EP0041005B1 - Verfahren zur mechanischen Energieerzeugung aus Wärme mit Mehrstoffgemischen als Arbeitsmittel - Google Patents

Verfahren zur mechanischen Energieerzeugung aus Wärme mit Mehrstoffgemischen als Arbeitsmittel Download PDF

Info

Publication number
EP0041005B1
EP0041005B1 EP81400755A EP81400755A EP0041005B1 EP 0041005 B1 EP0041005 B1 EP 0041005B1 EP 81400755 A EP81400755 A EP 81400755A EP 81400755 A EP81400755 A EP 81400755A EP 0041005 B1 EP0041005 B1 EP 0041005B1
Authority
EP
European Patent Office
Prior art keywords
mixture
temperature
heat
process according
anyone
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
EP81400755A
Other languages
English (en)
French (fr)
Other versions
EP0041005A1 (de
Inventor
Alexandre Rojey
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Priority to AT81400755T priority Critical patent/ATE14778T1/de
Publication of EP0041005A1 publication Critical patent/EP0041005A1/de
Application granted granted Critical
Publication of EP0041005B1 publication Critical patent/EP0041005B1/de
Expired legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/06—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids

Definitions

  • Such a fluid vaporizes and condenses at a substantially constant temperature.
  • the fluid mixture of the above patent is a non-azeotropic mixture of trifluoroethanol and water.
  • the present invention is based on the observation that the temperature of the external fluids with which the exchanges take place changes, as a general rule, during the exchange.
  • the mixture is vaporized according to a temperature interval A by taking heat from an external fluid 1 which constitutes the heat source and the temperature of which changes according to a temperature interval A '. It is then relaxed by producing mechanical energy which can be used directly or transformed into electrical energy, then it is condensed according to a temperature interval B by yielding heat to an external fluid Il which constitutes the cooling fluid and whose the temperature changes according to a temperature interval B '.
  • the temperature intervals A and B must be as close as possible to the temperature intervals A 'and B', which corresponds to the best conditions of thermal reversibility.
  • the temperature interval A ' according to which the heat is supplied to the cycle being fixed, the composition of the mixture is chosen so as to obtain a vaporization interval A close to the temperature interval A'.
  • the temperature interval A In the case of a binary mixture, the temperature interval A generally changes as shown in the diagram shown in Figure 1.
  • the vaporization temperatures at the pressure considered are T l and T ll , the vaporization of the mixture begins at the bubble temperature of the liquid T LB and ends at the dew temperature of the vapor T VR .
  • the spraying interval is therefore equal to the difference between the temperatures T LB and T VR and can be adjusted by choosing the appropriate composition.
  • the condensation interval B is generally close to the vaporization interval A. In this case, it is advantageous to adjust the flow rate of the cooling fluid, water or air, used to carry out the condensation so that the interval of temperature B 'is close to the condensation interval B.
  • the mixture is then expanded in the vane motor M1 which drives the alternator AT1.
  • An electrical power of 9 kW is collected at the terminals of the alternator.
  • the mixture comes out of the M1 vane motor at a pressure of 1.6 bars. It is gradually condensed A in the exchanger E102 from where it is collected in the reserve tank B1. Cooling is ensured by water which enters through line 7 at 12 ° C and exits through line 8 at 32 ° C.
  • the liquid mixture is taken up, through line 6, by the pump P1 and recycled to the evaporator E101.
  • the use of a mixture of butane and hexane makes it possible, during the vaporization and condensation stages, to follow the temperature evolution of the external fluids, the mixture of fluids vaporizing according to an evolution increasing temperature parallel to the decreasing evolution of temperature of the external fluid 1 and condensing according to a decreasing evolution of temperature parallel to the increasing evolution of temperature of the external fluid II.
  • These changes in temperature necessitate operating the heat exchanges at the evaporator and at the condenser under conditions as close as possible to the counter-current.
  • a pure counter-current heat exchange mode represents the preferred solution, but for implementation reasons, it is also possible to mount exchange surfaces in a generally counter-current arrangement, each of the exchange surfaces forming part of said arrangement operating under conditions different from the counter current, for example following a heat exchange with cross currents or with a circulation of one of the fluids taking place in U-shaped tubes.
  • the mixtures (M) used can be mixtures of two, three (or more) constituents (separate chemical compounds).
  • the constituents of the mixture can be hydrocarbons, the molecule of which comprises a number of carbon atoms of for example between 3 and 8, such as propane, normal butane and isobutane, normal pentane and isopentane, normal hexane and isohexane, normal heptane and isoheptane, normal octane and isooctane as well as aromatic hydrocarbons such as benzene and toluene and cyclic hydrocarbons such as cyclopentane and cyclohexane.
  • the mixture used can be a mixture of halogenated hydrocarbons of the “Freon” type such as chlorodifluoromethane (R-22), dichlorodifluoromethane (R-12 ), chloropentafluoroethane (R-115), difluoroethane (R-152), trichlorofluoromethane (R-11), dichlorotetrafluoroethane (R-114), dichlorohexafluoropropane (R-216), dichlorofluoromethane (R-21), trichlorotrifluoroethane (R-113).
  • halogenated hydrocarbons of the “Freon” type such as chlorodifluoromethane (R-22), dichlorodifluoromethane (R-12 ), chloropentafluoroethane (R-115), difluoroethane (R-152), trichlorofluoromethane (R-11), dichlorotetrafluor
  • One of the constituents of the mixture can be an azeotrope such as the R-502 azeotrope of R-22 and R-115 (48.8 / 52.2% by weight), the R-500 azeotrope of R-12 and of R-31 (78.0 / 22.0% by weight), the azeotropic R-506 of R-31 and of R-114 (55.1 / 44.9% by weight).
  • an azeotrope such as the R-502 azeotrope of R-22 and R-115 (48.8 / 52.2% by weight), the R-500 azeotrope of R-12 and of R-31 (78.0 / 22.0% by weight), the azeotropic R-506 of R-31 and of R-114 (55.1 / 44.9% by weight).
  • mixtures comprising water and at least one second water-miscible constituent such as mixtures formed of water and ammonia, mixtures formed of water and an amine such as methylamine or ethylamine, mixtures formed of water and an alcohol such as methanol, mixtures formed of water and a ketone such as acetone.
  • the composition of the mixture is chosen so that the vaporization intervals A and condensation B are as close as possible to the temperature intervals A 'and B' according to which evolve external fluids.
  • the difference between the temperature intervals A and A ′ is less than 5 ° C.
  • the pump P11 makes it possible to send a fraction of the liquid mixture via the conduit 12 into the exchanger E103 in which it vaporizes according to a temperature interval A, by exchanging heat with an external fluid which enters through the conduit 13 and leaves by the conduit 14.
  • the mixture leaves vaporized from the exchanger E103 by the conduit 15 and it is sent to the engine stage M2.
  • the pump P10 sends the remaining fraction of the liquid mixture via the pipe 16 into the exchanger E104, in which it vaporizes according to a temperature interval A 2 by exchanging heat with the external fluid which arrives through the pipe 14 and exits through the conduit 17.
  • the mixture leaves vaporized from the exchanger E104 and the steam thus obtained is mixed with the steam coming from the expansion through the stage M2, then expanded at the same time as the steam coming from the stage M2 in the 'motor stage M3 from which it' emerges through conduit 19.
  • the intermediate pressure level is chosen correctly, that is to say the pressure at which the mixture vaporizes in the exchanger E104, the temperature intervals A and A 2 can be consecutive and it is thus possible to follow with the mixture a change in temperature parallel to a change in temperature of the external fluid which supplies heat to the cycle, corresponding to a temperature interval A 'approximately twice as wide as in the case of the operating diagram represented in the Figure 2.
  • the condensed mixture is only partially vaporized in the exchanger E106 by taking heat from the external fluid which arrives via line 20 and leaves via line 21.
  • the liquid and vapor fractions are separated in the separator flask S1.
  • the steam fraction is expanded in the T3 turbine.
  • the liquid phase is sent to the exchanger E107 in which it exchanges heat with the condensed mixture which is sent to the evaporator, then expanded through the expansion valve V1 and mixed with the expanded vapor phase leaving the turbine T3 .
  • the liquid vapor mixture thus obtained is condensed by yielding heat to an external cooling fluid, collected in the reserve tank B3 and recycled by the pump P3 to the evaporator.
  • the operating conditions of a device operating according to the arrangement shown diagrammatically in FIG. 4 are the subject of Example 2.
  • This mixture is sent through line 31 into the exchanger E107 from which it emerges through line 22 at a temperature of 55 ° C. It is then sent to the exchanger E106 in which it partially vaporizes by taking a thermal power of 1,585 kW from a flow of water which arrives via line 20 at a temperature of 90 ° C and exits through line 21 at a temperature of 65 ° C.
  • the liquid-vapor mixture leaves the exchanger E106 through line 23 at a temperature of 85 ° C. and at a pressure of 20 bars. It is collected in the separator tank S1 in which the liquid phase and the vapor phase are separated. The liquid phase contains 52% ammonia by weight. It is evacuated via line 25 and sent to the exchanger E107.
  • the vapor phase is sent via line 24 to the turbine T3 in which it is expanded to a pressure of 8 bars. On the shaft of the turbine T3, a power of 100 kW is collected by means of the electric brake FE1.
  • the expanded vapor is evacuated through the pipe 26.
  • the liquid phase which leaves through the pipe 27 of the exchanger E107 is expanded through the expansion valve V1, from where it comes out through the pipe 28. It is then mixed with the vapor phase arriving through line 26 and the liquid-vapor mixture is sent through line 29 into the air cooler AR1, in which it is fully condensed B and from which it leaves through line 30 at a temperature of 28 ° C.
  • the AR1 air condenser is made up of tubes provided with fins inside which the mixture circulates by condensing, these tubes being arranged in five layers placed transversely to the air circulation but mounted against the current , the mixture thus circulating generally against the current of the cooling air.
  • the condensed mixture is collected in the reserve tank B3 from where it is taken up by the feed pump P3.
  • the operating diagram shown in Figure 4, makes it possible to adapt to variable operating conditions.
  • the pressure levels in the evaporator and in the condenser are reduced, which makes it possible to reduce the capacity of the system, c is the power delivered on the shaft.
  • the operating conditions are generally chosen so that the pressure of the mixture in the evaporator is between 3 and 30 bars and so that the pressure of the mixture in the condenser is between 1 and 10 bars.
  • the temperatures constituting the temperature range A are all greater than 50 ° C and less than 350 ° C and the temperatures constituting the temperature range B are all greater than 20 ° C and less than 80 ° C.
  • the evaporator and the condenser can be, for example, tube and shell exchangers, double-tube exchangers or plate exchangers.
  • a fluid which is a gas for example if air is used as coolant for the condenser, it is generally advantageous to provide the exchange surfaces with fins placed on the side of the gas to improve heat exchange with this gas.
  • a machine can be for example a turbine with one wheel or with several wheels, radial or axial, a screw machine of the same type as the screw compressors but operating in expansion, a vane motor or a reciprocating piston engine.
  • the mechanical power delivered can be very variable and range, for example, from a few kW to several megawatts.
  • the mixture of fluids must not form an azeotrope under the conditions of vaporization. This means that at least two constituents of this mixture do not form an azeotrope between them; however, each of the constituents can individually be an azeotrope.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Claims (12)

1. Verfahren zur Gewinnung mechanischer Energie, wobei man
a) progressiv ein Flüssigkeitsgemisch (M), welches mindestens zwei Bestandteile enthält, die untereinander kein Azeotrop bilden, unter Verdampfungsbedingungen verdampft und die Verdampfungswärme mindestens teilweise einer Außenflüssigkeit I entnimmt,
b) die auf diese Weise erhaltene Dampfphase unter Gewinnung von mechanischer Energie entspannt,
c) den auf diese Weise erhaltenen Dampf progressiv kondensiert und die Wärme an mindestens eine Außenflüssigkeit II abgibt, und
d) die aus Stufe c) stammende flüssige Phase im Kreislauf in die Stufe a) zurückführt,

dadurch gekennzeichnet, daß der mit den Außenflüssigkeiten und 11 in den Stufen a) bzw. c) bewirkte Wärmeaustausch im Gegenstrom erfolgt, wobei das Flüssigkeitsgemisch (M) in Stufe a) nach einer Temperatursteigerung (A) verdampft, welche parallel zur Temperatursenkung (A') der Außenflüssigkeit I erfolgt, und die Kondensation in Stufe c) nach einer Temperatursenkung (B) parallel zur Temperatursteigerung (B') der Außenflüssigkeit II bewirkt wird, wobei die Größe des Temperaturintervalls (B) mindestens 7°C und höchstens 30 °C beträgt.
2. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, daß das Flüssigkeitsgemisch an einem Punkt des Kreislaufs in zwei Fraktionen aufgetrennt wird und die erhaltenen Fraktionen an einem anderen Punkt des Kreislaufs wieder, vermischt werden, wobei die erste der abgetrennten Fraktionen die gesamten Stufen a), b) und c) durchläuft, während die zweite dieser Fraktionen mindestens eine der von der ersten Fraktion durchlaufenen Stufen nicht durchläuft.
3. Verfahren gemäß Ansprüchen 1 und 2, dadurch gekennzeichnet, daß die Differenz zwischen der Temperatur des Gemischs, welches das Intervall A durchläuft, und der Temperatur der Flüssigkeit I, welche das Intervall A' durchläuft, in jedem Fall kleiner als 5 °C ist.
4. Verfahren gemäß Ansprüchen 1 bis 3, dadurch gekennzeichnet, daß das Gemisch (M) in mindestens zwei Stufen auf verschiedenem Druckniveau verdampft wird, wobei eine erste Fraktion des Gemischs auf dem höchsten Druckniveau verdampft wird, indem man die Wärme in einem ersten Temperaturintervall entnimmt, die erhaltene Dampfphase von oben in eine Kraftmaschine schickt, in welcher die Entspannung erfolgt, wobei diese Kraftmaschine eine Reihe von Stufen (M2, M3) enthält, die mindestens gleich der Anzahl der Verdampfungsstufen ist, die restliche Fraktion in mindestens einer Stufe verdampft wird, welche auf einem Druckniveau erfolgt, das niedriger als das Druckniveau der ersten Stufe ist, wobei man die Wärme einem Temperaturintervall entnimmt, das mindestens teilweise unterhalb des ersten Temperaturintervalls liegt, die auf diese Weise erhaltenen Dampffraktionen in aufeinanderfolgende Stufen (M3) der Kraftmaschine schickt, in welchen die Entspannung an, dem Druckniveau des Dampfes entsprechenden Punkten erfolgt, das nach der Entspannung erhaltene Dampfgemisch kondensiert und die nach der Kondensation erhaltene flüssige Phase im Kreislauf in die Verdampfungsstufen zurückleitet.
5. Verfahren gemäß Ansprüchen 1 bis 4, dadurch gekennzeichnet, daß das Gemisch (M) partiell in einem Verdampfer E 106 verdampft wird, wobei die Wärme einer Außenflüssigkeit entnommen wird, die auf diese Weise erhaltene Dampfphase von der flüssigen Phase trennt, die Dampfphase unter Gewinnung von mechanischer Energie entspannt, die flüssige Phase in einen Austauscher E 107 schickt, in welchem sie die Wärme mit der kondensierten Mischung (M) austauscht, welche in den Verdampfer geschickt wird, die flüssige Phase anschließend entspannt und mit der entspannten Dampfphase vermischt, das auf diese Weise erhaltene Gemisch Flüssig/Dampf kondensiert, wobei die Wärme an eine Außenflüssigkeit abgegeben wird, das auf diese Weise erhaltene kondensierte Gemisch (M) im Kreislauf in den Verdampfer zurückleitet.
6. Verfahren gemäß Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß das Gemisch ein Kohlenwasserstoff-Gemisch ist, dessen Kohlenstoffzahl 3-8 beträgt.
7. Verfahren gemäß Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß das Gemisch ein Gemisch aus halogenierten Kohlenwasserstoffen ist.
8. Verfahren gemäß Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß das Gemisch ein Gemisch aus Wasser und mindestens einem mit Wasser mischbaren Bestandteil ist, und zwar aus der Alkohole, Ketone und Amine.
9. Verfahren gemäß Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß das Gemisch ein Gemisch aus Wasser und Ammoniak ist.
10. Verfahren gemäß Ansprüchen 1 bis 9, dadurch gekennzeichnet, daß das Temperaturintervall A in einem Temperaturbereich von 50 bis 350 °C und das Temperaturintervall B im Temperaturbereich von 20 bis 80 °C liegt.
11. Verfahren gemäß Ansprüchen 1 bis 10, dadurch gekennzeichnet, daß der Druck des Gemischs im Verdampfer 3 bis 30 bar und der Druck des Gemischs im Kühler 1 bis 10 bar beträgt.
12. Verfahren gemäß Ansprüchen 1 bis 11, dadurch gekennzeichnet, daß die durch Entspannung des Dampfphasengemischs gewonnene mechanische Energie in elektrische Energie umgewandelt wird.
EP81400755A 1980-05-23 1981-05-12 Verfahren zur mechanischen Energieerzeugung aus Wärme mit Mehrstoffgemischen als Arbeitsmittel Expired EP0041005B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT81400755T ATE14778T1 (de) 1980-05-23 1981-05-12 Verfahren zur mechanischen energieerzeugung aus waerme mit mehrstoffgemischen als arbeitsmittel.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8011649A FR2483009A1 (fr) 1980-05-23 1980-05-23 Procede de production d'energie mecanique a partir de chaleur utilisant un melange de fluides comme agent de travail
FR8011649 1980-05-23

Publications (2)

Publication Number Publication Date
EP0041005A1 EP0041005A1 (de) 1981-12-02
EP0041005B1 true EP0041005B1 (de) 1985-08-07

Family

ID=9242336

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81400755A Expired EP0041005B1 (de) 1980-05-23 1981-05-12 Verfahren zur mechanischen Energieerzeugung aus Wärme mit Mehrstoffgemischen als Arbeitsmittel

Country Status (6)

Country Link
US (1) US4422297A (de)
EP (1) EP0041005B1 (de)
JP (1) JPS5728819A (de)
AT (1) ATE14778T1 (de)
DE (1) DE3171684D1 (de)
FR (1) FR2483009A1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010024487A1 (de) * 2010-06-21 2011-12-22 Andreas Wunderlich Verfahren und Vorrichtung zur Erzeugung mechanischer Energie in einem Kreisprozess

Families Citing this family (36)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2499149A1 (fr) * 1981-02-05 1982-08-06 Linde Ag Procede de transformation d'energie thermique en energie mecanique
US4442675A (en) * 1981-05-11 1984-04-17 Soma Kurtis Method for thermodynamic cycle
US4506524A (en) * 1983-08-15 1985-03-26 Schlichtig Ralph C Absorption type heat transfer system functioning as a temperature pressure potential amplifier
US4827877A (en) * 1987-01-13 1989-05-09 Hisaka Works, Limited Heat recovery system utilizing non-azeotropic medium
US4779424A (en) * 1987-01-13 1988-10-25 Hisaka Works, Limited Heat recovery system utilizing non-azeotropic medium
US4785876A (en) * 1987-01-13 1988-11-22 Hisaka Works, Limited Heat recovery system utilizing non-azetotropic medium
US5186013A (en) * 1989-02-10 1993-02-16 Thomas Durso Refrigerant power unit and method for refrigeration
JP2503150Y2 (ja) * 1990-05-10 1996-06-26 中部電力株式会社 非共沸混合流体サイクルプラントの蒸気凝縮装置
US5255519A (en) * 1992-08-14 1993-10-26 Millennium Technologies, Inc. Method and apparatus for increasing efficiency and productivity in a power generation cycle
DE19653256A1 (de) * 1996-12-20 1998-06-25 Asea Brown Boveri Kondensator für binäre/polynäre Kondensation
US5842345A (en) * 1997-09-29 1998-12-01 Air Products And Chemicals, Inc. Heat recovery and power generation from industrial process streams
CA2393386A1 (en) * 2002-07-22 2004-01-22 Douglas Wilbert Paul Smith Method of converting energy
US6751959B1 (en) * 2002-12-09 2004-06-22 Tennessee Valley Authority Simple and compact low-temperature power cycle
US6820422B1 (en) * 2003-04-15 2004-11-23 Johnathan W. Linney Method for improving power plant thermal efficiency
US7124587B1 (en) * 2003-04-15 2006-10-24 Johnathan W. Linney Heat exchange system
US7305829B2 (en) * 2003-05-09 2007-12-11 Recurrent Engineering, Llc Method and apparatus for acquiring heat from multiple heat sources
US8117844B2 (en) * 2004-05-07 2012-02-21 Recurrent Engineering, Llc Method and apparatus for acquiring heat from multiple heat sources
US7074343B2 (en) * 2004-05-26 2006-07-11 E. I. Du Pont De Nemours And Company 1,1,1,2,2,4,5,5,5-nonafluoro-4-(trifluoromethyl)-3-pentanone refrigerant compositions comprising a hydrocarbon and uses thereof
US20070144195A1 (en) * 2004-08-16 2007-06-28 Mahl George Iii Method and apparatus for combining a heat pump cycle with a power cycle
US20060112693A1 (en) * 2004-11-30 2006-06-01 Sundel Timothy N Method and apparatus for power generation using waste heat
US7665304B2 (en) * 2004-11-30 2010-02-23 Carrier Corporation Rankine cycle device having multiple turbo-generators
US7270794B2 (en) * 2005-03-30 2007-09-18 Shipley Larry W Process for recovering useful products and energy from siliceous plant matter
JP2006322692A (ja) * 2005-05-20 2006-11-30 Ebara Corp 蒸気発生器、及び排熱発電装置
WO2011103560A2 (en) * 2010-02-22 2011-08-25 University Of South Florida Method and system for generating power from low- and mid- temperature heat sources
US20120006024A1 (en) * 2010-07-09 2012-01-12 Energent Corporation Multi-component two-phase power cycle
RU2457338C2 (ru) * 2010-08-26 2012-07-27 Игорь Анатольевич Ревенко Способ преобразования тепловой энергии в механическую, способ увеличения энтальпии и коэффициента сжимаемости водяного пара
CN101922864A (zh) * 2010-09-26 2010-12-22 中冶赛迪工程技术股份有限公司 钢铁企业分布式纯低温煤气余热回收利用系统
SE535318C2 (sv) * 2010-12-01 2012-06-26 Scania Cv Ab Arrangemang och förfarande för att omvandla värmeenergi till mekanisk energi
CN103717699B (zh) * 2011-04-21 2016-10-12 埃姆泰克能量公司 用于兰金循环的工作流体
US20130174552A1 (en) * 2012-01-06 2013-07-11 United Technologies Corporation Non-azeotropic working fluid mixtures for rankine cycle systems
ITBS20120008A1 (it) * 2012-01-20 2013-07-21 Turboden Srl Metodo e turbina per espandere un fluido di lavoro organico in un ciclo rankine
DE102012108468A1 (de) * 2012-09-11 2014-03-13 Amovis Gmbh Arbeitsmittelgemisch für Dampfkraftanlagen
CN103374332A (zh) * 2013-07-04 2013-10-30 天津大学 含有环戊烷的有机朗肯循环混合工质
US10436075B2 (en) * 2015-01-05 2019-10-08 General Electric Company Multi-pressure organic Rankine cycle
US11618684B2 (en) 2018-09-05 2023-04-04 Kilt, Llc Method for controlling the properties of biogenic silica
GB2581770B (en) * 2019-01-14 2023-01-18 Gas Expansion Motors Ltd Engine

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3516248A (en) * 1968-07-02 1970-06-23 Monsanto Co Thermodynamic fluids
DE2215868A1 (de) * 1971-04-01 1972-10-26 Thermo Electron Corp Verfahren zum Betreiben einer vor zugsweise nach dem Clausius Rankine Pro zeß betriebenen Kraft Erzeuger Anlage
FR2337855A1 (fr) * 1976-01-07 1977-08-05 Inst Francais Du Petrole Procede de production de chaleur utilisant une pompe de chaleur fonctionnant avec un melange de fluides

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR670497A (fr) * 1928-06-19 1929-11-29 Installation thermique pour véhicules, machines volantes, bateaux et autres embarcations marines
GB551292A (en) * 1942-01-23 1943-02-16 Brian Furmstone Rice Stack A heat engine employing mixed vapours
US3511049A (en) * 1968-10-07 1970-05-12 American Air Filter Co Motive fluid composition
US4242870A (en) * 1974-08-29 1981-01-06 Searingen Judson S Power systems using heat from hot liquid
DE2852076A1 (de) * 1977-12-05 1979-06-07 Fiat Spa Anlage zur erzeugung mechanischer energie aus waermequellen unterschiedlicher temperatur
JPS54105652A (en) * 1978-02-07 1979-08-18 Daikin Ind Ltd Rankine cycle working fluid
JPS55146208A (en) * 1979-05-01 1980-11-14 Daikin Ind Ltd Power generating apparatus

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3516248A (en) * 1968-07-02 1970-06-23 Monsanto Co Thermodynamic fluids
DE2215868A1 (de) * 1971-04-01 1972-10-26 Thermo Electron Corp Verfahren zum Betreiben einer vor zugsweise nach dem Clausius Rankine Pro zeß betriebenen Kraft Erzeuger Anlage
FR2337855A1 (fr) * 1976-01-07 1977-08-05 Inst Francais Du Petrole Procede de production de chaleur utilisant une pompe de chaleur fonctionnant avec un melange de fluides

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Handbuch der Kältetechnik (herausg. v. R. Plank) 6. Band, Teil A, page 494 (Springer 1969) *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010024487A1 (de) * 2010-06-21 2011-12-22 Andreas Wunderlich Verfahren und Vorrichtung zur Erzeugung mechanischer Energie in einem Kreisprozess

Also Published As

Publication number Publication date
US4422297A (en) 1983-12-27
FR2483009B1 (de) 1982-07-23
FR2483009A1 (fr) 1981-11-27
DE3171684D1 (en) 1985-09-12
ATE14778T1 (de) 1985-08-15
JPS5728819A (en) 1982-02-16
EP0041005A1 (de) 1981-12-02

Similar Documents

Publication Publication Date Title
EP0041005B1 (de) Verfahren zur mechanischen Energieerzeugung aus Wärme mit Mehrstoffgemischen als Arbeitsmittel
EP0162746B1 (de) Absorptionsverfahren zur Kälte- und/oder Wärmeerzeugung mit einem aus mehreren Bestandteilen bestehenden Gemisch als Arbeitsmittel
AU2004263612B2 (en) Method and device for carrying out a thermodynamic cycle
US9388797B2 (en) Method and apparatus for producing power from geothermal fluid
EP0057120B1 (de) Verfahren zum Heizen eines Raumes mittels einer Kompressionswärmepumpe mit einem Gemisch als Arbeitsmedium
FR2818365A1 (fr) Procede de refrigeration d'un gaz liquefie, gaz obtenus par ce procede, et installation mettant en oeuvre celui-ci
FR2826969A1 (fr) Procede de liquefaction et de deazotation de gaz naturel, installation de mise en oeuvre, et gaz obtenus par cette separation
EP2764243B1 (de) Verfahren und system zur umwandlung von meereswärmeenergie
FR3074846A1 (fr) Procede de stockage et de production d'energie par air comprime avec recuperation d'energie supplementaire
US20120067049A1 (en) Systems and methods for power generation from multiple heat sources using customized working fluids
WO2021019146A1 (fr) Procédé de production d'énergie électrique utilisant plusieurs cycles de rankine combinés
WO2021019143A1 (fr) Procédé de récupération d'énergie frigorifique avec production d'électricité ou liquéfaction d'un courant gazeux
FR2583988A1 (fr) Procede de distillation avec recuperation d'energie par recompression de vapeur a l'aide d'un ejecteur
FR2575812A1 (fr) Procede de production de froid et/ou de chaleur mettant en oeuvre un melange non-azeotropique de fluides dans un cycle a ejecteur
EP3191693B1 (de) System zur stromerzeugung basierend auf einem rankine-prozess
EP3429717B1 (de) Verfahren für energiesparende chromatographische trennung
FR3090734A1 (fr) Système de cogénération d'énergie électrique et d'énergie thermique par un module de cycle de Rankine
WO2019073132A1 (fr) Procede et appareil de separation d'air par distillation cryogenique
US3702534A (en) Power fluids for rankine cycle engines
FR2496754A1 (fr) Procede pour recuperer de l'energie, conformement a un cycle de rankine en serie, par gazeification de gaz naturel liquefie et utilisation du potentiel de froid
FR2670570A1 (fr) Fluide de travail pour pompes a chaleur a absorption fonctionnant a tres hautes temperatures.
EP4004348A1 (de) Verfahren zur erzeugung von elektrischer energie unter verwendung mehrerer kombinierter rankine-zyklen
CA2278654A1 (fr) Systeme frigorifique a absorption et melange de travail pour ce systeme
FR2607581A1 (fr) Convertisseur de chaleur ambiante
WO2022117407A1 (fr) Système et procédé de stockage et de récupération d'énergie par gaz comprimé avec cycle de rankine

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): AT BE CH DE GB IT NL SE

17P Request for examination filed

Effective date: 19820507

ITF It: translation for a ep patent filed
GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): AT BE CH DE GB IT LI NL SE

REF Corresponds to:

Ref document number: 14778

Country of ref document: AT

Date of ref document: 19850815

Kind code of ref document: T

REF Corresponds to:

Ref document number: 3171684

Country of ref document: DE

Date of ref document: 19850912

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19890403

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 19890412

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19890430

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19890518

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19890531

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19890731

Year of fee payment: 9

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19900201

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19900512

Ref country code: AT

Effective date: 19900512

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19900513

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Effective date: 19900531

Ref country code: CH

Effective date: 19900531

Ref country code: BE

Effective date: 19900531

BERE Be: lapsed

Owner name: INSTITUT FRANCAIS DU PETROLE

Effective date: 19900531

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19901201

GBPC Gb: european patent ceased through non-payment of renewal fee
NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

EUG Se: european patent has lapsed

Ref document number: 81400755.5

Effective date: 19910115