EP0053536B1 - Perfectionnement au procédé de production de froid mettant en oeuvre un cycle à démixtion - Google Patents

Perfectionnement au procédé de production de froid mettant en oeuvre un cycle à démixtion Download PDF

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Publication number
EP0053536B1
EP0053536B1 EP81401815A EP81401815A EP0053536B1 EP 0053536 B1 EP0053536 B1 EP 0053536B1 EP 81401815 A EP81401815 A EP 81401815A EP 81401815 A EP81401815 A EP 81401815A EP 0053536 B1 EP0053536 B1 EP 0053536B1
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EP
European Patent Office
Prior art keywords
phase
refrigerant fluid
solution
solvent
content
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP81401815A
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German (de)
English (en)
French (fr)
Other versions
EP0053536A2 (fr
EP0053536A3 (en
Inventor
Alexandre Rojey
Joseph Larue
Alain Barreau
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
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Publication date
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Priority to AT81401815T priority Critical patent/ATE20278T1/de
Publication of EP0053536A2 publication Critical patent/EP0053536A2/fr
Publication of EP0053536A3 publication Critical patent/EP0053536A3/fr
Application granted granted Critical
Publication of EP0053536B1 publication Critical patent/EP0053536B1/fr
Expired legal-status Critical Current

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Classifications

    • 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
    • F25B25/00—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00
    • F25B25/02—Compression-sorption machines, plants, or systems

Definitions

  • the invention relates to refrigeration machines using, to produce cold, the vaporization of a refrigerant.
  • the refrigerant in the vapor phase is compressed, condensed by yielding heat to an external fluid, most often water or air, then expanded and sent to the vaporization stage.
  • the refrigerant is vaporized in the exchanger E2 by cooling an external fluid. It is recycled to the compressor K1 either directly or through the exchanger E1 (this last arrangement is illustrated in fig. 1).
  • the compressed vapor phase VFC is mixed with a solvent phase S.
  • the mixture of vapor phase VFC and solvent phase passes through the exchanger C1 in which the vapor phase is condensed in the presence of the solvent.
  • the liquid phase thus obtained is cooled in the exchanger E1.
  • a demixing takes place which leads to the formation of two liquid phases, including a phase rich in solvent and a phase rich in refrigerant which are collected in the settling tank B1.
  • the solvent phase is driven by the pump P1 and recycled through the exchanger E1.
  • the liquid phase rich in refrigerant is expanded through the expansion valve V1 and sent to the exchanger E2.
  • the temperature T l of the mixture of refrigerant and solvent leaving the exchanger E1 and collected in the tank B1 is an essential parameter.
  • the lower this temperature T the lower the concentration of refrigerant in the solvent phase recycled from tank B1.
  • this temperature T d is lowered, the possibility of reducing the rate of solvent recirculation and also the dissolution pressure.
  • said vaporization of the part (F i ) is carried out simultaneously with the heat exchange of step (d).
  • said vaporization of the part (F,) is carried out in contact with the solution originating from step (a) after the latter has undergone the cooling of step (b).
  • the improved method according to the invention consists in separating the refrigerant leaving the tank B1 into two fractions.
  • a first fraction F 1 passes through the expansion valve V2 then is placed in heat exchange contact with the mixture of solvent and refrigerant, to lower the temperature to the required level. In particular, to lower this temperature T , it is necessary to increase the fraction F 1 of refrigerant passing through the expansion valve.
  • the remaining fraction F 2 is expanded through the expansion valve V3 and vaporized through the exchanger E2 to cool the external fluid which arrives in the exchanger E2.
  • the fraction F is expanded to an intermediate pressure between the low pressure and the high pressure of the cycle.
  • the mixture of solvent and refrigerant leaving the exchanger C1 is successively cooled in the exchanger E4 by heat exchange with the recycled solvent phase and then in the exchanger E5 by heat exchange with the fraction F 1 which is vaporized.
  • the vapor phase obtained by mixing the vapor fractions from the vaporization of the liquid fractions F 1 and F 2 is returned directly to the compressor K1. In this way, it is possible to use for the exchangers E4 and E5 conventional tube and shell exchangers.
  • a variant consists in exchanging heat between the fraction F 2 leaving the exchanger E2 and the solution leaving the condenser C1. This can be done, for example, in the exchanger E4 which is then a triple exchanger.
  • the invention applies to all mixtures of refrigerant and solvent which make it possible to carry out the dissolving step with transmission of the heat of dissolution to an external fluid and the liquid-liquid demixing step by lowering the temperature.
  • the solvent consists of the same liquid as that used to lubricate the compressor.
  • the dissolution step can advantageously be carried out at a temperature close to ambient temperature, this temperature being obtained by heat exchange with water or air.
  • This temperature can be, for example, between 20 and 50 ° C.
  • the solvent is a preferably polar solvent, which can be, for example, an alcohol, a ketone, an aldehyde, an ether, an ester, a nitro derivative, a nitrile, an amide or an amine.
  • the chemical formulas of such a solvent will for example be of the form R-OH, R-CO-R ', R-CHO, RO-R', R-NO z , R-CN, R-CONH 2 , R- NH 2 , R-NH-R 'or NRR'R ", R, R' and R" denoting alkyl radicals containing from 1 to 3 carbon atoms.
  • solvents may be suitable in some cases.
  • a hydrocarbon or a fluorinated and / or chlorinated hydrocarbon can be used as solvent.
  • the solvents can be used pure or as a mixture. In particular by using a mixture of two solvents whose solvent powers are different, it is possible, by modifying the relative proportions of these solvents, to adjust the concentration of refrigerant.
  • the solvent consists of the lubricant used in the compressor.
  • This lubricant can consist of a hydrocarbon base.
  • the refrigerant will preferably consist of a halogenated hydrocarbon or a “fluorocarbon” fluid of the “Freon” type such as R-22, R-23, R-13, R-115, R-13Bl or R-14.
  • This hydrocarbon base can be of the naphthenic type or of the paraffinic type. It has been observed that by lowering the temperature, the liquid-liquid demixing phenomena are more marked and the separation of the two liquid phases more advanced in the case of a paraffinic base than in the case of a naphthenic base.
  • lubricant by mixing the two types of lubricants, it is possible to adjust the mutual solubility so as to obtain a sufficient dissolution of the refrigerant at the temperature of the condenser C1 and a separation by demixing sufficiently advanced at the temperature T d . It is also possible to use a synthetic librifying agent as solvent. Different types of polymers can be used.
  • the lubricant can be, for example, of the polyolefin type or of the alkylphenyl type.
  • the low pressure of the cycle is generally between 1 and 10 atm.
  • the high pressure of the cycle is generally between 10 and 70 atm.
  • the compressor can be, for example, a piston compressor, a screw compressor, a centrifugal compressor, an axial compressor with one or more stages, intermediate coolings being able to be operated between the stages.
  • the exchangers used can be, for example, tube and shell exchangers, wound or plate.
  • Surface coatings can be used to facilitate vaporization or condensation of the products.
  • the expansion members can be regulated automatically.
  • the expansion valve V3 can be controlled so as to produce a refrigeration temperature imposed in the exchanger E2 and the expansion valve V2 can be controlled so as to produce a temperature T, imposed at the outlet of the exchanger E1.
  • the light phase leaves the balloon B1 through the conduit 3.
  • Part of this light phase (conduit 4) is expanded through the valve V3, which lowers its temperature, and enters the exchanger E2 through the conduit 5.
  • the refrigerant is vaporized by supplying cold to an external fluid entering the exchanger E2 by the conduit 16 and leaving by the conduit 17.
  • the other part of the light phase is sent by the conduit 7 to the valve V2 where it is relaxed, which lowers its temperature; it leaves via the conduit 8 to be mixed with the gaseous refrigerant which comes from the exchanger E2 by the conduit 6.
  • the gas-liquid mixture thus formed enters via the conduit 9 in the exchanger E1, in which the refrigerant vaporizes .
  • the refrigerant is entirely gaseous; it is sucked in by compressor K1, in which it undergoes two-stage compression with intermediate cooling.
  • the high pressure gas is sent through line 11 to the exchanger C1.
  • the heavy fraction of the balloon B1 is evacuated through the conduit 12 and passes into the exchanger E1 from where it exits through the conduit 13; it is taken up by the pump P1 and returned by the pipe 14 to be mixed in line with the high pressure refrigerant coming from the compressor K1, in the pipe 15.
  • the exchanger C1 there is a dissolution of the refrigerant in the solvent which is accompanied by an evolution of heat which is evacuated by an external fluid.
  • the light phase leaves the balloon B1 through the conduit 23. Part of this light phase enters through the conduit 24 in the sub-cooling exchanger E3. It exits through the conduit 25, is expanded through the valve V3 and enters the exchanger E2 through the conduit 26. In this exchanger, the refrigerant vaporizes by supplying cold to an external fluid which enters the exchanger E2 through the conduit 38 and out through the conduit 39.
  • the light phase leaves the exchanger E2 through the conduit 27 and enters the exchanger E3, from which it emerges through the conduit 28; by this same conduit, it enters the exchanger E1, it leaves it, entirely gaseous. This gas is sucked by the first stage of the compressor K1 through the conduit 31.
  • the gas passes through an intermediate cooler C2.
  • the second part of the light phase (line 29) coming from line 23, is expanded through valve V2, which lowers its temperature: it enters the exchanger E1 through line 30, it comes out entirely vaporized through the line 32: it is then mixed with the part which comes from the first compression stage.
  • the entire light gas phase is sucked in through the second stage of the K2 compressor.
  • the high pressure gas is sent through line 33 to the exchanger C1.
  • the heavy fraction of the balloon B1 is evacuated through the conduit 34 and passes through the exchanger E1; it comes out through the conduit 35; it is taken up by the pump P1 and returned by the conduit 36 to be mixed in line with the high pressure refrigerant coming from the compressor, in the conduit 37.
  • the exchanger C1 there is a dissolution of the gaseous refrigerant in the solvent which is accompanied by a release of heat, which is discharged by an external fluid.
  • the gas mixture (line 41) enters the exchanger E4 and then into the exchanger E5. It passes into the liquid state in the pipe 42 and settles in the tank B1. Part of the light phase is expanded in valve V2 and is sent to line 43; another part is expanded in the valve V3 and reaches the exchanger E2 via the conduit 44. It supplies cold to the fluid flowing in the conduits 46 and 47. It is evacuated via the conduit 45 and arrives at the compressor K1 after mixing with the light phase of the pipe 43. The resulting gas mixture is recompressed and is sent via the pipe 48 to the exchanger C1. The heavy liquid phase of the balloon B1 passes through the pipe 49, the exchanger E4 and the pipe 50 where its pressure is raised by the pump P1. It is then mixed with the light phase of line 48.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Steroid Compounds (AREA)
EP81401815A 1980-12-01 1981-11-18 Perfectionnement au procédé de production de froid mettant en oeuvre un cycle à démixtion Expired EP0053536B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT81401815T ATE20278T1 (de) 1980-12-01 1981-11-18 Einen entmischungszyklus verwendendes verfahren zur kaelteerzeugung.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8025514A FR2495293A1 (fr) 1980-12-01 1980-12-01 Perfectionnement au procede de production de froid mettant en oeuvre un cycle a demixtion
FR8025514 1980-12-01

Publications (3)

Publication Number Publication Date
EP0053536A2 EP0053536A2 (fr) 1982-06-09
EP0053536A3 EP0053536A3 (en) 1983-05-04
EP0053536B1 true EP0053536B1 (fr) 1986-06-04

Family

ID=9248553

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81401815A Expired EP0053536B1 (fr) 1980-12-01 1981-11-18 Perfectionnement au procédé de production de froid mettant en oeuvre un cycle à démixtion

Country Status (6)

Country Link
US (1) US4420946A (ja)
EP (1) EP0053536B1 (ja)
JP (1) JPS57120076A (ja)
AT (1) ATE20278T1 (ja)
DE (1) DE3174781D1 (ja)
FR (1) FR2495293A1 (ja)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3405631A1 (de) * 1984-02-17 1985-08-22 Hermann 8871 Rechbergreuthen Hahn Rohr mit verbindungselement
DE3612907A1 (de) * 1986-04-17 1987-11-12 Thermo Consulting Heidelberg Anlage zur rueckgewinnung von in der abluft der trockner von papiermaschinen enthaltener abwaerme
US4724679A (en) * 1986-07-02 1988-02-16 Reinhard Radermacher Advanced vapor compression heat pump cycle utilizing non-azeotropic working fluid mixtures
US4918942A (en) * 1989-10-11 1990-04-24 General Electric Company Refrigeration system with dual evaporators and suction line heating
US5582020A (en) * 1994-11-23 1996-12-10 Mainstream Engineering Corporation Chemical/mechanical system and method using two-phase/two-component compression heat pump
US5873260A (en) * 1997-04-02 1999-02-23 Linhardt; Hans D. Refrigeration apparatus and method
US6105388A (en) * 1998-12-30 2000-08-22 Praxair Technology, Inc. Multiple circuit cryogenic liquefaction of industrial gas
US6267907B1 (en) 1999-06-03 2001-07-31 The Lubrizol Corporation Lubricant composition comprising an aliphatic substituted naphthalene alone or in combination refrigeration systems
US6308531B1 (en) * 1999-10-12 2001-10-30 Air Products And Chemicals, Inc. Hybrid cycle for the production of liquefied natural gas
US6125656A (en) * 1999-11-03 2000-10-03 Praxair Technology, Inc. Cryogenic rectification method for producing nitrogen gas and liquid nitrogen
US6230519B1 (en) * 1999-11-03 2001-05-15 Praxair Technology, Inc. Cryogenic air separation process for producing gaseous nitrogen and gaseous oxygen
DE102004037537A1 (de) * 2004-08-03 2006-02-23 Robert Bosch Gmbh Einrichtung und Verfahren zum Steuern der Strömungsgeschwindigkeit einer Flüssigkeitsströmung in einer Hydraulikleitung
US11796229B2 (en) 2019-03-22 2023-10-24 Solvcor Technologies. Llc Systems and methods for high energy density heat transfer
EP3941991A4 (en) * 2019-03-22 2023-04-12 Solvcor Technologies, LLC REFRIGERATION CIRCUIT WITH LIQUID-LIQUID PHASE TRANSITIONS

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3477240A (en) * 1968-03-25 1969-11-11 Refrigeration System Ab Refrigerating method and system for maintaining substantially constant temperature

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1686935A (en) * 1924-05-31 1928-10-09 York Ice Machinery Corp Condenser
US2041725A (en) * 1934-07-14 1936-05-26 Walter J Podbielniak Art of refrigeration
DE953378C (de) * 1950-08-29 1956-11-29 Margarete Altenkirch Geb Schae Verfahren und Vorrichtung zum Betrieb einer Waermepumpe
DE1125956B (de) * 1961-05-25 1962-03-22 Giovanni Novaro Verfahren und Vorrichtung zur Kaelteerzeugung mit einer Absorptionskaeltemaschine und einem Verdichter fuer das Kaeltemittel zwischen Verdampfer und Absorber
FR2314456A1 (fr) * 1975-06-09 1977-01-07 Inst Francais Du Petrole Procede de production de froid
DE2628007A1 (de) * 1976-06-23 1978-01-05 Heinrich Krieger Verfahren und anlage zur erzeugung von kaelte mit wenigstens einem inkorporierten kaskadenkreislauf
US4171619A (en) * 1978-03-16 1979-10-23 Clark Silas W Compressor assisted absorption refrigeration system

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3477240A (en) * 1968-03-25 1969-11-11 Refrigeration System Ab Refrigerating method and system for maintaining substantially constant temperature

Also Published As

Publication number Publication date
FR2495293B1 (ja) 1984-07-13
JPH026989B2 (ja) 1990-02-14
DE3174781D1 (en) 1986-07-10
JPS57120076A (en) 1982-07-26
EP0053536A2 (fr) 1982-06-09
US4420946A (en) 1983-12-20
EP0053536A3 (en) 1983-05-04
ATE20278T1 (de) 1986-06-15
FR2495293A1 (fr) 1982-06-04

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