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EP3032203A1 - Procédé et installation combinée destinés à stocker et à récupérer l'énergie - Google Patents

Procédé et installation combinée destinés à stocker et à récupérer l'énergie Download PDF

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Publication number
EP3032203A1
EP3032203A1 EP14004152.6A EP14004152A EP3032203A1 EP 3032203 A1 EP3032203 A1 EP 3032203A1 EP 14004152 A EP14004152 A EP 14004152A EP 3032203 A1 EP3032203 A1 EP 3032203A1
Authority
EP
European Patent Office
Prior art keywords
heat exchange
operating mode
transfer fluid
heat transfer
mode
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Withdrawn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
EP14004152.6A
Other languages
German (de)
English (en)
Inventor
Alexander Alekseev
Christoph Stiller
Brian Stöver
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
Mitsubishi Power Europe GmbH
Original Assignee
Linde GmbH
Mitsubishi Hitachi Power Systems Europe 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, Mitsubishi Hitachi Power Systems Europe GmbH filed Critical Linde GmbH
Priority to EP14004152.6A priority Critical patent/EP3032203A1/fr
Priority to EP15003246.4A priority patent/EP3037764B1/fr
Priority to US14/961,341 priority patent/US20160160694A1/en
Publication of EP3032203A1 publication Critical patent/EP3032203A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • 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
    • 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
    • F25J1/0015—Nitrogen
    • 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
    • F25J1/0017—Oxygen
    • 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
    • F25J1/002—Argon
    • 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"
    • F25J1/0042—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 liquid expansion with extraction of work
    • 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
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation

Definitions

  • the present invention relates to a method and a combination plant for storing and recovering energy, in particular electrical energy, according to the preambles of the respective independent claims.
  • cryogenic air liquefaction product is stored as cryogenic storage liquid in a storage system with cryogenic tanks.
  • cryogenic air liquefaction product other cryogenic fluids can also be stored in the storage system. This mode of operation occurs during a period of time, referred to herein as the energy storage period.
  • a cryogenic process fluid is formed from the cryogenic storage fluid, which may also comprise other cryogenic fluids.
  • the cryogenic process liquid is warmed up, if necessary after increasing the pressure by means of a pump, to about ambient temperature or higher and thus converted into a gaseous or supercritical state.
  • An obtained pressure stream is expanded in an energy recovery unit in one or more expansion turbines with reheating to ambient pressure.
  • the released mechanical power is converted into electrical energy in one or more generators of the power generation unit and converted into electrical energy Fed into the grid. This mode of operation occurs during a period of time, referred to herein as the energy recovery period.
  • the released during the transfer of the cryogenic process liquid in the gaseous or supercritical state during the energy recovery period cold can be stored and used during the energy storage period to provide cold for the recovery of the air liquefaction product.
  • So is out of the WO 2014/026738 A2 It is known to cool the compressed feed air used to obtain the air liquefaction product in the energy storage period countercurrent to two cooled organic refrigerants at two different temperature levels and to heat the described cryogenic process liquid against the then heated refrigerant in the energy recovery period, whereby the refrigerant is cooled again.
  • compressed air storage power plants in which air is not liquefied, but compressed in a compressor and stored in an underground cavern.
  • the compressed air from the cavern is directed into the combustion chamber of a gas turbine.
  • the gas turbine is supplied via a gas line fuel, such as natural gas, and burned in the atmosphere formed by the compressed air.
  • the formed exhaust gas is expanded in the gas turbine, thereby generating energy.
  • the present invention is further to be distinguished from methods and apparatus in which an oxygen-rich fluid is introduced to promote oxidation reactions in a gas turbine. Corresponding methods and devices operate with air liquefaction products containing greater than 40 mole percent oxygen.
  • the object of the present invention is therefore to provide an efficient and safer method of storing and recovering energy using an air liquefaction product.
  • the present invention proposes a method for storing and recovering energy and a corresponding combination system with the features of the independent patent claims.
  • Preferred embodiments are the subject of the dependent claims and the following description.
  • a “power generation unit” is understood here to mean a plant or a plant part which is or is set up for generating electrical energy.
  • an energy-generating unit comprises at least one expansion turbine, which is advantageously coupled to at least one electric generator.
  • a relaxation machine coupled to at least one electric generator is commonly referred to as a "generator turbine”. The mechanical power released during the expansion of a pressurized fluid in the at least one expansion turbine or generator turbine can be converted into electrical energy in the energy generation unit.
  • Air separation plants have distillation column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • distillation columns for the recovery of nitrogen and / or oxygen in the liquid and / or gaseous state for example, liquid oxygen, LOX, gaseous oxygen, GOX, liquid nitrogen, LIN and / or gaseous nitrogen, GAN
  • distillation columns for nitrogen-oxygen Separation distillation columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • the present invention may include recovering an air liquefaction product using compressed feed air.
  • the plant components used for this purpose can be summarized under the term "air treatment unit". This is understood in the parlance of the present application, a plant which is set up to obtain at least one air liquefaction product using compressed feed air. Sufficient for an air treatment unit for use in the present invention is that it can be obtained by this a corresponding cryogenic air liquefaction product, which can be used as a storage liquid and transferred to a storage system.
  • This may be an air separation plant, as explained above, but also only one pure "air liquefaction plant", which has no distillation column system.
  • an air liquefaction plant may correspond to that of an air separation plant with the discharge of an air liquefaction product.
  • liquid air can also be produced as an air liquefaction product in an air separation plant.
  • a gas other than air can also be used, a corresponding system is also referred to more generally herein as a "gas treatment unit".
  • An “air product” is any product that can be produced, at least by compressing and cooling air, and in particular, but not necessarily, by subsequent cryogenic rectification.
  • these may be liquid or gaseous oxygen (LOX, GOX), liquid or gaseous nitrogen (LIN, GAN), liquid or gaseous argon (LAR, GAR), liquid or gaseous xenon, liquid or gaseous krypton, liquid or gaseous neon , liquid or gaseous helium, etc. but also, for example, liquid air (LAIR).
  • the terms “oxygen”, “nitrogen”, etc. designate in each case also cryogenic liquids or gases which have the respectively named air component in an amount which is above that atmospheric air. It does not have to be pure liquids or gases with high contents.
  • an "air liquefaction product” here means a corresponding liquid product at cryogenic temperature.
  • gas product or “gas liquefaction product” which can not be produced or not only from air but also from another gas.
  • a “heat exchanger” is used for the indirect transfer of heat between at least two, for example, in countercurrent flows, such as a warm compressed air stream and one or more cold streams or a cryogenic liquid air product and one or more hot streams.
  • a heat exchanger may be formed from a single or multiple heat exchanger sections connected in parallel and / or in series, e.g. from one or more plate heat exchanger blocks. In this case it is a plate heat exchanger (English: Plate Fin Heat Exchanger).
  • a heat exchanger for example, the "main heat exchanger" of an air treatment plant through which the majority of the fluids to be cooled or heated to be cooled or heated, has “passages” formed as separate fluid channels with heat exchange surfaces and parallel and through other passages separated, are combined to “passage groups”.
  • a “heat exchange unit” may include one or more heat exchanger blocks or sections.
  • pressure level and "temperature level” to characterize pressures and temperatures, thereby indicating that corresponding pressures and temperatures in a given plant need not be used in the form of exact pressure or temperature values to realize the innovative concept.
  • pressures and temperatures typically range in certain ranges that are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about an average.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include unavoidable or expected pressure drops, for example, due to cooling effects.
  • the pressure levels indicated here in bar are absolute pressures.
  • the present invention has been described above and will be described below with reference to air as a working medium. However, it is also suitable for use with other similarly liquefiable media, for example nitrogen, oxygen, argon and mixtures of these gases.
  • the present invention is based on a method of storing and recovering energy using a combination plant comprising a gas treatment unit and a power generation unit.
  • a cryogenic gas liquefaction product can be produced and a storage liquid can be provided using the gas liquefaction product.
  • the gas treatment unit is an air treatment unit.
  • the invention is not limited to the use of air.
  • the storage liquid can be, for example, a corresponding liquid gas.
  • the use of compressed feed air as compressed feed gas is in particular liquid air and / or any other liquid air product which can be formed from appropriately compressed feed air.
  • such a method comprises, in a second operating mode using the storage liquid, providing a cryogenic process liquid which is heated in the heat exchange system to obtain a pressurized fluid, which is subsequently expanded to perform work in the energy production unit, for example, a generator turbine there.
  • the second operating mode may, for example, directly connect to the first operating mode, but other operating modes may be provided between the first and the second operating mode.
  • the method proposed according to the invention corresponds to the state of the art, in which a liquid air product is generated from air, stored and later vaporized to a corresponding pressure fluid.
  • the storage liquid does not have to be formed exclusively from the gas liquefaction product, including, for example, external, cryogenic liquefaction products or other streams may be provided, ie be fed for example in a corresponding storage system. Accordingly, the phrase that "using the storage liquid, a cryogenic process liquid is provided” include that the cryogenic process liquid may also be provided using additional, including, for example, external, cryogenic liquefaction products or other streams.
  • the invention provides to cool the compressed feed gas in a first heat exchange unit of the heat exchange system in the first operating mode in countercurrent to a heat transfer fluid and to heat the process liquid in the first heat exchange unit in the second operating mode in countercurrent to the heat transfer fluid.
  • a heat transfer fluid in the present invention has the particular advantage that additional organic refrigerants, which, as mentioned, may contain flammable hydrocarbons are not passed through the same heat exchanger as the compressed feed gas or the process liquid and therefore not in leaks with oxygen may come into contact, which is optionally contained in the compressed feed gas or the process liquid.
  • the heat transfer fluid used is preferably free of or poor in oxidizing and combustible components, in particular oxygen-free in the sense explained below.
  • the heat transfer fluid is thus advantageously neither fire-promoting nor self-combustible, "fire-promoting" a property of a fluid is understood to maintain under the prevailing conditions in a corresponding heat exchanger combustion even in the absence of atmospheric oxygen.
  • the present invention provides that the heat transfer fluid is at least partially cooled by means of at least two further, at different temperature levels and each with at least one organic refrigerant heat exchange units of the heat exchange system in the first mode of operation and heated in the second mode of operation.
  • the operating mode referred to herein as the "first mode of operation” is the aforementioned mode of operation in the energy storage period that a corresponding combination unit performs in excess-current periods when sufficient electrical energy is available to compress gas and provide a gas liquefaction product.
  • the "second operation mode” designates the operation mode in the energy recovery period, that is, in power-lacking phases in which a corresponding pressure fluid is generated using the gas liquefaction product generated in the first operation mode.
  • the invention contemplates that the directions in which the heat transfer fluid and the feed gas are passed through the first heat exchange unit in the first mode of operation are opposite to the directions in which the heat transfer fluid and the process liquid are passed through the first heat exchange unit in the second mode of operation become. This allows each of the temperature profiles, according to which a cooling or heating of corresponding fluids takes place close to each other, because the heat transfer fluid and the feed gas, which flow in countercurrent to each other through the first heat exchange unit, each with the lowest possible temperature difference passed through them can be.
  • the invention further provides that the heat transfer fluid and the compressed feed gas in the first operating mode at a first pressure level and the heat transfer fluid and the process fluid in the second operating mode are passed through the first heat exchange unit at a second pressure level, wherein the first pressure level by at least 5 bar above the second lies.
  • the operating pressures of the heat transfer fluid are different in the first and second modes of operation.
  • a pressure control device can be provided.
  • the pressure of the heat transfer fluid in each case depends on the pressure of the feed gas or the process fluid in the first heat exchange unit, so that a particularly effective heat transfer is also possible for this reason.
  • the present invention contemplates providing additional cold storage fluids in the form of the organic refrigerants but not formed from the feed gas .
  • the at least two further cold storage fluids, ie the organic refrigerants are preferably configured to store cold at different temperature levels, ie they have, for example, different boiling points which make them suitable for use at different temperatures.
  • the cooling of the compressed feed gas in the first operating mode is particularly efficient.
  • the present invention allows by using a total of at least three cold storage fluids, namely from the condensed feed gas formed gas liquefaction product, the use of which a storage liquid is provided, and the at least two organic refrigerant, such as hydrocarbons, a particularly efficient operation.
  • an oxygen-free or substantially oxygen-free gas mixture is advantageously used as the heat transfer fluid. It is understood that a correspondingly "oxygen-free" gas mixture may also contain residual oxygen contents, for example 1%, 0.5%, 0.1% or 0.01% oxygen or less. Correspondingly low oxygen contents sufficiently reduce the risk of ignition when in contact with a flammable organic refrigerant.
  • a fluid containing predominantly nitrogen, neon, helium and / or argon is used as the heat transfer fluid. This is particularly suitable because it is possible by the use of a corresponding fluid to set particularly high temperature profiles in the heat exchangers used and to minimize thermodynamic losses. An example of this is in the attached FIG. 5 illustrated.
  • the heat transfer fluid is at least partially evaporated during cooling of the compressed feed gas and at least partially liquefied when heating the process liquid.
  • the present invention does not explicitly relate to methods in which corresponding heat transfer fluids are expanded and recompressed to thereby generate refrigeration.
  • a corresponding heat transfer fluid is preferably conducted in a circuit in which a maximum pressure difference of at most 5 bar, in particular at most 1 bar, 0.5 bar or less, occurs. The extraction of cold is thus not using the heat transfer fluid itself, this is only used for heat transfer, so it is not refrigerated relaxed and / or recompressed.
  • the at least two further heat exchange units comprise a second heat exchange unit, which is operated with a first organic refrigerant, which is transferred between two storage tanks.
  • a corresponding The second heat exchange unit can, compared to a third heat exchange unit, as explained below, be set up for operation at higher temperatures and be operated with a corresponding organic refrigerant.
  • This is transferred between the two storage containers, as mentioned, one of which is designed as a "warm” and a "cold” storage container.
  • Corresponding storage containers are preferably designed as insulated tanks.
  • the first organic refrigerant from the "cold" storage tank is passed through the second heat exchange unit, where it cools the heat transfer fluid, and then transferred to the "warm” storage tank.
  • a transfer takes place conversely when the cryogenic process fluid is heated in the second operating mode.
  • halogenated or non-halogenated alkanes or alkenes, alcohols and / or aromatics are suitable as organic refrigerants for comparatively higher temperatures.
  • halogenated or non-halogenated alkanes or alkenes such as ethane, ethylene, propane, propylene, butane, pentane, hexane and possibly also higher hydrocarbons may be used.
  • Halogenated hydrocarbons are in particular fluorinated and / or chlorinated.
  • alcohols such as methanol, ethanol, propanol, butanol, pentanol, hexanol and other alcohols and aromatics such as toluene.
  • the at least two further heat exchange units may advantageously comprise a third heat exchange unit operated at a lower temperature with respect to the second heat exchange unit, preferably with a second organic refrigerant transferred between two heat storage tanks and with a third organic refrigerant is transferred between two storage containers.
  • the method according to the invention can comprise, in an advantageous embodiment, that the second and the third organic refrigerants are an identical organic refrigerant, so that the provision of different refrigerants can be dispensed with.
  • the second and / or third organic Refrigerant in the present invention a halogenated or non-halogenated alkane or alkene having at most four carbon atoms, which is suitable for very low temperatures.
  • the organic refrigerant (s) (the first, the second and / or the third organic refrigerant) are warmed in the first operating mode to the same ("upper") temperature level from which they are cooled in the second operating mode , Conversely, in the second mode of operation, they are or are cooled to the same ("lower”) temperature level from which they are warmed in the first mode of operation. Due to unavoidable losses, the term "same temperature level” is understood to mean not only exactly the same temperature, but a temperature band of a width of up to, for example, 20 ° C. Of course, the aim is to achieve the lowest possible temperature difference between the two operating modes.
  • the heat exchange diagrams of the heat exchange system of the gas treatment unit can be made particularly favorable.
  • the first organic refrigerant i. the refrigerant of the second heat exchange unit
  • the first organic refrigerant in the first operating mode from a lower temperature level at -100 to -30 ° C, in particular at -60 to -40 ° C, to an upper temperature level at 0 to 80 ° C, in particular at 20 to 50 ° C, heated, and is cooled in the second operating mode from the upper temperature level to the lower temperature level.
  • the second organic refrigerant i. one of the refrigerants of the third heat exchange unit, in the first operating mode from a first temperature level at -200 to -140 ° C., in particular at -196 to 150 ° C., to a second temperature level at -100 to -30 ° C., in particular at 60 to -40 ° C, heated, and is cooled in the second operating mode from the second temperature level to the first temperature level.
  • the third organic refrigerant which is also a refrigerant of the third heat exchange unit, in the first mode of operation of a third Temperature level at -200 to -140 ° C, especially at -196 to -150 ° C, to a fourth temperature level at -140 to -60 ° C, especially at -100 to -60 ° C, heated and in the second operating mode of cooled to the fourth temperature level to the third temperature level.
  • the second organic refrigerant on the first and third organic refrigerants is supplied at the third temperature level of the third heat exchange unit, and the second organic refrigerant on the second and the third organic refrigerants are taken out at the fourth temperature level thereof.
  • the second organic refrigerant on the second and third organic refrigerants at the fourth temperature level is advantageously supplied to the third heat exchange unit, and the second organic refrigerant on the first and third organic refrigerants is taken at the third temperature level thereof.
  • a corresponding combination system is advantageously designed for carrying out a corresponding method.
  • the second organic refrigerant is advantageously completely, the third performed only in a section through the third heat exchange unit. As also with reference to the attached FIG. 5 explained, this results in particularly favorable temperature gradients in the first heat exchange unit.
  • organic refrigerants used differ in their chemical composition, in particular in their boiling point. They must be selected so that they are fluid throughout their workspace.
  • organic refrigerants are explicitly in the table on page 5 of WO 2014/026738 A2 listed substances for use in the invention as a first, second and / or third organic refrigerant in question.
  • Organic refrigerants can also be the following refrigerants according to the common DuPont nomenclature (see DIN 8960 section 6.3.2), namely halogenated and non-halogenated hydrocarbons with one carbon atom such as R-10, R-11, R-12, R-12B1 , R-12B2, R-13, R-13B1, R-14, R-20, R-21, R-22, R-22B1, R-23, R-30, R-31, R-32, R -40, R-41 and R-50, with 2 carbon atoms such as R-110, R-111, R-112, R-112a, R-113, R-113a, R-114, R-114a, R-115, R-116, R-120, R-122, R-123, R-123a, R-123b, R-124, R- 124a, R-125, R-131, R-132, R-133a, R-134, R-134a, R-141, R-141b, R-142, R-142b, R-143,
  • a fourth heat exchange unit can be used, by means of which the heat transfer fluid is partially cooled in the first operating mode, and which is operated with further compressed feed gas, which is depressurized.
  • additional cold to cover cold losses can be generated, as it is also known in air separation plants, there in the form of a so-called turbine flow.
  • the present invention also extends to a combination energy storage and recovery system having all the means to make it suitable for carrying out a previously discussed method.
  • a combination energy storage and recovery system having all the means to make it suitable for carrying out a previously discussed method.
  • a third heat exchange unit is designed such that it supplied in the first mode of operation, the second organic refrigerant on the first and the third organic refrigerant at the third temperature level and the second organic refrigerant on the second and the third organic refrigerant on the fourth temperature level can be removed and this further supplied in the second operating mode, the second organic refrigerant on the second and the third organic refrigerant at the fourth temperature level and the second organic refrigerant can be removed on the first and the third organic refrigerant at the third temperature level.
  • Figure 1A 1 illustrates a combination plant according to an embodiment of the invention in a first operating mode in the form of a process flow diagram.
  • the combination system which in FIG. 1B in a second mode of operation is indicated generally at 100 and includes an air handling unit 110 and a power generation unit 120.
  • feed air in the form of a stream a is sucked in via a filter 1 by means of a main air compressor 2 with intercoolers not specifically designated.
  • the feed air of the stream a is compressed in the main air compressor 2, for example to a pressure of about 5 to 7 bar.
  • a correspondingly compressed stream, now designated b, is fed to a cooling unit 3 which is operated with cooling water flows which are not separately designated, where the previously supplied heat of compression is withdrawn from the stream b.
  • a correspondingly cooled stream, now denoted by c, is freed from the predominant part of the water and carbon dioxide contained in an adsorptive cleaning unit 4, which may comprise, for example, a pair of molecular sieve filled, not separately designated adsorber containers.
  • a stream purified in this way, now denoted d, is fed to a secondary compressor 5 and subsequently recompressed to a pressure of, for example, about 9 bar.
  • a correspondingly recompressed stream, now denoted by e, is fed into a heat exchange system of the air treatment unit, which is designated here in its entirety by 10.
  • the compressed feed air of the stream e in a first heat exchange unit 11 is cooled against a flow f of a heat transfer fluid to obtain a corresponding cooled flow g.
  • the cooled stream g is relaxed in the example shown in a generator turbine 12 and possibly one of these downstream, not separately designated expansion valve.
  • the correspondingly relaxed stream g is transferred to a separator tank 13, in the bottom of which a liquid fraction and at the top of which a gaseous fraction is formed.
  • the liquid fraction from the bottom of the separator tank 13 is transferred in the form of the flow h into a storage system 20 in which it is stored in the first operating mode.
  • the storage system 20 may, in addition to the stream h, as already mentioned above, also be charged with further liquid cryogenic streams.
  • the storage system 20 is removed in the first mode of operation in the example shown no fluid.
  • the gaseous fraction from the top of the separator tank 13 is withdrawn in the form of the stream i and heated in a further heat exchange unit 14, here referred to as the fourth heat exchange unit 14 in comparison with the second and third heat exchange units 16 and 18 explained below.
  • the fourth heat exchange unit In the fourth heat exchange unit
  • cooling of the current i can be transferred to a current k, which likewise comprises a heat transfer fluid and is combined with a further corresponding current I to the already mentioned current f of the heat transfer fluid.
  • a current k which likewise comprises a heat transfer fluid and is combined with a further corresponding current I to the already mentioned current f of the heat transfer fluid.
  • the current f and the currents k and I two partial circuits of a heat transfer fluid are formed, which are driven by a pump 15 and in this, as well as in the first heat exchange unit 11, are linked together. It is, as already emphasized, that in the mentioned subcircuits no cold-performing relaxation of a corresponding heat transfer fluid takes place, this essentially
  • the current I is before the union of the stream f and the feed into the heat exchanger 11 by means of the pump 15, and after the distribution of the current f into the currents k and I downstream of the heat exchange unit 11, ie at its warm end, through the already mentioned two further heat exchange units 16 and 18, namely the second heat exchange unit 16 and the third heat exchange unit 18, performed in which the current I is cooled by means of organic refrigerant, which are respectively provided by refrigerant units 17 and 19. Details of the heat exchange units 16 and 18 and the refrigerant units 17 and 19 are described with reference to FIGS FIGS. 2A and 2B or 3A and 3B explained.
  • a partial flow m can be branched off from the compressed feed air of the flow d, cooled in the heat exchanger 14 to an intermediate temperature, cooled in a non-separately designated generator turbine and returned through the heat exchanger 14.
  • a correspondingly recirculated stream can be used, for example, in the form of the stream n as regeneration gas in the adsorptive purification unit 4.
  • the current i can, for example, be combined with the current d upstream of the secondary compressor 5.
  • FIG. 1B is the combination plant 100, which is already in Figure 1A illustrated in the first mode of operation, shown in the second mode of operation.
  • the flow e is not provided, the main compressor 2 and the booster 5 may be out of operation or operated in a standby mode.
  • the adsorptive cleaning device 4 can during the in FIG. 1B illustrated second operating mode, for example, be regenerated. Accordingly, no cooled, compressed feed air is released in the generator turbine 12 and no fluid is transferred into the storage system 20.
  • Refrigerant circuit realized by the flow k through the fourth heat exchange unit 14 is typically not in operation here.
  • the storage system 20 in the form of the current o, so a storage fluid, taken and provided in the form of a cryogenic process fluid.
  • a cryogenic air liquefaction product was fed from the sump of the separator tank 13.
  • the current o is heated and evaporated in the second operating mode in the heat exchanger 11.
  • the current o transmits its cold to a current p, from the same heat transfer fluid of the currents f, k and I of the first operating mode according to Figure 1A is formed here, but here for the better distinctness is called divergent.
  • the refrigerant circuit realized by the flow p also includes the already mentioned second and third heat exchange units 16 and 18 or the associated refrigerant units 17 and 19, which are described in the following FIGS. 2A and 2B or 3A and 3B are explained.
  • a gaseous or supercritical pressurized fluid in the form of the stream q is provided, which is supplied to the energy generating unit 120.
  • the power q is released, for example, to perform work and generate electrical energy in a generator turbine 121.
  • the stream q may previously be passed through a heat exchanger 122 and heated therein by means of an exhaust gas stream of a combustion chamber 123 or a heat engine in which a fuel is burned with air or another oxygen-containing gas.
  • FIG. 2A is the second heat exchange unit 16 with the associated refrigerant unit 17 of the system 100, as shown in the Figures 1A and 1B is shown in the first and second modes of operation illustrated in the first mode of operation.
  • the second heat exchange unit 16 as already in Figure 1A illustrates the current I of the heat transfer fluid out.
  • a gaseous stream r is passed, which flows out of a first refrigerant reservoir 171, is cooled in the second heat exchange unit 16 and then flows into a second refrigerant reservoir 172.
  • the gaseous stream r is non-condensing gas, for example nitrogen, at the temperatures described above.
  • the flow r is provided by increasingly displacing corresponding gas from the first refrigerant reservoir 171.
  • an organic refrigerant is taken from the second refrigerant storage 172 by means of a pump 173 in liquid form, passed through the heat exchanger 16 and fed into the first refrigerant storage 171.
  • a corresponding stream of the organic refrigerant is designated s.
  • FIG. 2B is the second heat exchange unit 16 with the associated refrigerant unit 17, which in FIG. 2A shown in the first mode of operation, shown in the second mode of operation.
  • a current p of the heat transfer fluid is passed through the second heat exchange unit 16.
  • the guidance of an organic refrigerant or a superimposed gas in the storage containers 171 and 172 takes place with respect to the first operating mode, which in FIG. 2A is shown in the second operating mode, which in FIG. 2B is shown, in the opposite direction. Corresponding currents are therefore illustrated by r 'and s'.
  • FIGS. 3A and 3B is the third heat exchange unit 18 with the associated refrigerant unit 19 of the system 100, as shown in the Figures 1A and 1B shown in the first and second modes of operation illustrated in the first and second modes of operation.
  • refrigerant unit 19 There are two organic refrigerant streams, for example, include propane as a refrigerant used.
  • propane as a refrigerant used.
  • the basic operation of the refrigerant unit 19 has already been described with reference to FIGS FIGS. 2A and 2B explained.
  • the first mode of operation as in FIG. 3A is illustrated, is a first refrigerant flow t completely through the third heat exchange unit 18, a second refrigerant flow u only through a portion of this third Heat exchange unit 18 out.
  • Corresponding refrigerant accumulators and pumps are designated here by 191 to 196. Again, those in the second mode of operation, which are in FIG. 2B is illustrated, reversely guided refrigerant flows denoted by t 'and u'.
  • FIG. 4A illustrates a combination plant according to a further embodiment of the invention in the first operating mode in the form of a process flow diagram, wherein only the heat exchange system 10 is illustrated here, its integration into the combination plant essentially the same as in the combination plant 100 according to FIGS Figures 1A and 1B can be. Again is in FIG. 4A the first and in FIG. 4B the second operating mode of the combination system illustrated.
  • the recompressed flow e is determined according to FIG. 4A before or in the heat exchange system 10 divided into two partial streams and cooled in the first heat exchange unit 11 and the fourth heat exchange unit 14.
  • a current k as in Figure 1A is shown, does not exist.
  • the current I corresponds according to FIG. 4A the current f.
  • the cooled current g is formed by combining the partial currents of the current e.
  • the current g is, as already to Figure 1A explained, liquefied and stored.
  • the currents i and m have already been explained above.
  • FIG. 4B is the combination system that is in FIG. 4A illustrated in the first mode of operation, shown in the second mode of operation. To details not explained here is on FIG. 1B directed.
  • the fourth heat exchange unit 14 is not flowed through by a partial flow of the liquefied air product or the storage liquid formed therefrom. Only by the first heat exchange unit 11, as already to FIG. 2B explained, a current 1 led.
  • FIG. 5 a heat exchange diagram achievable in accordance with an embodiment of the invention is illustrated and indicated generally at 500.
  • an exchanged heat in kW is plotted on the abscissa and a temperature in K on the ordinate.
  • 501 is a heat exchange profile for the compressed feed air
  • 502 is a heat exchange profile for the storage liquid formed from the liquefied air product
  • 503 and 504 illustrates heat exchange profiles for the heat transfer fluid. It can be seen from the heat exchange diagram 500 that the invention enables a particularly narrow guide of the heat exchange profiles 501 and 503 or 503 and 504.

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EP14004152.6A 2014-12-09 2014-12-09 Procédé et installation combinée destinés à stocker et à récupérer l'énergie Withdrawn EP3032203A1 (fr)

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EP14004152.6A EP3032203A1 (fr) 2014-12-09 2014-12-09 Procédé et installation combinée destinés à stocker et à récupérer l'énergie
EP15003246.4A EP3037764B1 (fr) 2014-12-09 2015-11-14 Procede et installation combinee destines a stocker et a recuperer l'energie
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EP3557165A1 (fr) 2018-04-19 2019-10-23 Linde Aktiengesellschaft Procédé de fonctionnement d'un échangeur thermique, système doté d'un échangeur thermique et installation d'alimentation en air dotée d'un tel système
EP3587971A1 (fr) 2018-06-25 2020-01-01 Linde Aktiengesellschaft Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant
EP3594596A1 (fr) 2018-07-13 2020-01-15 Linde Aktiengesellschaft Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant
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EP3719428A1 (fr) 2019-04-05 2020-10-07 Linde GmbH Procédé de fonctionnement d'un échangeur de chaleur, dispositif doté d'un échangeur de chaleur et installation dotée du dispositif correspondant
WO2020200521A1 (fr) 2019-04-05 2020-10-08 Linde Gmbh Procédé pour faire fonctionner un échangeur de chaleur, ensemble pourvu d'un échangeur de chaleur et installation pourvue d'un ensemble correspondant
WO2021037391A1 (fr) 2019-08-23 2021-03-04 Linde Gmbh Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant

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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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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
EP3557165A1 (fr) 2018-04-19 2019-10-23 Linde Aktiengesellschaft Procédé de fonctionnement d'un échangeur thermique, système doté d'un échangeur thermique et installation d'alimentation en air dotée d'un tel système
WO2019201475A1 (fr) 2018-04-19 2019-10-24 Linde Aktiengesellschaft Procédé pour faire fonctionner un échangeur de chaleur, ensemble pourvu d'un échangeur de chaleur et installation de traitement d'air pourvue d'un ensemble correspondant
EP3587971A1 (fr) 2018-06-25 2020-01-01 Linde Aktiengesellschaft Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant
WO2020011396A1 (fr) 2018-07-13 2020-01-16 Linde Aktiengesellschaft Procédé destiné à faire fonctionner un échangeur de chaleur, système pourvu d'un échangeur de chaleur et installation de traitement d'air pourvue d'un système correspondant
EP3594596A1 (fr) 2018-07-13 2020-01-15 Linde Aktiengesellschaft Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant
DE102019201336A1 (de) * 2019-02-01 2020-08-06 Siemens Aktiengesellschaft Gasverflüssigungsanlage sowie Verfahren zum Betrieb einer Gasverflüssigungsanlage
EP3719428A1 (fr) 2019-04-05 2020-10-07 Linde GmbH Procédé de fonctionnement d'un échangeur de chaleur, dispositif doté d'un échangeur de chaleur et installation dotée du dispositif correspondant
WO2020200521A1 (fr) 2019-04-05 2020-10-08 Linde Gmbh Procédé pour faire fonctionner un échangeur de chaleur, ensemble pourvu d'un échangeur de chaleur et installation pourvue d'un ensemble correspondant
JP2022526970A (ja) * 2019-04-05 2022-05-27 リンデ ゲゼルシャフト ミット ベシュレンクテル ハフツング 熱交換器を動作させるための方法、熱交換器を有する構成、および対応する構成を有するシステム
US12044471B2 (en) 2019-04-05 2024-07-23 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement
WO2021037391A1 (fr) 2019-08-23 2021-03-04 Linde Gmbh Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant
US12241692B2 (en) 2019-08-23 2025-03-04 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement

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EP3037764B1 (fr) 2017-09-20
US20160160694A1 (en) 2016-06-09

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