[go: up one dir, main page]

US20160160694A1 - Process and combined plant for storage and recovery of energy - Google Patents

Process and combined plant for storage and recovery of energy Download PDF

Info

Publication number
US20160160694A1
US20160160694A1 US14/961,341 US201514961341A US2016160694A1 US 20160160694 A1 US20160160694 A1 US 20160160694A1 US 201514961341 A US201514961341 A US 201514961341A US 2016160694 A1 US2016160694 A1 US 2016160694A1
Authority
US
United States
Prior art keywords
heat
operating mode
temperature level
transfer fluid
exchange
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.)
Abandoned
Application number
US14/961,341
Other languages
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
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
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: STOVER, BRIAN, STILLER, CHRISTOPH, ALEKSEEV, ALEXANDER
Publication of US20160160694A1 publication Critical patent/US20160160694A1/en
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: STILLER, CHRISTOPH, ALEKSEEV, ALEXANDER
Assigned to MITSUBISHI HITACHI POWER SYSTEMS EUROPE GMBH reassignment MITSUBISHI HITACHI POWER SYSTEMS EUROPE GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: STOVER, BRIAN
Abandoned legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—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 process and a combined plant for storage and recovery of energy, in particular electrical energy, according to the preambles of the respective independent claims.
  • DE 31 39 567 A1 and EP 1 989 400 A1 disclose using liquid air or liquid nitrogen, that is to say low-temperature air liquefaction products, for grid control and provision of control capacity in electric power grids.
  • compressed feed air is liquefied in an air separation plant with an integrated liquefier or in a dedicated air liquefaction plant, here generally, as explained below, also termed air treatment unit, in whole or in part to give such a low-temperature air liquefaction product.
  • the low-temperature air liquefaction product is stored as low-temperature stored liquid in a storage system having low-temperature tanks. In the storage system, in addition to the low-temperature air liquefaction product, further low-temperature fluids can also be stored. This operating mode proceeds in a period which here is termed energy storage period.
  • a low-temperature process liquid is formed from the low-temperature stored liquid, which low-temperature process liquid can likewise also comprise further low-temperature fluids.
  • the low-temperature process liquid is, optionally after pressure elevation by means of a pump, warmed to about ambient temperature or above, and thereby transformed into a gaseous or supercritical state.
  • a pressurized stream obtained in this case is expanded to ambient pressure in an energy production unit in one or more expansion turbines with intermediate warming.
  • the mechanical power released is transformed into electrical energy in one or more generators of the energy production unit and fed into an electric grid. This operating mode proceeds in a period which here is designated energy recovery period.
  • the cold liberated during the energy recovery period on conversion of the low-temperature process liquid to the gaseous or supercritical state can be stored and used during the energy storage period for providing cold for obtaining the air liquefaction product.
  • Compressed air storage power plants are also known in which air is not liquefied, but rather is compressed in a compressor and stored in an underground cavern.
  • the compressed air is passed from the cavern into the combustion chamber of a gas turbine.
  • fuel for example natural gas is fed to the gas turbine via a gas line and burnt in the atmosphere formed by the compressed air.
  • the exhaust gas formed is expanded in the gas turbine, as result of which energy is generated.
  • the present invention is, in addition, to be differentiated from processes and devices in which an oxygen-rich fluid is passed into a gas turbine for supporting oxidation reactions. Corresponding processes and devices operate with air liquefaction products which contain more than 40 mole percent oxygen.
  • 6,295,837 B1 is specifically tailored to combined processes with integrated gasification (integrated gasification combined cycle, IGCC), where nitrogen and oxygen are continuously required at a high pressure, typically more than 10 bar, and at the same time the vaporized natural gas can be used as secondary fuel for heat recovery.
  • integrated gasification combined cycle integrated gasification combined cycle
  • the process proposed in U.S. Pat. No. 6,295,837 B1 is unsuitable for a process for storage and recovery of energy, because it provides only cold transfer in one direction. This also applies to a process which is disclosed in U.S. Pat. No. 3,058,314 A.
  • US 2014/0245756 A1 discloses cryogenic energy storage systems and also processes for the storage of cold energy and reuse thereof.
  • the object of the present invention is therefore to provide a process which is efficient and simpler in terms of safety for storage and recovery of energy, for example using an air liquefaction product.
  • the present invention proposes a process for the storage and recovery of energy and a corresponding combined plant having the features: a process for storage and recovery of energy using a combined plant that comprises a gas treatment unit and an energy generation unit, wherein
  • the invention further discloses a combined plant for storage and recovery of energy, having a gas treatment unit and an energy generation unit, wherein the combined plant has means which are equipped
  • An “energy production unit” here is taken to mean a plant or a plant component which is equipped for generating electrical energy.
  • An energy production unit comprises here in the context of the present invention at least one expansion turbine which is advantageously coupled to at least one electrical generator.
  • An expansion machine coupled to at least one electrical generator is customarily also termed “generator turbine”. The mechanical power liberated in 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 production unit.
  • Air separation plants have distillation column systems which can be designed, for example, as two-column systems, in particular as classical Linde-double column systems, but also as three- or multicolumn systems.
  • distillation columns for producing nitrogen and/or oxygen in liquid and/or gaseous state for example liquid oxygen, LOX, gaseous oxygen, GOX, liquid nitrogen, LIN and/or gaseous nitrogen, GAN
  • distillation columns for producing further air components in particular the noble gases krypton, xenon and/or argon, can be provided.
  • the present invention can comprise the production of an air liquefaction product, using compressed feed air.
  • the plant components used therefor can be summarized under the expression “air treatment unit”. In the language use of the present application, this is taken to mean a plant which is equipped for producing at least one air liquefaction product, using compressed feed air. It is sufficient for an air treatment unit for use in the present invention that a corresponding low-temperature air liquefaction product can thereby be obtained that it usable as stored liquid and is transferable to a storage system.
  • This can be an air separation plant, as described above, but also merely a pure “air liquefaction plant”, which does not have a distillation column system.
  • an air liquefaction plant can correspond to that of an air separation plant having the delivery of an air liquefaction product.
  • liquid air can also be generated in an air separation plant as air liquefaction product.
  • a gas other than air can also be used, a corresponding plant here is also more generally termed “gas treatment unit”.
  • the compressed feed air from which the air liquefaction product is produced in corresponding air-treatment units can be provided in a known main (air) compressor having a booster or any other device equipped for the compression of air, as can also be used in conventional air separation plants.
  • a known main (air) compressor having a booster or any other device equipped for the compression of air as can also be used in conventional air separation plants.
  • An “air product” is any product that can be produced at least by compression and cooling of air and in particular, but not necessarily, by a subsequent low-temperature rectification.
  • it can in this case be a 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).
  • LOX, GOX liquid or gaseous oxygen
  • LIN liquid or gaseous nitrogen
  • LAR, GAR liquid or gaseous argon
  • LAIR liquid air
  • the expressions “oxygen”, “nitrogen” etc. in this case also denote respectively low-temperature liquids or gases that have the respectively cited air component in an amount which is above that of atmospheric air.
  • an “air liquefaction product” is taken to mean a corresponding liquid product at low temperature.
  • gas product or “gas liquefaction product” that cannot be produced, or cannot only be produced, from air, but also from another gas.
  • a “heat exchanger” serves for the indirect transfer of heat between at least two streams, e.g. conducted in counterflow to one another, for example a warm compressed air stream and one or more cold streams, or a low-temperature liquid air product and one or more warm streams.
  • counterflow heat exchangers are used.
  • a heat exchanger can be formed from a single heat-exchanger section, or a plurality of parallel-linked and/or serially-linked heat exchanger sections, e.g. of one or more plate heat exchanger blocks. In this case this is a plate heat exchanger (plate fin heat exchanger).
  • Such a heat exchanger for example also the “main heat exchanger” of an air treatment plant, via which the main fraction of the fluids that are to be cooled or warmed are cooled or warmed, respectively, has passages which are constructed as fluid channels that are separate from one another having heat exchange surfaces and are combined in parallel and separated by other passages to form “passage groups”.
  • a “heat-exchange unit” can have one or more heat-exchanger blocks or sections.
  • pressure level and “temperature level” for characterizing pressures and temperatures, whereby it must be stated that corresponding pressures and temperatures in a corresponding plant need not be used in the form of exact pressure or temperature values in order to implement the concept according to the invention.
  • pressures and temperatures are typically in certain ranges which are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about a mean value.
  • Corresponding pressure levels and temperature levels can in this case be in disjoint ranges or in ranges which overlap one another.
  • pressure levels include unavoidable or expected pressure drops, for example on account of cooling effects.
  • the pressure levels stated here in bar are absolute pressures.
  • the present invention has been described previously and will be described hereinafter with reference to air as a working medium. However, it is also suitable for use with other media that are liquefiable in similar manner, for example nitrogen, oxygen, argon and mixtures of these gases.
  • the present invention proceeds from a process for storage and recovery of energy using a combined plant that comprises a gas treatment unit and an energy generation unit.
  • a low-temperature gas liquefaction product can generated from compressed feed gas that is cooled in a heat-exchange system of the gas treatment unit, and using the gas liquefaction product, a stored liquid can be provided.
  • the compressed feed gas is compressed feed air
  • the gas treatment unit is an air treatment unit.
  • the stored liquid can be, as already mentioned, for example a corresponding liquid gas.
  • compressed feed air is used as compressed feed gas, it is, in particular, liquid air and/or any other liquid air product which can be formed from correspondingly compressed feed air.
  • such a process comprises providing, in a second operating mode, using the storage liquid, a low-temperature process liquid that is warmed in the heat-exchange system, obtaining a pressurized fluid that is then work-producingly expanded in the energy generation unit, for example in this case a generator turbine.
  • the second operating mode can, for example, follow the first operating mode directly, but also further operating modes can be provided between the first and second operating modes.
  • the process proposed according to the invention corresponds to the prior art in which a liquid air product is generated from air, stored and later vaporized to form a corresponding pressurized fluid.
  • “using the gas liquefaction product a stored liquid is provided” this may be taken to mean that the stored liquid need not be formed exclusively from the gas liquefaction product, also, for example external, low-temperature liquefaction products or other streams can be provided, that is to say, for example, can be fed into a corresponding storage system.
  • the wording that “using the stored liquid a low-temperature process liquid is provided”, is to comprise that the low-temperature process liquid also can be provided using additional, also, for example, external, low-temperature liquefaction products or other streams.
  • the invention provides the compressed feed gas is cooled in a first heat-exchange unit of the heat-exchange system in the first operating mode in counterflow to a heat-transfer fluid, and the process liquid is warmed in the first heat-exchange unit in the second operating mode in counterflow to the heat-transfer fluid.
  • a heat-transfer fluid in the context of the present invention has the particular advantage that additional organic coolants which, as mentioned, can contain combustible hydrocarbons, are not conducted through the same heat exchanger as the compressed feed gas and/or the process liquid, and therefore, in the event of leaks, cannot come into contact with oxygen which may be present in the compressed feed gas or the process liquid.
  • the heat-transfer fluid used is preferably free from, or low in oxidizing and combustible components, in particular is oxygen-free in the meaning explained hereinafter.
  • the heat-transfer fluid is therefore advantageously generally neither oxidizing nor combustible itself, wherein “oxidizing” is taken to mean a property of a fluid of supporting a combustion even in the absence of atmospheric oxygen, under the conditions prevailing in a corresponding heat exchanger.
  • the present invention provides that the heat-transfer fluid is cooled in the first operating mode at least in part by means of at least two further heat-exchange units of the heat-exchange system that are operated at different temperature levels and having in each case at least one organic coolant, and said heat-transfer fluid is warmed in the second operating mode.
  • the operating mode termed here as “first operating mode” is the abovementioned operating mode in the energy storage period that a corresponding combined plant carries out at times of electric current surplus when sufficient favorable electrical energy for compressing gas and providing a gas liquefaction product is available.
  • the “second operating mode” denotes the operating mode in the energy recovery period, that is to say in phases of electric power deficit, in which a corresponding pressurized fluid is generated, using the gas liquefaction product generated in the first operating mode.
  • the invention provides that the directions in which the heat-transfer fluid and the feed gas are conducted through the first heat-exchange unit in the first operating mode are opposite to the directions in which the heat-transfer fluid and the process liquid are conducted through the first heat-exchanger unit in the second operating mode.
  • This permits in each case the temperature profiles, according to which cooling and/or heating of corresponding fluids is performed, to be situated close to one another, because the heat-transfer fluid and the feed gas which flow in counterflow to one another through the first heat-exchange unit, in each case can be conducted therethrough with the lowest possible temperature difference.
  • the invention further provides that the heat-transfer fluid and the compressed feed gas are conducted, in the first operating mode, in each case at first pressure levels, and the heat-transfer fluid and the process liquid, in the second operating mode, are conducted in each case at second pressure levels through the first heat-exchange unit, wherein the first pressure levels are at least 5 bar above the second pressure levels.
  • the operating pressures of the heat-transfer fluid are different in the first and second operating modes.
  • a pressure control device can be provided. The pressure of the heat-transfer fluid is guided in this case in each case by the pressure of the feed gas, and/or of the process liquid in the first heat-exchange unit, in such a manner that for this reason also a particularly effective heat transfer is possible.
  • first pressure levels i.e. the first pressure level at which the heat-transfer fluid is conducted in the first operating mode through the first heat-exchange unit
  • first pressure level at which the compressed feed gas is conducted through the heat-exchange unit in the first operating mode are roughly the same.
  • second pressure levels i.e. the second pressure level at which the heat-transfer fluid is conducted through the first heat-exchange unit in the second operating mode
  • the second pressure level at which the process liquid is conducted through the first heat-exchange unit in the second operating mode are “roughly the same”, for example, if they do not differ from one another by more than 20%, in particular by no more than 10%, no more than 5%, or no more than 1%. “Roughly” the same pressure levels also include identical pressure levels. In such “roughly the same” pressure levels, the particularly effective heat transfer mentioned is possible. However, exactly the same pressures need not be used.
  • the first pressure levels of the first operating mode are advantageously at 50 to 120 bar, and/or the second pressure levels of the second operating mode are advantageously at 40 to 60 bar.
  • the pressure difference is at least 5 bar, the first pressure levels, however, can also be 10, 15, 20, 30, 40, 50, 60, 70 or 80 bar above the second pressure levels.
  • the present invention therefore provides, in addition to the stored liquid which is provided, using the compressed feed gas, and is stored in the first operating mode, and is vaporized in the second operating mode, providing further cold stored fluids in the form of the organic coolants.
  • the at least two further cold stored fluids that is to say the organic coolants, are in this case preferably arranged for storage of cold at different temperature levels, therefore 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 becomes particularly efficient. The same applies to the warming of the low-temperature process liquid in the second operating mode.
  • the present invention owing to the use of in total at least three cold stored fluids, namely the gas liquefaction product formed from the compressed feed gas, with the use of which a stored liquid is provided, and the at least two organic coolants, for example hydrocarbons, permits particularly efficient operation.
  • the heat-transfer fluid used is an oxygen-free or substantially oxygen-free gas mixture. It is self-evident that a correspondingly “oxygen-free” gas mixture can also have residual contents of oxygen, for example 1%, 0.5%, 0.1% or 0.01% oxygen or less. Correspondingly low oxygen contents reduce sufficiently the risk of inflammation on contact with an inflammable organic coolant.
  • the heat-transfer fluid used is a fluid predominantly containing nitrogen, neon, helium and/or argon. This is suitable, particularly, because it is possible by using a corresponding fluid to establish particularly narrow temperature profiles in the heat exchangers used and to minimize thermodynamic losses. An example thereof is illustrated in the accompanying FIG. 5 .
  • the heat-transfer fluid during cooling of the compressed feed gas, is at least in part vaporized, and on warming the process liquid is at least in part liquefied.
  • the present invention does not explicitly refer to processes in which corresponding heat-transfer fluids are expanded and recompressed in order thereby to generate cold.
  • 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 production of cold therefore proceeds not with the use of the heat-transfer fluid itself, this serves only for heat transfer, and is therefore not cold-producingly expanded and/or recompressed.
  • the at least two further heat-exchange units comprise a second heat-exchange unit that is operated with a first organic coolant that is transferred between two storage containers.
  • a corresponding second heat-exchange unit can in this case be equipped for operation at higher temperatures in comparison with a third heat-exchange unit, as is described hereinafter and can be operated with a corresponding organic coolant.
  • This is transferred between the two storage containers, as mentioned, of which one is designed as a “warm” storage container, and one as a “cold” storage container.
  • Corresponding storage containers are preferably constructed as insulated tanks.
  • the first organic coolant is conducted from the “cold” storage container through the second heat-exchange unit, where it cools the heat-transfer fluid, and is then transferred to the “warm” storage container.
  • a transfer in the reverse direction proceeds during a warming of the low-temperature process liquid in the second operating mode.
  • halogenated or non-halogenated alkanes or alkenes, alcohols and/or aromatics are suitable, as are known fundamentally.
  • halogenated or non-halogenated alkanes or alkenes such as ethane, ethylene, propane, propylene, butane, pentane, hexane and, optionally, also higher hydrocarbons may be used.
  • Halogenated hydrocarbons are in particular fluorinated and/or chlorinated.
  • suitable first organic coolants are alcohols such as methanol, ethanol, propanol, butanol, pentanol, hexanol, and further alcohols and aromatics such as, for example, toluene.
  • the at least two further heat-exchange units can advantageously comprise a third heat-exchange unit that, in comparison with the second heat-exchange unit, is operated at a lower temperature, preferably with a second organic coolant that is transferred between two heat-storage containers, and also with a third organic coolant that is transferred between two storage containers.
  • the process according to the invention in an advantageous embodiment, can comprise that the second and the third organic coolants are an identical organic coolant, and so the provision of different coolants can be dispensed with.
  • the second and/or third organic coolant in the context of the present invention, comprises a halogenated or non-halogenated alkane or alkene having at most four carbon atoms that is suitable for particularly low temperatures.
  • the organic coolant or coolants in this case are, in the context of the present invention, warmed in the first operating mode to in each case the same (“upper”) temperature level, from which they are cooled in the second operating mode. Conversely, it or they are cooled in the second operating mode to the same (“lower”) temperature level, from which they are warmed in the first operating mode. Because of unavoidable losses, here, “the same temperature level” is not to be taken to mean only exactly the same temperature, but a temperature band of a width of up to, for example, 20° C. Of course, a temperature difference as low as possible between the two operating modes should be sought.
  • the heat-exchange diagrams of the heat-exchange system of the gas treatment unit can be made particularly expedient by the heat-exchange units used.
  • a process is particularly advantageous in which the first organic coolant, i.e. the coolant of the second heat-exchange unit, is warmed in the first operating mode from a lower temperature level at ⁇ 100 to ⁇ 30° C., in particular ⁇ 60 to ⁇ 40° C., to an upper temperature level at 0 to 80° C., in particular 20 to 50° C., and in the second operating mode is cooled from the upper temperature level to the lower temperature level.
  • the first organic coolant i.e. the coolant of the second heat-exchange unit
  • a process is further advantageous, in which the second organic coolant, i.e. one of the coolants of the third heat-exchange unit, is warmed in the first operating mode from a first temperature level at ⁇ 200 to ⁇ 140° C., in particular ⁇ 196 to ⁇ 150° C., to a second temperature level at ⁇ 100 to ⁇ 30° C., in particular ⁇ 60 to ⁇ 40° C., and in the second operating mode is cooled from the second temperature level to the first temperature level.
  • the second organic coolant i.e. one of the coolants of the third heat-exchange unit
  • the third organic coolant which is likewise a coolant of the third heat-exchange unit, in the first operating mode is warmed from a third temperature level at ⁇ 200 to ⁇ 140° C., in particular ⁇ 196 to ⁇ 150° C., to a fourth temperature level at ⁇ 140 to ⁇ 60° C., in particular ⁇ 100 to ⁇ 60° C., and in the second operating mode is cooled from the fourth temperature level to the third temperature level.
  • the second organic coolant at the first temperature level and the third organic coolant at the third temperature level are fed to the third heat-exchange unit, and the second organic coolant at the second temperature level and the third organic coolant at the fourth temperature level are withdrawn therefrom.
  • the second organic coolant at the second temperature level and the third organic coolant at the fourth temperature level are fed to the third heat-exchange unit and the second organic coolant at the first temperature level and the third organic coolant at the third temperature level are withdrawn therefrom.
  • a corresponding combined plant is advantageously constructed for carrying out a corresponding process.
  • the second organic coolant in this case is advantageously conducted through the third heat-exchange unit completely, the third organic coolant, only in a section thereof.
  • particularly favorable temperature courses result therefrom in the first heat-exchange unit.
  • the organic coolants used differ in their chemical composition, in particular in their boiling point. They must be selected in such a manner that they are liquid in the respective entire working range.
  • the substances listed in the table on page 5 of WO 2014/026738 A2 come explicitly into consideration for use in the invention as first, second and/or third organic coolant.
  • Organic coolants can also be the following coolants according to the familiar DuPont nomenclature (cf. DIN 8960, section 6.3.2), namely halogenated and non-halogenated hydrocarbons having 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, having 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, R-143a,
  • a fourth heat-exchange unit can be used, by means of which the heat-transfer fluid is in part cooled in the first operating mode and which is operated with a further compressed feed gas that is cold-producingly expanded.
  • the first operating mode additionally cold can be generated to cover cold losses, as is also known in air separation plants, in this case in the form of what is termed a turbine stream.
  • the present invention also extends to a combined plant for storage and recovery of energy which has all the means that make it suitable for carrying out a process described above.
  • a combined plant for storage and recovery of energy which has all the means that make it suitable for carrying out a process described above.
  • a third heat-exchange unit is constructed in such a manner that, in the first operating mode, the second organic coolant at the first temperature level and the third organic coolant at the third temperature level can be fed to said third heat-exchange unit, and the second organic coolant at the second temperature level and the third organic coolant at the fourth temperature level can be withdrawn therefrom, and, further, in the second operating mode, the second organic coolant at the second temperature level and the third organic coolant at the fourth temperature level can be fed to said third heat-exchange unit, and the second organic coolant at the first temperature level and the third organic coolant at the third temperature level can be withdrawn therefrom.
  • FIG. 1A illustrates a combined plant according to an embodiment of the invention in a first operating mode in the form of a process flow diagram.
  • FIG. 1B illustrates the combined plant according to FIG. 1A in a second operating mode in the form of a process flow diagram.
  • FIG. 2A illustrates components of a heat-exchange system according to an embodiment of the invention in the first operating mode in the form of a process flow diagram.
  • FIG. 2B illustrates the components according to FIG. 2A in the second operating mode in the form of a process flow diagram.
  • FIG. 3A illustrates components of a heat-exchange system according to an embodiment of the invention in the first operating mode in the form of a process flow diagram.
  • FIG. 3B illustrates the components according to FIG. 3A in the second operating mode in the form of a process flow diagram.
  • FIG. 4A illustrates a combined plant according to a further embodiment of the invention in the first operating mode in the form of a process flow diagram.
  • FIG. 4B illustrates the combined plant according to FIG. 4A in the second operating mode in the form of a process flow diagram.
  • FIG. 5 illustrates heat-exchange profiles achievable according to an embodiment of the invention in a diagram.
  • valves and fittings for the sake of clarity, are not illustrated, but for explanation, fluid pathways that are blocked by valves and fittings, and/or correspondingly inactivated streams, are drawn criss-crossed.
  • Streams present predominantly or exclusively in gaseous form are illustrated in the form of non-filled (white) arrow triangles, predominantly or exclusively liquid streams are illustrated in the form of filled (black) arrow triangles.
  • the invention is illustrated with reference to an air treatment unit as gas treatment unit.
  • FIG. 1A illustrates a combined plant according to an embodiment of the invention in a first operating mode in the form of a process flow diagram.
  • the combined plant which is illustrated in FIG. 1B in a second operating mode is designated overall 100 , and comprises an air treatment unit 110 and an energy generation unit 120 .
  • feed air in the form of a stream a is taken in by suction via a filter 1 by means of a main air compressor 2 having intercoolers that are not drawn separately.
  • the feed air of the stream a is compressed in the main air compressor 2 to a pressure of approximately 5 to 7 bar, for example.
  • a correspondingly compressed stream, now designated b, is fed to a cooler unit 3 operated by cooling water streams that are not shown separately, where the previously fed heat of compression is withdrawn from the stream b.
  • a correspondingly cooled stream, now designated c, is freed from the predominant part of the water and carbon dioxide present in an adsorptive purification unit 4 which can comprise, for example, a pair of adsorber containers filled with molecular sieve that are not shown separately.
  • a stream purified in this manner, now designated d, is fed to a booster 5 and boosted therein to a pressure of, for example, approximately 9 bar.
  • a correspondingly boosted stream, now designated e is fed into a heat-exchange system of the air treatment unit, which is here designated overall 10 .
  • the compressed feed air of the stream e is cooled in a first heat-exchange unit 11 against a stream f of a heat-transfer fluid, obtaining a corresponding cooled stream g.
  • the stream f and the stream e are in this case each at pressure levels which are above and hereinafter designated as “first” pressure levels.
  • the stream f is brought by means of a pump 15 explained hereinafter to its “first” pressure level, the stream g by means of the compression explained. Values for the “first” pressure levels and possible deviations of these from one another have already been explained.
  • the cooled stream g in the example shown, is expanded in a generator turbine 12 and optionally an expansion valve which downstream thereof and is not shown separately.
  • the correspondingly expanded stream g is transferred to a separation container 13 , a liquid fraction forms in the sump thereof and at the top of which a gaseous fraction forms.
  • the liquid fraction from the sump of the separation container 13 is transferred in the form of the stream h to a storage system 20 , in which it is stored in the first operating mode.
  • the storage system 20 can in addition to the stream h, as already mentioned above, also be charged with further liquid low-temperature streams.
  • no fluid is withdrawn from the storage system 20 .
  • the gaseous fraction from the top of the separation container 13 is withdrawn in the form of the stream i and warmed in a further heat-exchange unit 14 , which here is designated a fourth heat-exchange unit 14 , as compared with the second and third heat-exchange units 16 and 18 explained hereinafter.
  • a further heat-exchange unit 14 in this case, cold can be transferred from the stream i to a stream k, which likewise comprises a heat-transfer fluid and is combined with a further corresponding stream l to form the abovementioned stream f of the heat-transfer fluid.
  • the stream f and the streams k and l form two subcircuits of a heat-transfer fluid that are driven by means of the pump 15 and, therein and also in the first heat-exchange unit 11 , are linked to one another. It is stressed, as already above, that in the subcircuits mentioned, no cold-producing expansion of a corresponding heat-transfer fluid proceeds, this serves substantially only for transferring heat, but not for the generation thereof.
  • a substream m can be branched off, cooled in the heat exchanger 14 to an intermediate temperature cold-producingly expanded in a generator turbine that is not shown separately and recirculated 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 stream i can be combined with the stream d, for example upstream of the booster 5 .
  • FIG. 1A Further components of the air-treatment unit 110 and components of the energy generation unit 120 , which is not in operation in the first operating mode shown in FIG. 1A will be described hereinafter with reference to FIG. 1B , in which the second operating mode is illustrated.
  • FIG. 1B the combined plant 100 , which has already been illustrated in the first operating mode in FIG. 1A , is shown in the second operating mode.
  • the stream e is not provided, the main compressor 2 and the booster 5 can be out of operation or be operated in a standby operation.
  • the adsorptive purification appliance 4 can be regenerated, for example, during the second operating mode illustrated in FIG. 1B .
  • the generator turbine 12 no cooled compressed feed air is expanded, and no fluid is transferred into the storage system 20 either.
  • the coolant circuit through the fourth heat-exchange unit 14 that is implemented in the first operating mode according to FIG. 1A by the stream k, is here typically not in operation.
  • fluid is withdrawn from the storage system 20 in the form of the stream o, that is to say a stored liquid, and provided in the form of a low-temperature process liquid.
  • a low-temperature air liquefaction product is fed from the sump of the separation container 13 into the storage system.
  • the stream o in the second operating mode, is warmed in the heat exchanger 11 and vaporized.
  • the stream o in this case transfers the cold thereof to a stream p which is formed from the same heat-transfer fluid of the streams f, k and l of the first operating mode according to FIG. 1A , but here, on account of clearer differentiability, is shown differently.
  • the streams o and p are each at pressure levels which are designated above and hereinafter as “second” pressure levels.
  • the stream o is brought to the “second” pressure level thereof by means of a pump that is not drawn separately, the stream p has this pressure level after it is conducted through the second heat-exchange unit 16 and the third heat-exchange unit 18 by means of the explained pump 15 .
  • Values of the “second” pressure levels and possible deviations thereof from one another have already been explained.
  • a coolant circuit implemented in the second operating mode according to FIG. 1B by the stream p also comprises the abovementioned second and third heat-exchange units 16 and 18 , and the associated coolant units 17 and 19 , which are explained in the FIGS. 2A and 2B, and 3A and 3B , hereinafter.
  • a gaseous or supercritical pressurized fluid in the form of the stream q is provided by the warming and vaporization of the stream o, that is to say of the low-temperature process liquid, which stream q is fed to the energy generation unit 120 .
  • the stream q is, for example, work-producingly expanded, with generation of electrical energy in a generator turbine 121 .
  • the stream q can be conducted in advance through a heat exchanger 122 and warmed therein by means of an exhaust gas stream of a combustion chamber 123 or a thermal engine, in which a fuel is burnt with air or another oxygen-containing gas.
  • FIG. 2A the second heat-exchange unit 16 with the associated coolant unit 17 of the plant 100 , as shown in FIGS. 1A and 1B in the first and second operating modes, is illustrated in the first operating mode.
  • the stream l of the heat-transfer fluid is conducted through the second heat-exchange unit 16 , as already illustrated in FIG. 1A .
  • a gaseous stream r is conducted in counterflow to the stream l, which stream r flows out of a first coolant store 171 , is cooled in the second heat-exchange unit 16 and then flows into a second coolant store 172 .
  • the gaseous stream r is gas which does not condense at the above described temperatures, for example nitrogen.
  • the stream r is provided by increasingly displacing corresponding gas from the first coolant store 171 .
  • an organic coolant is withdrawn in liquid form by means of a pump 173 from the second coolant store 172 , conducted through the heat exchanger 16 and fed into the first coolant store 171 .
  • a corresponding stream of the organic coolant is designated s.
  • the second heat-exchange unit 16 is shown in the second operating mode with the associated coolant unit 17 , which is shown in FIG. 2A in the first operating mode.
  • a stream p of the heat transfer fluid is conducted through the second heat-exchange unit 16 .
  • An organic coolant or a gas overlaying it is conducted into the storage containers 171 and 172 in the second operating mode, which is shown in FIG. 2B , in reverse direction in comparison with the first operating mode which is shown in FIG. 2A .
  • Corresponding streams are therefore illustrated with r′ and s′.
  • the third heat-exchange unit 18 with the associated coolant unit 19 of the plant 100 is illustrated in the first and second operating modes, which plant is shown in FIGS. 1A and 1B in the first and second operating modes.
  • Two organic coolant streams which, for example, comprise propane as coolant, are used.
  • the basic mode of functioning of the coolant unit 19 has already been explained with reference to FIGS. 2A and 2B .
  • a first coolant stream t is conducted completely through the third heat-exchange unit 18
  • a second coolant stream u only through a section of this third heat-exchange unit 18 Corresponding coolant stores and pumps are here designated 191 to 196 .
  • coolant streams which are conducted in reverse direction in the second operating mode which is illustrated in FIG. 2B are designated t′ and u′.
  • the respective gaseous fluid streams likewise used are designated in the two FIGS. 2A and 2B with v and w, and v′ and w′, respectively.
  • Coolants can also be exchanged between the two coolant circuits in the two modes of operation, as is illustrated by x and x′.
  • FIG. 4A illustrates a combined plant according to a further embodiment of the invention in the first operating mode in the form of a process flow diagram, where here only the heat-exchange system 10 is illustrated, the incorporation of which into the combined plant can be substantially the same as in the combined plant 100 according to the FIGS. 1A and 1B .
  • the first operating mode and in FIG. 4B the second operating mode, of the combined plant is illustrated.
  • the boosted stream e is divided into two substreams according to FIG. 4A upstream or in the heat-exchange system 10 and is cooled in the first heat-exchange unit 11 and also in the fourth heat-exchange unit 14 .
  • a stream k as is shown in FIG. 1A , therefore does not exist.
  • the stream l corresponds according to FIG. 4A to the stream f.
  • the cooled stream g is formed by combining the substreams of the stream e.
  • the stream g as already explained in FIG. 1A is vaporized and stored.
  • the streams i and m have also already been explained above.
  • FIG. 4B the combined plant is shown in the second operating mode, which combined plant is illustrated in FIG. 4A in the first operating mode.
  • FIG. 1B a substream of the liquefied air product or the stored liquid formed therefrom does not flow through the fourth heat-exchange unit 14 . Only a stream 1 is conducted through the first heat-exchange unit 11 , as already explained in FIG. 2B .
  • FIG. 5 a heat-exchange diagram achievable according to an embodiment of the invention is illustrated, and designated overall 500 .
  • an exchanged heat in kW is plotted on the abscissa and a temperature in K on the ordinate.
  • 501 illustrates a heat-exchange profile for the compressed feed air
  • 502 a heat-exchange profile for the stored liquid formed from the liquefied air product
  • 503 and 504 illustrate heat-exchange profiles for the heat-transfer fluid. It can be seen from the heat-exchange diagram 500 that the invention permits a particularly narrow guidance of the heat-exchange profiles 501 and 503 , and 503 and 504 , respectively.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US14/961,341 2014-12-09 2015-12-07 Process and combined plant for storage and recovery of energy Abandoned US20160160694A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP14004152.6A EP3032203A1 (fr) 2014-12-09 2014-12-09 Procédé et installation combinée destinés à stocker et à récupérer l'énergie
EP14004152.6 2014-12-09

Publications (1)

Publication Number Publication Date
US20160160694A1 true US20160160694A1 (en) 2016-06-09

Family

ID=52231787

Family Applications (1)

Application Number Title Priority Date Filing Date
US14/961,341 Abandoned US20160160694A1 (en) 2014-12-09 2015-12-07 Process and combined plant for storage and recovery of energy

Country Status (2)

Country Link
US (1) US20160160694A1 (fr)
EP (2) EP3032203A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11306234B2 (en) * 2018-04-19 2022-04-19 Daikin Industries, Ltd. Composition containing refrigerant and application thereof
WO2023244883A1 (fr) * 2022-06-16 2023-12-21 Praxair Technology, Inc. Système et procédé de stockage d'énergie d'azote liquide
US20240060715A1 (en) * 2022-08-22 2024-02-22 L'air Liquide, Societe Anonyme Pour L'etude Et L’Exploitation Des Procedes Georges Claude Liquefaction system and method for controlling turbine inlet temperature of liquefaction system

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
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
DE102019201336A1 (de) * 2019-02-01 2020-08-06 Siemens Aktiengesellschaft Gasverflüssigungsanlage sowie Verfahren zum Betrieb einer Gasverflüssigungsanlage
CN113646601B (zh) * 2019-04-05 2023-11-03 林德有限责任公司 用于操作热交换器的方法、具有热交换器的排布结构以及具有对应排布结构的系统
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
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

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20010004830A1 (en) * 1996-12-24 2001-06-28 Hitachi, Ltd. Cold heat-reused air liquefaction/vaporization and storage gas turbine electric power system

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3058314A (en) 1957-08-12 1962-10-16 British Oxygen Co Ltd Process and apparatus for the low temperature separation of air
DE3139567A1 (de) 1981-10-05 1983-04-21 Bautz, Wilhelm, 6000 Frankfurt Verfahren zur speicherung von elektrischer energie unter verwendung von fluessiggasen, insbesondere fluessiger luft
JPH04127850A (ja) * 1990-09-19 1992-04-28 Central Res Inst Of Electric Power Ind 液体空気貯蔵発電システム
JP2000337767A (ja) 1999-05-26 2000-12-08 Air Liquide Japan Ltd 空気分離方法及び空気分離設備
PL1989400T5 (pl) 2006-02-27 2023-10-09 Highview Enterprises Limited Sposób magazynowania energii i układ magazynowania energii kriogenicznej
GB2494400B (en) * 2011-09-06 2017-11-22 Highview Entpr Ltd Method and apparatus for power storage
EP2880268A2 (fr) 2012-08-02 2015-06-10 Linde Aktiengesellschaft Procédé et dispositif servant à produire de l'énergie électrique
GB2512360B (en) * 2013-03-27 2015-08-05 Highview Entpr Ltd Method and apparatus in a cryogenic liquefaction process
EP2835506A1 (fr) * 2013-08-09 2015-02-11 Linde Aktiengesellschaft Procédé pour la production d'énergie électrique et installation de production d'énergie
EP2835507B1 (fr) * 2013-08-09 2016-09-21 Linde Aktiengesellschaft Procédé pour la production d'énergie électrique et installation de production d'énergie
DE102014105237B3 (de) * 2014-04-11 2015-04-09 Mitsubishi Hitachi Power Systems Europe Gmbh Verfahren und Vorrichtung zum Speichern und Rückgewinnen von Energie

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20010004830A1 (en) * 1996-12-24 2001-06-28 Hitachi, Ltd. Cold heat-reused air liquefaction/vaporization and storage gas turbine electric power system

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11306234B2 (en) * 2018-04-19 2022-04-19 Daikin Industries, Ltd. Composition containing refrigerant and application thereof
WO2023244883A1 (fr) * 2022-06-16 2023-12-21 Praxair Technology, Inc. Système et procédé de stockage d'énergie d'azote liquide
US20240060715A1 (en) * 2022-08-22 2024-02-22 L'air Liquide, Societe Anonyme Pour L'etude Et L’Exploitation Des Procedes Georges Claude Liquefaction system and method for controlling turbine inlet temperature of liquefaction system

Also Published As

Publication number Publication date
EP3037764A1 (fr) 2016-06-29
EP3032203A1 (fr) 2016-06-15
EP3037764B1 (fr) 2017-09-20

Similar Documents

Publication Publication Date Title
US20160160694A1 (en) Process and combined plant for storage and recovery of energy
AU2021290222B2 (en) Staged cryogenic storage type supercritical compressed air energy storage system and method
Damak et al. Liquid Air Energy Storage (LAES) as a large-scale storage technology for renewable energy integration–A review of investigation studies and near perspectives of LAES
AU684885B2 (en) Method and apparatus for liquefying natural gas
Borri et al. A preliminary study on the optimal configuration and operating range of a “microgrid scale” air liquefaction plant for Liquid Air Energy Storage
RU2685778C1 (ru) Повышение эффективности системы производства спг путем предварительного охлаждения поступающего потока природного газа
Guizzi et al. Thermodynamic analysis of a liquid air energy storage system
CN1820163B (zh) 具有液化天然气再气化的动力循环
CN101108977B (zh) 在液化天然气制备中的一体化ngl回收
US9810103B2 (en) Method and device for generating electrical energy
US10177629B2 (en) Method for generating electrical energy and energy generation plant
CN101755037A (zh) 改进的溶剂提取和回收
SA05260115B1 (ar) إسالة غاز طبيعي
KR20050072782A (ko) 천연가스 액화용 모터 구동 압축기 시스템
EA034087B1 (ru) Система и способ производства сжиженного природного газа с удалением парникового газа
MX2013014870A (es) Proceso para la licuefaccion de gas natural.
CN102959352A (zh) 二氧化碳和氢气的分离
AU2009300946A1 (en) Method for producing liquid and gaseous nitrogen streams, a helium-rich gaseous stream, and a denitrogened hydrocarbon stream, and associated plant
CN112029530A (zh) 用脱氢装置对富烯烃压缩流出物蒸气流进行氢分离的工艺
US20150192065A1 (en) Process and apparatus for generating electric energy
KR20240096586A (ko) 수소 액화기
US20170131027A1 (en) Systems and Methods for LNG Refrigeration and Liquefaction
US20150192330A1 (en) Method and device for generating electrical energy
Cetin et al. Integration of cryogenic energy storage and cryogenic organic cycle to geothermal power plants
NO310163B1 (no) Fremgangsmåte og apparat for kondensering av hydrogen

Legal Events

Date Code Title Description
AS Assignment

Owner name: LINDE AKTIENGESELLSCHAFT, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ALEKSEEV, ALEXANDER;STILLER, CHRISTOPH;STOVER, BRIAN;SIGNING DATES FROM 20151214 TO 20160223;REEL/FRAME:037947/0140

AS Assignment

Owner name: LINDE AKTIENGESELLSCHAFT, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ALEKSEEV, ALEXANDER;STILLER, CHRISTOPH;SIGNING DATES FROM 20161128 TO 20161205;REEL/FRAME:041128/0117

Owner name: MITSUBISHI HITACHI POWER SYSTEMS EUROPE GMBH, GERM

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:STOVER, BRIAN;REEL/FRAME:041128/0153

Effective date: 20161129

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION