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EP2057353A1 - Système de moteur thermique - Google Patents

Système de moteur thermique

Info

Publication number
EP2057353A1
EP2057353A1 EP07800206A EP07800206A EP2057353A1 EP 2057353 A1 EP2057353 A1 EP 2057353A1 EP 07800206 A EP07800206 A EP 07800206A EP 07800206 A EP07800206 A EP 07800206A EP 2057353 A1 EP2057353 A1 EP 2057353A1
Authority
EP
European Patent Office
Prior art keywords
component
working fluid
heat engine
engine system
recuperator
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.)
Withdrawn
Application number
EP07800206A
Other languages
German (de)
English (en)
Inventor
Patrick Glynn
Colin Buckland
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Perpetuity Management Pty Ltd
Commonwealth Scientific and Industrial Research Organization CSIRO
Original Assignee
Perpetuity Management Pty Ltd
Commonwealth Scientific and Industrial Research Organization CSIRO
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
Priority claimed from AU2006904633A external-priority patent/AU2006904633A0/en
Application filed by Perpetuity Management Pty Ltd, Commonwealth Scientific and Industrial Research Organization CSIRO filed Critical Perpetuity Management Pty Ltd
Publication of EP2057353A1 publication Critical patent/EP2057353A1/fr
Withdrawn legal-status Critical Current

Links

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
    • F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
    • F01K17/06—Returning energy of steam, in exchanged form, to process, e.g. use of exhaust steam for drying solid fuel or plant
    • 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
    • F01K21/00—Steam engine plants not otherwise provided for
    • F01K21/04—Steam engine plants not otherwise provided for using mixtures of steam and gas; Plants generating or heating steam by bringing water or steam into direct contact with hot gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
    • F28D20/02—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using latent heat
    • F28D20/026—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using latent heat with different heat storage materials not coming into direct contact
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/14—Thermal energy storage

Definitions

  • the present invention relates to a heat engine system and to a method for producing work.
  • a heat engine is a system arranged to convert thermal energy to mechanical work.
  • the heat engine does this by transferring energy from a high temperature heat source (T H ) to a low temperature heat sink (T L ) .
  • T H high temperature heat source
  • T L low temperature heat sink
  • the efficiency of any heat engine is understood to be determined by, amongst other factors, the difference in temperature between the heat source and the heat sink.
  • the efficiency of various heat engines currently in use range from 3% to about 60%. Most automotive engines have an efficiency of approximately 25% and supercritical coal- fired power stations have an efficiency of approximately 35 - 41%. Because the efficiency of any heat engine is understood to be dependent on the temperature gradient between the heat source and heat sink, many attempts have been made to increase heat engine efficiencies by increasing this temperature gradient.
  • the most efficient heat engine is defined by the Carnot cycle and comprises a boiler, a turbine, a condenser and a pump.
  • the working fluid undergoes reversible isothermal heating from the high temperature reservoir in the boiler, reversible adiabatic expansion of the working fluid with a reduction in temperature from the high temperature (T H ) to the low temperature (T L ) , reversible isothermal cooling of the working fluid to the low temperature reservoir in the condenser, and reversible adiabatic compression of the working fluid with an increase in temperature from T L to T H in the pump.
  • the thermal efficiency (H TH ) of a heat engine operating according to the Carnot cycle is defined by the equation:
  • the ideal Rankine cycle involves reversible adiabatic compression from a low pressure to a high pressure by the pump, constant pressure (isobaric) heat transfer from the high temperature heat source in the boiler, reversible adiabatic expansion from the high pressure to the low pressure in the turbine, and a constant pressure (isobaric) transfer of heat from the working fluid to the low temperature heat sink in the condenser.
  • the Rankine cycle differs from the Carnot cycle primarily in that complete condensation of the working fluid from a vapour to a liquid in the condenser occurs in the Rankine cycle.
  • the reason for doing this is that whilst it reduces the efficiency of the heat engine, in practice, it is difficult for a pump to handle a mixture of liquid and vapour as is the case in the Carnot cycle.
  • a further difference is that if the working fluid is heated to a superheated vapour in the boiler, in the Carnot cycle all the heat transfer is at a constant temperature and hence during this process the pressure must be reduced.
  • Brayton cycle Another cycle is the Brayton cycle.
  • the Brayton cycle operates similarly to the Rankine cycle except that the working fluid exists only in the gaseous phase throughout the cycle (ie. the Brayton cycle does not involve condensing and boiling of the working fluid) .
  • a closed Brayton cycle the system involves isentropic compression, followed by isobaric heating, before isentropic expansion of the working fluid occurs to produce work, followed by isobaric cooling of the working fluid.
  • Gas turbines generally operate according to an open Brayton cycle, in which a combustible fuel is added to the working fluid after the compressor, whereupon combustion of the fuel raises the temperature of the working fluid prior to it being expanded in the turbine to produce work.
  • the exhaust from the turbine containing working fluid mixed with products of the combustion of the fuel is sent to waste and not returned to the inlet of the compressor.
  • the Rankine cycle with reheat the heat engine comprises two turbines in series.
  • Working fluid as a vapour from the boiler at high pressure enters the first turbine where it is expanded to a lower pressure.
  • the reduced pressure vapour exiting the first turbine re-enters the boiler where it is reheated before passing through the second turbine which operates at lower pressures .
  • One advantage of this system is that reheating of the working fluid between the turbines prevents the working fluid from condensing from a vapour to a liquid during expansion in the turbines which could result in significant damage to the turbine .
  • the regenerative Rankine cycle involves preheating of the working fluid prior to its entry to the boiler by splitting a small portion of steam from an intermediary stage in the turbine and mixing it with the liquid working fluid after it has been cooled in the condenser in a "feed water heater" which is located at an intermediary pumping stage prior to the inlet of the working fluid to the boiler.
  • a heat engine system for producing work by expanding a working fluid comprising first and second components
  • the system comprising, an apparatus for combining the second component of the working fluid as a liquid with the first component, the first component being a gas throughout the system, a compressor for compressing the first component, a pump for compressing at least most of the second component, a heater for heating the first and second components, an expander for expanding the first and second components to produce the work, and a recuperator for transferring at least some of the energy of the working fluid from the outlet of the expander, to the working fluid from the outlet of the apparatus, wherein a substantial portion of the energy transferred in the recuperator is at least a portion of the latent heat of the second component from the outlet of the expander.
  • the apparatus comprises an injector.
  • the apparatus comprises an atomiser.
  • the apparatus is arranged to spray the liquid second component into a space having the first component therein.
  • the apparatus is a diffuser.
  • the apparatus is arranged to diffuse the first component into the liquid second component .
  • the apparatus comprises multiple injectors, atomisers or diffusers.
  • the apparatus is located between the compressor and the recuperator, to enable the liquid second component to be combined with the gaseous first component after it has been compressed.
  • recuperator there is also some sensible heat transferred in the recuperator.
  • a substantial portion of the latent heat of the second component is transferred in the recuperator.
  • the recuperator converts at least some of second component from the outlet of the apparatus from liquid to gas.
  • the recuperator converts at least some of the second component from the outlet of the expander from gas to liquid.
  • the recuperator is generally in the form of a shell and tube heat exchanger.
  • the recuperator is generally in the form of a falling film condensor.
  • the recuperator is arranged to provide separation of a liquid fraction of the working fluid from a gaseous fraction upon cooling of the working fluid from the outlet of the expander.
  • the recuperator comprises a boiling side and a condensing side.
  • working fluid from the outlet of the apparatus enters the boiling side of the recuperator where the second component of the working fluid substantially boils as it receives energy from the working fluid on the condensing side.
  • working fluid from the outlet of the expander enters the condensing side of the recuperator where the second component of the working fluid substantially condenses as it loses energy to the working fluid on the boiling side.
  • the condensing side of the recuperator comprises a liquid separator basin that collects the liquid second component for recycling in the system.
  • the boiling side of the recuperator is the tubes of a shell and tube heat exchanger, and the condensing side is the shell of a shell and tube heat exchanger.
  • the system comprises multiple recuperators connected in parallel and/or series .
  • the pressure at the inlet to the expander is the pressure to which the first component is compressed in the compressor, less any losses in the system therebetween. Compression of the first component of the working fluid also increases its temperature. In an embodiment, the compressor compresses a small portion of the second component as a gas in addition to the first component.
  • the compressor is any suitable compressor such as an axial, centrifugal, reciprocating or scroll compressor for example.
  • the system comprises multiple compressors connected in parallel and/or series.
  • the system also comprises at least one cooler for cooling the first and/or second components prior to combining them in the apparatus.
  • At least one of the coolers comprises an inter-cooler in the compressor to provide inter-stage cooling of the first compressor.
  • At least one of the coolers comprises a post compressor cooler for cooling the first component after it has been compressed.
  • At least one of the coolers comprises a pre-compressor cooler for cooling the first component prior to it being compressed in the compressor.
  • the at least one cooler has a cooling source.
  • the cooling source is cooling water, ambient air or any suitable refrigeration system to which heat may be rejected.
  • the heat rejected to the at least one cooler may be used as a heat source for any other suitable process such as heating hot water, creating low pressure steam, desalination, as the heat input to a heat pump vapour compression system or as the heat input for any low temperature power generation or refrigeration cycle.
  • the at least one cooler comprises a liquid cooler for cooling the liquid second component .
  • liquid second component when combined with the first component by the apparatus is at ambient temperature.
  • the second component when combined with the first component cools the first component .
  • the at least one cooler acts to ensure that the temperature of the first component entering the apparatus is less than a temperature which would cause vaporisation of the second component upon its combination with the first component by the apparatus .
  • the pump compresses at least most of the second liquid component to a pressure above the ambient pressure.
  • the pump compresses at least most of the liquid second component to at or about the pressure to which the compressor compresses the first component .
  • the system comprises multiple pumps connected in parallel and/or series.
  • the working fluid is a gas- liquid mixture after the second component (liquid) has been combined with the first component (gas) by the apparatus .
  • the expander comprises any suitable unit for producing mechanical work by the expansion of a working fluid.
  • the expander may be a turbine, a positive displacement rotary expander, a scroll expander a linear expander or a reciprocating engine for example.
  • the expander may also comprise multiple turbines, rotary expanders, linear expanders or reciprocating engines, connected in either parallel or series, with or without inter-stage reheat.
  • the expander may or may not be directly coupled to the compressor to the drive the compressor.
  • the expander is in the form of a turbine.
  • the turbine has variable pitch blades .
  • the system may comprise any number of multiple expanders and/or compressors arranged in parallel or series.
  • the heater provides a heat input to the working fluid from any suitable heat source.
  • the heater heats the working fluid to a super-critical gas.
  • the heat source for the heater may be steam or any other heated medium generated by nuclear power, coal or another combustible fuel, hot exhaust gasses from a gas turbine, waste heat from any other process, direct heating from a furnace, electrical, solar thermal, stored heat or a thermal energy cell(s) for example.
  • the heat engine system also comprises a condenser for cooling the working fluid after it exits the recuperator.
  • the condenser is arranged to substantially condense the second component of the working fluid to a liquid.
  • the condenser may be in the form of a shell and tube heat exchanger, a radiator, a finned cooling coil with cooling fluid in serpentine coils, located inside a plenum with condensate recovery or any other suitable condenser.
  • one side of the condenser receives the working fluid exiting the condensing side of the recuperator.
  • cooling fluid flows through the other side of the condenser for cooling the working fluid to condense most of the second component of the working fluid to liquid.
  • the cooling fluid may be air, refrigerant of any composition or water or brine at or below ambient conditions .
  • the heat removed from the working fluid by the condenser may be used as the heat input to any other suitable system, such as an external heat engine, a heat pump, a refrigeration cycle, desalination or for process heating of water for example.
  • the condenser is a separator for separating the second component, as it condenses from the first component.
  • the separated second component is recycled to the apparatus.
  • the remaining working fluid which comprises the first component and any of the second component remaining as a gas, flows to the inlet to the compressor.
  • the system comprises multiple condensers connected in parallel and/or series.
  • the system also comprises a load, connected to the expander for converting the work produced by the expander to mechanical or electrical power.
  • the system is a closed system having substantially no mass inputs or outputs during operation of the system, other than replacement of incidental losses.
  • the system comprises a top-up feed of the working fluid for replacing any incidental losses.
  • Incidental losses may result from leaks, maintenance, or high-pressure or high-temperature releases for example .
  • the system comprises an energy transfer controller for controlling the energy transfer in the recuperator during operation of the system.
  • the energy transfer controller controls the energy transfer in the recuperator by changing the conditions at the inlet of the expander and subsequently the expansion done in the expander and hence the conditions at the outlet of the expander. In an embodiment, the energy transfer controller controls the energy transfer in the recuperator by changing the amount of the liquid second component combined with the first component in the apparatus.
  • the system comprises a mass flow controller for controlling the mass flow rate of the second component relative to the mass flow rate of the first component.
  • the mass flow controller comprises a variable speed control on the pump.
  • the mass flow controller comprises a pump diverter, arranged to divert flow of the second component from the outlet of the pump to the inlet of the pump.
  • the mass flow controller comprises variable inlet guide vanes in the compressor.
  • the mass flow controller comprises a variable speed control on the compressor.
  • the mass flow controller comprises a compressor diverter, arranged to divert flow of the first component from the outlet of the compressor to the inlet of the compressor.
  • the mass flow controller comprises appropriate valving on the apparatus.
  • the system comprises an energy storage unit upstream of the compressor for storing compressed working fluid (largely the first component with any gaseous second component) , for use in particular during start-up for example.
  • start-up may be effected by supplying power to the compressor, pump and expander shafts .
  • the first and second components of the working fluid are substances which are substantially inert with respect to each other.
  • the first and second components will not react with one another, nor substantially dissolve in one another, nor substantially dissociate at high temperatures .
  • the second component is a substance which has a high volumetric expansion ratio from liquid to gas.
  • the first component is a substance which is highly compressible as a gas.
  • the first component may be nitrogen, argon, helium, hydrogen or methane for example .
  • the second component may be water, propane, butane, ethanol or carbon dioxide for example.
  • a preferred working fluid is nitrogen as the first component and water as the second component.
  • the working fluid may comprise more components than the first and second components.
  • the heater is a heat exchanger. In an embodiment, the heater is a regenerative heater.
  • the regenerative heater comprises at least one volume of material arranged to be heated to at or above the melting temperature of the material, the heater also comprising passages through the at least one volume of material for the flow therethrough of the working fluid.
  • the regenerative heater comprises at least two volumes of material, preferably three.
  • the heater may comprise more than three volumes of material.
  • the passages are arranged for the working fluid to flow through the volumes of material in series.
  • the passages may be arranged for the working fluid to flow through the volumes of material in parallel.
  • the volume (s) of material is heated using a heating fluid flowing through spaces through the volume (s) of material.
  • the heating fluid may be steam or any other heated medium generated by nuclear power, coal or other combustible fuel or hot exhaust gases from a gas turbine for example .
  • the passages through which the working fluid flow are separate from the spaces through which the heating fluid flow.
  • the volume (s) of material may be heated using any other suitable means, such as waste heat from another process, direct heating from a furnace, electrical or solar thermal heat.
  • the materials in the volumes are different.
  • the different materials preferably have different melting temperatures.
  • the materials are of progressively decreasing melting temperatures from the first volume to the last volume, the passages being arranged for the flow of the working fluid through the last volume first and the first volume last.
  • working fluid flows counter- currently to the heating fluid.
  • the spaces are arranged for the flow of the heating fluid through the first volume first and the last volume last.
  • At least one of the volumes of material contains a mixture of two or more different materials .
  • one of the materials in the mixture of materials of the or each volume is for improving the heat transfer of the or each volume of material.
  • a material may be graphite.
  • one of the materials in the mixture of materials of the or each volume is for affecting the melting temperature of the or each volume of material .
  • aluminium is mixed with silicon to reduce the melting temperature of the volume of material.
  • the material in the volumes are each mixtures of the same materials but at different ratios .
  • the different ratios preferably have different melting temperatures.
  • phase change materials or "PCMs”
  • PCMs phase change materials
  • Any suitable phase change materials may be employed.
  • the first volume contains silicon, which has a melting temperature of about 1410 0 C
  • the second volume contains lithium fluoride, which has a melting temperature of about 870 0 C
  • the third volume contains magnesium oxide or calcite, which have a melting temperature of about 56O 0 C.
  • the volume (s) of material is held in a container (s) which is able to withstand the temperatures of the molten material (s) held therein.
  • the container (s) is manufactured from a ceramic, preferably silicon carbide.
  • the regenerative heater also comprises a number of valves on the inlets and outlets to the heater which can be used to control the flow rate of the working fluid and the heating fluid through the heater to maintain the temperature of the material (s) in the volume (s) so as to keep them in a molten phase and to control the temperature of the working fluid as it leaves the heater.
  • the system comprises multiple regenerative heaters. In one such embodiment, the system comprises three regenerative heaters, whereby while one heater is in operation a second is on stand-by and the other is shut-down for maintenance.
  • a method for producing work comprising the steps of: compressing a first component of a working fluid in a compressor, the first component being a gas at all times during the method; compressing at least most of a second component of the working fluid as a liquid in a pump; combining the second component as a liquid with the first component in an apparatus; heating the combined first and second components in a heater; expanding the heated first and second components to produce the work in an expander; and transferring in a recuperator at least some of the energy of the working fluid after it has been expanded to the working fluid prior to it being heated in the heater, wherein a substantial portion of the energy transferred is at least a portion of the latent heat of the second component after the working fluid has been expanded in the expander.
  • the step of combining the second component with the first component comprises spraying the liquid second component into a space having the first component therein.
  • the step of combining the second component with the first component comprises diffusing the first component into the liquid second component .
  • the step of combining the second component with the first component occurs after the steps of compressing the first component and compressing at least most of the second compound.
  • some of the energy transferred in the recuperator is sensible heat.
  • the step of transferring at least some of the energy in the recuperator converts at least some of the second component from liquid to gas prior to it being heated in the heater. In an embodiment, the step of transferring at least some of the energy in the recuperator converts at least some of the second component from gas to liquid after it has been expanded in the expander.
  • the method also comprises the step of separating a liquid fraction of the working fluid from a gaseous fraction after the working fluid has been expanded.
  • the step of separating occurs at least partially in the recuperator.
  • the method is a closed cycle method also comprising the step of repeating the steps of the method after at least some of the working fluid' s energy has been transferred in the recuperator to the working fluid which is yet to be heated in the heater.
  • the method also comprises the step of returning the first component to the compressor.
  • the method also comprises the step of returning at least most of the second component to the pump.
  • the step of compressing the first component occurs in at least two stages.
  • the step of compressing the first component occurs in only one stage.
  • the method also comprises the step of cooling the first and/or second components prior to the step of combining them.
  • the cooling step comprises cooling the first component between at least two of the stages of the compressor using an intercooler.
  • the cooling step comprises cooling the first component after the step of compressing the first component, preferably before the step of combining with the second component.
  • the cooling step comprises cooling the first component prior to the step of compressing the first component. In an embodiment, the cooling step comprises cooling the second component prior to combining the second component with the first component.
  • the liquid second component when combined with the first component in the apparatus is at ambient temperature.
  • the step of compressing at least most of the second component compresses at least most of the second component to a pressure above the ambient pressure. In an embodiment, the step of compressing at least most of the second component compresses most of the second component to at or about the pressure to which the first component is compressed in the compressor.
  • the method comprises the step of maintaining the temperature of the first component prior to the step of combining with the second component to a temperature which is less than one which would cause vaporisation of the second component during the combining step.
  • the step of separating the liquid fraction from the gaseous fraction of the working fluid comprises separating at least most of the second component as a liquid from the first component as a gas .
  • the step of separating does not completely separate all of the second component from the first component. Some of the second component remains as a gas mixed with the first component.
  • the step of separating occurs at least in part in the recuperator.
  • the step of separating the first component from the second component occurs at least in part in a condenser, and preferably after at least some of the energy of the working fluid has been transferred in the recuperator to the working fluid which is yet to be heated in the heater.
  • the step of separating the first component from the second component comprises cooling the working fluid to condense at least most of the second component.
  • the method also comprises the step of controlling the energy transferred in the recuperator.
  • the step of controlling the energy transferred in the recuperator comprises changing the conditions of the working fluid prior to expanding it in the expander. In an embodiment, the step of controlling the energy transferred in the recuperator comprises changing the amount of the second component which is combined with the first component in the apparatus .
  • the method also comprises the step of controlling the mass flow rate of the second component relative to the mass flow rate of the first component .
  • the step of heating comprises transferring heat from a high temperature source to the working fluid in the heater, such as for example by using a heating medium in a heat exchanger.
  • the step of heating comprises flowing the combined first and second components through at least one volume of material which is heated to at or above the melting temperature of the material.
  • the step of heating comprises flowing the combined first and second components through at least two volumes of material, preferably three.
  • the step of heating also comprises heating the at least one volume of material using a heating fluid.
  • heating the at least one volume of material comprises flowing the heating fluid through spaces through the volume (s) of material.
  • the step of heating comprises flowing the heating fluid through the at least one volume of material in a counter current direction to the flow of the combined first and second components.
  • the step of heating comprises heating the working fluid to a super-critical gas.
  • Figure 1 is a schematic view of a heat engine system according to embodiments of the present invention
  • Figure 2 is a schematic view of the heat engine regenerative heater for heating the working fluid of the heat engine system according to an embodiment of the present invention
  • Figure 3 is a schematic view of a HYSYS ® model of a system heat engine according to an embodiment of the present invention.
  • a heat engine system 10 produces work by expanding a working fluid.
  • the working fluid comprises first and second components, the first component being a gas throughout the system 10.
  • the system 10 comprises an apparatus 11 for combining the second component of the working fluid as a liquid with the first component.
  • the apparatus 11 may comprise an injector or atomiser arranged to spray the liquid second component as a mist into a space of sufficient volume having the first component therein.
  • the apparatus 11 may alternatively comprise a diffuser, which is arranged to diffuse the first component into the liquid second component.
  • the system 10 also comprises a compressor 12 for compressing the first component of the working fluid, a pump 19 for compressing at least most of the second component, a heater 13 for heating the first and second components and an expander 14 for expanding the first and second components to produce the work.
  • the apparatus 11 is located after the compressor 12 and the pump 19, to enable the liquid second component to be combined with the gaseous first component after they have been compressed.
  • the system 10 also comprises a recuperator 15 for transferring some of the energy of the working fluid from the outlet of the expander 14, to the working fluid from the outlet of the apparatus 11.
  • a substantial portion of the energy transferred in the recuperator 15 is at least some of the latent heat of the second component of the working fluid (ie. the energy associated with the phase change of a material such as between liquid and gaseous states) .
  • the recuperator 15 at least some of second component from the outlet of the apparatus 11, which is liquid, is converted to gas and at least some of the second component from the outlet of the expander 14, which is gas, is converted to liquid.
  • the change of phase for the second component of the working fluid produces a large expansion in the volume of the working fluid, thus substantially increasing the volumetric flow through and hence the work produced by the expander 14 compared to a gas turbine in a conventional Brayton cycle for the same mass flow rate. Furthermore, the recycling of energy, particularly the latent heat, in the recuperator 15, reduces the load on the heater 13 and hence the energy input to the system 10. These factors enable the system 10 to operate with greater comparative power, improved efficiency and less net energy consumption to produce the same work (in the expander 14) as for an equivalently sized conventional system.
  • the compressor 12 has interstaged cooling provided by an intercooler 18.
  • the primary purpose of this is to ensure that the temperature of the first component entering the apparatus 11, is less than a temperature which would cause vaporisation of the second component upon its combination with the first component in the apparatus 11.
  • This enables the recuperator 15 to provide efficient transfer of the substantial portion of the latent heat of the second component of the working fluid as described above.
  • Ensuring that the temperature of the first component exiting the compressor 12 is at this temperature may alternatively (or in combination with the intercooler 18) be provided by post compression cooling of the first component, pre-compression cooling of the first component or by pre-cooling the second component prior to it being combined with the first component in the apparatus 11 as outlined in Figure 1.
  • the intercooler 18 has a cooling source (as do any of the other coolers described above) for cooling the first component between stages of the compressor 12.
  • the cooling source may be cooling water, ambient air or any suitable refrigeration system to which heat from the first component may be rejected. It is noted that the heat rejected from the compressor 12 by cooling of the first component (either using the intercooler 18, or by pre or post compression cooling) may be used as a heat input to any other suitable process such as for heating hot water, creating low pressure steam, desalination, as the heat input to a heat pump vapour compression system or for any low temperature power generation or refrigeration cycle.
  • the compressor 12 is any suitable compressor such as an axial, centrifugal, reciprocating or scroll compressor for example.
  • the expander 14 comprises any suitable unit for producing mechanical work by the expansion of a working fluid.
  • the expander 14 may or may not be directly coupled to the compressor 12.
  • the expander 14 may be a turbine, a positive displacement rotary expander, a linear expander, a scroll expander or a reciprocating engine for example.
  • the expander 14 may also comprises multiple turbines, rotary expanders, linear expanders or reciprocating engines, connected in either parallel or series, with or without inter-stage reheat.
  • the expander 14 is in the form of a turbine which may or may not have variable pitch blades. In this embodiment, all the working fluid at the outlet of the expander 14 is in the gas phase.
  • the system 10 may comprise any number of multiple expanders and/or compressors arranged in parallel or in series.
  • the heater 13 provides a heat input to the working fluid from any suitable heat source, which heats the working fluid to a super-critical gas (ensuring that all of the second component is vaporised) .
  • the heat source for the heater 13 may be steam or any other heated medium generated by nuclear power, coal or another combustible fuel, hot exhaust gasses from a gas turbine, waste heat from any other process, direct heating from a furnace, solar thermal, electrical, stored heat or a thermal energy cell(s) for example.
  • One suitable heater 13 which provides a heat input from stored heat source is shown in Figure 2, and will be described in more detail further on in the specification.
  • the heat engine system 10 also comprises a condenser 16 for cooling the working fluid after it exits the expander 14 (and also the recuperator 15) to substantially condense the second component of the working fluid to a liquid.
  • a condenser 16 for cooling the working fluid after it exits the expander 14 (and also the recuperator 15) to substantially condense the second component of the working fluid to a liquid. This enables the majority of the second component to be readily separated from the first component (which is a gas) prior to the first component (and any residual gaseous second component) being compressed in the compressor 12. The separated second component is recycled to the pump 19.
  • the system 10 also comprises a load 17, connected to the expander 14 for converting the work produced by the expander 14 to mechanical or electrical power.
  • the system 10 is a closed system, with theoretically no mass inputs or outputs during operation of the system 10, other than replacement of incidental losses. However, a top-up of either of the components of the working fluid may need to be provided due to some incidental losses such as those resulting from leaks, maintenance, or high-pressure or high-temperature releases for example.
  • the gaseous first component of the working fluid enters the compressor 12 through inlet 20, where it is compressed. Compression of the first component of the working fluid tends to increase its temperature, however, the interstage cooler 18 ensures that this rise is not significant enough to cause the temperature of the first component to be above a temperature at which combination with the second component would cause vaporisation of the second component .
  • the first component flows from the outlet 21 of the compressor 12 to the apparatus 11, where the liquid second component is combined with the first component through second component inlet 22 having been compressed in the pump 19.
  • the liquid second component may be at ambient temperature (or lower) and may cool the working fluid.
  • the liquid second component is compressed in the pump 19 to a pressure greater than ambient, and preferably to at or about the pressure of the first component at the outlet of the compressor 12, prior to being combined with the first component. Because there are gas and liquid components of the working fluid compressed separately in the compressor 12 and pump 19 respectively-/ the compressor 12 can be smaller than a compressor which is compressing an equivalent mass flowrate of working fluid which is all gas. This is advantageous to the system because compressing a gas requires much more work than compressing (in a pump) an equivalent mass flowrate of liquid. Therefore, the overall efficiency of the system(s) is improved by this arrangement of the pump 19 and the compressor 12.
  • the working fluid as a gas-vapour mixture exits the apparatus 11 through outlet 23.
  • the recuperator 15 is generally in the form of a shell and tube heat exchanger, preferably a falling film condenser and comprises a boiling side 24 (shell) and a condensing side 25 (tubes) .
  • Working fluid from the outlet 23 of the apparatus 11 enters the boiling side 24 of the recuperator 15 where the second component of the working fluid substantially boils as it receives energy from the working fluid on the condensing side 25.
  • the working fluid exiting the boiling side 24 of the recuperator flows to the inlet 26 of the heater 13, where it is heated. From the heater 13, the working fluid flows to the inlet 27 of the expander 14. The working fluid is expanded in the expander 14 to produce the work. The working fluid at the outlet 28 of the expander 14 is consequently lower in pressure and temperature. In the embodiment shown in Figure 1, the conditions of the working fluid at the outlet 28 of the expander 14 are such that both the first and second components are a gas.
  • the working fluid from the outlet 28 of the expander 14 is received by the condensing side 25 of the recuperator 15 where the second component of the working fluid substantially condenses as it loses energy to the working fluid on the boiling side 24.
  • the recuperator 15 is also arranged to act as a separator on the condensing side to provide a separation of a liquid fraction of the working fluid (the second component) from a gaseous fraction (primarily the first component) .
  • the condenser 16 may be a shell and tube heat exchanger but alternatively may be a radiator, a finned cooling coil with cooling fluid in serpentine coils, located inside a plenum with condensate recovery or any other suitable condenser.
  • Cooling fluid 29 (possibly air, water or refrigerant of any composition at or below ambient conditions) flows through the other side of the condenser 16, cooling the working fluid so that most of the (remaining) second component of the working fluid is condensed into a liquid.
  • the liquid second component is separated from the first component in the condenser 16, which is thus acting as a separator.
  • the separated second component 30, is recycled to the pump 19.
  • the remaining working fluid which comprises the first component and any of the second component remaining as a gas flows to the inlet 20 to the compressor 12.
  • the liquid fraction of the working fluid exiting the condensing side 25 of the recuperator 15 may bypass the condenser 16 and flow to the pump 19 as shown in Figure 1.
  • the liquid fraction of the working fluid exiting the condensing side 25 of the recuperator 15 may also be sent to the condenser 16.
  • the pump 19 pumps the liquid second component from the condenser 16 and the recuperator 15 back to the apparatus 11.
  • the energy transfer in the recuperator 15 is controlled to maintain the optimum system efficiency using an energy transfer controller. This is compared to conventional heat engines in which it is the conditions across the expander 14 that are controlled.
  • Temperature and pressure sensors at the inlets and outlets of both the condensing and boiling sides 24, 25 of the recuperator 15 monitor the conditions across the recuperator 15.
  • the energy transfer in the recuperator 15 is subsequently controlled by changing the conditions at the inlet of the expander and subsequently the expansion done in the expander 14 and hence the conditions at the outlet 28 of the expander 14.
  • the conditions at the inlet of the expander may be changed by, for example, changing the amount of compression carried out in the compressor 12 and/or pump 19 as well as changing the amount of heat transfer to the working fluid in the heater 13.
  • the energy transfer controller may also control the energy transferred in the recuperator 15 by changing the amount of the liquid second component combined with the first component in the apparatus 11.
  • the system 10 may also comprise a mass flow controller for controlling the mass flowrate of the second component relative to the mass flowrate of the first component. If the mass flow rate of the second component relative to the first component becomes too high, then the second component may not completely evaporate which could cause problems, particularly in the expander 14 if it is in the form of a turbine.
  • the mass flow controller may comprise variable speed controllers on the compressor 12 and pump 19, respectively.
  • the mass flow controller may comprise variable inlet guide vanes.
  • the mass flow controller may in addition to or alternatively comprise diverters on the compressor 12 and/or the pump 19 which divert flow from the outlet of the compressor and/or pump to their respective inlets.
  • the mass flow controller may also comprise appropriate valving on the apparatus 11.
  • the system may also comprise an energy storage unit located upstream from the compressor 12 for storing compressed working fluid from the compressor.
  • the energy storage unit may be used in particular during start-up of the system 10, during which the expander 14 is gradually increased from zero to full capacity. Rather than wasting the energy of the compressed working fluid from the compressor during this time, by bypassing the expander 14, some of the working fluid is diverted to the energy storage unit. The working fluid held in the energy storage unit can be reintroduced to the system cycle once the expander 14 has reached full capacity.
  • the system 10 may be started up by supplying power to the compressor, pump and expander shafts.
  • system controllers provide the system 10 with a high degree of operational flexibility, thus enabling the system 10 (in particular the expander 14) to closely follow the load 17 should it vary.
  • the mass flow controller enables the pump 19 and the compressor 12 to each be turned down to 30 - 50% of their full load.
  • the first and second components of the working fluid should be substances which are substantially inert with respect to each other, both chemically and physically, ie. they will not react with one another nor substantially dissolve in one another nor substantially dissociate at high temperatures. It is also desirable if the second component is a substance which has a high volumetric expansion ratio from liquid to gas. Further, it is also desirable if the first component is a substance which is highly compressible as a gas.
  • the first component may be nitrogen, argon, helium, hydrogen or methane for example.
  • the second component may be water, propane, butane, ethanol or carbon dioxide for example.
  • a preferred working fluid is nitrogen as the first component and water as the second component. It is noted that the working fluid may comprise more components than the first and second components, ie. different substances. However, these additional components will each generally follow the flow path of either the first component (as a gas) or the second component (as a liquid and a gas) in the system 10 as described above.
  • the heater 13 is shown in an embodiment, as a regenerative heater. It is noted that in other embodiments, the heater 13 may be a heat exchanger or another type of suitable heater.
  • the heater 13 of Figure 2 comprises first, second and third volumes 40, 41, and 42 respectively, of material. It is readily understood that the heater 13 may comprise less or more volumes of material to that shown in Figure 2.
  • the heater 13 also comprises passages through the volumes 40, 41, 42 of material for the flow therethrough of the working fluid.
  • the working fluid is thus heated by the volumes 40, 41, 42 of material.
  • the passages are arranged for the working fluid to flow through the volumes 40, 41, 42 of material in series.
  • the passages may be arranged for the working fluid to flow through the volumes 40, 41, 42 of material in parallel.
  • the volumes of material 40, 41, 42 are heated using a heating fluid flowing through spaces through the volumes of material 40,
  • the heating fluid may be steam or any other heated medium generated by nuclear power, coal or other combustible fuel or hot exhaust gasses from a gas turbine.
  • the volumes 40, 41, 42 of material may be heated using any other suitable means, such as waste heat from another process, direct heating from a furnace, electrical or solar thermal heat.
  • the passages through which the working fluid flow are separate from the spaces through which the heating fluid flow. This enables continuous operation of the heater 13 as well as preventing any mixing of the two fluids, which avoids problems such as contamination, particularly dust contamination, oxygenation and carbonation of the working fluid.
  • the materials in the volumes 40, 41, 42 may be different and in one embodiment are of progressively decreasing melting temperatures from the first volume 40 to the third volume 42.
  • phase change materials or "PCMs”. Any suitable phase change materials may be employed.
  • the first volume 40 contains silicon, which has a melting temperature of about 1410 0 C
  • the second volume 41 contains lithium fluoride, which has a melting temperature of about 870 0 C
  • the third volume 42 contains magnesium oxide or calcite, which have a melting temperature of about 560 0 C.
  • the volumes of material 40, 41, 42 are all held in containers, which are of a material which is able to withstand the temperatures of the molten materials held therein.
  • a particularly suitable material in this regard is a ceramic material, preferably silicon carbide.
  • the volumes of material are a ceramic material, preferably silicon carbide.
  • each volume of material 40, 41, 42 may contain a mixture of two or more different materials.
  • each volume of material 40, 41, 42 comprises the mixture of the same materials but at different ratios.
  • the different ratios preferably have different melting temperatures, thus providing the graduated heating of the working fluid flowing through the volumes of material 40, 41, 42.
  • at least one of the materials in the mixture of materials of each volume is for affecting the melting temperature of the volumes of material.
  • aluminium may be mixed with silicon to reduce the melting temperature of the silicon.
  • one of the materials in the mixture of materials may be for improving the heat transfer of the volume of material.
  • Such a material for example is graphite, which may be added to salts for example such as lithium fluoride, magnesium oxide, calcite or sodium chloride to improve the heat transfer of these materials.
  • salts for example such as lithium fluoride, magnesium oxide, calcite or sodium chloride.
  • the working fluid flows counter-currently to the heating fluid, entering the heater 13 through the inlet 26 to be heated firstly by the lowest temperature volume of material, in this case the third volume 42, and finally by the highest temperature volume of material, in this case the first volume 40 before exiting to the inlet 27 of the expander 14.
  • the heating fluid heats the volumes 40, 41, 42 in reverse order, that is, it enters the heater 13 through inlet 43 to heat the first volume 40, which is required to be at the highest temperature, first and heats the third volume 42 last.
  • the material in each or two of the volumes 40, 41, 42 is the same.
  • the volumes may not be as readily heated to at or above the melting temperature of the material using the heating fluid in series because as the heating fluid flows through the heater 13, it loses energy and heat as it flows through the volumes 40, 41, 42.
  • the volumes 40, 41, 42 in this embodiment may need to be heated in parallel or alternatively by a different source of heat.
  • the heater 13 also comprises a number of valves 45 on the inlets and outlets to the heater 13 which can be used to control the flow rate of the working fluid and the heating fluid through the heater 13 to maintain the temperature of the phase change materials in the volumes 40, 41, 42 so as to keep them in a molten phase and to control the temperature of the working fluid as it leaves the heater.
  • the flowrate of the working fluid is also controlled with respect to its temperature at the outlet of the heater 13 (ie. the inlet 27 to the expander 14) .
  • the temperature of the working fluid required at the inlet 27 of the expander is much less than the melting temperature of silicon (and hence the temperature of the first volume 40) .
  • the heater 13 advantageously enables quick start-up of the heat engine system 10.
  • the expander inlet temperatures can be varied and controlled by a modulating bypass control valve that diverts flow around the regenerative heater 13. This will allow the precise setting of expander inlet temperatures with variable output. This level of temperature control cannot be achieved with conventional gas turbines that rely on internal combustion. Also, when this control is used with the other control elements as described previously, good efficiency is attained when the system is turned down.
  • a model of a heat engine system according to embodiments of the present invention was constructed in HYSYS ® .
  • Figure 3 provides a schematic view of the model. The model was prepared on the basis of an approximately
  • the model system was calculated to produce a net shaft power output of 0.9736 MW at 58.95% efficiency.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention concerne un système de moteur thermique permettant de produire de l'énergie mécanique par expansion d'un fluide de travail comprenant un premier et un second composant. Ce système comprend un appareil servant à combiner le second composant du fluide de travail sous forme de liquide avec le premier composant, le premier composant étant un gaz circulant dans tout le système; un compresseur pour comprimer le premier composant; une pompe pour comprimer au moins la majeure partie du second composant; un réchauffeur pour chauffer le premier et le second composant; un dispositif d'expansion pour dilater le premier et le second composant pour produire l'énergie mécanique; ainsi qu'un récupérateur pour transférer au moins une partie de l'énergie du fluide de travail en provenance de la sortie du dispositif d'expansion au fluide de travail en provenance de la sortie de l'appareil, une partie substantielle de l'énergie transférée dans le récupérateur représentant au moins une partie de la chaleur latente du second composant en provenance de la sortie du dispositif d'expansion.
EP07800206A 2006-08-25 2007-08-24 Système de moteur thermique Withdrawn EP2057353A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
AU2006904633A AU2006904633A0 (en) 2006-08-25 A heat engine system and a regenerative heater
AU2006904634A AU2006904634A0 (en) 2006-08-25 A heat engine system
PCT/AU2007/001226 WO2008022406A1 (fr) 2006-08-25 2007-08-24 Système de moteur thermique

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EP2057353A1 true EP2057353A1 (fr) 2009-05-13

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EP (1) EP2057353A1 (fr)
AU (1) AU2007288134A1 (fr)
BR (1) BRPI0716589A2 (fr)
EA (1) EA014465B1 (fr)
WO (1) WO2008022406A1 (fr)

Families Citing this family (61)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2419621A4 (fr) 2009-04-17 2015-03-04 Echogen Power Systems Système et procédé pour gérer des problèmes thermiques dans des moteurs à turbine à gaz
EP2446122B1 (fr) 2009-06-22 2017-08-16 Echogen Power Systems, Inc. Système et procédé pour gérer des problèmes thermiques dans un ou plusieurs procédés industriels
US8247915B2 (en) 2010-03-24 2012-08-21 Lightsail Energy, Inc. Energy storage system utilizing compressed gas
US8436489B2 (en) 2009-06-29 2013-05-07 Lightsail Energy, Inc. Compressed air energy storage system utilizing two-phase flow to facilitate heat exchange
US8146354B2 (en) 2009-06-29 2012-04-03 Lightsail Energy, Inc. Compressed air energy storage system utilizing two-phase flow to facilitate heat exchange
US8196395B2 (en) 2009-06-29 2012-06-12 Lightsail Energy, Inc. Compressed air energy storage system utilizing two-phase flow to facilitate heat exchange
CN102483010B (zh) 2009-07-10 2015-03-18 埃塔里姆有限公司 用于在热能与机械能之间进行转换的斯特林循环转换器
WO2011017476A1 (fr) 2009-08-04 2011-02-10 Echogen Power Systems Inc. Pompe à chaleur avec collecteur solaire intégré
US8869531B2 (en) 2009-09-17 2014-10-28 Echogen Power Systems, Llc Heat engines with cascade cycles
US8613195B2 (en) 2009-09-17 2013-12-24 Echogen Power Systems, Llc Heat engine and heat to electricity systems and methods with working fluid mass management control
US9115605B2 (en) 2009-09-17 2015-08-25 Echogen Power Systems, Llc Thermal energy conversion device
US8813497B2 (en) 2009-09-17 2014-08-26 Echogen Power Systems, Llc Automated mass management control
US9243518B2 (en) * 2009-09-21 2016-01-26 Sandra I. Sanchez Waste heat recovery system
US20110271676A1 (en) * 2010-05-04 2011-11-10 Solartrec, Inc. Heat engine with cascaded cycles
WO2012019161A1 (fr) * 2010-08-05 2012-02-09 Cummins Intellectual Properties, Inc. Refroidissement de charge critique en termes d'émissions utilisant un cycle organique de rankine
CN103562535A (zh) 2010-11-18 2014-02-05 埃塔里姆有限公司 斯特林循环换能装置
US8616001B2 (en) 2010-11-29 2013-12-31 Echogen Power Systems, Llc Driven starter pump and start sequence
US8857186B2 (en) 2010-11-29 2014-10-14 Echogen Power Systems, L.L.C. Heat engine cycles for high ambient conditions
DE102012101862A1 (de) * 2011-05-28 2012-11-29 Ed. Züblin Ag Mehrteiliger Hochtemperaturwärmespeicher aus Speichermaterialien unterschiedlicher Temperaturbeständigkeit
US20120319410A1 (en) * 2011-06-17 2012-12-20 Woodward Governor Company System and method for thermal energy storage and power generation
US9745899B2 (en) * 2011-08-05 2017-08-29 National Technology & Engineering Solutions Of Sandia, Llc Enhancing power cycle efficiency for a supercritical Brayton cycle power system using tunable supercritical gas mixtures
WO2013055391A1 (fr) 2011-10-03 2013-04-18 Echogen Power Systems, Llc Cycle de réfrigération du dioxyde de carbone
GB201207497D0 (en) * 2012-04-30 2012-06-13 Isentropic Ltd Valve control
US20150121866A1 (en) * 2012-05-03 2015-05-07 International Engine Intellectual Property Company Llc Rankine cycle mid-temperature recuperation
CA2882290A1 (fr) 2012-08-20 2014-02-27 Echogen Power Systems, L.L.C. Circuit de fluide de travail super critique comprenant une turbopompe et une pompe de demarrage en une configuration en serie
US8820083B2 (en) * 2012-09-26 2014-09-02 Supercritical Technologies, Inc. Thermodynamic cycle with compressor recuperation, and associated systems and methods
US9118226B2 (en) * 2012-10-12 2015-08-25 Echogen Power Systems, Llc Heat engine system with a supercritical working fluid and processes thereof
US9341084B2 (en) 2012-10-12 2016-05-17 Echogen Power Systems, Llc Supercritical carbon dioxide power cycle for waste heat recovery
WO2014117068A1 (fr) 2013-01-28 2014-07-31 Echogen Power Systems, L.L.C. Procédés permettant de réduire l'usure des composants d'un système de moteur thermique au démarrage
EP2948649B8 (fr) 2013-01-28 2021-02-24 Echogen Power Systems (Delaware), Inc Procédé de commande d'un robinet de débit d'une turbine de travail au cours d'un cycle de rankine supercritique au dioxyde de carbone
CA2903784C (fr) * 2013-03-04 2021-03-16 Echogen Power Systems, L.L.C. Systemes de moteur thermique possedant des circuits de dioxyde de carbone supercritique a haute energie nette
EP2971621B1 (fr) * 2013-03-14 2020-07-22 Echogen Power Systems LLC Système de gestion de masse pour un circuit de fluide actif supercritique
US9540961B2 (en) 2013-04-25 2017-01-10 Access Energy Llc Heat sources for thermal cycles
US20150000260A1 (en) * 2013-06-26 2015-01-01 Walter F. Burrows Environmentally friendly power generation process
US9874112B2 (en) * 2013-09-05 2018-01-23 Echogen Power Systems, Llc Heat engine system having a selectively configurable working fluid circuit
WO2015034987A1 (fr) * 2013-09-05 2015-03-12 Echogen Power Systems, L.L.C. Système de moteur thermique ayant un circuit de fluide de travail pouvant être conçu de façon sélective
US20150107249A1 (en) * 2013-10-22 2015-04-23 Access Energy Llc Extracting Heat From A Compressor System
JP6217426B2 (ja) * 2014-02-07 2017-10-25 いすゞ自動車株式会社 廃熱回収システム
WO2016073252A1 (fr) 2014-11-03 2016-05-12 Echogen Power Systems, L.L.C. Gestion de poussée active d'une turbopompe à l'intérieur d'un circuit de circulation de fluide de travail supercritique dans un système de moteur thermique
JP6690822B2 (ja) * 2015-08-13 2020-04-28 ガス エクスパンション モーターズ リミテッド 熱力学エンジン
CN105317584B (zh) * 2015-11-12 2017-03-29 重庆长安汽车股份有限公司 汽车发动机能量回收系统及回收方法
US10724471B2 (en) * 2015-12-21 2020-07-28 Cummins Inc. Integrated control system for engine waste heat recovery using an organic Rankine cycle
CN105507971B (zh) * 2016-02-05 2017-04-19 江苏朗禾农光聚合科技有限公司 太阳能热动力储能系统
US10017032B2 (en) * 2016-02-16 2018-07-10 The Boeing Company Thermal management systems and methods
US11585608B2 (en) * 2018-02-05 2023-02-21 Emerson Climate Technologies, Inc. Climate-control system having thermal storage tank
US11149971B2 (en) 2018-02-23 2021-10-19 Emerson Climate Technologies, Inc. Climate-control system with thermal storage device
IT201800006187A1 (it) 2018-06-11 2019-12-11 System for recovering waste heat and method thereof/sistema per recuperare calore residuo e relativo metodo
US10883388B2 (en) 2018-06-27 2021-01-05 Echogen Power Systems Llc Systems and methods for generating electricity via a pumped thermal energy storage system
US11346583B2 (en) 2018-06-27 2022-05-31 Emerson Climate Technologies, Inc. Climate-control system having vapor-injection compressors
US12152508B2 (en) * 2018-07-23 2024-11-26 Javier Carlos Velloso Mohedano Facility for generating mechanical energy by means of a combined power cycle
EP3670853A1 (fr) * 2018-12-17 2020-06-24 CTB Clean Tech Brokers IVS Appareil de pompe à chaleur et réseau de chauffage urbain comprenant un appareil de pompe à chaleur
JP7493346B2 (ja) * 2020-02-03 2024-05-31 三菱重工コンプレッサ株式会社 回転機械
US11435120B2 (en) 2020-05-05 2022-09-06 Echogen Power Systems (Delaware), Inc. Split expansion heat pump cycle
EP4150196B1 (fr) * 2020-05-13 2023-11-01 Just in Time Energy Co. Cycle d'énergie de recondensation pour regazéification de fluide
US11629638B2 (en) 2020-12-09 2023-04-18 Supercritical Storage Company, Inc. Three reservoir electric thermal energy storage system
CN112832907B (zh) * 2021-03-31 2023-08-11 西安热工研究院有限公司 一种混合物跨临界循环太阳能光热发电系统及方法
CN113431654A (zh) * 2021-05-31 2021-09-24 国投云顶湄洲湾电力有限公司 一种冷凝热回收利用装置及其工作方法
CN114484398B (zh) * 2022-02-25 2023-09-29 上海诺通新能源科技有限公司 一种带储热功能的热泵蒸汽供应系统
US11814963B2 (en) 2022-03-14 2023-11-14 Argyle Earth, Inc Systems and methods for a heat engine system
AU2024289421A1 (en) 2023-02-07 2025-09-11 Supercritical Storage Company, Inc. Waste heat integration into pumped thermal energy storage
CN119085143B (zh) * 2024-08-30 2025-07-04 内蒙古电力勘测设计院有限责任公司 一种光火储耦合互补调峰系统及预测方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6052996A (en) * 1998-02-13 2000-04-25 Clark; John C. Heat-work cycle for steam cycle electric power generation plants
JP2002371861A (ja) * 2001-06-12 2002-12-26 Ishikawajima Harima Heavy Ind Co Ltd 蒸気噴射ガスタービン発電装置
WO2006028444A1 (fr) * 2004-09-02 2006-03-16 Terran Technologies, Inc. Moteur thermique basse temperature
CA2479985A1 (fr) * 2004-09-17 2006-03-17 Eric L. Bibeau Systeme ameliore de conversion energetique a partir d'un flux de fluide thermique

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2008022406A1 *

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BRPI0716589A2 (pt) 2013-10-01
EA200970217A1 (ru) 2009-08-28
EA014465B1 (ru) 2010-12-30
WO2008022406A1 (fr) 2008-02-28
AU2007288134A1 (en) 2008-02-28
US20100287934A1 (en) 2010-11-18

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