EP2880268A2 - Procédé et dispositif servant à produire de l'énergie électrique - Google Patents

Procédé et dispositif servant à produire de l'énergie électrique

Info

Publication number
EP2880268A2
EP2880268A2 EP13792251.4A EP13792251A EP2880268A2 EP 2880268 A2 EP2880268 A2 EP 2880268A2 EP 13792251 A EP13792251 A EP 13792251A EP 2880268 A2 EP2880268 A2 EP 2880268A2
Authority
EP
European Patent Office
Prior art keywords
air
liquid
heat exchanger
refrigerant
temperature level
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Withdrawn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
EP13792251.4A
Other languages
German (de)
English (en)
Inventor
Alexander Alekseev
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Priority to EP13792251.4A priority Critical patent/EP2880268A2/fr
Publication of EP2880268A2 publication Critical patent/EP2880268A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/14—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the cycle used, e.g. Stirling cycle
    • 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
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B11/00—Compression machines, plants or systems, using turbines, e.g. gas turbines
    • F25B11/02—Compression machines, plants or systems, using turbines, e.g. gas turbines as expanders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0251—Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation

Definitions

  • the invention relates to a method and apparatus for generating electrical energy according to the preamble of patent claim 1 and a corresponding device.
  • a “cryogenic liquid” is understood to mean a liquid whose boiling point is below the ambient temperature and, for example, is 220 K or lower, in particular lower than 200 K.
  • the cryogenic liquid can be used in its function as a "high pressure stream"
  • the "heat exchanger system” serves to cool the feed air of the
  • Air treatment plant in indirect heat exchange with one or more cold streams. It may be formed from a single or multiple parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • Methods and apparatuses which use liquid air or liquid nitrogen to regulate the network and provide control power in power grids.
  • the ambient air is liquefied in an air separation plant with integrated condenser or in a separate liquefaction plant and stored in a liquid tank designed as a cryogenic storage tank.
  • the liquefied air is removed from the store, brought to the higher pressure in a pump, then warmed to about ambient or higher. This warm high pressure air is then in a
  • Relaxation unit consisting of a turbine or several turbines with intermediate heating to ambient pressure relaxed.
  • the mechanical energy generated in the turbine unit becomes electrical energy in a generator
  • CONFIRMATION COPY converted and fed as particularly valuable energy into the electrical grid.
  • Such systems are described in WO 2007096656 and in DE 3139567 A1.
  • the deep-cold liquid under very high pressure (200 bar) becomes indirect in the heat exchanger system
  • the cold of the cryogenic liquid is thus on two different
  • Heat transfer medium such as atmospheric air or hot (water) steam goes the
  • the first phase (energy storage / liquefaction) of the process according to US 2001004830 A1 consists of several steps: the incoming air (10 to 15 bar) is first brought into indirect heat exchange with the second liquid refrigerant and cooled (to -150 ° C), then compressed (up to 40 bar), thereby warmed (-60 ° C at the outlet) and then brought into indirect heat exchange with the first liquid refrigerant and cooled again (to -170 ° C).
  • the invention has for its object to improve such a system in terms of its efficiency and in particular to allow a relatively simple apparatus design. This object is solved by the characterizing features of claim 1. According to the invention occurs in the first mode of operation in the
  • Air compression unit compressed feed air in the heat exchanger system under the same pressure in indirect heat exchange with the first liquid refrigerant and with the second liquid refrigerant. So there is no need to use a machine to increase the pressure between the heat exchange with the first brine and the heat exchange with the second brine. This reduces the number of hardware components such as heat exchangers, turbines and / or compressors; the costs for the entire liquid storage system are reduced and increases the efficiency of this application.
  • Heat exchangers, coolers, adsorbers, etc. are.
  • Both brine are warmed in the invention in the first operating mode to the same temperature level T2 or T4, from which they are cooled in the second operating mode from. Conversely, they are in the second
  • Temperature is to be understood, but a temperature band of a width of up to 20 K.
  • the goal is, of course, the smallest possible temperature difference between the two operating modes.
  • the temperature levels are preferably in the following ranges: T1 (first refrigerant, lower level):
  • T2 (second refrigerant, upper level):
  • T3 (second refrigerant, lower level):
  • T4 (second refrigerant, upper level):
  • the two refrigerants differ in their chemical composition, in particular in their boiling point. They must be selected so that they are fluid throughout their workspace. Suitable for this purpose are, for example, ethanol (C 2 H 5 OH) as the first (warmer) refrigerant and propane (C 3 H 8 ) as the second (colder) refrigerant.
  • ethanol C 2 H 5 OH
  • propane C 3 H 8
  • the substances listed in the following table for use in the invention as the first or second refrigerant in the invention in question.
  • liquid refrigerants and mixtures thereof can be used in the invention. This can do that
  • Heat exchange diagram to be further optimized; However, the apparatus and control engineering effort is higher.
  • liquid reservoirs of liquid refrigerant are provided for each of the temperature levels of one.
  • cooled coolant is available at the same temperature level for the first operating mode for cooling (and vice versa).
  • the heating and cooling of the brine is carried out in the heat exchanger system of the air treatment plant, anyway for the cooling of the Feed air in the first operating mode and the heating of the cryogenic liquid in the second operation is present.
  • mechanical energy is generated from the high-pressure storage fluid in the second operating mode by either the storage fluid itself or a fluid derived from it in the gas expansion unit is expanded to perform work.
  • the derived fluid may be formed, for example, by a mixture of the storage fluid with one or more other fluids, or by a reaction product of the storage fluid with one or more other substances.
  • the latter can be formed, for example, by combustion exhaust gas, if the storage fluid contains oxygen and is used to burn a fuel.
  • the heating of the first refrigerant in the first operating mode is
  • the same pumps can be used, one for the transport of the first and the second
  • the temperature ranges of the two brine can basically be disjoint (T4 ⁇ T1). Preferably, however, they overlap each other by the first
  • Temperature level T1 is more than 18 K, in particular 20 to 70 K below the fourth temperature level T4. This allows a particularly effective optimization of the heat exchange diagram.
  • the air compression unit in the second operating mode, can be switched off; In this case, heat for (pseudo) evaporation of the cryogenic liquid is supplied solely by the natural gas to be liquefied. In many cases, however, it may be favorable, albeit in the second operating mode Compressed air compressed in the air compression unit and cooled in the heat exchanger system. It appears unfavorable at first, in the second
  • Air compression unit does not have to be switched off and on when switching between the operating modes, but continues to run continuously.
  • the compressed amount of feed air can be obtained as high-pressure gas and from this additional electrical energy can be obtained.
  • a "gas turbine system” comprises a gas turbine (gas turbine expander) and a combustion chamber. In the gas turbine, hot gases are released from the combustion chamber to perform work.
  • the gas turbine system may also include a gas turbine driven gas turbine compressor. Some of the mechanical energy generated in the gas turbine is usually used to drive the gas turbine compressor. Another part is regularly converted to generate electrical energy in a generator. At least part of the generation of mechanical energy from the gaseous high-pressure storage fluid is carried out in this variant in the gas turbine system of the power plant, ie in an already existing in the power plant apparatus for converting pressure energy into mechanical drive energy. An additional separate system for work-performing expansion of the high-pressure storage fluid may be less complicated in the invention or completely omitted. In the simplest case, in the invention, the entire generation of mechanical energy from the gaseous high-pressure storage fluid in the
  • the high-pressure storage fluid is then, for example, under the pressure at which it (pseudo) is evaporated, the
  • the gas expansion unit has a hot gas turbine system which has at least one heater and one hot gas turbine.
  • the generation of electrical energy from the gaseous high-pressure storage fluid is at least partially carried out as a work-performing expansion in a hot gas turbine system having at least one heater and a hot gas turbine.
  • the generation of energy from the high pressure storage fluid takes place outside of the gas turbine system.
  • the "hot gas turbine system” may be formed in one stage with a heater and a single-stage turbine. Alternatively, it may have multiple turbine stages, preferably with reheat. In any case, it makes sense to provide another heater behind the last stage of the hot gas turbine system.
  • Hot gas turbine system is preferably coupled to one or more generators for generating electrical energy.
  • heating is meant a system for indirect heat exchange between a heating fluid and the gaseous storage fluid. This can transfer residual heat or waste heat to the storage fluid and to generate energy in the
  • Hot gas turbine system can be used.
  • Gas expansion unit has both one or more hot gas turbines and one or more gas turbine systems.
  • the high-pressure gaseous storage fluid is expanded in two steps, wherein the first step as work-performing relaxation in the hot gas turbine system and the second step in the
  • Gas turbine system can be performed, wherein the high pressure gaseous storage fluid fed to the hot gas turbine system and there to a
  • the air treatment plant in which in the first operating mode the cryogenic
  • Liquid is generated, may be formed as a cryogenic air separation plant or as an air liquefaction plant.
  • a "cryogenic air separation plant” is charged with atmospheric air and has a distillation column system for decomposing atmospheric air into its physical components, particularly nitrogen and oxygen.
  • the feed air is first cooled to near its dew point and then introduced into the distillation column system.
  • the distillation column system of the invention may be configured as a one-column nitrogen-oxygen separation system, as a two-column system (e.g.
  • Example as classic Linde double column system or as a three- or multi-column system. It may, in addition to the columns for nitrogen-oxygen separation other devices for recovering high purity products and / or other air components, in particular of noble gases, for example, an argon and / or a krypton xenon recovery.
  • nitrogen-oxygen separation other devices for recovering high purity products and / or other air components, in particular of noble gases, for example, an argon and / or a krypton xenon recovery.
  • An "air liquefaction plant” does not contain a distillation column part. Incidentally, their construction corresponds to that of a cryogenic air separation plant with the discharge of a liquid product. Of course, liquid air can also be generated as a by-product in a cryogenic air separation plant.
  • the cryogenic liquid may be formed by liquefied air and / or liquid nitrogen, or generally by a fluid containing less oxygen than the atmospheric air. Also, a combination of two or more storage fluids of the same or different composition from the same air treatment plant or from a plurality of air treatment plants can be used in the invention.
  • nitrogen is meant herein pure or substantially pure nitrogen as well as a mixture of air gases whose nitrogen content is higher than that of the atmospheric air, for example, the liquid nitrogen has a nitrogen content of at least 90%, preferably at least 99%. All percentages here and below refer to the molar amount, unless stated otherwise.
  • the high pressure stream under the same superatmospheric pressure in the heat exchanger system (21) undergoes indirect heat exchange with the second liquid refrigerant and with the first liquid refrigerant. So there is no need to use a machine to increase the pressure between the heat exchange with the second brine and the heat exchange with the first brine.
  • Control device is here to be understood a device which the automatic control of the system at least during the first
  • FIGS. 2a and 2b show a more detailed illustration of a first embodiment of an air treatment plant which can be used in the invention
  • Figures 3a and 3b show a more detailed illustration of a second embodiment of an air treatment plant which can be used in the invention
  • FIGS. 2a and 2b show a more detailed illustration of a first embodiment of an air treatment plant which can be used in the invention
  • Figures 3a and 3b show a more detailed illustration of a second embodiment of an air treatment plant which can be used in the invention
  • Figure 4 possible embodiments of the gas expansion unit.
  • Air treatment plant 100 a liquid tank 200 and a gas expansion unit 300.
  • the first operating mode low-current phase - usually at night
  • atmospheric air AIR
  • feed air is used as feed air in the first operating mode
  • Air treatment plant 100 initiated.
  • a cryogenic liquid 101 is generated, which is formed for example as liquid air.
  • the air treatment plant is operated as a condenser (in particular as an air liquefier).
  • the cryogenic liquid 101 is introduced into the liquid tank 200, which is operated at a low pressure LP of less than 2 bar.
  • the feed air is sucked through a filter 1 by an air compression unit 2 and compressed to a pressure MP (4 to 8 bar, especially 5 to 8 bar), cooled in a pre-cooler 3 and dried in a Molsiebadsorber station 4 and cleaned of contaminants such as C02 and hydrocarbons.
  • the compressed and purified air is cooled in a heat exchanger system 21 and liquefied.
  • the cryogenic liquid 101 is led into the liquid tank 200.
  • the heat exchanger system 21 is shown very schematically in Figures 1a and 1b, further details being shown in Figures 2a to 3b.
  • a first cold refrigerant reservoir 151 contains liquid ethanol (C 2 H 5 OH) as a "first refrigerant" at a first temperature level T1 of -1 10 ° C under a low pressure of less than 2 bar.
  • the liquid first refrigerant is fed by means of a first brine pump 29 via line 161 at T1 into a first passage group of the heat exchanger system 21.
  • T2 liquid ethanol
  • T2 second, higher temperature level of 19 ° C again and in a first warm Refrigerant storage 152 is initiated, which is operated at the second temperature level and also at a low pressure of less than 2 bar.
  • a second cold refrigerant reservoir 153 contains liquid propane (C 3 H 8 ) as a "second refrigerant" at a third temperature level T3 of -180 ° C under a low pressure of less than 2 bar.
  • the liquid second refrigerant is fed by means of a second brine pump 28 via line 163 at T3 in a second passage group of the heat exchanger system 21, at its cold end.
  • T4 liquid state
  • FIG. 1 b shows the second mode of operation (peak current phase - usually during the day).
  • the cryogenic liquid 103 for example, liquid air
  • Liquid tank 200 removed, brought in a pump 27 to an elevated pressure of HP1 (HP1 is greater than 12 bar, for example equal to about 60 bar), and as
  • the vaporized high pressure storage fluid 104 is pressurized to HP1
  • Gas expansion unit 300 passed.
  • the power P3 available at the gas expansion unit 300 in the second operating mode is, for example, 20 to
  • Passage groups of the heat exchanger system 21 are sent as in the first mode of operation, but in the opposite direction.
  • the first refrigerant is thereby conveyed via the pump 29 and line 162 from the first hot refrigerant reservoir 152 to the warm end of the heat exchanger system and after cooling from the second temperature level T2 to the first temperature level T1 via line 164 in introduced the first cold refrigerant reservoir 151.
  • the second refrigerant will be through the pump 28 and line 164 from the second warm
  • Refrigerant on the one hand and the evaporation of the high pressure current cryogenic liquid and the cold transfer to the brine on the other hand are carried out in the same process units.
  • the same apparatuses can thus be used. This results in a relatively low expenditure on equipment.
  • the air compression unit 2 can be switched off in a first embodiment during the second operating mode (see Figure 2b below); In a second embodiment variant (FIG. 3b, bottom), it continues to run in the second operating mode and supplies additional compressed air into the line 104 to the gas expansion unit 300.
  • a liquefaction phase (continuous operation in the first operating mode) and an evaporation phase (continuous operation in the second operating mode) can each take one to ten hours.
  • One or more evaporation and liquefaction phases can be run during one day.
  • the air treatment plant can be switched off in the transitional period between any two such phases.
  • FIGS. 2 a and 2 b show a possible design of the air treatment system 100 of FIG. 1, which is designed here as an air liquefier.
  • FIG. 2a again shows the first operating mode (the liquefaction phase).
  • ambient air AIR
  • MP 4 to 8 bar, in particular 5 to 8 bar
  • the compressed and purified air below MP is split into a first partial flow and a second partial flow.
  • the first partial flow is passed to a separate compressor, the cycle compressor 1 1 and there from the pressure MP to a higher pressure HP2 from 50 to 100 bar compressed, in an aftercooler to about
  • Phase separator (separator) 23 fed ..
  • the gaseous fraction from the phase separator 23 is passed through the heat exchanger system 21, there warmed up and out together with the air from the Molsiebadsorber station 4 to the suction port of the cycle compressor 1 1 and thus forms an air circuit ,
  • the second partial stream is recompressed in a secondary compressor 6a with aftercooler to a still higher pressure MP2 and then cooled in the heat exchanger system 12 from about ambient temperature to a first intermediate temperature of 140 to 180 K.
  • a turbine 5b the second partial flow is expanded to the low pressure LP (LP ⁇ 2 bar) to perform a work.
  • the after-compressor 5a is driven by the turbine 12b via a common shaft.
  • the working expanded second partial flow of feed air is reheated in the heat exchanger system 21 to ambient temperature and blown off into the atmosphere (amb).
  • a subset may also be used as the regeneration gas for the molecular sieve adsorber station 4.
  • the regeneration gas is warmed up by steam, electric heater or natural gas firing (heat quantity Q).
  • the Molsiebadsorber station 4 is not regenerated during the first operating mode, but only in the second operating mode. If the continuous operation in the first operating mode lasts less than about 6 hours, this is easily possible. The Molsiebadsorber station is then not switched within an operating mode; she can then also by means of a single
  • Adsorber container be realized or by means of several containers that are operated in parallel.
  • the liquid from the phase separator 23 is subcooled in a subcooler 24 and for the most part (101) as a cryogenic liquid in the liquid tank 200th directed.
  • a liquid air portion 26 is used, which is removed after the subcooling 24, relaxed in a throttle valve 25 to the pressure LP and passed together with the turbine exhaust gas through the heat exchanger system 21.
  • Air compression unit 2 and the Joule-Thomson stage (throttle valves, separator 23 and subcooler 24) turned off.
  • Liquid air (LAIR) 103 is removed from the liquid tank 200, brought in the pump 27 to the required pressure HP1, for example, 50 to 80 bar, preferably 40 to 80 bar, introduced as a high-pressure stream into the heat exchanger system 21 and there pseudo-evaporated and warmed to about ambient temperature.
  • HP1 for example, 50 to 80 bar, preferably 40 to 80 bar
  • the pseudo-evaporated air is finally sent to the gas expansion unit 300 as high-pressure gaseous storage fluid 104.
  • a part of the high-pressure gaseous storage fluid 104, a part of the high-pressure gaseous storage fluid heated in the gas expander 300, or a part of the exhaust gas of the gas expander 300 may be used as a regeneration gas (see FIG not shown in the drawing).
  • the heat exchanger system 21 of the air treatment system is used for both air liquefaction and brine heating (in the first operating mode) as well as for the air evaporation and refrigerant cooling (in the second operating mode).
  • the second variant of the invention is operated in the first operating mode according to FIG. 3 a like the first variant (FIG. 1 a).
  • FIG. 3b essentially corresponds to FIG. 1b, but here too, in the second operating mode, the air compression unit 2, the cycle compressor 11 and the turbine / compressor combination 5a / 5b remain in operation.
  • FIG. 4 shows possible embodiments of the gas expansion unit 300.
  • a conventional gas turbine is used for relaxation, the compressed air from the air treatment plant is fed into the gas turbine before the combustion chamber.
  • the heat of the flue gas at the outlet can be used in a heat recovery steam generator (HRSG) (4a); alternatively it is used differently, for example for preheating the compressed air from the air treatment plant (4b).
  • HRSG heat recovery steam generator
  • a rebuilt gas turbine is used for relaxation, in this gas turbine, the compressor part is removed.
  • the compressed air from the air treatment plant is fed into the combustion chamber of the rest of the gas turbine.
  • the heat of the flue gas can be used in a similar way to the gas turbine process.
  • the compressed air from the air treatment plant is first warmed up and expanded in several successively connected turbine / turbine stages; between the individual expansion stages, the air is additionally warmed up.
  • the embodiments 4a and 4b and 4c and 4d can be combined.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Motor Or Generator Cooling System (AREA)

Abstract

L'invention concerne un procédé et un dispositif servant à la production d'énergie électrique dans un système combiné de centrale électrique et d'installation de traitement de l'air. La centrale électrique comporte une première unité d'expansion de gaz (300) qui est reliée à un générateur pour la production d'énergie électrique. L'installation de traitement de l'air comporte une unité de compression de l'air (2), un système échangeur de chaleur (21) et un réservoir de fluide (200). Dans un premier mode de fonctionnement, de l'air de process est comprimé dans l'unité de compression de l'air (2) dans l'installation de traitement de l'air et est refroidi dans le système échangeur de chaleur (21) par échange avec un premier et un deuxième caloporteur froid; à partir de l'air de process comprimé et refroidi est produit un fluide accumulateur qui est stocké comme liquide cryogénique (101) dans le réservoir de fluide (200). Dans un deuxième mode de fonctionnement, du liquide cryogénique (103) est prélevé dans le réservoir de fluide (200) et est évaporé ou pseudo-évaporé sous une pression supérieure à la pression atmosphérique, et est réchauffé par échange dans le système échangeur de chaleur (21) avec un deuxième (164) et un premier caloporteur froid (162); le fluide accumulateur gazeux haute pression (104) ainsi produit est détendu dans l'unité d'expansion de gaz (300). Dans le premier mode de fonctionnement, dans le système échangeur de chaleur (21), l'air de process comprimé dans l'unité de compression de l'air (2) subit sous la même pression un échange de chaleur indirect avec le premier caloporteur froid liquide et le deuxième caloporteur froid liquide.
EP13792251.4A 2012-08-02 2013-08-02 Procédé et dispositif servant à produire de l'énergie électrique Withdrawn EP2880268A2 (fr)

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EP13792251.4A EP2880268A2 (fr) 2012-08-02 2013-08-02 Procédé et dispositif servant à produire de l'énergie électrique
PCT/EP2013/002305 WO2014026738A2 (fr) 2012-08-02 2013-08-02 Procédé et dispositif servant à produire de l'énergie électrique

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US9608498B2 (en) 2013-03-21 2017-03-28 Linde Aktiengesellschaft Method and device for generating electrical energy
EP2930322A1 (fr) * 2014-04-11 2015-10-14 Linde Aktiengesellschaft Procédé et installation de stockage et de récupération d'énergie
EP3032203A1 (fr) 2014-12-09 2016-06-15 Linde Aktiengesellschaft Procédé et installation combinée destinés à stocker et à récupérer l'énergie
EP3293475A1 (fr) * 2016-09-07 2018-03-14 Linde Aktiengesellschaft Procédé et appareil de stockage et de récupération d'énergie
DE202017004193U1 (de) 2017-08-10 2017-09-14 Linde Aktiengesellschaft Anlage zum Speichern und Rückgewinnen von Energie
GB201717040D0 (en) * 2017-10-17 2017-11-29 Innovatium Llp Compressed air storage
WO2022064533A1 (fr) * 2020-09-25 2022-03-31 Energy Dome S.P.A. Centrale et procédé de stockage d'énergie
WO2023244883A1 (fr) 2022-06-16 2023-12-21 Praxair Technology, Inc. Système et procédé de stockage d'énergie d'azote liquide

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DE19527882A1 (de) * 1995-07-29 1997-04-17 Hartmann Joerg Dipl Math Verfahren zur Energiespeicherung mittels flüssiger Luft
DE19757588A1 (de) 1996-12-24 1998-07-02 Hitachi Ltd Stromerzeugungssystem mit Gasturbine und Energiespeicher
US20090145130A1 (en) * 2004-08-20 2009-06-11 Jay Stephen Kaufman Building energy recovery, storage and supply system
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