Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
  • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
  • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
  • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
  • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
  • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
  • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
  • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
  • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
  • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
  • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
  • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
  • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
  • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
  • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
  • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
  • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
  • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
  • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
  • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
  • F25J3/04224—Cores associated with a liquefaction or refrigeration 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
  • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
  • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
  • F25J3/0426—The cryogenic component does not participate in the fractionation
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
  • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
  • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
  • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
  • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
  • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
  • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
  • F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of 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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
  • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
  • F25J3/04448—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
  • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
  • F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
  • F25J3/04581—Hot gas expansion of indirect heated nitrogen
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  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04763—Start-up or control of the process; Details of the apparatus used
  • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
  • F25J3/04812—Different modes, i.e. "runs" of operation
  • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
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  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04763—Start-up or control of the process; Details of the apparatus used
  • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
  • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
  • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04763—Start-up or control of the process; Details of the apparatus used
  • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
  • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
  • F25J3/04884—Arrangement of reboiler-condensers
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  • 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
  • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
• • 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
  • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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  • 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
  • F25J2210/42—Nitrogen
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  • 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
  • F25J2210/50—Oxygen
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  • 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
  • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
  • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
  • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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  • 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
  • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
  • F25J2250/00—Details related to the use of reboiler-condensers
  • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
• • 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
  • F25J2250/00—Details related to the use of reboiler-condensers
  • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
  • F25J2250/40—One 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
  • F25J2250/00—Details related to the use of reboiler-condensers
  • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
  • F25J2250/50—One fluid being 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
  • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
  • F25J2260/50—Integration in an installation using oxygen, e.g. in the burner of a glass facility, waste incineration or oxygen based process [OBP] in general

Definitions

• the invention relates to a method for producing at least one air product, an air separation plant and a method and a device for generating electrical energy according to the preambles of the independent claims.
• condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
• Each condenser evaporator has a
• Condensing passages or evaporation passages exist.
• the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow.
• Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
• Evaporation space of a condenser-evaporator may be formed as a bath evaporator, falling film evaporator or forced-flow evaporator.
• the low-pressure column bottom evaporator is in the evaporation chamber a
• Low-pressure column intermediate evaporator is in the evaporation chamber a
• a method of the type mentioned and a corresponding device with three columns are known from.
• processes for generating electrical energy for example the known oxyfuel process and so-called combined gasification combined cycle (IGCC)
• IGCC combined gasification combined cycle
• oxygen or oxygen-enriched gas mixtures for example for combustion or for partial oxidation, needed.
• processes and devices for the cryogenic separation of air can be used, as known, for example, from Hausen / Linde, Tiefftemperaturtechnik, 2nd edition 1985, Chapter 4 (pages 281 to 337).
• distillation column systems are used, which may be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
• devices for obtaining further air components in particular the noble gases krypton, xenon and / or argon, may be provided.
• Methods and apparatus for generating electrical energy should be designed for large load ranges and fast load changes to intercept power surges that may result from the availability or unavailability of other power feeders. Also air separation plants, which supply oxygen or appropriate gas mixtures for this, should have an in the
• the possible degree of flexibilization depends on the liquefaction capacity of the air separation plant.
• air separation plants for supplying power generation processes and apparatuses have a low liquefaction capacity, since these are designed for the production of large quantities of gaseous oxygen and nitrogen products, the air separation plant at
• Ambient temperature are taken.
• the refrigeration requirement of such plants is relatively small, so that they are not designed to provide a sufficient amount of cold for the exclusive provision of larger amounts of liquid air products. Therefore, a separate liquefaction plant (LIN, LOX or LAIR condenser) can be installed in appropriate plants and switched on during the liquefaction phase. Flexibilization can also be achieved by designing the refrigeration capacity (and thus the liquefaction capacity) of the process or plant to be higher than the actually required amounts of gaseous oxygen and nitrogen products.
• Object of the present invention is to provide methods of the type mentioned above and corresponding devices that have a large range of variation in their energy consumption and have a comparatively low energy consumption in all the corresponding mode of operation.
• An “air separation plant” is fed with possibly dried and purified air, which by means of a “main air compressor” in the form of at least one
• an air separation plant has a distillation column system for separating the air into its physical components, in particular into nitrogen and oxygen.
• the air is cooled to near its dew point and introduced into the distillation column system, as explained above.
• a pure "air liquefaction plant” or “liquefaction plant” does not include a distillation column system.
• the structure of an air liquefaction plant may correspond to that of an air separation plant with the discharge of an air liquefaction product.
• liquid air can be generated as a by-product in an air separation plant.
• a “liquid air product” is any product which can be prepared, at least by compressing, cooling and then releasing air in the form of a cryogenic liquid. In particular, this may, as mentioned, to
• liquid oxygen and “liquid nitrogen” in each case also designate cryogenic liquids which have oxygen or nitrogen in an amount which is above that of atmospheric air. It does not necessarily have to be pure liquids with high contents of oxygen or nitrogen. Under liquid nitrogen is therefore understood as pure or substantially pure nitrogen, as well as a mixture of liquefied air gases, the nitrogen content higher than that of
• atmospheric air is.
• it has a nitrogen content of at least 90, preferably at least 99 mole percent.
• cryogenic liquid or a corresponding fluid, liquid air product, stream, etc., is understood to mean a liquid medium whose boiling point is significantly 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 in the above sense.
• a "heat exchanger” is used for the indirect transfer of heat between at least two countercurrently flowed, for example, a warm compressed air stream and one or more cold streams or a cryogenic liquid air product and one or more warm streams.
• a heat exchanger may be formed from a single or a plurality of heat exchanger sections connected in parallel and / or in series, for example one or more
• a heat exchanger for example, the "main heat exchanger” used in an air separation plant, which is characterized in that the main part of the streams to be cooled or heated to be cooled or heated by him, has “passages”, which are as separate fluid channels with heat exchange surfaces are formed.
• a “warm side” temperature of a heat exchanger is the temperature at which the streams to be cooled are fed to the heat exchanger. If necessary, several streams to be cooled the
• the hot-side temperature can also refer to the average value or the lowest or highest temperature of the supplied streams to be cooled.
• a “compressor” is a device that is capable of compressing at least one
• gaseous stream of at least one inlet pressure at which it is supplied to the compressor to at least one final pressure at which this
• a compressor forms a structural unit, which, however, can have a plurality of “compressor stages” in the form of known piston, screw and / or paddle wheel or turbine arrangements (ie axial or radial compressor stages).
• This also applies to a "main air compressor” of an air separation plant, which is characterized by the fact that all or predominantly the amount of air that is fed into the air separation plant is compressed by it.
• these compressor stages are driven by means of a common drive, for example via a common shaft.
• compressors e.g. a main and a post-compressor of an air separation plant, may be coupled together.
• a “secondary compressor” is designed to further increase the pressure of an already pressurized stream.
• a “cold compressor” is characterized in that it can be supplied with a corresponding current at low temperature, in particular cryogenic.
• Cold compressor is set up according to the prior art.
• An "expansion turbine” that has a common shaft with more
• Expansion turbines or energy converters such as oil brakes, generators or compressors can be coupled, is set up for relaxation of a gaseous or at least partially liquid stream.
• Expansion turbines for use in the present invention be designed as a turboexpander. If a compressor is driven with one or more expansion turbines and this, however, operated without externally, for example by means of an electric motor, supplied energy, the term "turbine-driven" compressor is used here. Arrangements of turbine-driven compressors and
• Expansion turbines are also referred to as "booster turbines”. Under one
• Pressure nitrogen turbine or “PGAN turbine” is referred to in the context of this application, an expansion turbine, by means of which a generated in the air separation plant and a distillation column system removed nitrogen-rich
• the relaxed pressure stream can then be heated, for example in the main heat exchanger and blown off to the environment.
• a relaxation turbine called “medium pressure turbine” becomes specific in the art
• a medium-pressure turbine relaxes a compressed by a main air compressor and possibly in one
• Main heat exchanger in the medium-pressure column is a compressed by a main air compressor and possibly in one
• Tank system has isolation means.
• the present application is used for the characterization of pressures and
• pressure level and "temperature level”, which is to express that appropriate pressures and temperatures must not be used in the form of exact pressure or temperature values in order to realize the inventive 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
• the pressure levels indicated here in bar are absolute pressures.
• Liquid air products or corresponding liquid streams can be converted by heating in a gaseous or in a supercritical state.
• a regular phase transition by evaporation occurs when heating occurs at subcritical pressure.
• no phase transition in the true sense occurs when heating above the critical temperature, but a transition from the liquid to the supercritical state. If the term "evaporation" is used in the context of this application, this also includes the conversion from the liquid to the supercritical state.
• the invention is based on a method for producing at least one air product using an air separation plant comprising a main air compressor, a main heat exchanger and a distillation column system.
• the method comprises, as already mentioned, a first and a second operating mode, wherein in the first operating mode at least one in the
• the at least one stored in the first operating mode and / or at least one further, at least not generated in the second operating mode, and / or externally supplied and / or otherwise intermediately stored liquid air product (eg liquid air, liquid nitrogen or liquid oxygen) is fed into the distillation column system.
• liquid air product eg liquid air, liquid nitrogen or liquid oxygen
• Hot side temperature of the main heat exchanger is supplied to a cold compressor, in the cold compressor of a first superatmospheric
• Pressure level is compressed to a second superatmospheric pressure level, and at the second superatmospheric pressure level in at least one
• Air separation plant often readily possible because due to the inevitable heat input through the insulation and losses in the (main) heat exchanger (hot-side temperature difference) always a certain amount of cold is needed. This amount of cold is usually supplied by a used expansion turbine.
• Relaxation machine be switched off. This allows a corresponding saving of drive power at the main air compressor and / or a downstream compressor, if a so-called medium-pressure turbine is used, is relaxed in the additional compressed air.
• the corresponding method is implemented on the basis of a so-called injection turbine, by means of which air is released into the low-pressure column of the distillation column system used. If a so-called pressurized nitrogen or PGAN turbine is used, as shown in the figures shown in the context of this application, the leads
• an external expansion machine can be used, which is supplied to the corresponding pressure stream after heating in an upstream heater and the pressure flow to the for the respective application required pressure (eg for use as a regeneration) relaxed.
• Heat exchangers unfavorably change (“warp"), causing the
• Temperature of one or more emerging from the heat exchanger flows is always lower. Above a certain limit, a safe or default mode of operation of the air separation plant is no longer guaranteed.
• Infeed is then no longer possible, unless the heat input into the coldbox is increased by an additional heat source.
• any known heat generating device e.g. an air, steam, gas electrically or otherwise heated heat exchanger can be used.
• Liquids or liquid air products is performed) compressed after the shutdown of a corresponding expansion turbine (eg a pressure nitrogen turbine, as shown in the figures, but also, for example, a Einblaseturbine) available amount of pressurized nitrogen in the cold compressor, then warmed in a preheater and in a relaxed relaxation turbine.
• a corresponding expansion turbine eg a pressure nitrogen turbine, as shown in the figures, but also, for example, a Einblaseturbine
• an external expansion turbine with upstream preheater is not satisfactory in all cases, since such hardware components are extremely expensive and must be operated with considerable energy.
• a separate (medium-pressure) steam system is typically provided for operating a corresponding preheater.
• the associated losses are high.
• a method or a system without such devices is therefore particularly desirable and advantageous in terms of cost reduction and energy saving.
• the use of cold compressors in air separation plants per se is known.
• US Pat. No. 7,272,954 B2 uses a cold compressor for compressing a
• Throttling current is, as explained, for this reason compacted in order to subsequently make a corresponding relaxation in the high-pressure column for the production of additional cold.
• the inductor current is here so on a higher
• High-pressure column fed but previously relaxed again.
• the first superatmospheric pressure level is below the operating pressure of the high-pressure column.
• first operating mode of a corresponding air separation plant gaseous air products are not necessarily provided, for example to an oxyfuel or an IGCC process.
• the first mode of operation may also include taking out liquid air products from a corresponding installation and transferring them into storage tanks provided for this purpose (during the aforementioned low-flow or excess-time periods).
• Operating mode is characterized mainly by the fact that additional cold air is generated in the air separation plant, for example by means of a pressurized nitrogen, a Einblase- and / or a medium-pressure turbine.
• additional cold air is generated in the air separation plant, for example by means of a pressurized nitrogen, a Einblase- and / or a medium-pressure turbine.
• the first operating mode at most small quantities of air products previously stored in a tank system are fed into the distillation column system used and, if necessary, further separated, so that the mentioned negative effects of excessive
• Plants are stored or provided in the storage tanks, for example by means of a separate condenser.
• the Cold compressor used to ensure a heat input and simultaneously make a compression of a corresponding pressure flow.
• the invention thus provides an air separation plant, which enables cost-effective means a particularly advantageous operation even when larger amounts, for example, previously stored in storage tanks, liquid air products. This can be significantly reduced in particular compared to air separation plants with heated heat exchangers, but also compared to systems with cold compressors and external expansion turbines, the cost.
• Operation mode may be included, in which the at least one and / or at least one further gaseous pressure stream in a expansion turbine can be relaxed cold. The process can be switched as needed between the two operating modes.
• Distillation column system which is a high pressure column and a
• Low pressure column includes, the high pressure column at a higher
• Operating pressure is operated as the low pressure column.
• Distillation column systems for example, double column systems or systems with separate high and low pressure columns
• the process is thus suitable for retrofitting a large number of existing air separation plants with corresponding distillation column systems.
• the first pressure level corresponds to the operating pressure of the low-pressure column and / or the second pressure level to
• a distillation column system which additionally comprises a medium-pressure column which is operated at an operating pressure which is between the
• first pressure level correspond to the operating pressure of the low-pressure column and the second pressure level correspond to the operating pressure of the medium-pressure column or the high-pressure column.
• first pressure level may correspond to the operating pressure of the medium-pressure column and the second pressure level may correspond to the operating pressure of the high-pressure column.
• the at least one gaseous pressure stream may be formed from at least a portion of a stream which is one at the first pressure level
• Operating pressure operated distillation column of the distillation column system is removed, ie a low-pressure column or, if present, optionally also a medium-pressure column.
• the at least one gaseous pressure stream can then at least partially be transferred to a distillation column at a higher pressure level (in the case of removal from the low-pressure column, therefore
• the at least one gaseous pressure stream may also be formed from at least part of a stream which is conveyed by means of the
• a "medium-pressure flow” which is intended in part for feeding into a medium-pressure column of the distillation column system and is present at a corresponding pressure. Such, then compressed in the cold compressor gaseous pressure stream, can then be fed to the operated at a corresponding pressure level distillation column.
• the at least one gaseous pressure stream at the second pressure level can also be combined with at least one further stream. If such a second pressure level corresponds, for example, to the operating pressure of the high-pressure column, a correspondingly compressed gaseous pressure stream can therefore be combined with a corresponding compressed-air flow which is provided by a main air compressor at this second pressure level and cooled in the main heat exchanger. If the compressed gaseous pressure stream is not yet at a desired temperature, the at least one gaseous pressure stream after compression in the
• Cold compressor be cooled at least partially in the main heat exchanger. This is also an advantageous measure to counteract an unfavorable change in temperature profiles of the main heat exchanger caused by the feed of liquid air products by targeted introduction of temperature.
• a corresponding stream can be used, for example, as a regeneration gas in a cleaning device with adsorber containers and is available for this purpose at a particularly favorable pressure and temperature level.
• Such an air separation plant has a main air compressor, a main heat exchanger and a
• a distillation column system and is arranged for operation in the illustrated first and the explained second operating mode, wherein means are provided which are adapted to at least one in the first operating mode in the
• Control technology trained switching means include.
• the air separation plant has a cold compressor. Furthermore, means are provided which are set up in the second operating mode for the at least one gaseous pressure stream a temperature level that is below a hot side temperature of the
• Main heat exchanger is to supply the cold compressor to compress in the cold compressor from a first superatmospheric pressure level to a second superatmospheric pressure level, and then at the second pressure level at least partially feed into at least one distillation column of the distillation column system.
• this may be an oxyfuel or IGCC process or a corresponding device.
• FIG. 2 shows the air separation plant according to FIG. 1 in a second operating mode in the form of a schematic plant diagram
• FIG. 3 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 4 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 5 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 6 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 7 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 6 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 7 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• FIG. 8 shows an air separation plant according to an embodiment of the invention in the second operating mode in the form of a schematic plant diagram
• Figure 9 shows a way to arrange a cold compressor in one
• Figure 10 shows a way to arrange a cold compressor in one
• FIGS. 1 to 10 partially identical systems and components of such systems are shown in different operating modes, which differ, inter alia, in the position of a multiplicity of valves in corresponding lines, so that liquid and gaseous streams are guided through different system components.
• the valves are not illustrated.
• Shutdown lines are crossed (-x-).
• FIG. 1 shows a non-inventive air separation plant 1 10 in the form of a schematic system diagram.
• the air separation plant 10 is shown in Figure 1 in a first mode of operation in which it does not receive appreciable quantities of liquid air products from "external sources", e.g. from a storage tank or an air liquefaction plant.
• the illustrated first mode of operation for example, for the production of liquid air products in low-cost or
• Another operating mode may also include the exclusive or predominant provision of gaseous air products.
• the air separation plant 110 comprises as central components a main air compressor 10, a skin heat exchanger 20 and a distillation column system 30, which in the illustrated example is a multi-column system with a high-pressure column 31, a medium-pressure column 32 and a low-pressure column, the low-pressure column having a first section 38 and a second portion 33. These two sections are connected via a gas line k, which has no pressure-changing measures and thus form a uniform distillation space, which is not to be distinguished from a one-piece low-pressure column in terms of separation efficiency, pressure and temperatures.
• the operating pressure of the high pressure column 31 is, for example, 5.0 to 5.5 bar at the top
• the operating pressure of the low pressure column 33 is, for example, 1, 3 to 1, 4 bar at the top.
• the operating pressure of the medium-pressure column 32 is between the operating pressure of the high-pressure column 31 and the operating pressure of the low-pressure column 33.
• the main air compressor 10 is adapted to provide at least a first compressed air flow a and a second compressed air flow I.
• the pressure level of the first compressed air flow a is at the operating pressure of the high pressure column 31 (therefore also referred to as "high pressure air", HPAIR), the
• the provision of appropriate compressed air streams a and I is basically known and will not be explained in detail here.
• 10 atmospheric air can be sucked through a filter in a main air compressor and compressed in several stages to said pressures.
• the first compressed air flow a can be taken, for example, at the end of a multi-stage compression, the second compressed air flow I at an intermediate point.
• the air can be cooled after compression in a direct contact cooler in direct heat exchange with cooling water.
• the cooling water may be supplied from an evaporative cooler and / or from an external source.
• the compressed and cooled air can then be in a cleaning device getting cleaned.
• the cleaning device may comprise a pair of containers filled with a suitable adsorbent material.
• a nitrogen-rich regeneration gas here in the form of the stream v explained below, is used
• the cooled compressed air stream which is also denoted by a, is fed into the high-pressure column 31 downstream of the main heat exchanger 20 and liquefied to a further part in a bath evaporator or condenser 34 which is filled with an oxygen-rich liquid (see below). From the liquefied portion, in turn, a portion is fed liquid into the medium-pressure column 32 and passed a further portion through a subcooler 35 and expanded into the low pressure column 33.
• the second compressed air flow I is to a proportion through a passage 24 of the
• Main heat exchanger 20 and cooled there to near dew point.
• another portion is passed through a heat exchanger element 44, which may also be integrated in the main heat exchanger 20, where it is used to evaporate an oxygen-rich liquid stream n (see below).
• the subsequently reunited fractions are fed into the medium-pressure column 32.
• each oxygen-enriched liquid streams are withdrawn, as stream h through the
• an oxygen-rich liquid stream i is withdrawn, increased pressure by means of a pump 36, transferred via a flash valve (without designation) in a low-pressure column intermediate evaporator 37, partially evaporated there against a nitrogen-rich stream r (see below), and in the first section 38 of the low pressure column, in the swamp a
• Low-pressure column bottom evaporator 39 is arranged.
• the two condenser evaporators, the low-pressure column intermediate evaporator 37 and the low-pressure column bottom evaporator 39 designed as a falling film evaporator.
• Liquid and gaseous fractions obtained from the head of the oxygen column 38 are referred to as Stream k partially returned to the low pressure column 33.
• effluent is applied as reflux liquid to the first section 38 of the low-pressure column.
• a liquid, oxygen-rich stream is withdrawn and transferred to the secondary condenser 34, which is designed as a condenser-evaporator with liquid bath (bath evaporator).
• the secondary condenser 34 From the top of the secondary condenser 34, a gaseous, oxygen-rich stream m is withdrawn, heated in the main heat exchanger 20 and to provide a gaseous
• Oxygen printed product (referred to herein as GOX). From the bottom of the secondary condenser 34, a liquid, oxygen-rich stream is withdrawn, from which a partial flow n liquid pressure increases, evaporated in the heat exchanger element 44 and also used to provide the gaseous oxygen pressure product. A partial flow o, however, is partially subcooled in the subcooler 35 and to
• LOX liquid, oxygen-rich air product
• the liquid air product can be transferred to and stored in a suitable storage tank 61.
• LOX liquid, oxygen-rich air product
• a nitrogen-rich gaseous stream p is withdrawn and liquefied in the falling-film evaporator or condenser 39.
• a partial flow is returned to the high pressure column 31, a further partial flow (see link A) is passed through the subcooler 35 and then into the
• a nitrogen-rich gaseous stream r is withdrawn and liquefied to a part in the falling film evaporator or condenser 37.
• a partial flow is returned to the medium-pressure column 32, a further partial flow s passed through the subcooler 35 and then partially into the
• Low pressure column 33 relaxed and partially provided in the form of a liquid, nitrogen-rich air product (here referred to as LIN). This can also be stored in a suitable storage tank 62.
• LIN liquid, nitrogen-rich air product
• Another (larger) partial flow t of the flow r is in the illustrated first operating mode, bypassing a cold compressor 45 in the main heat exchanger 20 heated.
• a portion thereof, illustrated here as stream u can be taken from the main heat exchanger 20 at an intermediate temperature and then cold-expanded in a "cold" expansion turbine 46 (so-called pressurized nitrogen turbine), which may be coupled to a generator, for example.
• the portion not expanded in the expansion turbine 45 is provided in the form of a gaseous nitrogen-rich air product (here designated MPGAN).
• MPGAN gaseous nitrogen-rich air product
• the partial flow v is used as regeneration gas (REGGAS) in the main air compressor 10 or a cleaning device associated therewith (see above).
• REGGAS regeneration gas
• the partial flow w is heated by means of a heat exchanger 51 operated with a hot water flow and subsequently expanded in a further expansion turbine 52, which can likewise be coupled to a generator.
• a nitrogen-rich stream y is withdrawn, heated in the main heat exchanger 20 and discharged from the air separation plant 1 10.
• the use of the expansion turbine 46 serves to ensure that it is always required due to an unavoidable heat incidence through the insulation and losses in the main heat exchanger (hot-side temperature difference)
• the expansion turbine 46 can be turned off. This results in the example shown that a large usable amount of a corresponding nitrogen-rich air product is available under pressure, from which energy can be recovered.
• Relaxation turbine (analogous to the expansion turbine 46) is relaxed, however, can reduce the drive power in the main air compressor 10 done.
• FIG. 2 shows a corresponding second operating mode of the air separation plant 110.
• an oxygen-rich liquid air product (LOX) transferred from the storage tank 61 in the bath evaporator or condenser 34 (see link B) and on the other hand, a liquid air product (for example, liquefied air from an external condenser, here referred to as LAIR), fed from a further storage tank 63 in the low pressure column 33.
• LAIR liquid air product
• Relaxation turbine 46 are turned off.
• MPGAN gaseous nitrogen-rich air product
• stream x corresponding nitrogen-rich air product
• the air must be preheated.
• the cold compressor 45 is also in operation in the second operating mode.
• the cold compressor 45 By the cold compressor 45, however, not only heat can be introduced into the system but affect the overall process by targeted compression of certain streams (here stream t) and improve what with other heat-generating devices, such as air, steam, gas electric or otherwise heated heat exchangers, would not be possible.
• the pressure increase caused by the cold compressor 45 can be utilized in the expansion turbine 52.
• a particular advantage over the air separation plant according to the invention not shown in FIG. 10 results from the air separation plant 100 according to the invention shown and described below, in which the cold compressor 45 is used as a so-called feed compressor and integrated into the distillation column system 30.
• At least one gaseous pressure stream (see subsequent streams b through g) will be on one Temperature level, which is below a hot-side temperature of the main heat exchanger 20, the cold compressor 45 supplied in the cold compressor 45 from a first superatmospheric pressure level to a second
• Cold Compressor 45 for example, a corresponding gaseous pressure flow (eg air from the main air compressor 10 in the form of the flow e explained below or a nitrogen-rich, gaseous pressure stream from one of the distillation columns in the form of the below-explained streams b to d, f and g) of a pressure level, used for a low pressure or medium pressure column 32 or 33, or more generally for a lower pressure column operating pressure, to a pressure level used for a medium pressure or high pressure column 31 or 32, more generally a higher pressure column than operating pressure , condensed.
• a corresponding gaseous pressure flow eg air from the main air compressor 10 in the form of the flow e explained below or a nitrogen-rich, gaseous pressure stream from one of the distillation columns in the form of the below-explained streams b to d, f and g
• a corresponding gaseous pressure flow eg air from the main air compressor 10 in the form of the flow e explained below or a
• FIG. 3 shows a corresponding air separation plant 100 according to a
• Embodiment of the invention in the second mode of operation is the first
• Operation mode is not shown again, but basically corresponds to that in Figure 1:
• a corresponding current is passed through the expansion turbine 46, the cold compressor 45 is bypassed.
• oxygen-rich liquid air product (LOX) from the storage tank 61 in the bath evaporator or condenser 34 transferred (see link B) and on the other hand, a liquid air product (for example, liquefied air from an external LOX) from the storage tank 61 in the bath evaporator or condenser 34 transferred (see link B) and on the other hand, a liquid air product (for example, liquefied air from an external
• LOX oxygen-rich liquid air product
• LAIR Condenser
• the cold compressor 45 is charged with a partial stream b of the nitrogen-rich stream y withdrawn from the low-pressure column 33, which is thus present at the above-mentioned superatmospheric pressure level at the top of the low-pressure column 33, for example 1, 3 to 1, 4 bar.
• this partial flow b is compressed from said ("first") superatmospheric pressure level to a higher ("second") superatmospheric pressure level, which here corresponds to the operating pressure of the medium-pressure column 32.
• the partial flow b compressed as explained is then supplied to a passage 25 of the main heat exchanger 20 at an intermediate temperature and cooled accordingly. After cooling, the current b in the top of the medium-pressure column 32 is abandoned.
• FIG. 4 shows a further air separation plant according to an embodiment of the invention in the second operating mode.
• the cold compressor 45 is also charged here with a partial flow of withdrawn from the low-pressure column 33 nitrogen-rich stream y, which is denoted by c and at the above-mentioned superatmospheric pressure level at the top of the low-pressure column 33, for example 1, 3 to 1, 4 bar, is present ,
• this partial flow c is changed from the above-mentioned ("first") superatmospheric pressure level to a higher (“second”) superatmospheric pressure level, but here the operating pressure of the
• High pressure column 31 corresponds, compressed.
• the partial flow c as described is then supplied to a passage 27 of the main heat exchanger 20 at an intermediate temperature and cooled accordingly. After cooling, the current c in the top of the high pressure column 31 is abandoned. Further streams j (MPGAN) and z (partly used as regeneration gas, REGGAS, possibly only in the first
• FIG. 5 shows a further air separation plant according to an embodiment of the invention in the second operating mode.
• the cold compressor 45 is charged here with a stream d, which is taken from the head of the medium-pressure column 32 and therefore at the aforementioned superatmospheric pressure level at the top of the
• FIG. 6 shows a further air separation plant according to an embodiment of the invention in the second operating mode.
• the cold compressor 45 is here charged with a partial flow e of the pressure flow I from the main air compressor 10, which is present at the above-mentioned superatmospheric pressure level, which corresponds to the operating pressure of the medium-pressure column 32.
• the partial flow e is taken from the main heat exchanger 20 at the cold end, so that its temperature level below the
• FIG. 7 shows a further air separation plant according to an embodiment of the invention in the second operating mode.
• the cold compressor 45 is charged here with a stream f, the low pressure column 33 is removed and therefore at the above-mentioned superatmospheric pressure level of the low pressure column 33, for example, 1, 3 to 1, 4 bar, and at its temperature level.
• this partial flow f is compressed from the said ("first") superatmospheric pressure level to a higher (“second”) superatmospheric pressure level, which in turn corresponds here to the operating pressure of the medium-pressure column 32.
• the partial flow f compressed as explained is then supplied to the passage 24 of the main heat exchanger 20 at an intermediate temperature and thus combined with the flow I.
• the current referred to here with I is cooled accordingly. After cooling, the current I is fed into the medium-pressure column 32.
• Further streams j (MPGAN) and z (partly used as regeneration gas, REGGAS, possibly only in the first
• Air separation plant to be discharged.
• FIG. 8 shows a further air separation plant according to an embodiment of the invention in the second operating mode.
• the cold compressor 45 is also charged here with a stream g, the low pressure column 33 is removed and therefore at the above-mentioned superatmospheric pressure level of the low pressure column 33, for example, 1, 3 to 1, 4 bar, and at its temperature level.
• superatmospheric pressure level to a higher (“second") superatmospheric pressure level, which in turn corresponds to the operating pressure of the high pressure column 31, for example, 5.0 to 5.5 bar, compressed.
• the partial flow g compressed as explained is then supplied to the passage 21 of the main heat exchanger 20 at an intermediate temperature and thus combined with the flow a.
• the current further here designated by a is cooled accordingly. After cooling, the current is a u.a. in the
• Figures 9 and 10 show alternative ways to arrange a
• a stream compressed by the cold compressor 45 is supplied to the main heat exchanger 20 on the warm side.
• a stream is taken from the main heat exchanger 20 at a first intermediate temperature, then compressed, and the main heat exchanger 20 at a second intermediate temperature

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• 2014
  • 2014-07-10 AU AU2014289591A patent/AU2014289591A1/en not_active Abandoned
  • 2014-07-10 EP EP14739044.7A patent/EP3019804A2/de not_active Withdrawn
  • 2014-07-10 KR KR1020167003543A patent/KR20160032160A/ko not_active Application Discontinuation
  • 2014-07-10 TW TW103123850A patent/TW201518664A/zh unknown
  • 2014-07-10 CN CN201480039508.0A patent/CN105378411B/zh active Active
  • 2014-07-10 US US14/903,720 patent/US20160370111A1/en not_active Abandoned
  • 2014-07-10 WO PCT/EP2014/001891 patent/WO2015003808A2/de active Application Filing

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