EP0053536A2 - Einen Entmischungszyklus verwendendes Verfahren zur Kälteerzeugung - Google Patents

Einen Entmischungszyklus verwendendes Verfahren zur Kälteerzeugung Download PDF

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Publication number
EP0053536A2
EP0053536A2 EP81401815A EP81401815A EP0053536A2 EP 0053536 A2 EP0053536 A2 EP 0053536A2 EP 81401815 A EP81401815 A EP 81401815A EP 81401815 A EP81401815 A EP 81401815A EP 0053536 A2 EP0053536 A2 EP 0053536A2
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EP
European Patent Office
Prior art keywords
phase
liquid phase
solution
solvent
refrigerant
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.)
Granted
Application number
EP81401815A
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English (en)
French (fr)
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EP0053536A3 (en
EP0053536B1 (de
Inventor
Alexandre Rojey
Joseph Larue
Alain Barreau
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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/de
Publication of EP0053536A3 publication Critical patent/EP0053536A3/fr
Application granted granted Critical
Publication of EP0053536B1 publication Critical patent/EP0053536B1/de
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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
    • 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 (the latter arrangement is illustrated in Figure 1).
  • the compressed vapor phase VFC is mixed with a solvent phase S.
  • the mixture of vapor phase VFC and solvent phase passes through 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 81.
  • 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 d of the mixture of refrigerant and solvent leaving the exchanger E1 and collected in the tank 81 is an essential parameter.
  • the lower this temperature T d the lower the concentration of refrigerant in the solvent phase recycled from tank 81.
  • 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 ) of the light liquid phase is carried out simultaneously with the heat exchange of step (d).
  • said vaporization of the part (F I ) of the light liquid phase is carried out in contact with the solution originating from stage (a) after the latter has undergone the cooling of stage (b) .
  • the improved method according to the invention consists in separating the refrigerant leaving the tank 81 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 1 is expanded to an intermediate pressure between the low pressure and the high pressure of the cycle.
  • 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 dissolution step can advantageously be carried out at a temperature close to room 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, a nitro derivative, a nitrile, an amide or an amine.
  • the chemical formulas of such a solvent will be for example of the form R-OH, R-CO-R ', R-CHO, RO-R', R-N0 2 , R-CN, R-CONH 2 , R- NH2, R-NH-R 'or NRR'R'', R, R' and R "denoting alkyl radicals containing from 1 to 3 carbon atoms.
  • the solvent can be, for example methanol, ethanol, propanol, butanol, acetone, acetaldehyde, propionitrile, nitropropane, ethyl ether, tetrahydrofuran, dimethylformamide, ammonia, methylamine or trimethylamine.
  • the solvent can also be a perfluorinated product such as FC75 with chemical formula C a F 16 O and FC77 with chemical formula C a F 18 .
  • solvents may be suitable in some cases.
  • a hydrocarbon or a halogenated hydrocarbon can be used as a 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 can also be a lubricant and in particular the lubricant used in the compressor, if the compressor used is a lubricated 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 -13B1 or R-14.
  • This hydrocarbon base can be of the naphthenic type or of the paraffinic 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 may for example be a piston compressor, a screw compressor, a centrifugal compressor, an axial compressor with one or more stages, intermediate cooling operations being able to be carried out 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 d imposed at the outlet of the exchanger E1.
  • the liquid mixture consists of ethane and acetone; the composition in molar fraction is: ethane: 0.6 - acetone: 0.4.
  • the temperature is 35 ° C and the pressure is 4.25 MPa.
  • the flow rate is 10750 Kg / h.
  • the mixture passes through the exchanger E1 from where it leaves via line 2 at a temperature of -70 ° C. The lowering of temperature produces in the mixture a demixing into two liquid phases which are separated in the flask B1.
  • the light phase consists of 96% molar of ethane and 4% molar of acetone and leaves the flask 81 via line 3 with a flow rate of 3250 kg / h.
  • Part of this light phase (line 4), i.e. 2,340 kg / h, is expanded through the valve V3 to a pressure of 0.2 MPa, which lowers its temperature to -75 ° C, and enters the exchanger E2 through line 5.
  • the ethane is vaporized at a temperature of -75 ° C, supplying cold to an external fluid entering the exchanger E2 through line 16 and exiting through the duct 17.
  • the amount of cold produced is 273.2 kW.
  • the other part of the light phase i.e.
  • the heavy fraction of the flask 61 is made up of 36% molar of ethane and 64% molar of acetone: it is evacuated via line 12 and passes into the exchanger E1 from where it leaves via line 13 at a temperature of 30 ° C; it is taken up by the pump P1 and returned by the pipe 14 to be mixed in line with the high pressure ethane from the compressor K1, in the pipe 15.
  • the exchanger C1 there is a dissolution of the gaseous ethane in acetone which is accompanied by a release of heat which is evacuated by an external fluid.
  • the temperature is 30 ° C and the pressure is 4.15 MPa.
  • the flow rate is 14630 Kg / h.
  • the mixture passes through the exchanger E1 from which it leaves via the conduit 22 at a temperature of -40 ° C. The lowering of the temperature produces in the mixture a demixing into two liquid phases which are separated in the flask 81.
  • the light phase contains 90% by weight of ethane; it leaves the balloon B1 via the conduit 23 with a flow rate of 3350 Kg / h. Part of this light phase, ie 1976 Kg / h, enters via line 24 in the subcooling exchanger E3. It emerges from it through line 25 at a temperature of -6 ° C, is expanded through valve V3 to a pressure of 0.12 MPa and enters exchanger E2 through line 26. In this exchanger, the ethane vaporizes at a temperature of -85 ° C, supplying cold to an external fluid which enters the exchanger E2 by the conduit 38 and leaves it by the conduit 39: the amount of cold produced is 207.2 kW.
  • the light phase leaves the exchanger E2 through the conduit 27 at a temperature of -85 ° C and enters the exchanger E3, from which it emerges at a temperature of -45 ° C through the conduit 28; by this same conduit, it enters the exchanger E1, it leaves it at a temperature of 25 ° C, entirely gaseous.
  • This gas is sucked in by the first stage of the compressor K1 through the pipe 31.
  • the gas is at a pressure of 0.707 MPa, it passes through an intermediate cooler C2 which reduces its temperature to 30 ° C. .
  • the second part of the light phase (line 29), or 1374 Kg / h, from line 23, is expanded through the valve V2 to a pressure of 0.707 MPa, which lowers its temperature to -43 ° C: it enters the exchanger E1 through the conduit 30, it comes out entirely vaporized and at a temperature of 25 ° C through the conduit 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 compressor, from where it emerges at a pressure of 4.25 MPa.
  • the high pressure gas is sent through line 33 to the exchanger C1.
  • the heavy fraction of flask B1 contains 25.3% by weight of ethane. It is discharged through line 34 and passes through the exchanger E1; it comes out through the conduit 35 at a temperature of 25 ° C; it is taken up by the pump P1 and returned by line 36 to be mixed in line with the high pressure ethane coming from the compressor, in line 37.
  • exchanger C1 there is a dissolution of the ethane gas in the solvent which is accompanied by an evolution of heat, which is evacuated by an external fluid.
  • the resulting gas mixture is recompressed to 4.2 MPa and is sent via line 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 to 4.2 MPa. It is then mixed with the light phase of line 48.
  • Example 2 Although in Example 2, an equimolar mixture of acetone and methanol was used, it was found that a mixture of 20 to 80 mol% of acetone and 80 to 20 could be used successfully. % in moles of methanol.

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  • 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 Einen Entmischungszyklus verwendendes Verfahren zur Kälteerzeugung Expired EP0053536B1 (de)

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 true EP0053536A2 (de) 1982-06-09
EP0053536A3 EP0053536A3 (en) 1983-05-04
EP0053536B1 EP0053536B1 (de) 1986-06-04

Family

ID=9248553

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81401815A Expired EP0053536B1 (de) 1980-12-01 1981-11-18 Einen Entmischungszyklus verwendendes Verfahren zur Kälteerzeugung

Country Status (6)

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

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1987006284A1 (fr) * 1986-04-17 1987-10-22 Tch Thermo-Consulting-Heidelberg Gmbh Systeme pour la recuperation de la chaleur perdue contenue dans l'air d'evacuation provenant des sechoirs pour machines a papier
EP1340951A2 (de) * 1999-10-12 2003-09-03 Air Products And Chemicals, Inc. Hybridkreislauf zur Verflüssigung von Erdgas

Families Citing this family (12)

* 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
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
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 (de) * 2019-03-22 2023-04-12 Solvcor Technologies, LLC Kältekreislauf mit flüssig-flüssig-phasenübergängen

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US3477240A (en) * 1968-03-25 1969-11-11 Refrigeration System Ab Refrigerating method and system for maintaining substantially constant temperature
FR2314456A1 (fr) * 1975-06-09 1977-01-07 Inst Francais Du Petrole Procede de production de froid
FR2356097A1 (fr) * 1976-06-23 1978-01-20 Krieger Heinrich Procede et installation pour produire du froid avec au moins un circuit en cascade incorpore
US4171619A (en) * 1978-03-16 1979-10-23 Clark Silas W Compressor assisted absorption refrigeration system

Family Cites Families (1)

* 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

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US3477240A (en) * 1968-03-25 1969-11-11 Refrigeration System Ab Refrigerating method and system for maintaining substantially constant temperature
FR2314456A1 (fr) * 1975-06-09 1977-01-07 Inst Francais Du Petrole Procede de production de froid
FR2356097A1 (fr) * 1976-06-23 1978-01-20 Krieger Heinrich Procede et installation pour produire du froid avec au moins un circuit en cascade incorpore
US4171619A (en) * 1978-03-16 1979-10-23 Clark Silas W Compressor assisted absorption refrigeration system

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1987006284A1 (fr) * 1986-04-17 1987-10-22 Tch Thermo-Consulting-Heidelberg Gmbh Systeme pour la recuperation de la chaleur perdue contenue dans l'air d'evacuation provenant des sechoirs pour machines a papier
EP1340951A2 (de) * 1999-10-12 2003-09-03 Air Products And Chemicals, Inc. Hybridkreislauf zur Verflüssigung von Erdgas
EP1340951A3 (de) * 1999-10-12 2003-11-26 Air Products And Chemicals, Inc. Hybridkreislauf zur Verflüssigung von Erdgas
USRE39637E1 (en) 1999-10-12 2007-05-22 Air Products And Chemicals, Inc. Hybrid cycle for the production of liquefied natural gas

Also Published As

Publication number Publication date
FR2495293B1 (de) 1984-07-13
JPH026989B2 (de) 1990-02-14
DE3174781D1 (en) 1986-07-10
JPS57120076A (en) 1982-07-26
US4420946A (en) 1983-12-20
EP0053536A3 (en) 1983-05-04
ATE20278T1 (de) 1986-06-15
FR2495293A1 (fr) 1982-06-04
EP0053536B1 (de) 1986-06-04

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