EP0041005B1 - Procédé de production d'énergie mécanique à partir de chaleur utilisant un mélange de fluides comme agent de travail - Google Patents

Procédé de production d'énergie mécanique à partir de chaleur utilisant un mélange de fluides comme agent de travail Download PDF

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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
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German (de)
English (en)
French (fr)
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EP0041005A1 (fr
Inventor
Alexandre Rojey
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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 AT81400755T priority Critical patent/ATE14778T1/de
Publication of EP0041005A1 publication Critical patent/EP0041005A1/fr
Application granted granted Critical
Publication of EP0041005B1 publication Critical patent/EP0041005B1/fr
Expired legal-status Critical Current

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    • 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.

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  • 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)
EP81400755A 1980-05-23 1981-05-12 Procédé de production d'énergie mécanique à partir de chaleur utilisant un mélange de fluides comme agent de travail Expired EP0041005B1 (fr)

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 (fr) 1981-12-02
EP0041005B1 true EP0041005B1 (fr) 1985-08-07

Family

ID=9242336

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81400755A Expired EP0041005B1 (fr) 1980-05-23 1981-05-12 Procédé de production d'énergie mécanique à partir de chaleur utilisant un mélange de fluides comme agent de travail

Country Status (6)

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

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

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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
US4785876A (en) * 1987-01-13 1988-11-22 Hisaka Works, Limited Heat recovery system utilizing non-azetotropic medium
US4779424A (en) * 1987-01-13 1988-10-25 Hisaka Works, Limited Heat recovery system utilizing non-azeotropic 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
RU2397334C2 (ru) * 2008-11-17 2010-08-20 Игорь Анатольевич Ревенко Способ преобразования тепловой энергии в механическую, способ увеличения энтальпии и коэффициента сжимаемости водяного пара
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
US20140305125A1 (en) * 2011-04-21 2014-10-16 Emmaljunga Barnvagnsfabrik Ab Working fluid for rankine cycle
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
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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

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

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