EP0134431B1 - An den Ericsson- Prozess angenähertes thermodynamisches Verfahren - Google Patents

An den Ericsson- Prozess angenähertes thermodynamisches Verfahren Download PDF

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Publication number
EP0134431B1
EP0134431B1 EP84106748A EP84106748A EP0134431B1 EP 0134431 B1 EP0134431 B1 EP 0134431B1 EP 84106748 A EP84106748 A EP 84106748A EP 84106748 A EP84106748 A EP 84106748A EP 0134431 B1 EP0134431 B1 EP 0134431B1
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EP
European Patent Office
Prior art keywords
heat
mixture
substances
boiling point
substance
Prior art date
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EP84106748A
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German (de)
English (en)
French (fr)
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EP0134431A3 (en
EP0134431A2 (de
Inventor
Serafin Mendoza Rosado
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Individual
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Individual
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Publication of EP0134431A3 publication Critical patent/EP0134431A3/de
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02G—HOT GAS OR COMBUSTION-PRODUCT POSITIVE-DISPLACEMENT ENGINE PLANTS; USE OF WASTE HEAT OF COMBUSTION ENGINES; NOT OTHERWISE PROVIDED FOR
    • F02G2250/00—Special cycles or special engines
    • F02G2250/09—Carnot cycles in general

Definitions

  • the invention relates to a method for converting thermal energy into mechanical energy with the aim of improving its efficiency in approximation to the Ericsson cycle, in particular a method for producing mechanical work in a single cyclic process by means of a mixed process fluid consisting of a plurality of substances. which have different boiling points.
  • the En-Flex system uses a mixture of a low-boiling substance such as Freon and a high-boiling substance such as a eutectic mixture of 26.5% diphenyl and 73.5% diphenyl oxide (hereinafter referred to as D-A).
  • the former is used in the cycle as a process fluid, while the latter is used as a heat storage substance only in the liquid phase.
  • the type of mixture is similar to that of the proposed process, the duty cycle itself bears no resemblance to the process according to the invention because the D-A is never evaporated. Only the freon evaporates.
  • a process fluid which consists of a group of substances with different vapor pressures at given temperatures, so that the saturation pressure of the least volatile substance at the thermal level of the heat source is greater than the saturation pressure of the most volatile substance at the thermal level of the heat sink, but is sufficiently close to it.
  • the substances to be used as process fluid can be miscible or immiscible in the liquid state.
  • the fluids mentioned were chosen mainly because of their easy procurement, their low cost and the great experience in their use in heat transfer processes. Nevertheless, the fluid DA has a significant disadvantage, which is in its thermal stability range. Although this is relatively high (over 673 ° K according to the manufacturer's information) and enables easy regeneration, this also limits the highest value of the process heat to this temperature and thus also the absolute conversion efficiency (if the heat source delivers or enables higher temperatures). Of course, this disadvantage does not arise when using fluids with a higher thermal stability.
  • the distilled water as a more volatile process fluid, does not appear to meet the process conditions.
  • it is a composite with a smaller molecular mass and therefore also with a very large latent heat of the phase change under conditions which are within the working range of the critical temperature with respect to the mean specific heat of the liquefied fluids. And therefore it causes the slope of the heating isobars of said liquid phase to be very high. Practically - within the above-mentioned limits - this isobar is very close to the isoentropic curve in the context of the course of the process, because the other isobaric curves of the same have significantly smaller slopes.
  • FIG. 2 shows a T-s diagram of the reversible cycle course which the cyclical process according to the invention approximates with the mixture of water and D-A.
  • the shaded areas represent the loss of the reversible cycle compared to the ideal Ericsson cycle.
  • FIG. 1 shows a Ts diagram of the (theoretical) Ericsson process mentioned above in advance. Thereafter, during a first isothermal change of state at a high temperature level T 1, heat Q 1 is absorbed by the source and work W 1 is given. During the second opposite isothermal change of state at a low temperature level T2, heat Q2 is released to the sink and work W2 is taken up. During the completion of the isobaric state change with identical mean specific heat, the process fluid exchanges heat Q3 with itself by regenerating itself.
  • FIG. 2 shows the corresponding diagram of the two-stage method according to the invention. The isobars forming part of the diagram correspond to the mean specific conversion heat values. The areas shown in broken lines in FIG. 2 indicate the low losses in the method according to the invention compared to the ideal process.
  • FIG. 3 shows a process with two stages of expansion.
  • Figure 4 provides the various elements of a process four stages of expansion.
  • the preferred process fluid has the characteristics described in more detail above in order to achieve the desired high efficiency when used in the process according to the invention.
  • Figure 3 which relates to the process with two expansion stages, the heat is recovered by the heat exchangers CI, C-II and EI.
  • FIG. 4 shows a process with four expansion stages, in which the three stages of heat recovery are formed by the heat exchangers CI to C-III and EI to E-III.
  • the process variables are defined for the inlets and outlets of the corresponding elements shown in FIG. 3.
  • Example II the various process sizes at the inlets and outlets of the different elements are shown, which are shown in FIG.
  • the process variables illustrate that the process shows improved results in practical use, in the sense of a higher efficiency in relation to the efficiency of the theoretical process cycle.
  • the main aim of these examples is not to achieve the highest possible conversion of thermal into mechanical energy by the presented method, but rather to provide the proof that at two predetermined and - to make the absolute value of the converted energy worthwhile - sufficiently different temperature levels (in the example given, they are between 668 ° K and 298 ° K.
  • the practical application of this method makes it possible to approximate the theoretical efficiency of the Ericsson cycle between said thermal levels, with an efficiency that is far higher than that of any other real known method.
  • Liquid collection container (DL-I)
  • the pipe outlet steam from the heat exchanger E-III enters this turbine.
  • Water is usually used as the cooling fluid and circulates in the housing of the heat exchanger.
  • the liquid DA is supplied from this container DL-III.
  • the container DL-IV is provided with the appropriate vacuum unit to create and maintain the necessary process conditions.
  • the fluids chosen for the process example are selected according to the criteria already mentioned and are logically not optimal in order to achieve a good conversion efficiency under the given conditions.
  • the method calculated as an example has not been optimized in any way.
  • the pressure drops in the turbines were set quite arbitrarily and the minimum gradients in the heat exchangers could be optimized by approximation. So e.g. Under these conditions, the heat exchanger E-II could allow an additional water evaporation of about 1 kg / s.
  • the absolute efficiency can be increased, namely by using a fluid that is thermally stable even at higher temperatures, or by using the same fluids from the example after an optimization of the process and by the provision of higher temperature levels in the first process stage (Brayton or Rankine cycle).
  • the isentropic efficiency of the first 3 turbines would be very high, in the order of 90%.
  • the isentropic efficiency of the last turbine would be somewhat lower, on the order of 80%.
  • thermodynamic method allows a practical approximation of the conversion efficiency of the thermal energy contained between two specific and sufficiently separated temperature levels (heat source / heat discharge) to the conversion efficiency of a thermodynamic consisting of two isotherms (absorption and release) and two isobars Cycle that achieves the same efficiency as the Ericsson cycle.
  • thermodynamic consisting of two isotherms (absorption and release) and two isobars Cycle that achieves the same efficiency as the Ericsson cycle.

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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)
  • Breeding Of Plants And Reproduction By Means Of Culturing (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Steering Control In Accordance With Driving Conditions (AREA)
  • Diaphragms For Electromechanical Transducers (AREA)
  • Shaping Of Tube Ends By Bending Or Straightening (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Presses And Accessory Devices Thereof (AREA)
  • Adhesives Or Adhesive Processes (AREA)
  • Lubricants (AREA)
  • Power Steering Mechanism (AREA)
EP84106748A 1983-06-13 1984-06-13 An den Ericsson- Prozess angenähertes thermodynamisches Verfahren Expired - Lifetime EP0134431B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84106748T ATE68558T1 (de) 1983-06-13 1984-06-13 An den ericsson- prozess angenaehertes thermodynamisches verfahren.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ES523210 1983-06-13
ES523210A ES8605328A1 (es) 1983-06-13 1983-06-13 Un procedimiento de generacion de energia mecanica trabajando con una mezcla de fluidos de distintos puntos de ebullicion.

Publications (3)

Publication Number Publication Date
EP0134431A2 EP0134431A2 (de) 1985-03-20
EP0134431A3 EP0134431A3 (en) 1985-11-27
EP0134431B1 true EP0134431B1 (de) 1991-10-16

Family

ID=8485855

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84106748A Expired - Lifetime EP0134431B1 (de) 1983-06-13 1984-06-13 An den Ericsson- Prozess angenähertes thermodynamisches Verfahren

Country Status (8)

Country Link
US (1) US4691523A (ja)
EP (1) EP0134431B1 (ja)
JP (1) JPS6062608A (ja)
AT (1) ATE68558T1 (ja)
CA (1) CA1241845A (ja)
DE (1) DE3485169D1 (ja)
ES (1) ES8605328A1 (ja)
IL (1) IL72045A (ja)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4876855A (en) * 1986-01-08 1989-10-31 Ormat Turbines (1965) Ltd. Working fluid for rankine cycle power plant
JP2801477B2 (ja) * 1992-09-22 1998-09-21 キヤノン株式会社 画像信号処理装置
JPH0794815B2 (ja) * 1993-09-22 1995-10-11 佐賀大学長 温度差発電装置
EP1433450A1 (en) * 2002-12-23 2004-06-30 The Procter & Gamble Company Polymeric compositions for moisture vapour permeable structures with improved structural stability and structures comprising said compositions
US8459031B2 (en) * 2009-09-18 2013-06-11 Kalex, Llc Direct contact heat exchanger and methods for making and using same
FR3022296B1 (fr) * 2014-06-16 2016-07-01 Arkema France Systeme de controle d'un cycle de rankine

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3006146A (en) * 1958-09-19 1961-10-31 Franklin Institute Closed-cycle power plant
DE1551260A1 (de) * 1966-11-02 1970-03-19 Siemens Ag Verfahren zur Carnotisierung von Kreisprozessen fuer Dampfkraftanlagen und Anordnung zur Durchfuehrung des Verfahrens
CA945383A (en) * 1971-04-01 1974-04-16 Dean T. Morgan Working fluid for rankine cycle system
US3774393A (en) * 1971-08-17 1973-11-27 Du Pont Method of generating power
US4439988A (en) * 1980-11-06 1984-04-03 University Of Dayton Rankine cycle ejector augmented turbine engine
FR2499149A1 (fr) * 1981-02-05 1982-08-06 Linde Ag Procede de transformation d'energie thermique en energie mecanique

Also Published As

Publication number Publication date
ES8605328A1 (es) 1986-04-01
EP0134431A3 (en) 1985-11-27
IL72045A0 (en) 1984-10-31
CA1241845A (en) 1988-09-13
EP0134431A2 (de) 1985-03-20
JPS6062608A (ja) 1985-04-10
ATE68558T1 (de) 1991-11-15
ES523210A0 (es) 1986-04-01
DE3485169D1 (de) 1991-11-21
US4691523A (en) 1987-09-08
IL72045A (en) 1993-01-14

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