WO2006105815A1 - Procede de transformation d'energie calorifique en energie mecanique avec un rendement eleve - Google Patents

Procede de transformation d'energie calorifique en energie mecanique avec un rendement eleve Download PDF

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Publication number
WO2006105815A1
WO2006105815A1 PCT/EP2005/051574 EP2005051574W WO2006105815A1 WO 2006105815 A1 WO2006105815 A1 WO 2006105815A1 EP 2005051574 W EP2005051574 W EP 2005051574W WO 2006105815 A1 WO2006105815 A1 WO 2006105815A1
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Prior art keywords
component
energy
mixture
heat
evaporator
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PCT/EP2005/051574
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German (de)
English (en)
Inventor
Erwin Oser
Michael Rannow
Original Assignee
Erwin Oser
Michael Rannow
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 Erwin Oser, Michael Rannow filed Critical Erwin Oser
Priority to PCT/EP2005/051574 priority Critical patent/WO2006105815A1/fr
Priority to EP05733484A priority patent/EP1866522A1/fr
Publication of WO2006105815A1 publication Critical patent/WO2006105815A1/fr

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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
    • 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
    • F01K25/065—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 with an absorption fluid remaining at least partly in the liquid state, e.g. water for ammonia
    • 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
    • F01K25/08—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 special vapours

Definitions

  • the invention relates to a process for the conversion of thermal energy into mechanical energy with high efficiency, in which in a vaporizer a first component (s) is vaporized together with a second component (s) which are expanded in an expansion device, thermal energy being at least partially converted into mechanical energy is converted. Furthermore, the invention relates to a system for converting heat energy into mechanical energy. From the prior art, a variety of devices and methods for recovering mechanical energy are known. There are, for example, thermal power plants are known in which in a boiler, a working fluid, eg steam at a high pressure isobarically heated to the boiling point, evaporated and then i ⁇ a superheater is still overheated.
  • a working fluid eg steam at a high pressure isobarically heated to the boiling point
  • the steam is then adiabatically expanded in a turbine while performing work and liquefied in a condenser with heat release.
  • the liquid is pressurized by a feed water pump and returned to the boiler.
  • a disadvantageous feature of the known relaxation processes for the conversion of heat energy into mechanical energy is that the condensation heat arising from the condensation of the working fluid is obtained as waste heat due to the process, whereby the efficiency is adversely affected.
  • Cogeneration plants are usually operated according to the priority of the useful energy in so-called “current-controlled” or “heat-managed” mode of operation.
  • these modes of operation are compromises: if the focus is on heat, then electricity generation depends on the actual heat consumption, and if electricity generation is in the foreground, the associated heat of condensation must be removed, regardless of whether it is actually needed in thermal engineering processes or whether, as in the case of the large power stations for power generation, it must be run off as waste heat.
  • the invention has for its object to provide a method and apparatus for converting heat energy into mechanical energy with high efficiency available, and to avoid at least one of the aforementioned disadvantages.
  • a method for the conversion of thermal energy into mechanical, electrical and / or thermal energy with high efficiency by relaxation of a gaseous mixture in an expansion device (4) connected to an evaporator (3) is provided, according to
  • a separating device (2) At least a first component of a mixture with the supply of heat energy from an energy source (1) expelled and into a Evaporator (3) is transferred, wherein the mixture comprises at least a first component and at least one expulsion means, wherein the expulsion means is fed separately to an expeller scrubber (6),
  • the mixture formed from the expelled first component (s) and the second component (s) is fed and vented as vapor in the form of a compressed gas to at least one low-pressure expansion device (4), the energy released during the expansion being partially converted into mechanical, electrical and / or thermal energy is convertible,
  • the relaxed mixture is supplied to at least one Austrreibericascher (6), wherein the Austreibungssch is added to the mixture, wherein the first component and the Austreibungsstoff form a mixture with the release of heat energy, while at least a first component of the mixture energy is removed and the second component / n thereby undergoes a temperature increase and separated from the mixture,
  • mixture means a composition comprising at least one first component and at least one second component, hereinafter referred to as the working agent.
  • the working medium is preferably present as an azeotropic mixture or as a mixture with a boiling point reduction, based on the boiling point of the component with the highest boiling point, wherein working materials in the form of mixtures are preferred which have a boiling point reduction of at least 5 ° C, preferably of at least 10 ° C. , more preferably at least 15 ° C, even more preferably at least 20 ° C, and most preferably of at least 25 ° C, based on the boiling point of the component with the highest boiling point.
  • Azeotropic mixtures which can be suitably used according to the invention can be selected from the group comprising pyridine / water, water / ethanol, water / ethyl acetate, water / dioxane, water / carbon tetrachloride, water / benzene, water / toluene, ethanol / ethyl acetate, ethanol / Benzene, ethanol / chloroform, ethanol / carbon tetrachloride, ethyl acetate / carbon tetrachloride, methanol / carbon tetrachloride, methanol / benzene, chloroform / acetone, toluene / acetic acid, acetone-carbon disulfide and / or water / silicone.
  • Equally suitable azeotrope mixtures useful in this invention may also be multicomponent systems, i. these azeotrope mixtures comprise at least three components, or at least four components.
  • all the azeotrope mixtures known in the literature, to which reference is made in this context in the full list, can be used as far as they are suitable according to the invention.
  • the first component (s) can be selected from the group comprising water, alcohol, acid, ketone, aldehyde and / or silicone, wherein the mixture comprising first and second components is particularly preferably an aqueous silicone solution.
  • the use of water as at least a first component is advantageous because the heat of condensation of water, i. from gas to liquid is particularly high.
  • the heat energy released in this case can be used advantageously for heating the second component (s).
  • one component preferably the second component, has a low volume-specific or low molar enthalpy of vaporization. This ensures that a large amount of motive steam is generated with a given amount of heat energy.
  • at least one component of the working medium, preferably the second component may preferably have a boiling point in the range from 20 ° C to 250 ° C, preferably from 40 ° C to 200 ° C, preferably from 60 ° to 150 ° C, more preferably from 80 ° C - 120 ° C, and most preferably from 90 ° C to 100 ° C.
  • At least one component of the working medium may preferably have a molar heat of vaporization in the range of 5 KJ / mol-15 KJ / mol, preferably 6 KJ / mol-14 KJ / mol, preferably 7 KJ / mol-13 KJ / mol, more preferably 8 KJ / mol - 12 KJ / mol, and most preferably 9 KJ / mol - 10 KJ / mol.
  • At least one component of the working medium may according to the invention preferably have a low specific heat capacity [cp] of ⁇ 1.2 J / g, preferably of 0.4 J / g-1 J / g, preferably of 0.5 J / g - 0.9 J / g, and most preferably from 0.6 J / g - 0.8 J / g.
  • the working fluid is a solvent mixture comprising organic and / or inorganic solvent components.
  • solvent mixtures include mixtures of water and silicones.
  • Silicones and / or derivatives thereof which can preferably be used according to the invention have a boiling point in the range from 20 ° C.-250 ° C., preferably from 40 ° C. to 200 ° C., preferably from 60 ° C. to 150 ° C., more preferably from 80 ° C. 120 ° C and most preferably from 90 ° C to 100 ° C.
  • Silicones and / or derivatives thereof which can preferably be used according to the invention can have a molar heat of vaporization in the range from 5 KJ / mol - 15 KJ / mol, preferably from 6 KJ / mol - 14 KJ / mol, preferably 7 KJ / mol - 13 KJ / mol, more preferably 8 KJ / mol - 12 KJ / mol, and most preferably 9 KJ / mol - 10 KJ / mol.
  • Silicones and / or derivatives thereof which may preferably be used according to the invention may have a low specific heat capacity [cp] of ⁇ 1.2 J / g, preferably of 0.4 J / g-1 J / g, preferably of 0.5 J / g-0 , 9 J / g, and most preferably from 0.6 J / g - 0.8 J / g.
  • the working fluid may comprise a mixture of water and at least one or more SiI / kon.
  • At least one component preferably the first component, can be a protic solvent.
  • mixture means a composition comprising at least a first component and at least one expulsion agent.
  • Propellants which can be suitably used according to the invention can be selected from the group comprising zeolites, silicates, inorganic acids, in particular phosphoric acid, halogen acids, sulfuric acid, silicic acid, organic acids, inorganic salts and / or organic salts.
  • the expulsion means have a significantly higher evaporation point than the first component (s) and second component (s).
  • the evaporation point of the expelling agent is chosen so high that in the thermal separation of the mixture only the first component is evaporated and the expulsion means, also referred to as absorbent and / or adsorbent, remains in the separator.
  • the absorbent is an alkaline silicate solution, wherein the absorbed in the alkaline silicate solution water of the first component is desorbed, for example by heating.
  • Suitable salts are alkali metal and / or alkaline earth metal salts, in particular their halogen salts, such as Li Br, LiGI, MgCl 2 and the like.
  • absorbent and / or adsorbent all substances are suitable in principle, the r a solvent of the A beitsffens absorb and / or adsorb. However, those absorbents and / or adsorbents which release the absorbed and / or adsorbed first component (s) with a low expenditure of energy are preferred.
  • the absorbent / adsorbent can easily be separated from the second component (s) after receiving a first component (s).
  • the absorbent / adsorbent for receiving at least a first component (s) of the working fluid may advantageously be chosen such that the overall efficiency of the inventive system for converting heat energy from fluids into mechanical, electrical and / or thermal energy is determined over 24 hours including that for separation the first component (s) of the absorbent / adsorbent is preferably still> 40%.
  • the mixture is separated into first component and expulsion means.
  • the expelling agent is preferably a substance which absorbs or binds, for example absorbed and / or adsorbed, the first component (s) in the sense of a dilution effect.
  • the expelling agent is therefore a salt or a saline solution.
  • the expelling agent is a gel or a solid.
  • Heat energy that separates the desorbable first component from the expelling agent in the separator may be provided in any form, such as fossil, bioenergy or solar energy. However, it can also be provided from other sources of energy with good efficiency, such as from the group comprising heat pump / s, fuel cell (s) or in the form of waste heat, depending on the temperature level either directly or after transformation with the help of one or more heat pump (s) the temperature required for the desorption is brought.
  • the energy source (s) for generating the amount of heat needed to separate the batch may be and / or at least an exhaust heat source, a waste heat source of combustion processes, a geothermal source, a solar collector, a heat pump, a fuel cell, a waste heat source of cooling processes, an internal combustion engine, a combined heat and power plant partially generated by means of the low-pressure expansion device.
  • the mixture in the separator which is designed as a thermal expeller system, is separated into first component and expulsion means. It is advantageous if the expulsion agent is separated off in liquid form by evaporating the first component (s) from the mixture.
  • the mixture is exposed to an overpressure, preferably of about 1 bar atmospheric pressure. It is preferred that the mixture of first component (s) and expelling agent is present in the separator in free-flowing and preferably in liquid form.
  • the thermally separated or desorbed in the separator first component (s) of the batch is transferred to an evaporator with overpressure, for example 1 bar overpressure, referred to as gas or as steam.
  • a second component (s) may be added to the first component (s) as described above.
  • This formed from the first component / n and second component / n pressurized flowable and preferably liquid mixture, also referred to as working fluid is evaporated and the steam at an overpressure, for example, 1 bar, and elevated temperature, a low-pressure relaxation device supplied by means of which the working fluid is expanded, for example to atmospheric pressure, and cooled.
  • In the evaporator may be a liquid and vapor phase of the first and second components.
  • the low-pressure expansion device may particularly preferably be a Roots blower or an oval wheel pump. It may also be preferred if the low-pressure expansion device is designed with at least one injection opening, through which an absorbent or a protic solvent can be introduced into the expansion device.
  • the low-pressure expansion device can be connected to a generator.
  • the expanded gaseous working fluid is then fed to an expeller scrubber.
  • an expelling agent is added to the working fluid mixture.
  • the first component (s) is at least partly wise, preferably completely, absorbed.
  • the absorption energy released in this case can be used to separate the second component (s) from the first component.
  • at least a portion of the required energy preferably all of the energy required to raise the temperature and separate the second component (s) from the batch, is obtained by absorption and / or adsorption energy of the first component in the presence of the expelling agent.
  • the remaining after the Austrreiber scrubber second component, which according to the invention after relaxation has absorbed heat due to the absorption of the first component, and was thereby heated to a temperature above the boiling temperature of the mixture is passed into a heat exchanger and condensed.
  • the heat exchanger is preferably an evaporator in which the first and second components are evaporated as working fluid, but may also be a heat exchanger in which heat energy is transferred to a heat-consuming process before the cooled second component is passed into the evaporator.
  • the heat energy withdrawn from the process by such a prior heat transfer is returned to it by a larger heat input into the expeller system.
  • a return flow with valve between evaporator and expeller system ensures that the composition of the mixture is stabilized at the desired azeotropic mixing ratio.
  • Excess thermal energy may also be supplied to a generator, the evaporator and / or the separator.
  • the heat energy contained in the temperature-increased second component (s) can be at least partially removed by means of a heat exchanger and / or used for evaporation of additional second component (s) in the evaporator, wherein the heat exchanger is optionally connected to a coupling device.
  • the coupling device may be a heating network and / or another heat consumer.
  • a part of the first component (s) can also be condensed in a heat exchanger, which is preferably integrated in the evaporator, wherein the condensation energy released in this case can be used at least partially for the evaporation of the working medium, for example in the evaporator.
  • the first gaseous or vaporous component (s) attaches to the expelling agent releasing absorption energy.
  • the expelling agent is a salt solution
  • a so-called dilution effect occurs in which the salt solution absorbs and / or adsorbs the first component (s).
  • the first component (s) is contacted with the expulsion means, the first component at least partially changing its aggregate state from gaseous to liquid and / or the first component being condensed, absorbed and / or adsorbed by the expulsion means, whereby heat energy is released.
  • the released absorption energy enables thermal separation of the second component from the first component in the expeller scrubber. This is energetically particularly advantageous because the aggregation change from gaseous to liquid, especially in water releases a lot of heat energy that can be transferred to the second component (s).
  • the condensed first component (s) forms a mixture with the expulsion means which is supplied to the separation device.
  • the expelling agent comprises at least one ionic compound, preferably at least one salt solution, more preferably at least one silicate solution, and most preferably at least one alkaline silicate solution.
  • the mixture can be fed by means of at least one pump from Australer scrubber via at least one recuperator, for heat exchange between flow of the second component / s and return of the batch, the separator and expelling means are conveyed from the separator back to the absorption device.
  • the return circuit of the second component (s) is isolated from the recirculation loop of the expulsion medium.
  • the ratio between generated mechanical or electrical energy and accumulated heat loss, determined by the method during conventional thermal expansion processes, is canceled according to the invention by omitting the condensation of the working medium after the expansion.
  • the pressure reduction required for the relaxation is not realized by condensation of the entire motive steam, but by absorption of a portion of the motive steam.
  • the required volume reduction is not realized by cooling, but by a decrease in the number of particles in the motive steam.
  • As a particularly elegant feature of the solution according to the invention is to be considered that by appropriate selection of an azeotropic mixture with boiling point minimum as a working medium by the absorption of the first component, the released absorption energy is transferred to the remaining vaporous second component. As a result, it is heated beyond the evaporation temperature of the mixture in spite of the relaxation.
  • the invention can further be provided that with the heat energy, if necessary after a transformation to a higher temperature level by means of one or more heat pumps arranged one behind the other, desorbs the absorbed first component of a working fluid in an expelling unit and with the increased Desorpti- onstemperatur vapor in the evaporator vaporized and working fluid evaporates, that the relaxation takes place in a low-pressure expansion device and the energy contained in the relaxed vaporized working medium with the absorption energy transmitted during the absorption of the first component, vapor remaining second component either in the evaporator is traceable and usable for the evaporation of additional working fluid is, or can be used in an intermediate heat exchanger at the elevated temperature level for heat-consuming processes.
  • An essential feature of the method according to the invention is the relaxation of the working fluid in a low-pressure expansion device, wherein the energy contained in the relaxed vaporous working fluid is traceable to the evaporator and for the purpose of evaporation additional working fluid is available.
  • the working fluid to be relaxed is formed by a mixture, and the method preferably comprises at least a first component of the working fluid, which is absorbed in and / or after the low-pressure expansion device by means of an absorbent and / or adsorbed by means of an adsorbent, wherein heat energy the remaining, vaporous second component / s passes, which is traceable.
  • the mixture of working fluids at a certain mixing ratio of the components is a boiling point azeotrope.
  • the evaporation temperatures can be lowered, depending on the type, so that they are below the condensation temperatures of the individual components. If the first component is adiabatically absorbed from the vapor mixture, the corresponding heat is transferred to the second component remaining in vapor form. The removal of the heat of condensation can be done at an elevated temperature level.
  • the second vaporous component in the evaporator of the working fluid itself are condensed under release of the heat of condensation, so that the corresponding proportion of the heat energy can be returned to the process.
  • the working medium for the low-pressure relaxation for example an azeotropic mixture of water and perchlorethylene
  • the absorption in which according to the invention the resulting heat of absorption is transferred to the second component remaining in vapor form, whereby this component is heated to a temperature level above the boiling temperature of the azeotropic mixture, can take place in and / or after the expansion device.
  • the relaxation of the azeotropic mixture heat energy can be converted into mechanical energy and with the help of a generator into electrical energy and at the same time the relaxed work equipment, the process in the relaxation process has already done "work" by the separation (
  • the remaining working medium can be returned after the expansion, for example in order to release its heat in a heat exchanger
  • the remaining working medium Only second component
  • a heat exchanger evaporator
  • the efficiency of the process for converting thermal energy into mechanical and / or electrical energy can be substantially improved. Furthermore, the vaporous second component in a heat exchanger can transfer heat to a heat consuming process before returning to the evaporator.
  • the working medium for the low pressure relaxation is preferably formed by an azeotropic mixture with boiling point minimum or nearly azeotropic mixture.
  • an azeotropic mixture with boiling point minimum or nearly azeotropic mixture.
  • the invention is described with an azeotropic mixture, of course, the invention can also be based on almost azeotropic mixtures or non-azeotropic mixtures. High efficiencies can be achieved especially with an azeotropic or an almost azeotropic mixture.
  • an azeotropic mixture depending on the type of their evaporation temperatures can be lowered so that they are below the evaporation temperatures of the individual components.
  • the absorbent is a reversibly immobilizable solvent which in the non-immobilized state of matter is the first component of the working fluid.
  • the reversible solvent in the boiling agent may advantageously be altered by physico-chemical changes in which it can be changed from the non-immobilized state to the reversibly immobilized state by ionization or complexation from the vapor phase and in the non-immobilized form as an absorbent works for the work equipment.
  • the vaporous working fluid before the relaxation already contains the absorbent (in the non-immobilized state).
  • the reversibly immobilized solvent is in a vaporous state and undergoes physico-chemical changes - such as pH shift, change in mole fraction and temperature in its volatility and / or in its vapor pressure - to the liquid state (comparable to steam as Solvent in non-immobilized form and water as reversibly immobilisable solvent).
  • physico-chemical changes such as pH shift, change in mole fraction and temperature in its volatility and / or in its vapor pressure - to the liquid state (comparable to steam as Solvent in non-immobilized form and water as reversibly immobilisable solvent).
  • the advantage here is that the working fluid consists of two components, wherein at the same time the one component in the reversible immobilized state acts as an absorbent for the other component.
  • pH-dependent reversible immobilizable solvents for example, cyclic nitrogen compounds - such as pyridines - can be used.
  • the absorption of the first component can already take place, for example, in the low-pressure expansion device.
  • an expeller scrubber also referred to in the present description as an absorption device, for example, is designed as a scrubber, the low pressure relaxation Vor- direction downstream.
  • the ionization of the reversibly immobilizable solvent can be carried out in the absorption device by electrolysis or by addition of electrolytes, whereby the solvent is formed in its immobilized form as an absorbent from the working fluid.
  • the vapors of the working medium flowing through the absorbent are also ionized, so that the vapor pressure is lowered so that the vapor of the reversible immobilisable component is deposited in the working medium.
  • the azeotropic working fluid is thus passed through the absorbent, which absorbs (absorbs) the first component, with the released absorption energy being transferred to the remaining vaporous second component.
  • the absorbent can then be passed back into the evaporator, where it is converted, for example by deionization in a non-ionic state and is re-evaporated with the condensed phase of the remaining second component as an azeotrope.
  • the molar ratio of the working fluid is selected such that the pressure in the expansion decreases by reducing the number of remaining in the gas phase molecules more than the pressure increases by the heating of the remaining gas, so that the structure of an otherwise resulting back pressure after the expansion device is avoided.
  • a device may be used in which neither the mass of the steam nor the pressure ratio, but only the pressure difference is relevant.
  • the low pressure expansion device is designed as a Roots blower - as Roots blower - or in the form of oval wheel pumps. It is advantageous that the Roots blower can work as a relaxation devices (relaxation motors) with a pressure difference of 500 mbar with full efficiency and can be used in a closed system at pressures of 10 to 0.5 bar.
  • the Roots blower can be designed with at least one injection opening, through which the absorbent and / or a protic solvent can be introduced into the Roots blower.
  • a pressure-controlled injection takes place to prevent liquid damage. Another advantage is that in the said expansion devices only the pressure difference and not the mass or the expansion ratio is decisive for the efficiency.
  • the Roots blower on a gas-tight seal between the pumping chamber and the gear compartment, wherein in another embodiment, the Roots blower comprises multi-bladed rotors.
  • the Roots blower further comprises a shaft which can be connected to the generator, whereby the mechanical can be converted into electrical energy.
  • a Wälzkolbenmotor as Niederbuchenthovsvortechnisch - especially when using waste heat with a temperature of less than about 100 ° C for driving, for example, pumps or generators - opens up the possibility, on the one hand to support the process by injection of absorbents, and other because of the low pressure and temperature differences, the remaining energy in the relaxed vaporous working fluid, as described above, to transform back to an elevated temperature level and thus to make traceable.
  • the Roots blower relaxes a pressurized working fluid and not compressed.
  • Another object of the invention relates to a system for the conversion of heat energy into mechanical, electrical and / or thermal energy.
  • a plant for the conversion of thermal energy into mechanical, electrical and / or thermal energy which comprises the following components: a) an evaporator unit (3) in which a mixture formed from first component (s) and second component (s) is obtained , b) a low-pressure expansion device (4), which is optionally connected to a generator (5), wherein the low-pressure expansion device (4) of the evaporator unit (3) is connected downstream, c) an expeller scrubber (6) the expeller scrubber (6) is preferably integrated into the low-pressure expansion device (4) and / or is connected downstream of the low-pressure expansion device (4), d) a separation device (2) which is designed as a thermal expulsion system, in which the first component / n is separated from the expulsion means, e) at least one additional energy source (1), which forms the Ausreibersystem as separating device (2) istenergi e for the purpose of separating the first component (s) from the expulsion means (s).
  • the heat energy for desorption or separation of the absorbed first component (s) in the separation device can be provided by any energy source.
  • a suitable energy source (s) (1) according to the invention may be at least one exhaust heat source, a waste heat source of combustion processes, a geothermal source, a solar collector, a heat pump, a fuel cell, a waste heat source of cooling processes, an internal combustion engine and / or a combined heat and power plant.
  • the heat energy must be provided at one or two different temperature level / s on the one hand above the set in the evaporator evaporation temperature of the azeotropic working medium mixture and on the other hand above for the desorption or separation of the absorbed first component / s in the expeller or for the release in the case of another physico-chemical process for the separation of the first component.
  • the heat energy from the combustion of fossil or biogenic energy carriers, solar heat, fuel cell (s) as well as waste heat from upstream thermal processes can, if necessary, be obtained by appropriate transformation of the temperature level with the aid of one or more heat pumps.
  • the heat energy can also be incurred by accumulating heat at incinerators or from the heat loss from the condensation in conventional thermal expansion processes to generate electricity.
  • the conventional methods of generating electricity by relaxing high-tension water vapor and requiring the condensation of water vapor after the turbine involve large amounts of waste heat that must be traversed as heat losses in cooling towers.
  • the fiction, contemporary method offers the possibility to convert at least partially this heat energy into mechanical energy. Prerequisite is the transformation with the help of one or more heat pumps to a sufficiently high temperature level.
  • the exceeding of the evaporation temperature of the azeotropic working medium mixture in the evaporator is sufficient in connection with energy production plants, since the required, generally higher desorption temperature in the generator can preferably be applied from heat energy which can be taken directly from the primary combustion.
  • Particularly suitable is the proposed method for converting the waste heat generated at known motor-driven block heating power plants (CHP).
  • CHP motor-driven block heating power plants
  • the established converted primary energy into useful energy in the following relations: about 36% mechanical energy, 34% engine waste heat in the cooling water circuit, 26% exhaust gas, 4% radiation losses.
  • the inventive method can be used in this ratio particularly advantageous for the conversion of CHP waste heat, since the waste heat is obtained at two different temperature levels, the engine heat in the cooling water circuit at about 90 ° to 100 0 C, exhaust gas to about 400 0 C. This can These waste heat can be used essentially without further transformation of the temperature level.
  • the exhaust heat is advantageously fed directly into the expeller, the engine waste heat in support of evaporation in the evaporator.
  • the heat generated in the CHP waste heat can also be transformed by heat exchange processes to temperature levels, so that the resulting heat energy can be used as much as possible in the system according to the invention.
  • Another advantage is that, in a conventional manner, part of the waste heat produced can also be used for heat-consuming processes.
  • the energy source (s) may be a heat pump (s), a fuel cell and / or solar system (s). Preference is given to the use of at least one heat pump in view of the advantageous energy balance.
  • Heat pumps can be used advantageously at low ambient temperatures. Solar systems require a sufficiently high solar radiation, so that in colder regions often the use of heat pumps may be preferred. Fuel cells can also be used due to their high efficiency.
  • the system according to the invention may comprise at least one pump, by means of which the mixture comprising first component (s) and expulsion means from the expeller scrubber to the separation device, optionally via a recuperator, after heat exchange between flow of the second component (s) and return of the batch, to the separation device and expulsion means from the separation device back to the absorption device.
  • the absorption device may preferably be embodied as a scrubber, wherein first component (s) is condensed, adsorbed and / or absorbed by means of expulsion means.
  • the system can be designed such that the recirculation loop of the second component (s) from the extruder scrubber to the evaporator passes through the low-pressure expansion device back to the extruder scrubber, separate from the expulsion line loop of the expulsion medium from the extruder scrubber via the separator to the extruder scrubber, wherein preferably the return line circuit of the second component / n is a pump interposed, the second component / n under pressure into the evaporator passes and in the return line circuit of the expelling means optionally a recuperator is interposed.
  • the return line circuit of the second component / s has at least one heat exchanger unit, the heat exchanger unit preferably having a coupling device.
  • the return line loop of the first component is passed from the separator to the evaporator via the low-pressure expansion device for Austrreiber Reginascher back to the separator, from the evaporator to Austreiber Reginascher first and second components are performed together and the Austrreiber scrubber back to the separator first Component / s are performed together with the expulsion means, wherein preferably in the return line loop from Austreiber scrubber to the separation device optionally a recuperator is interposed.
  • a return line with valve can be arranged between the separator and the evaporator.
  • the first component can be passed from the separator as vapor or gas in the evaporator.
  • the second component can be derived as steam or gas from the Austreiber Reginascher.
  • the second component emits thermal energy to the working fluid in the evaporator, the second component is condensed in this case and after the heat exchange, the condensate of the second component is fed to the evaporator.
  • Working fluid is supplied under pressure to the low pressure relaxation device. Here the working fluid is depressurized and, if necessary, lowered in temperature. The energy released in this case can be converted for conversion into mechanical and / or electrical energy.
  • the expelling agent may be supplied in flowable form, preferably in liquid form, to the expeller scrubber to absorb the first component.
  • the condensate, also referred to as a mixture, of the first component and expelling agent is fed in a flowable form, preferably as a liquid, to the separating device.
  • a recuperator be interposed for the purpose of heat exchange. The thermal energy thus obtained can be supplied to the separating device and / or to the evaporator.
  • the object of the invention relates to a system with an evaporator in which a working medium comprising first and second component (s), hereinafter also referred to as a mixture, preferably forms an azeotropic mixture which evaporates in the evaporator and optionally experiences an increase in pressure.
  • This compressed gaseous mixture is a low-pressure expansion device, with an absorption device which is integrated in the low-pressure expansion device and / or the low-pressure expansion device is fed downstream, wherein in the absorption device, a first component of the working fluid is absorbable by an absorbent and Heat is transferable to the remaining, vaporous second component, which is traceable.
  • the working medium mixture of the first component (s) and the second component (s) is depressurized and, if appropriate, the working medium mixture undergoes a temperature reduction.
  • the available heat energy is not available at a sufficiently high temperature level, first the heat energy with the aid of at least one heat source or energy source, preferably heat pump, to the required temperature level for the evaporation of the working fluid or for the separation of the first component from the expelling means transformed by thermal desorption.
  • at least one heat source or energy source preferably heat pump
  • the described absorption-desorption process with an azeotropic mixture is used as the working medium while dispensing with the low pressure release as a chemisorption heat pump.
  • the operation of this heat pump therefore corresponds mutatis mutandis to the above.
  • the absorption heat energy of the first component released from the mixture of first component and expelling agent is used to evaporate the second component (s) of the working medium, which is then transformed to a higher temperature level by thermal energy input, optionally by means of a heat pump to evaporate a "second" working fluid for the low pressure relaxation, which is then expanded in a low-pressure expansion device, wherein the energy released in this case is at least partially converted into mechanical and / or electrical energy.
  • a heat pump according to the invention is provided with at least one mechanical compressor.
  • the temperature increase of the working fluid is carried out by mechanical compression and, on the other hand, the temperature of the working fluid is additionally increased by means of a compressor by heat exchange with a second component / s, which is in heat energy exchange with the working fluid, and / or on the other hand in addition, by means of an operating medium acting as an absorbent, wherein the absorbent absorbs a first component of the working fluid, which is formed by a mixture, in and / or after the compressor, wherein heat is transferred to the remaining, vaporous second component.
  • the efficiency can be significantly improved by the inventive method.
  • the temperature increase of the working fluid is due to the compression of the working fluid.
  • the compressor is preferably designed as a liquid-superposed compressor.
  • this may be a liquid ring pump or a liquid-superposed screw compressor. It is particularly advantageous that these liquid-superposed compressor can be operated with high-boiling equipment. Since in the fluid superimposed compressors the equipment does not have a lubricating function but a pure sealing function, in the method according to the invention virtually any working medium up to water can be used, which have high molar heat of evaporation, have large temperature jumps in the low pressure range and allow high operating temperatures of the compressor.
  • Another advantage of the inventive process separation of compression and heating in the liquid ring pump is the ability to realize temperatures of the working fluid after the temperature increase of about 180 4 O can.
  • resources such as high-boiling silicone oils or diester oils or plasticizers such as dioctyl phthalate with viscosities up to 50 centistoke (cts).
  • the boiling temperature of the operating fluid is higher than the temperature of the working fluid after the temperature increase.
  • the working agent is a one-component solvent, for example water or a higher-boiling solvent.
  • the compressor is followed by a separation arrangement.
  • a separation arrangement ensures that these shares are collected and returned to the compressor.
  • an aerosol separator may be connected downstream of the separation arrangement, which can collect the smallest particles (droplets) of the equipment from the vaporous working medium, which are also conveyed to the compressor.
  • Any accumulating oil can be conveyed back into the compressor in a further embodiment of the invention.
  • the separator and / or the Aerosolabscheider downstream of a condenser, wherein the resulting condensate of the first component / s and / or working fluid is supplied to the evaporator.
  • the first component (s) and / or working fluid condense under an elevated pressure generated by the compressor, and first component (s) and / or working fluid can release heat at a high temperature level.
  • the resulting condensate preferably returns via an expansion valve back to the evaporator.
  • a particularly preferred embodiment of the invention relates to the use of heat energy from the atmospheric air as an energy source with the dissolved therein as humidity water vapor.
  • the occurring when using heat pump / s as an energy source condensate water is processed in an additional process step to process water and / or to water with drinking water quality.
  • the atmospheric air with the water vapor dissolved in it constitutes a large, practically inexhaustible energy reservoir.
  • this energy reservoir which is formed by the sensible heat of the air and the latent heat of the water vapor, everywhere the world, so it is available regardless of location. This energy reservoir is constantly refilled by the sunlight.
  • the conversion of the thermal energy contained in humid air into mechanical energy is an indirect use of the heat energy from solar radiation.
  • a particularly preferred embodiment of the method according to the invention provides for absorbing the heat energy from moist ambient air into an evaporator for evaporating a suitable working medium and, if necessary, for transformation to a higher temperature level depending on the real ambient conditions with temperature and humidity to relax with one or more heat pumps, the steam via a low-pressure expansion device according to the above, with some of the heat energy is converted into mechanical energy and the energy contained in the relaxed working medium is traceable.
  • the gaseous components are cooled, on the other hand, depending on the temperature levels of the heat exchange processes, the air humidity contained predominantly condenses, the high heat of condensation of the water being recovered for the process.
  • the conversion can be advantageously realized without the interposition of a heat pump.
  • the average working time of the plant according to the invention for converting thermal energy of fluids into mechanical energy at an initial fluid temperature of 25 ° C determined over 24 hours makes up 2.5 to 12.
  • the average work digit may be 3 to 10 or 4 to 8 for systems according to the invention.
  • the average work rate for plants according to the invention is 5 to 6.
  • the overall efficiency of the inventive system for converting thermal energy into mechanical energy is preferably> 40%, preferably> 50% and particularly preferably> 60%.
  • 15% to 40%, preferably 20% to 35% and preferably 25% to 30%, of the released energy can be used for the conversion into mechanical energy by the relaxation of the working medium at the low-pressure expansion device.
  • the temperature of the working fluid upstream of the low-pressure expansion device is higher than the temperature of the working fluid downstream of the low-pressure expansion device and upstream of the absorption device.
  • the temperature of the working fluid in the evaporator unit is higher than the temperature of the working fluid after the low-pressure expansion device and before the absorption device.
  • the temperature of the working medium in the evaporator may be 10 ° C to 250 ° C, preferably 20 ° C to 200 ° C, preferably 30 ° C to 150 ° C, more preferably 40 ° C to 130 ° C and particularly preferably 50 ° C to 100 Make out ° C. Most preferably, the temperature of the working fluid in the evaporator is above the boiling point.
  • the excess pressure of the working fluid, based on normal pressure (atmospheric pressure), before the low-pressure expansion device can be in the range of 0.3 bar to 15 bar. Higher pressures are possible, but such systems require increased material costs, so that the pressure of the working fluid in the supply line from the evaporator to the low-pressure expansion device preferably in the range of 1 bar to 10 bar, more preferably in the range of 1, 5 bar to 8 bar , more preferably in the range of 2 bar to 6 bar and also preferably in the range of 3 bar to 4 bar lie.
  • the pressure difference .DELTA.P of the working fluid upstream of the low-pressure expansion device and immediately after relaxation of the working fluid but before the absorption device should ⁇ P 0.1 bar to 5 bar, preferably ⁇ P 0.5 bar to 3 bar and preferably ⁇ P
  • the separator also referred to as Ausreiberaggregat
  • the separated vaporous first component may have a steam temperature of about 120 ° C and an overpressure, based on atmospheric pressure, of about 1 bar.
  • the Austreibericascher prevails normal pressure, wherein the second component of the working fluid has an evaporation temperature of about 90 ° C to 120 ° C.
  • Figure 1 shows a plant for the conversion of thermal energy into mechanical / electrical and thermal useful energy in a variable ratio.
  • the externally introduced heat energy of the energy source (1) heats a separator (2), in which there is an alkaline silicate solution as absorption solution with absorbed water.
  • the absorption solution is heated by the introduced heat energy so that the absorbed water desorbs and as vapors into the evaporator (3) and heated by heat exchange or condensation heats the second component therein and forms a mixture of first and second component, hereinafter referred to as Work equipment called.
  • Work equipment for the mixture used as working fluid, an azeotropic mixture of water and silicone is selected by way of example.
  • the motive steam generated in the evaporator (3) is expanded via the expansion device (4), wherein the energy of the motive steam of the working fluid is at least partially converted into mechanical force, which is converted into electrical energy by means of the connected generator (5).
  • the relaxed working fluid is in the downstream Austreibericascher (6) with a Austreibungsstoff, hereinafter also referred to as absorption solution, washed from the expeller unit (2), wherein the water content is absorbed in the relaxed motive steam.
  • absorption solution a Austreibungsmittel
  • the pressure reduction desired for the relaxation is realized by the absorption on the one hand by reducing the number of particles
  • the released absorption energy is transferred to the vaporous second component, in this case silicone.
  • this second component is heated to a temperature level which is above the vaporization temperature of the azeotropic mixture used as the working medium. This temperature level adjusts itself according to the pressure conditions set in the system.
  • the thus heated vaporous second component is supplied via a steam line to a heat exchanger unit (8), and there in the heat exchange energy to a coupling device, such as a heating circuit (9), for example, for supplying heat-consuming processes. Cooled or partially condensed, the second component leaves the heat exchanger unit (8) and is conducted in a line through and / or to the evaporator (3), for the purpose of heat exchange with the boiling in the evaporator boiling means, wherein the second component guided while releasing its heat of condensation completely condensed to the working fluid.
  • a coupling device such as a heating circuit (9)
  • the condensed working fluid is then conveyed back to the evaporator (3) with the pump (7).
  • the absorption solution is circulated between the separation device (2) and expeller scrubber (6), wherein a recuperator (11) between supply and return causes cooling of the absorption solution before entering the Austrreiber stiischer and thus an improvement in the absorption capacity with respect to the first component.
  • the achieved decoupling of absorption and desorption temperature improves the stability of the absorption / desorption or condensation process.
  • a backflow line between separating device (2) and evaporator (3) serves to stabilize the composition of the mixture.
  • the system according to the invention can be used to convert thermal energy into mechanical, electrical and / or thermal energy.
  • the system according to the invention can be used in particular for heating and / or for supplying energy to buildings and the like.
  • the system according to the invention may be used alone or in combination with conventional drive systems, e.g. Internal combustion engines or batteries.
  • conventional drive systems e.g. Internal combustion engines or batteries.
  • hybrid drives can be realized.
  • the inventive system can be used alone or in combination with at least one combustion or electric motor in the embodiment of a hybrid drive to drive very different mobile systems.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un procédé et un dispositif de transformation d'énergie calorifique en énergie mécanique, électrique, et/ou thermique, avec un rendement élevé, par dilatation d'un mélange gazeux, dans un dispositif de dilatation (13) qui est relié à un évaporateur (3). Le procédé selon l'invention consiste: à expulser au moins un premier composant d'un mélange comprenant au moins un premier composant et au moins un agent d'expulsion, dans un dispositif de séparation (2), par apport d'énergie calorifique provenant d'une source d'énergie (1), et à transférer ce premier composant dans un évaporateur (3), l'agent d'expulsion étant introduit séparément dans un épurateur d'agent d'expulsion (6); à ajouter au moins un deuxième composant au(x) premier(s) composant(s) expulsé(s) se trouvant dans l'évaporateur (3), de façon à former un mélange; à introduire le mélange formé par le(s) premier(s) composant(s) expulsé(s) et le(s) deuxième(s) composant(s) en tant que vapeur sous la forme d'un gaz comprimé dans au moins un dispositif de dilatation basse pression (4), et à le dilater, l'énergie libérée par le processus de dilatation pouvant être transformée partiellement en énergie mécanique, électrique, et/ou thermique; à introduire le mélange dilaté dans au moins un épurateur d'agent d'expulsion (6), l'agent d'expulsion étant ajouté audit mélange, le premier composant et l'agent d'expulsion formant un mélange par libération d'énergie calorifique, ce qui extrait de l'énergie au moins du premier composant du mélange, augmente la température du/des deuxième(s) composant(s), et sépare ce(s) dernier(s) du mélange; à extraire le mélange de l'épurateur d'agent d'expulsion (6) et à le réintroduire dans le dispositif de séparation (2), et à extraire le(s) deuxième(s) composant(s) de l'épurateur d'agent d'expulsion (6) et à le(s) réintroduire dans l'évaporateur (3).
PCT/EP2005/051574 2005-04-08 2005-04-08 Procede de transformation d'energie calorifique en energie mecanique avec un rendement eleve WO2006105815A1 (fr)

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CN110330469A (zh) * 2019-07-27 2019-10-15 河南心连心化学工业集团股份有限公司 一种粗糠醇分离过程中的能量回收装置以及能量回收方法
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CN103502582A (zh) * 2011-05-02 2014-01-08 哈里公司 混合嵌入式组合循环
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WO2012151055A3 (fr) * 2011-05-02 2013-01-03 Harris Corporation Cycle combiné imbriqué hybride
US9038389B2 (en) 2012-06-26 2015-05-26 Harris Corporation Hybrid thermal cycle with independent refrigeration loop
US9574563B2 (en) 2013-04-09 2017-02-21 Harris Corporation System and method of wrapping flow in a fluid working apparatus
US9297387B2 (en) 2013-04-09 2016-03-29 Harris Corporation System and method of controlling wrapping flow in a fluid working apparatus
US9303514B2 (en) 2013-04-09 2016-04-05 Harris Corporation System and method of utilizing a housing to control wrapping flow in a fluid working apparatus
US9303533B2 (en) 2013-12-23 2016-04-05 Harris Corporation Mixing assembly and method for combining at least two working fluids
WO2018069845A1 (fr) * 2016-10-11 2018-04-19 Enslin Johan Adam Utilisation régénérative de la chaleur dans un cycle thermodynamique
CN111852599A (zh) * 2019-04-30 2020-10-30 中国船舶重工集团公司第七一一研究所 船舶余热回收发电系统
CN110206602A (zh) * 2019-05-23 2019-09-06 中国能源建设集团广东省电力设计研究院有限公司 一种基于核电站的热电系统及其控制方法
CN110330469A (zh) * 2019-07-27 2019-10-15 河南心连心化学工业集团股份有限公司 一种粗糠醇分离过程中的能量回收装置以及能量回收方法
WO2022233554A1 (fr) * 2021-05-07 2022-11-10 Fraunhofer-Gesellschaft Zur Foerderung Der Angewandten Forschung E.V. Procédé de préparation de vapeur de traitement et installation technologique destinée à utiliser de la vapeur de traitement

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