EP2835506A1 - Procédé pour la production d'énergie électrique et installation de production d'énergie - Google Patents

Procédé pour la production d'énergie électrique et installation de production d'énergie Download PDF

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Publication number
EP2835506A1
EP2835506A1 EP13003985.2A EP13003985A EP2835506A1 EP 2835506 A1 EP2835506 A1 EP 2835506A1 EP 13003985 A EP13003985 A EP 13003985A EP 2835506 A1 EP2835506 A1 EP 2835506A1
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Prior art keywords
stream
heat exchanger
compressed air
operating mode
refrigerant
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EP13003985.2A
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German (de)
English (en)
Inventor
Alexander Dr. Alekseev
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Linde GmbH
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Linde GmbH
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Publication date
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Priority to EP13003985.2A priority Critical patent/EP2835506A1/fr
Publication of EP2835506A1 publication Critical patent/EP2835506A1/fr
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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
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/004—Accumulation in the liquid branch of the circuit
    • 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
    • F01K13/00—General layout or general methods of operation of complete plants
    • F01K13/02—Controlling, e.g. stopping or starting
    • 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
    • F25J1/003—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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air

Definitions

  • the invention relates to a method for generating electrical energy in a combined power generation plant comprising an air treatment unit and a power plant unit, and a corresponding power generation plant according to the preambles of the independent claims.
  • air in an air separation plant with an integrated condenser or in a dedicated liquefaction plant is liquefied in whole or in part to form such an air liquefaction product.
  • the air liquefaction product is stored in a tank system with cryogenic tanks. This mode of operation is referred to herein as "liquefaction operation”.
  • the air liquefaction product is withdrawn from the tank system, pressure increased by a pump and warmed to about ambient temperature or higher and thus converted to a gaseous or supercritical state.
  • a thus obtained high-pressure stream is expanded in a power plant unit in an expansion turbine or more expansion turbines with reheating to ambient pressure.
  • the thereby released mechanical power is converted into electrical energy in one or more generators of the power plant unit and fed into an electrical grid. This mode of operation is referred to herein as "picking operation".
  • the released during the transfer of the air liquefaction product in the gaseous or supercritical state cold can also be stored during the extraction operation and used during the liquefaction operation to provide cold for the recovery of the air liquefaction product.
  • compressed air storage power plants are known in which the feed 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 economics of such methods and devices are greatly affected by the overall efficiency.
  • the invention has for its object to improve appropriate methods and devices in their economics.
  • a “power station unit” is understood here to mean a system or a system component which is or is set up for the generation of electrical energy.
  • a power plant unit comprises at least one expansion turbine, which is coupled to at least one generator. The released during the relaxation of a fluid in the at least one expansion turbine mechanical power can therefore be converted into electrical energy.
  • An “air treatment unit” is understood here to mean an installation which is set up for the purpose of obtaining at least one "air liquefaction product" from air.
  • this can be an air separation plant which can be set up to obtain corresponding air fractions or else only a liquefaction unit of such a plant or a dedicated liquefaction unit.
  • 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 tank system.
  • An "air separation plant” is charged with atmospheric air and has a distillation column system for decomposing the atmospheric air into its physical components, particularly nitrogen and oxygen.
  • the air is first cooled to near its dew point and then introduced into the distillation column system.
  • methods and apparatus for cryogenic separation of air are known Hausen / Linde, Tiefftemperaturtechnik, 2nd edition 1985, chapter 4 (pages 281 to 337 ) known.
  • an "air liquefaction plant” does not include a distillation column system.
  • their structure corresponds to that of an air separation plant with the delivery of an air liquefaction product.
  • liquid air can be generated as a by-product in an air separation plant.
  • an “air liquefaction product” is any product that can be produced, at least by compressing, cooling, and then deflating air in the form of a cryogenic liquid.
  • an air liquefaction product may be liquid air, liquid oxygen, liquid nitrogen and / or a liquid noble gas such as liquid argon.
  • liquid oxygen and liquid nitrogen in each case also designate a cryogenic liquid which has oxygen or nitrogen in an amount above that atmospheric air lies. It does not necessarily have to be pure liquids with high contents of oxygen or nitrogen.
  • Liquid nitrogen is thus understood to mean either pure or substantially pure nitrogen, as well as a mixture of liquefied air gases whose nitrogen content is higher than that of the atmospheric air. For example, it has a nitrogen content of at least 90, preferably at least 99 mole percent.
  • cryogenic liquid or a corresponding fluid, air liquefaction product, electricity, etc.
  • a liquid medium is understood, the boiling point is well below the respective ambient temperature and, for example, 200 K or less, in particular 220 K or less.
  • cryogenic media are liquid air, liquid oxygen and liquid nitrogen.
  • a “heat exchanger system” is used to transfer heat indirectly between at least two countercurrent streams, such as a warm compressed air stream and one or more cold streams or a cryogenic air liquefaction product, and one or more hot streams.
  • a heat exchanger system may be formed of a single or multiple heat exchanger sections connected in parallel and / or in series, e.g. from one or more plate heat exchanger blocks.
  • a “compressor system” is a device designed to compress at least one gaseous stream from at least one inlet pressure at which it is supplied to the compressor system to at least one final pressure at which it is taken from the compressor system.
  • the compressor system forms a structural unit, which, however, can have a plurality of "compressor stages” in the form of known piston, screw and / or Schaufelrad- or turbine assemblies (ie radial or Axialverêtrchn).
  • these compressor stages are driven by means of a common drive, for example via a common shaft and / or a common electric motor.
  • Several compressor systems for example a main compressor and a secondary compressor of an air treatment unit, can form a "compressor arrangement".
  • a “cold compressor system”, such as the compressor systems just discussed, may have one or more compressor stages driven by a common shaft, is a compressor system that compresses gas streams in the cryogenic state.
  • Cold compressors are characterized in particular by at least one radial compressor stage, a low-temperature housing and / or an electric drive unit with integrated storage.
  • a “single cold compressor system” or a “single compressor system” is designed as a structural unit, which is present only once in a corresponding system, but may include one or more compressor stages. If several compressor stages are provided, these are coupled via a common shaft to a common compressor drive.
  • the single cold compressor system or the single compressor system fluid is supplied in particular in the form of only one fluid stream, which is compacted with the one compressor stage in one step or with multiple compressor stages successively in several steps.
  • Partial expansion turbines may be designed for use in the present invention as a turboexpander. If one or more expansion turbines designed as turboexpanders are coupled to one or more compressor stages, for example in the form of centrifugal compressor stages, and if necessary mechanically braked, but these are operated without externally supplied energy, for example by means of an electric motor, the term “booster turbine” is used for this purpose. used. Such a booster turbine compresses at least one current by the relaxation of at least one other current, but without external, for example by means of an electric motor, supplied energy.
  • a "gas turbine” is understood to mean an arrangement of at least one combustion chamber and at least one of these downstream expansion turbines (the gas turbine in the narrower sense). In the latter, hot gases are released from the combustion chamber to perform work.
  • a gas turbine may further comprise at least one of the expansion turbine via a common shaft driven compressor stage, typically with at least one radial compressor stage, have. Some of the mechanical energy generated in the expansion turbine is usually used to drive the at least one compressor stage. Another part is regularly converted to generate electrical energy in a generator.
  • a "combustion turbine” only has the aforementioned combustion chamber and one of these downstream expansion machine.
  • a compressor is usually not provided.
  • a hot gas turbine In contrast to a gas turbine, instead of a combustion chamber, a "hot gas turbine” has a heater.
  • a hot gas turbine can be designed in one stage with a heater and an expansion turbine. Alternatively, however, several expansion turbines, preferably with intermediate heating, may be provided. In any case, in particular downstream of the last expansion turbine, a further heater can be provided.
  • the hot gas turbine is also preferably coupled to one or more generators for generating electrical energy.
  • a “heater” is understood to mean a system for indirect heat exchange between a heating fluid and a gaseous fluid to be heated.
  • a heating fluid By means of such a heater, residual heat, waste heat, process heat, solar heat, etc. can be transferred to the gaseous fluid to be heated and used for energy generation in a hot gas turbine.
  • a "waste heat steam generator”, also referred to as a heat recovery steam generator (HRSG), is capable of generating steam by heating water or for further heating, e.g. from cold steam to superheated steam, by means of a waste heat stream, for example one of a still hot or postheated gas stream downstream of a gas turbine or hot gas turbine.
  • HRSG heat recovery steam generator
  • a "tank system” is understood to mean an arrangement having at least one cryogenic storage tank which is designed to store a cryogenic air liquefaction product.
  • a corresponding tank system has insulation means and is mounted, for example, together with an air treatment unit in a cold box.
  • 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 pressure drops or expected pressure drops, for example, due to cooling effects.
  • the pressure levels indicated here in bar are absolute pressures.
  • cryogenic air liquefaction products or corresponding liquid streams are "converted into a gaseous or supercritical state by heating in the context of the present application, this includes, on the one hand, a regular phase transition by evaporation, if this takes place at subcritical pressure. However, if such cryogenic air liquefaction products or corresponding liquid streams are heated at a pressure which is above the critical pressure, when heated above the critical temperature, no phase transition in the strict sense, but a transition from the liquid to the supercritical state, for which here Term “pseudoevaporating" is used.
  • a "collecting stream” is understood to mean a total of two or more streams, for example two or more compressed air streams at the same or different pressure, which is transferred from a first functional or constructional unit of a plant into a second functional or structural unit.
  • a collecting stream is transferred from an air treatment unit into a power plant unit.
  • a collecting stream can be routed in one or more lines.
  • a "formation" of a corresponding collective stream is therefore its provision by the first functional or structural unit to the second functional or structural unit.
  • the two or more streams will be there especially in a common direction. However, this need not necessarily be done, a collecting stream, as mentioned, are also performed in two or more lines.
  • the present invention is based on a previously explained method for generating electrical energy in a combined power generation plant comprising an air treatment unit and a power plant unit.
  • a first warm compressed air flow in a heat exchanger system is cooled to a first cold compressed air flow.
  • a first cryogenic liquid stream of an air liquefaction product is produced, which is stored in a tank system.
  • the first cryogenic liquid stream is liquefied air or another air fraction, such as liquid nitrogen or a nitrogen-enriched fraction.
  • the cryogenic liquid stream contains significantly less than 40 mole percent oxygen.
  • a second warm compressed air stream in the heat exchanger system is cooled to a second cold compressed air stream, the second cold compressed air stream being compressed in a cold compressor system to a first high pressure stream.
  • the second cold compressed air stream is fed to the cold compressor system at the lowest temperature level which can be provided by the heat exchanger system, in particular at -140 to -180 ° C., for example at -150 to -170 ° C.
  • the first compressed air flow of the first mode of operation is provided by compression in a main compressor system and repressurization in a post-compressor system.
  • Both the main and the Nachverêtrsystem can thereby comprise a plurality of compressor stages, which, as already explained above, are driven by a common compressor drive via a common shaft.
  • the main compressor system and the Nachverêtrsystem can also have means for intermediate and post-cooling.
  • a compressed-air flow downstream of the after-compressor system can be increased again by a booster turbine.
  • the correspondingly compressed first compressed air flow can also be at least partially expanded in an expansion turbine integrated in the heat exchanger system, which can be coupled to a generator, for example, whereby cold can be generated for operation of the heat exchanger system.
  • the second warm compressed air flow of the second operating mode is preferably compressed only by compression in the main compressor system. It is thus preferably provided at a lower pressure level than the first compressed air flow and fed into the heat exchanger system.
  • the first and second warm compressed air streams are respectively cooled to the first and second cold compressed air streams, wherein equal or different temperature levels can be generated by removing the first and second cold compressed air streams from the heat exchanger system at different locations.
  • the first and the second warm compressed air stream in the heat exchanger system which may in particular comprise two heat exchanger blocks, passed through different passages.
  • the first and the second warm compressed air stream can each be provided in different volume flows.
  • the first warm compressed air flow of the first mode of operation is diverted from a main stream that has been compressed in the main and in the Nachverêtrsystem.
  • a remaining flow is also cooled in the heat exchanger system or in a part of this heat exchanger system, for example a first heat exchanger block.
  • the correspondingly cooled residual flow is subsequently expanded in an expansion turbine, which is part of the previously explained booster turbine, by means of which the first warm compressed air flow is provided.
  • the cooling required for Heilverflüs Trent is generated and uses the released mechanical power.
  • the residual stream which has been relieved in the booster turbine can then preferably be warmed up in the heat exchanger system and, for example, fed again to the after-compressor system. Details of this are shown in the attached figures and will be explained in more detail with reference to these.
  • a second cryogenic liquid stream is also removed from the tank system, pressure-increased by means of a pump and heated in the heat exchanger system and thus converted into a gaseous or supercritical state, ie vaporized or pseudo-vaporized to a second high pressure stream.
  • the second high-pressure stream is combined with the first high-pressure stream, which, as explained above, is obtained from the second cold compressed air stream by means of the cold-compressor system, to form a collecting stream.
  • the collecting stream which is present at a pressure level of in particular 12 bar or more, or a stream derived from the collecting stream, is expanded in at least one expansion turbine coupled to a generator of the illustrated power plant unit.
  • a "collecting stream" can also be conducted at several pressure levels in different lines.
  • the volume flow of the collecting stream advantageously comprises at most 110% of the combined volume flows of the first and second high-pressure streams.
  • the collecting stream is formed exclusively from the first and the second high-pressure stream, which does not preclude, however, diverting partial streams from the first and / or the second high-pressure stream before combining them with the collecting stream and being able to be fed again to the respective streams.
  • These can be used, for example, for the regeneration of a cleaning system or adsorbent container used herein. It follows that no further streams are combined to form the collecting stream. This means that advantageously only a single second compressed air flow generated with a cold compressor system is used or only a single cold compressor system is used in the system according to the invention.
  • the cold compressor system used to compress the second cold compressed air stream is advantageously the only cold compressor system used in the power plant. It should be noted that a cold compressor system is powered by means of a drive powered by external energy, such as an electric motor, and thereby different from a booster turbine.
  • the first and second cryogenic liquid streams are stored in and removed from the same tank system, the first and second cryogenic liquid streams i.d.R. an identical composition, ie consist of the same air liquefaction product.
  • first operating mode preferably only the first warm and the first cold compressed air flow are provided and that in the second operating mode, preferably only the second hot and the second cold compressed air flow are provided.
  • Corresponding streams may, unless otherwise indicated, each have an identical composition and / or identical temperature levels and / or be conducted in the same lines. Therefore, a distinction between "first" and "second" hot and cold compressed air streams is therefore partially made to identify differences between the first and second modes of operation.
  • the evaporation or pseudo-vaporization of the second cryogenic liquid stream is carried out in the heat exchanger system of the air treatment unit.
  • the cryogenic liquid stream is not introduced into a separate heat exchanger and evaporated or pseudo-vaporized, for example against atmospheric air or hot (water) steam, but this step is performed in the heat exchanger system of the air treatment unit, anyway the cooling of the first warm compressed air flow in the first operating mode is present.
  • feed air in the form of the second warm compressed air flow in the heat exchanger system is also cooled in the second operating mode.
  • a required for the evaporation of the second cryogenic liquid flow heating medium is generated using the existing air treatment unit and this does not have to be turned off.
  • the second operating mode in which the energy price is high, to continue operating the air treatment unit and in particular a corresponding main compressor system.
  • this high operational advantages are connected, because the main compressor system when switching between the operating modes does not have to be switched off and on, but can continue to run continuously.
  • the first high-pressure stream can be obtained in an especially energy-efficient manner, since the compaction generally requires less energy at low temperatures. Therefore, in this way, additional electrical energy can be obtained very favorably from the first high-pressure current.
  • the first hot compressed air stream in the first operating mode in the heat exchanger system, is cooled at least partially against a flow of a liquid refrigerant, and the second low-temperature liquid stream in the second operating mode in the heat exchanger system partly against a flow of liquid Is heated refrigerant.
  • the heat exchange diagram of a heat exchanger system used can be made particularly favorable.
  • a liquid refrigerant in particular methanol (range up to -95 ° C) is used.
  • a liquid refrigerant for use in the invention is particularly selected based on its boiling point. This must be selected so that the liquid refrigerant is liquid in the entire work area. Suitable for this purpose, as mentioned, in particular methanol, but also ethanol.
  • the nideder strip alcohols listed in the following table can also be used as a refrigerant in the present invention.
  • liquid or the liquid refrigerant are guided in corresponding heat exchanger sections or heat exchanger blocks of the heat exchanger system and stored in suitable cold-insulated refrigerant tanks.
  • the respective flow of liquid refrigerant in the first operating mode is advantageously taken from a first coolant tank, heated in the heat exchanger system and transferred to a second coolant tank.
  • the flow of liquid refrigerant is taken from the second refrigerant tank, cooled in the heat exchanger system, and transferred to the first refrigerant tank.
  • a non-condensing gas for example nitrogen, superimposed on the liquid refrigerant in the first and second refrigerant tanks is advantageously used here. This is taken from the first refrigerant tank in the first operating mode, cooled in the heat exchanger system and transferred to the second refrigerant tank. In the second mode of operation, the illustrated flow of non-condensing gas is taken from the second refrigerant tank, heated in the heat exchanger system, and transferred to the first refrigerant tank.
  • a completely self-sufficient, reversible cooling possibility for the currents described above is created on the whole, which does not rely on the supply of external refrigerants and is capable of reversibly storing the respective supplied or discharged cold.
  • the cold (thermal energy) resulting from the evaporation or pseudo-vaporization of the second cryogenic liquid stream in the second operating mode could also be converted into mechanical energy (compressed air energy) by means of an additional cold compressor system.
  • this process is also highly irreversible, causing thermodynamic losses and has a negative effect on the efficiency of a corresponding system.
  • the method according to the invention proves to be particularly advantageous over likewise fundamentally possible methods, in which the provision of the currents relaxed in the power unit takes place by means of at least two parallel-connected cold compressor systems.
  • the at least two cold compressor systems can have the same or different inlet temperature.
  • the second operating mode at least part of the generation of electrical energy from the collecting stream is carried out in an expansion turbine of a gas turbine of the power station unit.
  • the expansion turbine of the gas turbine is supplied with a current derived from the collecting stream.
  • the collecting stream is introduced into a combustion chamber of the gas turbine into which a fuel, for example natural gas, biogas or the like, is simultaneously introduced.
  • the fuel is burned in the combustion chamber in an atmosphere created at least in part by the collection stream.
  • the combustion chamber also other streams, such as an oxygen-rich stream, are supplied.
  • the expansion turbine of the gas turbine is thus supplied with a fluid derived from the collecting stream (by the admission of the exhaust gas of the combustion in the combustion chamber and the partial conversion of the oxygen possibly contained in the collecting stream).
  • a fluid derived from the collecting stream by the admission of the exhaust gas of the combustion in the combustion chamber and the partial conversion of the oxygen possibly contained in the collecting stream.
  • the volume is further increased.
  • only part of the collected stream, for example 4 to 5%, is chemically reacted in the combustion chamber with the fuel by combustion, i.
  • the fuel is reacted in the combustion chamber with a significantly more than stoichiometric amount of the collecting stream or the oxygen contained therein.
  • At least part of the generation of mechanical energy from the collecting stream or a stream derived therefrom is carried out in this variant in the gas turbine of the power plant unit, ie in an apparatus already present in the power plant unit for converting pressure energy into mechanical drive energy.
  • An additional separate system for work-performing expansion of the collecting stream or a stream derived therefrom can be less complicated in the context of the invention or omitted altogether.
  • the entire generation of mechanical or electrical energy from the collecting stream or a current derived therefrom in the gas turbine can be made.
  • the expansion turbine in which the collecting fluid or the fluid derived therefrom is expanded part of a hot gas turbine, which comprises at least one heater in addition to the expansion turbine.
  • the heater is operated in particular by means of solar heat and / or waste heat from other processes, so that the process is particularly economical.
  • the two variants mentioned can also be combined by using a power station unit with both one or more hot gas turbines and with one or more gas turbines.
  • the collecting stream or a stream derived therefrom, for example, relaxed in two steps, the first step as work-performing relaxation in the hot gas turbine (after previous heating in a heater) and the second step as work-related relaxation in the gas turbine (after passing through the combustion chamber) performed become.
  • the collecting stream is in particular in the hot gas turbine of a Hot gas turbine inlet pressure relaxed on a hot gas turbine outlet pressure.
  • the hot gas turbine outlet pressure increases again in the downstream combustion chamber of the gas turbine, so that a corresponding flow is again pressure-increased fed to the expansion turbine of the gas turbine.
  • this may also be formed with an axle or shaft which is equipped with expansion turbines arranged on both sides of the generator.
  • expansion turbines arranged on both sides of the generator.
  • a corresponding expansion turbine can also be followed by other plants or facilities for the recovery of energy.
  • at least one waste heat steam generator can be provided.
  • the waste heat steam generator which may for example be connected downstream of a gas turbine or hot gas turbine, residual heat can be used from an exhaust gas stream obtained there to generate steam.
  • the steam can in turn be used to operate a generator.
  • cryogenic, liquefied stream into the tank system under superatmospheric pressure, for example at a pressure level of 8 to 12 bar or at atmospheric pressure.
  • Storage at superatmospheric pressure makes it possible to dispense with subcooling of a corresponding flow, which reduces the refrigeration requirement and thus the amount of air required in the system.
  • the power generating plant also provided according to the invention benefits from the advantages explained above, to which reference is expressly made.
  • This has in particular a control device which at least accomplishes the automatic control of the power generation plant during the first operating mode and during the second operating mode.
  • Figure 1A shows a power plant according to an embodiment of the invention in a first mode of operation.
  • the power generation plant is designated 100 in total. It has components of an air handling unit, dashed and total of 10, and components of a power plant unit, which are dashed and total 20.
  • the Indian Figure 1A shown first operating mode of the power generation plant 100 corresponds to the previously explained in more detail liquefaction operation.
  • a main compressor system 11 of the air treatment unit 10 which may be preceded by an air filter 111, ambient air AIR is sucked in and compressed.
  • the main compressor system 11 may comprise a plurality of compressor stages (here without a separate designation) as well as means for intermediate and after-cooling.
  • the compressor stages of the main compressor system 11 can be driven by a common compressor drive M.
  • aftercooling it is also possible, for example, to provide a heat exchanger 112 which can be operated with a stream taken downstream in the air treatment unit 10 (see links 1 and 2).
  • a stream a provided by the main compressor system 11 may be supplied to a purification system 12 having suitable means for purifying the flow a, for example a pair of adsorbent vessels 121 and 122 filled, for example, with molecular sieve.
  • the latter can be used in alternating operation for the purification and regenerated, including suitable switching means (not illustrated in detail) are provided.
  • streams can be used which are taken downstream in the air treatment unit 10 (see links 3 and 4).
  • a correspondingly purified stream b can then be fed to a post-compressor system 13 of the air treatment unit 10.
  • the secondary compressor system 13 like the main compressor system 11, can have a plurality of compressor stages (not designated in any more detail) with means for intermediate and after-cooling and can be driven by means of a common compressor drive M.
  • a current c thus obtained can be further increased in pressure in a compressor stage 141 of a booster turbine 14.
  • the compressor stage 141 of the booster turbine 14 is mechanically coupled to an expansion turbine 142 which may be driven by means of an expanding stream diverted downstream from the stream d (see below).
  • a further pressure d in the booster turbine 14 can be fed into a heat exchanger system 15 of the air treatment unit.
  • the heat exchanger system 15 of the air treatment unit 10 has a first heat exchanger block 151 and a second heat exchanger block 152.
  • the stream d is split into a first substream e and a second substream f. Both partial flows are supplied to the first heat exchanger block 151 of the heat exchanger system 15 at its warm end.
  • the first partial flow e passes through the first heat exchanger block 151 of the heat exchanger system 15 up to its cold end. He is then relaxed in the expansion turbine 142 of the previously explained Boosterturbine 14. After expansion, this stream is fed to the cold end of the second heat exchanger block 152 of the heat exchanger system 15 and heated there. After further heating in the first heat exchanger block 151 of the heat exchanger system 15, the correspondingly obtained warm stream is fed again to the after-compressor system 13.
  • the second partial flow f (the previously mentioned “first warm compressed air flow”) passes through the first heat exchanger block 151 of the heat exchanger system 15 almost to its cold end and is taken there as stream g. After a further cooling in the second heat exchanger block 152 of the heat exchanger system 15, this is present as stream h (the "first cold compressed air stream”).
  • the stream h is then liquefied and subcooled in a liquefaction system 16 comprising a braked turbine 161, a separator 162 and a subcooler 163.
  • the subcooler 163 may also be operated with a partial flow j of a cryogenic liquid stream i obtained by the liquefaction.
  • the stream j is warmed in the heat exchanger system 15 and discharged to the amb environment.
  • the deep-drawn liquid stream i withdrawn from the sump of the separator 162 is fed into a tank system 17 as a cryogenic air liquefaction product.
  • the cryogenic air liquefaction product is also referred to as LAIR and represents liquefied air in the example shown.
  • LAIR cryogenic air liquefaction product
  • liquid nitrogen products, impure nitrogen and the like can also be used as air liquefaction products.
  • the cooling of the corresponding streams in the first heat exchanger block of the heat exchanger system 17 takes place at least in part by means of expansion cooling, which is generated by the expansion turbine 142. Further cold is provided in the context of the present invention by means of a refrigerant system 18.
  • the refrigerant system 18 shown in FIGS. 3A and 3B 3B is illustrated in detail, has at least two refrigerant tanks and is adapted to be used in the Figure 1A illustrated first mode of operation to conduct a cooled liquid refrigerant as stream k from the cold end to the warm end through the heat exchanger block 151 of the heat exchanger system 15.
  • the cooled liquid refrigerant is thus heated against a stream e or f to be cooled in the first heat exchanger block 151 of the heat exchanger system 15.
  • the use of the refrigerant system 18 allows the reversible supply of cold to the streams passing through the first heat exchanger block 151 of the heat exchanger system 15.
  • the power plant unit 20 is in the in Figure 1A
  • the first operating mode shown is not in operation or is fed exclusively by means of a fuel F.
  • the power plant unit 20 will therefore be described with reference to the following FIG. 1 B explained in more detail.
  • FIG. 1B shows the power generation plant 100, which is also in Figure 1A is shown in the multiply explained second operating mode, the removal operation.
  • the stream b likewise provided in the removal operation is not recompressed in the after-compressor system 13 in the second operating mode.
  • this stream b (the "second warm compressed air stream") is completely cooled in the first heat exchanger block 151 and the second heat exchanger block 152 of the heat exchanger system 15.
  • a cold compressed air flow m obtained thereby (the "second cold compressed air flow") is then compressed in a multi-stage cold compressor 19, the compressor stages of which can in turn be driven by means of a common compressor drive M.
  • a partially heated and compressed stream n obtained by the heat of compression and the compressor capacity of the cold compressor 19 is further heated in the first heat exchanger block 151 of the heat exchanger system 15 and leaves it as a warm high pressure stream o ("first high pressure stream").
  • the cryogenic air liquefaction product LAIR fed into the first operating mode from the tank system 17 is taken as stream p (the "cryogenic liquid stream"), liquid pressure increased by a pump 171, and stream q at superatmospheric pressure in the tank Heat exchanger system 15 is converted into a gaseous or supercritical state.
  • the stream q is first supplied to the second heat exchanger block 152 of the heat exchanger system 15 and taken almost at its warm end.
  • the withdrawn stream is then passed through the first heat exchanger block 151 of the heat exchanger system 15 and expanded in an expansion turbine 152, which may be coupled to a generator G.
  • additional energy and cold can be gained.
  • the correspondingly relaxed stream which has undergone renewed cooling due to the expansion, is fed again near its cold end to the first heat exchanger block 151 of the heat exchanger system 15. It leaves the first heat exchanger block 151 of the heat exchanger system 15 as a warm high pressure stream s ("second high pressure stream").
  • the first high-pressure stream o and the second high-pressure stream s are combined to form a collecting stream t and discharged from the air treatment unit 10.
  • the collecting stream t is introduced into the power plant unit 20.
  • the collecting stream t first passes through a heat exchanger 21. Subsequently, the collecting stream t is passed through a combustion chamber 22, in which a suitable fuel F, for example natural gas, is burned. By the formed exhaust gas, the volume of the collecting stream t increases, and it is obtained from the collecting stream derived current u.
  • a suitable fuel F for example natural gas
  • This is supplied to an expansion turbine 23, which may be formed for example as part of a gas turbine and is coupled to a generator G.
  • the mechanical power dissipated by the relaxation of the current u derived from the collecting current t can thus be converted into electrical energy.
  • the heat exchanger 21, which is used for further heating of the collecting stream t can be operated by means of an exhaust gas v from the expansion turbine 23.
  • Regenerating gas can also be heated for regeneration in the cleaning unit 12 by means of the heat exchanger 21 (cf., link 1 to stream s, links 1 and 2 in the heat exchanger 112, links 2 and 3 in the heat exchanger 21, links 3 and 4 in the cleaning system 12 , Link 4 to stream t).
  • the heat exchanger 21 cf., link 1 to stream s, links 1 and 2 in the heat exchanger 112, links 2 and 3 in the heat exchanger 21, links 3 and 4 in the cleaning system 12 , Link 4 to stream t).
  • FIGS. 2A and 2 B show a power generation plant 200 according to another embodiment of the invention, in which the air treatment unit 10 and the tank system 17 are arranged for a pressure storage of the cryogenic air liquefaction product LAIR.
  • a corresponding power generation plant 200 is shown again in the already explained operating modes (liquefaction operation and removal operation). The operation of the system is not explained repeatedly.
  • the energy generation plant 200 or its air treatment unit 10 differs from the energy generation plant 100 or its air treatment unit 10 in particular by the absence of the heat exchanger or subcooler 163, which is operated with the current j. Due to the pressure storage of the cryogenic air liquefaction product LAIR in the tank system 17, a corresponding system can therefore be operated more efficiently, because no portion of the cryogenic air liquefaction product LAIR (cf flow j in FIG Figure 1A ) must be used for the subcooling in the heat exchanger 163.
  • the in the FIGS. 1A to 2B shown currents can be present in particular at the following pressure levels: Stream a, b 3 to 8 bar, in particular 4 to 6 bar Electricity c 30 to 100 bar, in particular 30 to 50 bar Stream d, e, f 45 to 100 bar, in particular 50 to 70 bar Electricity i 1 to 8 bar, in particular 1 to 6 bar Stream n, o, s, t, u 10 to 40 bar, in particular 12 to 20 bar Electricity q 30 to 100 bar, in particular 40 to 80 bar Electricity v Atmospheric pressure or 1 to 1.2 bar
  • FIGS. 3A and 3B show a refrigerant system 18, which in its basic. Function has already been explained above, in the previously explained operating modes (first operating mode or liquefaction operation in Figure 3A, second operating mode or removal operation, in FIG. 3B ). The already partially explained currents I and k are in the figures 3A and 3B shown again. Furthermore, FIGS. 3A and 3B show 3B the first heat exchanger block 151 of the heat exchanger system 15, which has already been explained above in its integration into corresponding power generation plants 100 and 200 or their air treatment units 10.
  • the first heat exchanger block 151 of the heat exchanger system 15 is flowed through here only by a current e or f (liquefaction operation) and o or s (removal operation).
  • a current e or f liquefaction operation
  • o or s removal operation
  • cold is transferred from a liquid refrigerant to the flows e or f
  • cold is transferred from the cold flows o or s to the liquid refrigerant.
  • the designation of the currents k and I corresponds to that of the FIGS. 1A to 2B ,
  • the refrigerant system 18 comprises a first refrigerant tank 181 and a second refrigerant tank 182, in each of which the liquid refrigerant is superimposed by a gaseous, non-condensing medium, for example gaseous nitrogen.
  • the gaseous nitrogen forms the current I, the liquid refrigerant the current k.
  • the liquid refrigerant from the second refrigerant tank 182 is pumped by means of a pump 183 from the cold end to the warm one End passed through the first heat exchanger block 151 of the heat exchanger system 15 as a current k.
  • the current k can thereby heat up.
  • FIGS. 4 to 8 different embodiments of the power plant unit 20 are shown, which can be used alternatively or optionally in combination in the context of the present invention. Already explained elements are not discussed again for clarity.
  • FIG. 4 illustrated embodiment of the power plant unit 20 in all FIGS. 4 to 8 can be realized as so-called "Power Island" is, as already explained above, a combustion chamber 22 is present.
  • a heat exchanger 21 is not shown in the example shown, but can also be realized here.
  • a waste heat steam generator 24 is additionally provided here. In this way, by means of the generator G, which is coupled to the expansion turbine 23, a first power component P1, and via the waste heat steam generator 24, a second power component P2 can be obtained.
  • the waste heat steam generator 24 is configured, for example, to generate high-pressure steam, which can be used in a downstream turbine and / or in other system components.
  • FIG. 5 illustrated embodiment of the power plant unit 20 differs from that in the FIGS. 1A to 2B shown embodiments, characterized in that instead of the combustion chamber 22, a supplied with externally supplied heat Q1 heater 25 is provided.
  • This can represent, for example, waste heat of another process, heat from a heat storage system and / or heat from a solar system.
  • a particularly resource-saving operation of a corresponding system can be realized.
  • FIGS. 6 to 8 Power plant units 20 are shown, which allow a reduction of an axle load on a generator G.
  • the elements used in this case have already been explained predominantly.
  • the reduction of the axle load on the generator G results essentially by the provision of paired components.
  • the combustion chamber 22 easily available.
  • a stream from the combustion chamber 22 is divided downstream of the combustion chamber 22 into two sub-streams (without designation), which are separately fed into each one expansion turbine 23 a and 23 b and relaxed in this.
  • the generator G the common mechanical power of the expansion turbines 23a and 23b can thus be set into electrical power P.
  • FIGS. 7 and 8 illustrated embodiments two expansion turbines 23a and 23b are provided in each case.
  • two separate combustion chambers 22a and 22b are present, which in FIG. 8 embodiment shown further comprises two separate heat exchanger blocks 21 a and 21 b. Due to the symmetrical arrangement of the expansion turbines 23a and 23b in the previously explained FIGS. 6 to 8 the axle load is transmitted symmetrically to the generator G.

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015181553A3 (fr) * 2014-05-30 2016-03-31 Highview Enterprises Limited Perfectionnements apportés à des unités de purification d'air
EP3037764A1 (fr) * 2014-12-09 2016-06-29 Linde Aktiengesellschaft Procede et installation combinee destines a stocker et a recuperer l'energie

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
JPH04132837A (ja) * 1990-09-20 1992-05-07 Mitsubishi Heavy Ind Ltd ガスタービン発電設備
US20030101728A1 (en) * 1996-12-24 2003-06-05 Harumi Wakana Cold heat reused air liquefaction/ vaporization and storage gas turbine electric power system
WO2007096656A1 (fr) 2006-02-27 2007-08-30 Highview Enterprises Limited Procédé de stockage d'énergie et système de stockage d'énergie cryogénique
GB2494400A (en) * 2011-09-06 2013-03-13 Highview Entpr Ltd Cryogenic energy storage system
EP2604824A1 (fr) * 2011-12-13 2013-06-19 Linde Aktiengesellschaft Procédé et installation pour la production d'énergie électrique

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
JPH04132837A (ja) * 1990-09-20 1992-05-07 Mitsubishi Heavy Ind Ltd ガスタービン発電設備
US20030101728A1 (en) * 1996-12-24 2003-06-05 Harumi Wakana Cold heat reused air liquefaction/ vaporization and storage gas turbine electric power system
WO2007096656A1 (fr) 2006-02-27 2007-08-30 Highview Enterprises Limited Procédé de stockage d'énergie et système de stockage d'énergie cryogénique
GB2494400A (en) * 2011-09-06 2013-03-13 Highview Entpr Ltd Cryogenic energy storage system
EP2604824A1 (fr) * 2011-12-13 2013-06-19 Linde Aktiengesellschaft Procédé et installation pour la production d'énergie électrique

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Tieftemperaturtechnik", 1985, article "Verfahren und Vorrichtungen zur Tieftemperaturzerlegung von Luft sind z.B", pages: 281 - 337

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015181553A3 (fr) * 2014-05-30 2016-03-31 Highview Enterprises Limited Perfectionnements apportés à des unités de purification d'air
US10591210B2 (en) 2014-05-30 2020-03-17 Highview Enterprises Limited Air purification units
EP3037764A1 (fr) * 2014-12-09 2016-06-29 Linde Aktiengesellschaft Procede et installation combinee destines a stocker et a recuperer l'energie

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