CF3CF2CF2CH2CH3, CH3CF2CF2CF3, CF3CH2CHFCH2CF3, CH2FCF2CF2CF2CF3, CHF2CF2CF2CF3, CH 3 CF(CHFCHF 2 )CF 3 , CH 3 CH(CF 2 CF3)CF3,
  • representative compounds of Formula III include CHF2(CF2)4CF2H, (CF3CH2)2CHCF3, CH 3 CHFCF2CHFCHFCF3, HCF2CHFCF2CF 2 CHFCF2H, H 2 CFCF 2 CF2CF2CF2H, CHF2CF2CF2CF2CHF2, CH 3 CF(CF 2 H)CHFCHFCF 3 , CH 3 CF(CF 3 )CHFCHFCF 3 , CH 3 CF(CF3)CF 2 CF2CF3,
  • representative compounds of Formula IV include CH3CHFCH2CF2CHFCF2CF3, CH3(CF 2 )5CH 3 , CH 3 CH 2 (CF2)4CF3, CF 3 CH2CH2(CF 2 )3CF3, CH2FCF 2 CHF(CF2)3CF3, CF 3 CF2CF2CHFCHFCF2CF3, CH3CF2C(CF3)2CF2CH3, CF3CF2CF2CHFCF2CF2CF3, CH 3 CH(CF3)CF2CF2CF2CH 3 ,
  • Useful HFCs of Formula V include CH3CH2CH2CH2CF2CF2CF2CF3, CH (CF 2 )6CH3, CHF2CF(CF3)(CF2)4CHF2, CHF 2 CF(CF3)(CF2)4CHF2, CH3CH2CH(CF3)CF 2 CF2CF 2 CF3, CH 3 CF(CF2CF3)CHFCF 2 CF2CF3,
  • HFCs include CF 3 CFHCFHCF 2 CF 3 , C 5 F n H, C 6 F 13 H, CF3CF2CH2CH2F, CHF2CF2CF2CHF2, 1 ,2-dihydroperfluorocyclopentane and 1,1,2- trihydroperfluorocyclopentane.
  • Useful HFCs include HFCs available under the VERTRELTM, available from E. I. duPont de Nemours & Co., and under the ZEORORA- HTM, available from Nippon Zeon Co. Ltd., Tokyo, Japan.
  • HFEs are chemical compounds containing carbon, fluorine, hydrogen, one or more ether oxygen atoms, and optionally one or more additional catenary heteroatoms within the carbon backbone, such as sulfur or trivalent nitrogen.
  • the HFE can be straight-chained, branched-chained, or cyclic, or a combination thereof, such as alkylcycloaliphatic.
  • the HFE is free of unsaturation.
  • n is a number from 1 to 3 inclusive and R ⁇ and R2 are the same or are different from one another and are selected from the group consisting of alkyl, aryl, and alkylaryl groups. At least one of Rj and R2 contains at least one fluorine atom, and at least one of Rj and R2 contains at least one hydrogen atom, either or both groups R ⁇ and R2 can optionally contain one or more catenary heteroatoms, and preferably the total number of fluorine atoms in the HFE at least equals the total number of hydrogen atoms. R ⁇ and R2 may also be linear, branched, or cyclic, and may contain one or more unsaturated carbon-carbon bonds, though preferably R ⁇ and R2 are both saturated.
  • Preferred HFEs include: (1) segregated HFEs, wherein ether-bonded alkyl or alkylene, etc., segments of the HFE are either perfluorinated (for example, perfluorocarbon) or non-fluorinated (for example, hydrocarbon), but not partially fluorinated; and (2) non-segregated HFEs, wherein at least one of the ether-bonded segments is neither perfluorinated nor fluorine-free but is partially fluorinated (that is, contains a mixture of fluorine and hydrogen atoms).
  • Segregated HFEs include HFEs which comprise at least one mono-, di-, or trialkoxy-substituted perfluoroalkane, perfluorocycloalkane, perfluorocycloalkyl- containing perfluoroalkane, or perfluorocycloalkylene-containing perfluoroalkane compound. These HFEs are described, for example, in PCT Publication No.
  • Rf -(O-R h ) x wherein: x is from 1 to about 3, and Rf is a perfluorinated hydrocarbon group having a valency x, which can be straight, branched, or cyclic, etc., and preferably contains from 3 to about 7 carbon atoms, and more preferably contains from 3 to about 6 carbon atoms; each Rft is independently a linear or branched alkyl group having from 1 to about 3 carbon atoms; wherein either or both of the groups Rf and R n can optionally contain one or more catenary heteroatoms; and wherein the sum of the number of carbon atoms in the Rf group and the number of carbon atoms in the Rft group(s) is preferably between 4 and about 9.
  • Rf groups include C3F7-isomers (that is, n-, iso-), C4F9- isomers (that is, n-, iso-, sec-, tert-), C5F11 - isomers, C5F13- isomers, and perfluorocyclohexyl; and most preferable R groups include methyl and ethyl.
  • Representative compounds described by Formula VII useful in the present invention include, but are not limited to, the following compounds:
  • Particularly preferred segregated HFEs of Formula VII include «-C3F7OCH3, (CF 3 ) 2 CFOCH3, 77-C4F9OCH3, (CF3) 2 CFCF 2 OCH3, «-C 3 F 7 OC2H5 5 «-C 4 F 9 OC 2 H5,
  • azeotropes and azeotrope-like compositions which are blends of segregated HFEs with non-halogenated organic compounds.
  • azeotropes and azeotrope-like compositions consisting of blends of C4F9OCH3, C4F9OC2H5 and C3F7OCH3 with organic solvents.
  • Such blends of C4F9OCH3 with organic solvents are described in PCT Publication No. WO 96/36689.
  • Useful binary C4F9OCH3/solvent azeotropes and azeotrope-like compositions include blends of C4F9OCH3 with the following solvents: straight chain, branched chain and cyclic alkanes having from 6 to 8 carbon atoms; cyclic and acyclic ethers having from 4 to 6 carbon atoms; acetone; chlorinated alkanes having 1, 3 or 4 carbon atoms; chlorinated alkenes having 2 carbon atoms; alcohols having from 1 to 4 carbon atoms; partially fluorinated alcohols having 2 to 3 carbon atoms; 1-bromopropane; acetonitrile; HCFC-225ca (l,l-dichloro-2,2,3,3,3- pentafluoropropane); and HCFC-225cb (1,3-dichloro-l,
  • Useful ternary C4F9OCH3/solvent azeotropes and azeotrope-like compositions include blends of C4F9OCH3 with the following solvents pairs: trans- 1,2-dichloroethylene and alcohols having from 1 to 4 carbon atoms; trans- 1,2- dichloroethylene and partially fluorinated alcohols having 2 to 3 carbon atoms; trans- 1,2- dichloroethylene and acetonitrile; and HCFC-225 and alcohols having from 1 to 2 carbon atoms.
  • Such blends of C4F9OC 2 H5 with organic solvents are described in PCT
  • Useful binary C4F9OC 2 H5/solvent azeotropes and azeotrope-like compositions include blends of C4F9OC 2 H5 with the following solvents: straight chain, branched chain and cyclic alkanes having from 6 to 8 carbon atoms; esters having 4 carbon atoms; ketones having 4 carbon atoms; disiloxanes having 6 carbon atoms; cyclic and acyclic ethers having from 4 to 6 carbon atoms; alcohols having from 1 to 4 carbon atoms; partially fluorinated alcohols having 3 carbon atoms; chlorinated alkanes having 3 or 4 carbon atoms; chlorinated alkenes having 2 or 3 carbon atoms; 1- bromopropane; and acetonitrile.
  • Useful binary C3F7OCH3/solvent azeotropes and azeotrope-like compositions include blends of C3F7OCH3 with the following solvents: straight chain, branched chain and cyclic alkanes having from 5 to 7 carbon atoms; methyl formate; acetone; methanol; l,l,l,3,3,3-hexafluoro-2-propanol; methylene chloride and trans- 1,2-dichloroethylene.
  • Useful ternary C3F7OCH3/solvent azeotropes and azeotrope- like compositions include blends of C3F7OCH3 with the following solvents pairs: trans-
  • Useful non-segregated HFEs include alpha-, beta- and omega-substituted hydrofluoroalkyl ethers such as those described in U.S. Patent No. 5,658,962 (Moore et al.), and those described by Marchionni et al. in "Hydrofluoropolyethers," Journal of Fluorine Chemistry 95 (1999), pp. 41-50, which can be described by the general structure shown in Formula VIII:
  • X is either F, H, or a perfluoroalkyl group containing from 1 to 3 carbon atoms which is optionally hydro-substituted in the omega position; each Rf' is independently selected from the group consisting of -CF 2 -, -C 2 F4-, and
  • R" is a divalent organic radical having from 1 to about 3 carbon atoms, and may be perfluorinated, unfluorinated or partially fluorinated; and y is an integer from 1 to 7; wherein when X is F, R" contains at least one F atom; and wherein preferably the total number of carbon atoms is between about 3 and about 8.
  • Representative compounds described by Formula VIII useful in the present invention include, but are not limited to, the following compounds:
  • Preferred non-flammable, non-segregated HFEs include C4F9OC F4H,
  • HCF2OCF2OC2F4OCF2H and mixtures thereof.
  • Non-segregated HFEs are available from Ausimont Corp., Milano, Italy, under the H-GALDENTM.
  • HHFEs are defined as ether compounds containing fluorine, non-fluorine halogen (that is, chlorine, bromine, and/or iodine) and hydrogen atoms.
  • An important subclass of HHFEs is perfluoroalkylhaloethers (PFAHEs).
  • PFAHEs are defined as ether compounds wherein on one side of the ether oxygen atom is a perfluoroalkyl group and on the other side of the ether oxygen atom is a carbon backbone substituted with carbon-bonded hydrogen atoms and halogen atoms, wherein at least one of the halogen atoms is chlorine, bromine, or iodine.
  • Useful PFAHEs include those described by the general structure shown in Formula IX:
  • Rf' ' is a perfluoroalkyl group preferably having at least about 3 carbon atoms, most preferably from 3 to 6 carbon atoms, and optionally containing a catenary heteroatom such as nitrogen or oxygen;
  • X is a halogen atom selected from the group consisting of bromine, iodine, and chlorine; "a” preferably is from about 1 to 4; "b” is at least 1 ; "c” can range from 0 to about 2; “d” is at least 1 ; and b+c+d is equal to 2a+l .
  • PFAHEs are described in PCT Publication No. WO 99/14175.
  • Useful PFAHEs include c-C 6 F ⁇ -OCH 2 Cl, (CF 3 ) 2 CFOCHCl 2 , (CF 3 ) 2 CFOCH 2 Cl, CF3CF2CF2OCH2CI,
  • Suitable hydrochlorocarbons and hydrobromocarbons include HCCs and HBCs such as trans- 1,2-dichloroethylene, trichloroethylene, perchloroethylene, 1,1,1- trichloroethane and n-propyl bromide.
  • Suitable fluorinated compounds containing at least one aromatic moiety include fluorinated monoalkyl-, dialkyl- and trialkyl-substituted aromatic compounds, including toluene and xylene derivatives. Preferred among these compounds are fluoroalkyl substituted compounds, such as hexafluoroxylene, benzotrifluoride and p- chlorobenzotrifluoride. Such compounds are commercially available, for example, under the OXSOLTM, available from Occidental Chemical Corp., Niagara Falls, New York.
  • Suitable perfluoroiodides include PFIs such as perfluoropropyl iodide (C3F7I) and perfluorobutyl iodide (C4F9I).
  • Perfluoroolefins (PFOs) suitable for use as heat-transfer fluids are normally liquid perfluoroolefin compounds, perfluoroaromatic compounds, and perfluorocycloolefin compounds.
  • the PFOs can contain some residual carbon-bonded hydrogen (generally less than about 0.4 mg/g and preferably less than about 0.1 mg/g, for example, 0.01 to 0.05 mg/g) but are preferably substantially completely fluorinated.
  • the PFOs can contain from about 5 to about 10 carbon atoms and can contain one or more catenary heteroatoms, for example, trivalent nitrogen or divalent oxygen atoms.
  • blowing agent compounds include hexafluoropropene dimers, for example, perfluoro(4- methylpent-2-ene) and perfluoro(2-methylpent-2-ene); hexafluoropropene trimers, for example, perfluoro(4-methyl-3-isopropylpent-2-ene) and perfluoro(2,4-dimethyl-3- ethylpent-2-ene); tetrafluoroethylene oligomers, for example, perfluoro(3-methylpent-2- ene), perfluoro(3,4-dimethylhex-3-ene), and perfluoro(2,4-dimethyl-4-ethylhex-2-ene); perfluoro(l-pentene); perfluoro(2-pentene); perfluoro(l-hexene); perfluoro(2 -hexene); perfluoro(3-hexene); perfluflufluor
  • the heat source depends on the system or application for which the apparatus of the present invention is being used.
  • the heat source is the electrochemical reaction which transfers heat to the heat-transfer fluid.
  • Other examples include, but are not limited to the windings in an electrical transformer, integrated circuits in an electronics module, and power electronics in a rectifier.
  • the heat-transfer fluid receives energy from the heat source in the evaporator.
  • the evaporator comprises the surface from which heat is being removed or dissipated and a container for heat-transfer fluid.
  • the surface and container can be the same.
  • the condenser comprises the surface on which heat is being deposited.
  • the condenser comprises a first and a second end.
  • the heat-transfer fluid receives energy from the heat source in the evaporator (if the apparatus is to be used for cooling). For example, in the case of a transformer, the windings which generate heat comprise the evaporator. In the case of an electronics module, the integrated circuits and various other components comprise the evaporator. The size and shape of the evaporator depend upon the system/application.
  • the heat-transfer fluid boils or evaporates to form a vapor.
  • the vapor then travels to the condenser.
  • the heat-transfer fluid has an evaporation temperature.
  • the evaporating surface temperature is preferably at a temperature at least about 10 °C more than the evaporation temperature of the heat-transfer fluid.
  • the condenser is typically connected directly to the evaporator such that the evaporator is in fluid connection with the condenser. For example, there may be one large open tube such that falling condensate is not entrained by the rising vapor. This type of connection may not be practical for commercial applications because these applications often require remote location of the condenser if it is not desirable to dissipate the condenser heat in the same location as the evaporator.
  • the condenser is likely plumbed to the evaporator by some type of line.
  • a large, vertical pipe which runs from the evaporator to the condenser would carry the vapor and returning condensate in a counterflow arrangement as is shown in Fig. 3.
  • the heat-transfer fluid in the evaporator 32 is heated from the heat source 30 and forms a vapor.
  • This vaporized fluid then flows through a vertical pipe 34 from 34b (that is, evaporator first connector) to 34a (that is, condenser first connector) into the condenser 36.
  • the vapor condenses into a liquid condensate and flows down vertical pipe 34 from 34a to 34b into the evaporator. Heat flows out the condenser 36 into the heat sink 37.
  • V v liquid velocity (m/s)
  • d diameter of the fluid passage (m)
  • g acceleration of gravity (m/s ⁇ )
  • a small vapor line such as those used in commercial refrigeration systems can be used in conjunction with a separate liquid return line.
  • This configuration is shown in Fig. 4.
  • the heat-transfer fluid in the evaporator 42 is heated from the heat source 40 and forms a vapor.
  • This vaporized fluid then flows through a vertical pipe 44 (vapor line) from 44a (that is, evaporator first connector outlet) to 44b (that is, condenser first connector inlet) into the condenser
  • the vapor condenses into a liquid condensate and flows down the vertical pipe 45 (liquid return line) from 45a (that is, condenser first connector outlet) to 45b (that is, evaporator first connector inlet) into the evaporator 42. Heat flows out the condenser 46 into the heat sink 47.
  • the heat-transfer fluid in the evaporator 52 is heated from the heat source 50 and forms a vapor.
  • This vaporized fluid then flows through the vertical pipe 54 (vapor line) from 54a (that is, evaporation first connector outlet) to 54b (that is, condenser first connector inlet) into the condenser 56 (that is, the top region of the condenser).
  • the vapor condenses into liquid condensate and flows downward through the condenser 56 and then flows down the vertical pipe 55 (liquid return line) from 55a to 55b into the evaporator 52. Heat flows out the condenser into the heat sink 57.
  • a natural result of separate vapor and liquid lines is the propensity of liquid condensate in the evaporator to "back up" in the direction of the condenser through the liquid return line. Any time the vapor line is sized too small, the resulting pressure drop in the vapor line results in liquid back-flowing up the liquid return line.
  • condensers are typically flow-though type condensers often with very small fluid passages. If these condensers are used with the configuration shown in Fig. 5, the non-condensable gas may be entrained right through the condenser by the fast moving vapors. Because the non-condensable gas separates and collects into the expansion device, a condenser with rather large, open passages is preferred. When oriented vertically, these passages permit condensed liquid to form a film on the interior walls of the condenser tubes and flow back to the evaporator as required by the configurations shown in Figs. 3 and 4.
  • Equation A The same criteria outlined in Equation A for sizing the plumbing preferably are followed when sizing the condenser tubes and headers so that rising vapors will not entrain the falling liquid film. Furthermore, the condenser is sized to dissipate the maximum expected evaporator heat input.
  • a stable interface forms between saturated vapor and a mixture of non-condensable gas and vapor which is above the saturated vapor. No condensation occurs above this interface.
  • This interface is automatically located such that enough of the condenser has been wetted with saturated vapor to condense the vapor and to keep the system operating at the selected operating pressure.
  • the interface drops (as the expansion device contracts) and thus reduces the effective condenser surface area.
  • the system remains at the selected operating pressure.
  • the interface rises (as the expansion device rises) and increases the effective condenser surface area.
  • the system remains at atmospheric pressure.
  • the expansion device is a passively controlled device which allows the above-mentioned interface to rise and fall as previously described without causing the system pressure to change to an extent that would cause the evaporator temperature to go out of the specified/desired range and without allowing fluid vapor to leak out.
  • non-condensable gas and heat-transfer fluid vapor enters the condenser and is in fluid connection with the expansion device 38, 48, and 58.
  • the expansion device will self-regulate. Thus, the expansion device will expand as the system pressure increases and contracts when this pressure decreases
  • the condenser comprises a second connector and the expansion device comprises a first connector.
  • a tube for example, Tygon tubing, brazed copper, steel, polyvinylchloride, etc. is interconnected with the condenser second connector and the expansion device first connector.
  • the expansion device may be a large ground glass syringe which maintains the system at atmospheric pressure.
  • this type of expansion device is not practical for commercial applications because it is relatively fragile and cannot be used with systems having pressurization.
  • Commercially available bellows or bladder-type expansion vessels may be used for this purpose.
  • Commercially available products include: metal bellows such as those manufactured by Senior Flexonics, Sharon, Massachusetts; reinforced polyethylene expansion devices with polymeric bladders such as those manufactured by WellMate Division of Structural Group, Chardon, Ohio; or a polymeric bellows, available from Marsh Bellofram Corp., Newell, West Virginia.
  • the bladder is chosen preferably such that non-condensable gases, such as air, do not diffuse into the system and accumulate in such a way as to raise the system pressure above its intended level. Such gas accumulation can destroy the functionality of the design unless some type of purge is incorporated which removes only an acceptable amount of gas. Purging gas when the system is non- operational is one way to accomplish this. Another way to purge gas that has accumulated due to diffusion through a membrane or seal is to allow the system to vent to atmosphere (purge) in a controlled manner, expelling the accumulated gas. The purging preferably occurs in a manner that will conserve the heat-transfer fluid whilst allowing the excess non-condensable gases to escape. There are several methods that allow this purging to occur in a controlled manner.
  • a volume-based purge indicator works as follows: a piston/cylinder expansion chamber is embodied as a syringe with a barrel and plunger located in a gravitational field, and having the plunger oriented such that gravity acts to push the plunger into the barrel of the syringe. A small hole is drilled into the syringe barrel. The position of the hole along the barrel determines the expansion reservoir volume at which purging begins. As non- condensable gas infiltrates the system, it collects (under normal two-phase operation) in the piston/cylinder expansion chamber.
  • the plunger of the syringe extends axially from the cylinder of the syringe barrel.
  • the piston exposes the hole in the barrel allowing the excess non- condensable gas to be purged from the expansion chamber.
  • an external force for example, a spring force or the influence of gravity
  • Another indicator that can be used to determine whether to purge excess non-condensable gas is based on the internal pressure of the expansion chamber.
  • the internal pressure can be monitored and controlled by a simple, self re-sealing pressure relief device commonly available as commercial products.
  • the ability to accommodate non-condensable gas in a two-phase heat transfer system provides utility in the following ways: (1) accommodating some non-condensable gas in the heat-transfer fluid allows normal handling of the heat- transfer fluid during fill, shipment, power down etc. Normal handling means the heat-transfer fluid can be exposed to atmospheric air during the filling process or while the system is opened for maintenance; (2) some non-condensable gas in the two-phase heat transfer system, when properly accommodated, allows for a robust heat transfer system with consistent evaporator and condenser behavior.
  • the utility of controlling the volume of non-condensable gas by a volume- indicated or pressure-indicated purge allows the system to operate properly despite the infiltration of non-condensable gas that may occur over time; and allows the sizing of a smaller expansion reservoir than is required had not a purge mechanism been provided.
  • the volume of the expansion device is preferably sized according to one of the following equations:
  • Psat(T) is the heat-transfer fluid saturation pressure at temperature
  • I > atm + I > exp' q 0 p is the heat flux during operation;
  • q cr jt is the critical film boiling heat flux of the heat-transfer fluid for the application geometry;
  • q mc is the incipient heat flux required for the application geometry and the incipient heat flux is that required to initiate boiling;
  • Q ev is the maximum total heat being produced at the evaporating surface;
  • Tcold i the coldest conceivable temperature the system can reach when it is non-operational; Tsat(P) i s the heat-transfer fluid saturation temperature at pressure
  • T ev is the desired operating temperature of the evaporating surface
  • ⁇ cond * s the condenser temperature
  • T op is the heat-transfer fluid boiling temperature during operation ⁇ T ev - ⁇ T sat ;
  • Vf is the volume of heat-transfer fluid when system is non- operational Tcoid
  • V is the free volume or headspace volume when the system is non-operational at T co ld;
  • V eX p is the expansion device volume; and x is the solubility (volume percent) of air in the heat-transfer fluid at Tcoid-
  • Equation (B) which is relevant for configurations such as those depicted in Figs. 3 and 4, the expansion device is large enough to accommodate whatever non- condensable gas may have been in the system before startup assuming the system leaked to atmospheric pressure. After startup, this non-condensable gas migrates into the expansion device and this gas is saturated with vapor at the expansion device ambient temperature (as a worst case).
  • Equation (C) which is relevant for the configuration shown in Fig. 5, the expansion device is again large enough to accommodate whatever non-condensable gas may have been in the system before startup assuming the system leaked to atmospheric pressure. However, during operation, saturated vapor may condense in the expansion device heating it to the condensation temperature, thereby raising the partial pressure of vapor in the expansion device and necessitating a larger expansion device.
  • the expansion device may be sized smaller than described above if the temperature fluctuations expected from this are manageable for the application. These specifications are not, therefore, intended to be limiting.
  • Equation (D) indicates that the system operating pressure is chosen such that no structural or mechanical limitations are violated.
  • An example is the safe operating pressure for a seal or component.
  • Equation (E) indicates that the heat flux at the evaporation surface is large enough to permit two-phase heat transfer.
  • This incipient heat flux is well known in the art and is strongly dependent not only on the heat-transfer fluid being used, but on the geometry of the particular application.
  • the heat flux is lower than the critical or film boiling heat flux which is also commonly known in the art. If this constraint is not met, evaporator surface temperatures can rise sharply and lead to system failure.
  • Equation (F) indicates that the condenser has sufficient capacity to dissipate all heat generated by the evaporator at a time when the heat sink temperature is the warmest conceivable, generally 55 °C.
  • the heat sink depends on the system or application for which the apparatus of the present invention is being used.
  • the heat sink may be an air stream.
  • Other examples include, but are not limited to, cooling fluids in the case of liquid or gas (for example, air) cooled condensers and a process stream in the case when the process stream is heated at a constant temperature.
  • the heat-transfer fluid has an evaporation temperature.
  • the heat sink is preferably at a temperature at least about 10 °C less than the evaporation temperature.
  • Fig. 6 depicts an example of the apparatus of the present invention as built in a laboratory.
  • the evaporator 62 is a 50 milliliter, 3-neck spherical Pyrex flask which is heated with a conventional mantle 60.
  • the condenser 66 is a standard 12 centimeter long, 1.2 centimeter I.D. Pyrex single tube-in-shell (tube 66a, shell 66b), water-cooled condenser. The water flows in 67a and out 67b of the shell of the condenser.
  • the expansion device 68 is a 75 ml Perfectum MicromateTM ground glass syringe, available from Popper and Sons, New Hyde Park, New York.
  • the expansion device 68 does, however, float freely so that any rise in system pressure will permit the syringe plunger to rise 69.
  • the heat-transfer fluid may be used as a lubricant and sealant for the syringe plunger.
  • the system Prior to startup, the system contained a significant amount of air. There was air in the condenser 66 as well as in the headspace of the evaporator. Additionally, air dissolved into the heat-transfer fluid, in this case ⁇ F ⁇ 4, was used and may be 50 volume percent air under ambient pressure and at room temperature. Upon startup, the dissolved air was liberated. Because the air was less dense than the vapor being generated, the air migrated toward the top of the system. An interface between saturated vapor and the air/vapor mixture formed as the vapor pushed up into the condenser. This is a phenomenon commonly observed during distillations and reflux experiments. As this happened, the expansion device 68 expanded and accommodated the air/vapor mixture.
  • Fig. 2a shows actual operating temperatures during changes in the cooling water temperature using the laboratory apparatus described above. If the same system is operated in a saturation state with all of the air removed, the system behaves as shown in Fig. 2b (comparative).
  • Fig. 2c shows actual evaporator operating temperature over time using a configuration similar to Fig. 5.
  • an adjuster device can be added which applies pressure to the expansion device.
  • the adjuster device may be a mechanical pressure regulator or gas source which induces a system operating pressure, throughout the operating range of the expansion device, sufficiently adjustable that the system pressure and thus the operating temperature do not fall outside of specifications. Though the system now operates at a positive pressure, the applied pressure can be modulated to adjust the operating temperature. This further device permits the use of heat- transfer fluids with much lower boiling points.
  • the present invention also provides a method for two-phase heat transfer without de-gassing the heat-transfer fluid.
  • This method comprises the steps of a method suitable for two-phase heat transfer comprising the steps of: (a) providing non-condensable gas; (b) causing energy to flow from a heat source to an evaporator which contains heat-transfer fluid as a condensate; (c) after step (b), said condensate absorbing energy from said evaporator and forming a vapor; (d) after step (c), causing a heat sink to come into contact with a condenser containing said vapor to form in-part condensate of said vapor and to remove energy; (e) after step (d), causing the condensate to return to said evaporator; (f) after step (c), causing some vapor to flow through to an expansion device where said expansion device adjusts to provide sufficient volume for said vapor; (g) causing some non-condensable gas to flow through to an expansion device
  • the present invention is used to cool a proton exchange membrane fuel cell (PEMFC) using a hydrofluoroether fluid methoxynonafluorobutane which is sold by Minnesota Mining and Manufacturing as 3MTM NOVECTM HFE-7100.
  • This heat-transfer fluid has an atmospheric boiling point of 61 °C and possesses the requisite dielectric properties to keep adjacent cooling plates electrically isolated.
  • the fuel cell is used to power a 2000 square foot home in Arizona where ambient temperatures are expected to range between 32 °F (0 °C) and 120 °F (48.9 °C).
  • the fuel cell stack is composed of a series of 100+ electrochemical cells between which are placed roughly as many cooling plates which contain the HFE fluid.
  • These plates are in fluid connection with one another such that they share a bottom header and a top header.
  • the top header is connected to the condenser as shown in Fig. 3.
  • the condenser is constructed such that the vapors can rise into the vertically oriented condenser tubes without entraining the falling condensate as described by Equation (A).
  • the outdoor-located expansion reservoir is sized such that it can accommodate any air which might leak into the system at 32 °F (0 °C) when the system is non operational and accommodate that air at 120 °F (48.9 °C).
  • Equation (B) the volume must be roughly 4.3 liters.
  • the proton exchange membrane fuel cell (PEMFC) described above may also be cooled using the lower boiling hydrofluorocarbon fluid 1,1,1,3,3- pentafluoropropane. In such a configuration, the system operating pressure is above atmospheric and the seals are designed to accommodate this increased pressure.
  • the proton exchange membrane fuel cell (PEMFC) described above may also be cooled using the lower hydrofluorocarbon fluid 2,3- dihydrodecafluoropentane, available from E. I. du Pont de Nemours & Co.
  • the system operating pressure is still slightly above atmospheric and the various variables described above take on the following values:

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Abstract

L'invention concerne un appareil convenant au transfert de chaleur en deux phases, dans lequel des fluides volatils, tels que des composés organiques halogénés volatils peuvent être utilisés comme fluides caloporteurs sans dégazage initial ou sans qu'il soit nécessaire de maintenir l'appareil/le système à l'état dégazé. L'appareil est, de préférence, du type à automodulation. Il comporte une source de chaleur (30), un évaporateur (32), un condensateur (36), une source de froid (37) et un détendeur (38) conçu pour maintenir une pression de fonctionnement constante et une température constante de la source de chaleur (30).
PCT/US1999/029486 1999-05-18 1999-12-13 Transfert de chaleur en deux phases, sans degazage WO2000070289A1 (fr)

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1459379A1 (fr) * 2001-12-27 2004-09-22 Showa Denko K.K. Dispositif de refroidissement par ebullition pour composant generateur de chaleur
WO2010081957A1 (fr) * 2009-01-19 2010-07-22 Commissariat A L'energie Atomique Et Aux Energies Alternatives Radiateur pour chauffage domestique a fluide caloporteur diphasique
WO2010120220A1 (fr) * 2009-04-16 2010-10-21 Telefonaktiebolaget L M Ericsson (Publ) Agencement de transfert thermique et boîtier électronique comprenant un agencement de transfert thermique et procédé de commande de transfert thermique
ITRM20110447A1 (it) * 2011-08-25 2013-02-26 I R C A S P A Ind Resistenz E Corazzate E Radiatore a scambio termico bifasico con ottimizzazione del transitorio di ebollizione
RU2643930C2 (ru) * 2016-07-04 2018-02-06 Александр Михайлович Деревягин Способ и устройство для теплопередачи
US9894815B1 (en) 2016-08-08 2018-02-13 General Electric Company Heat removal assembly for use with a power converter
WO2019116260A1 (fr) * 2017-12-13 2019-06-20 3M Innovative Properties Company 1-alcoxypropènes perfluorés, compositions, et procédés et appareils pour leur utilisation
US10638648B2 (en) 2016-04-28 2020-04-28 Ge Energy Power Conversion Technology Ltd. Cooling system with pressure regulation
CN113717699A (zh) * 2021-07-15 2021-11-30 浙江巨化技术中心有限公司 一种组合物、含硅液冷剂及其制备方法以及浸没冷却系统
CN114144922A (zh) * 2019-06-26 2022-03-04 阿尔普拉兹公司 液体传热混合物及其用途
US11535579B2 (en) 2017-12-13 2022-12-27 3M Innovative Properties Company Hydrofluoroolefin ethers, compositions, apparatuses and methods for using same
US11551827B2 (en) 2017-12-13 2023-01-10 3M Innovative Properties Company Perfluorinated 1-alkoxypropenes in dielectric fluids and electrical devices

Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2500388A (en) 1948-07-21 1950-03-14 Minnesota Mining & Mfg Fluorocarbon ethers
US2519983A (en) 1948-11-29 1950-08-22 Minnesota Mining & Mfg Electrochemical process of making fluorine-containing carbon compounds
US2594272A (en) 1948-09-10 1952-04-29 Minnesota Mining & Mfg Cyclic fluoroalkylene oxide compounds
US2616927A (en) 1950-05-12 1952-11-04 Minnesota Mining & Mfg Fluorocarbon tertiary amines
US3250808A (en) 1963-10-31 1966-05-10 Du Pont Fluorocarbon ethers derived from hexafluoropropylene epoxide
US3250807A (en) 1963-08-23 1966-05-10 Du Pont Dicarboxylic acids of fluorocarbon ethers and fluorides, esters, amides and salts thereof
US3274239A (en) 1962-08-31 1966-09-20 Du Pont Fluorocarbon ethers
EP0000786A1 (fr) * 1977-08-12 1979-02-21 Hitachi, Ltd. Dispositif de refroidissement fermé, du type à ébullition
US4330033A (en) * 1979-03-05 1982-05-18 Hitachi, Ltd. Constant pressure type ebullient cooling equipment
DE3613459A1 (de) * 1986-04-21 1987-10-22 Inst Fuer Kerntechnik & Energ Waermeuebertragungsvorrichtung
US4788339A (en) 1985-09-06 1988-11-29 Minnesota Mining And Manufacturing Company Perfluoroaminoethers
US4799537A (en) * 1987-10-13 1989-01-24 Thermacore, Inc. Self regulating heat pipe
US5394936A (en) * 1993-03-12 1995-03-07 Intel Corporation High efficiency heat removal system for electric devices and the like
WO1996022356A1 (fr) 1995-01-20 1996-07-25 Minnesota Mining And Manufacturing Company Procede et composition de nettoyage
WO1996036688A1 (fr) 1995-05-16 1996-11-21 Minnesota Mining And Manufacturing Company Compositions du type azeotrope et leurs applications
US5631306A (en) 1993-12-29 1997-05-20 Minnesota Mining And Manufacturing Company Foamable composition containing unsaturated perfluorochemical blowing agent
US5658962A (en) 1994-05-20 1997-08-19 Minnesota Mining And Manufacturing Company Omega-hydrofluoroalkyl ethers, precursor carboxylic acids and derivatives thereof, and their preparation and application
WO1998037163A1 (fr) 1997-02-19 1998-08-27 Minnesota Mining And Manufacturing Company Compositions azeotropiques de methoxy-perfluoropropane et leur utilisation

Patent Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2500388A (en) 1948-07-21 1950-03-14 Minnesota Mining & Mfg Fluorocarbon ethers
US2594272A (en) 1948-09-10 1952-04-29 Minnesota Mining & Mfg Cyclic fluoroalkylene oxide compounds
US2519983A (en) 1948-11-29 1950-08-22 Minnesota Mining & Mfg Electrochemical process of making fluorine-containing carbon compounds
US2616927A (en) 1950-05-12 1952-11-04 Minnesota Mining & Mfg Fluorocarbon tertiary amines
US3274239A (en) 1962-08-31 1966-09-20 Du Pont Fluorocarbon ethers
US3250807A (en) 1963-08-23 1966-05-10 Du Pont Dicarboxylic acids of fluorocarbon ethers and fluorides, esters, amides and salts thereof
US3250808A (en) 1963-10-31 1966-05-10 Du Pont Fluorocarbon ethers derived from hexafluoropropylene epoxide
EP0000786A1 (fr) * 1977-08-12 1979-02-21 Hitachi, Ltd. Dispositif de refroidissement fermé, du type à ébullition
US4330033A (en) * 1979-03-05 1982-05-18 Hitachi, Ltd. Constant pressure type ebullient cooling equipment
US4788339A (en) 1985-09-06 1988-11-29 Minnesota Mining And Manufacturing Company Perfluoroaminoethers
DE3613459A1 (de) * 1986-04-21 1987-10-22 Inst Fuer Kerntechnik & Energ Waermeuebertragungsvorrichtung
US4799537A (en) * 1987-10-13 1989-01-24 Thermacore, Inc. Self regulating heat pipe
US5394936A (en) * 1993-03-12 1995-03-07 Intel Corporation High efficiency heat removal system for electric devices and the like
US5631306A (en) 1993-12-29 1997-05-20 Minnesota Mining And Manufacturing Company Foamable composition containing unsaturated perfluorochemical blowing agent
US5658962A (en) 1994-05-20 1997-08-19 Minnesota Mining And Manufacturing Company Omega-hydrofluoroalkyl ethers, precursor carboxylic acids and derivatives thereof, and their preparation and application
WO1996022356A1 (fr) 1995-01-20 1996-07-25 Minnesota Mining And Manufacturing Company Procede et composition de nettoyage
WO1996036688A1 (fr) 1995-05-16 1996-11-21 Minnesota Mining And Manufacturing Company Compositions du type azeotrope et leurs applications
WO1998037163A1 (fr) 1997-02-19 1998-08-27 Minnesota Mining And Manufacturing Company Compositions azeotropiques de methoxy-perfluoropropane et leur utilisation

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
KIRK-OTHMER: "Encyclopedia of Chemical Technology", vol. 10, 1980, JOHN WILEY & SONS, pages: 874 - 881, 3RD ED
MARCHIONNI ET AL: "Hydrofluoropolyethers", JOURNAL OF FLUORINE CHEMISTRY 95, 1999, pages 41 - 50

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1459379A1 (fr) * 2001-12-27 2004-09-22 Showa Denko K.K. Dispositif de refroidissement par ebullition pour composant generateur de chaleur
EP1459379A4 (fr) * 2001-12-27 2006-06-07 Showa Denko Kk Dispositif de refroidissement par ebullition pour composant generateur de chaleur
US7093647B2 (en) 2001-12-27 2006-08-22 Showa Denko K.K. Ebullition cooling device for heat generating component
US20120002954A1 (en) * 2009-01-19 2012-01-05 Stephane Colasson Radiator For Domestic Heating With A Two-Phase Heat-Transfer Fluid
FR2941290A1 (fr) * 2009-01-19 2010-07-23 Commissariat Energie Atomique Radiateur pour chauffage domestique a fluide caloporteur diphasique.
US8909034B2 (en) * 2009-01-19 2014-12-09 Commissariat A L'energie Atomique Et Aux Energies Alternatives Radiator for domestic heating with a two-phase heat-transfer fluid
WO2010081957A1 (fr) * 2009-01-19 2010-07-22 Commissariat A L'energie Atomique Et Aux Energies Alternatives Radiateur pour chauffage domestique a fluide caloporteur diphasique
WO2010120220A1 (fr) * 2009-04-16 2010-10-21 Telefonaktiebolaget L M Ericsson (Publ) Agencement de transfert thermique et boîtier électronique comprenant un agencement de transfert thermique et procédé de commande de transfert thermique
US8650891B2 (en) 2009-04-16 2014-02-18 Telefonaktiebolaget L M Ericsson (Publ) Heat transfer arrangement and electronic housing comprising a heat transfer arrangement and method of controlling heat transfer
ITRM20110447A1 (it) * 2011-08-25 2013-02-26 I R C A S P A Ind Resistenz E Corazzate E Radiatore a scambio termico bifasico con ottimizzazione del transitorio di ebollizione
WO2013027193A1 (fr) * 2011-08-25 2013-02-28 I.R.C.A. S.P.A. Industria Resistenze Corazzate E Affini Radiateur d'échange de chaleur biphase avec optimisation de la transition d'ébullition
US9581390B2 (en) 2011-08-25 2017-02-28 I.R.C.A. S.P.A. Industria Resistenze Corazzate E Affini Biphasic heat exchange radiator with optimisation of the boiling transient
US10638648B2 (en) 2016-04-28 2020-04-28 Ge Energy Power Conversion Technology Ltd. Cooling system with pressure regulation
RU2643930C2 (ru) * 2016-07-04 2018-02-06 Александр Михайлович Деревягин Способ и устройство для теплопередачи
US9894815B1 (en) 2016-08-08 2018-02-13 General Electric Company Heat removal assembly for use with a power converter
EP3498063B1 (fr) * 2016-08-08 2021-03-31 General Electric Company Ensemble d'évacuation de chaleur destiné à être utilisé avec un convertisseur de puissance
WO2019116260A1 (fr) * 2017-12-13 2019-06-20 3M Innovative Properties Company 1-alcoxypropènes perfluorés, compositions, et procédés et appareils pour leur utilisation
CN111479900A (zh) * 2017-12-13 2020-07-31 3M创新有限公司 全氟化1-烷氧基丙烯、组合物、及其使用方法和设备
CN111479900B (zh) * 2017-12-13 2022-03-29 3M创新有限公司 全氟化1-烷氧基丙烯、组合物、及其使用方法和设备
US11535579B2 (en) 2017-12-13 2022-12-27 3M Innovative Properties Company Hydrofluoroolefin ethers, compositions, apparatuses and methods for using same
US11551827B2 (en) 2017-12-13 2023-01-10 3M Innovative Properties Company Perfluorinated 1-alkoxypropenes in dielectric fluids and electrical devices
US11673861B2 (en) 2017-12-13 2023-06-13 3M Innovative Properties Company Perfluorinated 1-alkoxypropenes, compositions, and methods and apparatuses for using same
CN114144922A (zh) * 2019-06-26 2022-03-04 阿尔普拉兹公司 液体传热混合物及其用途
CN113717699A (zh) * 2021-07-15 2021-11-30 浙江巨化技术中心有限公司 一种组合物、含硅液冷剂及其制备方法以及浸没冷却系统

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