CN105378411B - Produce method, the air separation plant, the method and apparatus produced electricl energy of at least one air products - Google Patents

Produce method, the air separation plant, the method and apparatus produced electricl energy of at least one air products Download PDF

Info

Publication number
CN105378411B
CN105378411B CN201480039508.0A CN201480039508A CN105378411B CN 105378411 B CN105378411 B CN 105378411B CN 201480039508 A CN201480039508 A CN 201480039508A CN 105378411 B CN105378411 B CN 105378411B
Authority
CN
China
Prior art keywords
pressure
air
superpressure
tower
stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201480039508.0A
Other languages
Chinese (zh)
Other versions
CN105378411A (en
Inventor
A·阿列克谢耶夫
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of CN105378411A publication Critical patent/CN105378411A/en
Application granted granted Critical
Publication of CN105378411B publication Critical patent/CN105378411B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J3/04472—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
    • F25J3/04521—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
    • 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
    • F25J3/04763—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
    • 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
    • F25J3/04763—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
    • 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
    • F25J2200/34—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
    • 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
    • F25J2210/42—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—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
    • 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
    • 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
    • F25J2245/42—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

Abstract

The present invention relates to the methods for producing at least one air products, wherein use air separation equipment (100), the air separation equipment has main air compressor (10), main heat exchanger (20) and distillation column system (30), this method includes the first operational mode and the second operational mode, wherein in the first operating mode, the at least one liquid air product (LIN generated in the distillation column system (30) of storage, LOX), and in the second operating mode, by at least one liquid air product (LIN stored in the first operating mode, LOX, LAIR) and/or at least one other liquid air products are sent into the distillation column system (30).The method is characterized in that, in the second operating mode, at least one gaseous state pressurized stream (b-g) is incited somebody to action in temperature levels feeding cold compressor (45) of the hot side temperature lower than the main heat exchanger (20), the second superpressure stress level is compressed to by the first superpressure stress level in the cold compressor (45), and at least one destilling tower (31,32) that the second superpressure stress level is sent into the distillation column system (30).The invention further relates to the method and apparatus corresponding air separation equipment (100) and produced electricl energy.

Description

Produce the methods of at least one air products, air separation plant, the method produced electricl energy and Device
Technical field
The present invention relates to the methods according at least one air products of production of the preambles of independent claims, air Separation equipment and the method and apparatus produced electricl energy.
Background technique
" condenser/evaporator " is that the heat for instigating the first condensed fluid stream and the second evaporative fluid stream that indirect heat exchange occurs is handed over Parallel operation.Various condenser/evaporators all have the liquefied room being made of respectively liquefier channel and evaporation channel and vaporization chamber.It is first-class Body stream condenses (liquefaction) in liquefied room, and second fluid stream is evaporated in vaporization chamber.Vaporization chamber and liquefied room by depositing between each other It is formed in the channel group of heat exchange relationship.The vaporization chamber of condenser/evaporator may be configured to bath evaporator (Badverdampfer), drop Film evaporator forces flow evaporator device.
In lower pressure column tower bottom evaporator, the bottom liquid of lower pressure column is at least partly evaporated in vaporization chamber.In lower pressure column In central evaporator, the intermediate liquid of lower pressure column at least partly evaporates in vaporization chamber.
The prior art
The method of aforementioned type and related device comprising three towers are known.
In the known method produced electricl energy, such as known oxygen-enriched combusting method and so-called integral coal gasification joint It recycles (Integrated Gasification Combined Cycle, IGCC), needs using oxygen or oxygen coalescence gas mixing Object, such as realizing burning or partial oxidation.It can be used and be for example disclosed in Hausen/Linde, Tieftemperaturtechnik, 2.Auflage 1985, Kapitel 4 (Hausen/Linde, cryogenic technique, 1985 2 editions, the 4th chapter, page 281 to 337) cryogenic air separation process and device oxygen or corresponding oxygen coalescence gas mixing are provided Object.
Distillation column system is used in such method and apparatus (herein referred to as " air separation equipment "), such as can be constructed At double tower system, especially classics Linde double tower system, but it also may be configured to three towers or many tower systems.Furthermore settable to be used for Extract the device of the rare gas such as other constituent of air especially krypton, xenon and/or argon.
The method and apparatus produced electricl energy should change design for big loading range and fast load, so as to inhale Receive the power swing caused because other energy supplier is available or unavailable.Be provided oxygen and/or corresponding gas mixing The air separation equipment of object should also realize the operational mode of the flexibility and changeability in respective range.
Conventional air separation equipment is also influenced by the violent electricity price of power grid utilization rate and correspondingly variation degree.
In the case, possible flexibility ratio depends on the liquefying power of air separation equipment.Can be higher with liquefying power, Then more low-price electricities can be stored in the form of liquid air product.However, what the method and apparatus to produce electricl energy were supplied Air separation equipment only has low liquefying power, this is because it is designed to mass production at ambient temperature by the sky The gaseous oxygen and gaseous nitrogen product that gas separation equipment extracts.The chilling requirement of relevant deviceIt is relatively low, because This its also can not provide enough cooling capacity to only provide larger amount of liquid air product
Therefore, liquefaction device (LIN liquefier, LOX liquefier or the LAIR liquefaction of separation can be installed in relevant device Device), and accessed in liquefaction stage.By the way that the refrigerating capacity (and therefore corresponding liquefying power) of method or equipment is designed to height In the gaseous oxygen and gaseous nitrogen product of actually required amount, certain flexibility also may be implemented.
If larger amount of liquid air product is sent into corresponding air separation equipment, may be apparently higher than the desired amount of Cooling capacity can enter the air separation equipment.In the case where no counter-measure, this will lead to each temperature in heat exchanger Distribution shifts, and the temperature of the one or more strands of streams by heat exchanger discharge becomes lower and lower.From the specific limit It is worth, just can not ensures the reliability service of air separation equipment again.The problem can be heated by using heat generating device such as air Type, vapor heating type, gas hot type, electric heating type heat exchanger or the heat exchanger that otherwise heats and solved Certainly.But the reason of such solution is especially in terms of the energy and be proved to be unfavorable.
Summary of the invention
The purpose of the present invention is to provide the method for aforementioned type and corresponding device, energy consumption variation range is big and in institute There is energy consumption under corresponding operational mode lower.
The purpose is divided by the method for at least one air products of production of the feature with independent claims, air It is realized from equipment and the method and apparatus produced electricl energy.Preferred embodiment is each dependent claims and is described below Theme.
Before illustrating achievable advantage within the scope of the present invention, several terms used in this application are subject to Explanation.
" air separation equipment " with through air that is dry and purifying being optionally charging, be by " main air compressor " with At least the form of one compressed air stream provides.As previously mentioned, air separation equipment has for dividing air into its object Manage the distillation column system of component especially nitrogen and oxygen.As previously mentioned, air is cooled to close to its dew point thus, and import distillation In Tower System.Unlike this, pure " air liquefaction plant " or " liquefying plant " does not include distillation column system.In addition, air fluid The structure for changing equipment can correspond to supply the structure of the air separation equipment of air liquefaction product.Certainly, it is set in air separation Liquid air can also be generated as byproduct in standby.
" liquid air product " refer to it is any can at least through air is compressed, cool down and subsequent expansion to Product made of in the form of cryogenic liquid.As previously mentioned, it especially can be liquid oxygen (LOX), liquid nitrogen (LIN), liquid argon (LAR) Or liquid air (LAIR).Here, term " liquid oxygen " and " liquid nitrogen " also respectively refer to oxygen content and/or nitrogen content is more than atmospheric air Cryogenic liquid.Therefore its neat liquid that need not be oxygen and/or nitrogen with high-content.Therefore, liquid nitrogen refers not only to pure Nitrogen or almost pure nitrogen also refer to that nitrogen content is more than the liquefied air admixture of gas of atmospheric air.Its nitrogen content is, for example, at least 90 moles of %, preferably at least 99 moles of %.
" low temperature (deep cooling) " liquid or corresponding fluid, liquid air product, stream etc. refers to its boiling point far below respective Environment temperature and for example, 200K or lower, especially 220K or lower liquid medium.The cryogenic media in above-mentioned meaning Example is liquid air, liquid oxygen and liquid nitrogen.
The indirect heat transfer between stream that " heat exchanger " is used to guide each other with adverse current at least two strands, such as one heat Compressed air stream and one or more strands of cold flows or one low temperature liquid air products and one or more strands of hot-fluids.Heat exchanger can To be formed by an individual heat transfer section or be formed by multiple in parallel and/or concatenated heat transfer sections, such as It is formed by one or more heat-exchangers of the plate type blocks.Heat exchanger, such as be characterized in that used in the air separation equipment With its cooling or " main heat exchanger " of the major part for heating stream to be cooled or to be heated, has and be configured to contain heat exchange " channel " of the fluid passage being separated from each other in face." hot side " that corresponding heat exchanger has temperature different at runtime and " cold side "." hot side " temperature of heat exchanger refers to temperature when stream to be cooled is admitted to heat exchanger.Because may have more Stock stream to be cooled is admitted to heat exchanger with different temperatures level, so hot side temperature alsos relate to its average value or sent The minimum or maximum temperature of the stream to be cooled entered.
" compressor " is that at least one gaseous flow is compressed at least one final pressure by least one initial pressure Device, the gaseous flow are sent into compressor under the initial pressure, which is discharged under the final pressure by compressor assembly. Compressor forms a structural unit herein, but can have multiple known piston components, screw arbor assembly and/or impeller sets " compression stage " of the form of part and/or turbine assembly (i.e. axial-flow type or radial-flow type compression stage).This is also applied for air separation and sets Standby " main air compressor ", which is characterized in that whole or the master of the air capacity being admitted in air separation equipment are compressed with it Want part.These compression stages are for example driven using common axis especially with common driving device.Multiple compressors Such as air separation equipment main compressor and rear compressor can be connected to each other." rear compressor (supercharger) " is for further Improve the pressure for the stream being pressurized." cold compressor " is characterized in that, can at low temperature, especially under cryogenic, It will stream accordingly into wherein.In the case, cold compressor is set up according to the prior art.
" expansion turbine " can be pivotally connected to other expansion turbines or energy converter such as oil pressure system by common Dynamic device, generator or compressor, for expanding the stream of gaseous flow or at least partly liquid.Expansion turbine can especially be made It is turbo-expander for the present invention.If compressor is driven by one or more expansion turbines, but in not external example It is run in the case where the energy such as supplied by motor, is then referred to herein as " turbine drives " compressor.Turbine driven compressor " pressurized turbo machine " is also referred to the component (configuration) of expansion turbine." pressurization nitrogen turbine (Druckstickstoffturbine) " or " PGAN turbine " refers in the application scope for making in air separation equipment The expansion turbine of middle generation and the pressurized stream expansion by the nitrogen enrichment of distillation column system discharge.Then the pressurized stream example expanded It can such as be heated in main heat exchanger, and be emitted into ambient enviroment.Expansion turbine referred to as " middle-pressure turbine " is special It is used in combination with the three-tower system for including high-pressure tower, medium pressure column and lower pressure column.Middle-pressure turbine is for making to compress by primary air Machine compresses and the compressed air stream optionally recompressed in rear compressor is expanded into medium pressure column after cooling in main heat exchanger. Unlike this, " injection turbine (Einblaseturbine) " is compressed and optionally in rear pressure for making by main air compressor The lower pressure column of three towers or double tower system is expanded into after the compressed air stream recompressed in contracting machine is cooling in main heat exchanger.With This is different, is referred to as " restraining stream (Drosselstrom) " by the stream that expansion valve is expanded into high-pressure tower.The stream is in advance for example It is higher than height by the way that the rear compressor among main air compressor or downstream is arranged in and/or is compressed to by turbine driven compressor Press the stress level of the operating pressure of tower.
In the scope of the application, " groove tank system " refers to the low temperature that storing liquid air products are used for including at least one The configuration of storage tank.Corresponding groove tank system has insulating part.
The application characterizes pressure and temperature using term " stress level " and " temperature levels ", it is indicated above that without with essence The form of true pressure value or temperature value realizes design of the invention using corresponding pressure and temperature.But these pressure Usually change in for example +/- 1%, 5%, 10%, 20% or even 50% particular range around average value with temperature. In the range of corresponding stress level and temperature levels may be at disjoint range herein or overlap each other.Such as pressure water Flat especially includes the inevitable or foreseeable pressure loss for example generated due to cooling effect.This is correspondingly also suitable In temperature levels.Absolute pressure is referred to bar stress level provided herein.
Liquid air product or corresponding liquid stream can be transformed into gaseous state or supercriticality by heating.If in Asia It is heated under critical pressure, then normal phase transformation is realized by evaporation.If but heating liquid under the pressure for being higher than critical pressure State air products do not occur the phase transformation on practical significance when being heated beyond critical-temperature then, but are transformed into super face by liquid Boundary's state.It further include by the transformation of liquid to supercriticality if using term " evaporation " in the application scope.
Advantages of the present invention
The present invention relates to a kind of method for generating at least one air products, this method uses air separation equipment, tool There are main air compressor, main heat exchanger and distillation column system.As previously mentioned, this method includes first and second operational mode, Wherein under first operational mode, storage at least one results from the liquid air product in the distillation column system, and at this Under second operational mode, by least one liquid air product stored under first operational mode and/or at least one Other liquid air products that affirmative does not generate under second operational mode and/or the liquid air product by outside conveying And/or the liquid air product (such as liquid air, liquid nitrogen or liquid oxygen) otherwise kept in is sent into the distillation column system.
According to the present invention, in the second operating mode, at least one gaseous state pressurized stream is in the hot side for being lower than main heat exchanger It is admitted to cold compressor on the temperature levels of temperature, from the first superpressure (superatmospheric pressure) stress level in the cold compressor It is compressed into the second superpressure stress level and is admitted at least one steaming of distillation column system on the second superpressure stress level Evaporate tower.This destilling tower is run with the operating pressure for being equal to the second superpressure stress level.Compared with prior art, this method has all More advantages:
As previously mentioned, less amount of cryogenic liquid or liquid can be fed to the ice chest of air separation equipment easily under normal circumstances State air products, because because of insulation and the internal loss of (master) heat exchanger (the hot side temperature difference) reason, heat leakUnavoidably, to need certain cooling capacity always.This cooling capacity is usually by expansion turbine used It provides.
If being able to satisfy chilling requirement by above-mentioned feeding, the expanding machine can be disconnected.Using so-called middle-pressure turbine and In the case where its internal further expanding compressed air, this can accordingly save main air compressor and/or be set to the primary air pressure Driving power after contracting machine is subsequent on compressor.If in the lower pressure column to expand the air into distillation column system used Correlation method is realized on the basis of injection turbine, then can obtain similar effect.If using the nitrogen that pressurizes shown in the application schema Turbine or PGAN turbine, disconnecting turbine just can make have a large amount of pressurization nitrogen available, and squeeze operation therefrom can be recycled Consumed energy.External expansion machine can be used thus, corresponding pressurized stream is admitted to the expansion after heating in front-mounted heating device Machine, then pressure (being used for example as regeneration gas) needed for making the pressurized stream be expanded to associated uses.
If will be cold more than the cold input needed within one section of long period by feeding cryogenic liquid or liquid air product Case will cause the Temperature Distribution in heat exchanger used that disadvantageous changes (" deformation ") occurs, to make one or more outflows The temperature of the stream of heat exchanger is lower and lower.It just can not ensure air separation equipment reliability service again from a certain limit value or by rule Fixed operation.Further feeding can not be realized in the case of this again, except non-used additional heating source improves the heat leak of ice chest.Such as preceding institute It states, for any known heat-producing unit, such as air hot type, vapor heating type, gas hot type, electricity can be used up to this purpose Power hot type heat exchanger or the heat exchanger otherwise heated.
For above situation, use cold compressor (as previously mentioned, i.e. intake air temperature is lower than the compressor of environment temperature) It is particularly advantageous, because cold compressor is not only system heat supply, but predetermined substance stream can be compressed by selectivity to influence simultaneously Improve overall procedure.Correlation method by following Fig. 1 and Fig. 2 shows.This method is (to feed corresponding cryogenic liquid or liquid sky Under " second " operational mode of gas product) with cold compressor compression corresponding expansion turbine is disconnected (such as shown in above-mentioned schema Pressurization nitrogen turbine, but also can be for example injection turbine) after available pressurization nitrogen quantity, then should with preheater heating Pressurization nitrogen simultaneously makes its expansion with individual expansion turbine.However, the external expansion turbine with forward type preheater is not Satisfactory using effect can be all obtained under any circumstance, because such hardware component is very expensive and operation energy consumption pole It is high.For example, individually (middle pressure) vapour system must usually be arranged when running corresponding preheater.Thus high loss can be generated.Therefore In the sense that reducing cost and energy conservation, the method and apparatus without using such device is especially worthy of expecting and advantageous.
It is known per se in air separation equipment using cold compressor.As disclosed in US 7272954B2, cold pressing Contracting machine is used to compression restraining stream.But this purposes and the target of methods described herein and relevant device are far from each other: such as Preceding described, compression restraining stream is precisely in order to can implement the operation for being expanded into high-pressure tower, to achieve the purpose that additionally to freeze.Cause This, restraining stream is compressed into higher superpressure stress level, but is not admitted to high pressure on the higher superpressure stress level Tower, but reexpand before this.Furthermore within the scope of the present invention, the first superpressure stress level is lower than high-pressure tower operating pressure.
Under " the first operational mode " that respective air separation equipment has been referred to repeatedly, not necessarily for example, oxygen-enriched combusting Method or IGCC method provide gaseous air product.First operational mode also may include extracting liquid air products simultaneously from relevant device (electricity price is cheap or electric energy superfluous period) is conducted into ad hoc storage tank.The characteristics of first operational mode, essentially consists in, such as by means of Pressurization nitrogen turbine, injection turbine and/or middle-pressure turbine is helped to generate additional cooling capacity in air separation equipment.First The air products that groove tank system will be at most stored under operational mode before this on a small quantity are sent into distillation column system used and when needed Processing is further separated, in order to avoid cooling capacity is inputted because excessiveAnd there is aforementioned ill effect.
And it is general not by pressurization nitrogen turbine, injection turbine and/or middle pressure whirlpool under aforementioned " the second operational mode " Turbine generates additional cooling capacity, because in this operating mode, the air products for being stored in storage tank before this are admitted to distillation used Tower System simultaneously further separates processing when needed.It also can be by attachment device or equipment, such as by individual liquefier The air products such as this are stored in storage tank or are provided.Second operational mode ensures heat input using cold compressor, while right Corresponding pressurized stream is compressed.
Thus the present invention provides a kind of air separation equipment, even if being largely for example stored in storage tank before this being fed It is remained in the case where liquid air product to be realized with a low cost particularly advantageous operation.Especially and comprising being heated type heat exchanger Air separation equipment and comprising cold compressor compared with the equipment of external expansion turbine, cost can be greatly reduced whereby.
Certainly, this method also may include aforementioned first operational mode, and in this operating mode, at least one gaseous state pressurizes for this Stream and/or at least one other gaseous state pressurized stream in expansion turbine swell refrigeration (entspannt)。 In the case, this method can switch between two operational modes as needed.
This method is preferably applied to following scenario described: using distillation column system comprising high-pressure tower and lower pressure column, the wherein height Tower is pressed to be higher than the operating pressure of the lower pressure column and run.Such distillation column system (such as double tower system or the separation of high and low pressure tower System) it has substantially been known in the art.Therefore this method is suitable for numerous existing air separation equipments and installs corresponding destilling tower system additional System.
In such distillation column system, first pressure level is equal to lower pressure column operating pressure, and/or, second pressure is horizontal Equal to high-pressure tower operating pressure.The present invention realizes corresponding boost in pressure herein, and realizing while quantitative input cooling capacity will Pressurized stream imports distillation column system.
If the use of distillation column system further comprising medium pressure column, and the medium pressure column is between high-pressure tower and lower pressure column Operating pressure operation between operating pressure is just able to achieve special beneficial effect and more flexible processing procedure control.
Correspondingly, first pressure level can be equal to lower pressure column operating pressure at this time, and during second pressure level can be equal to Press the operating pressure of tower or high-pressure tower.As an alternative, first pressure level can be equal to medium pressure column operating pressure, and second Stress level can be equal to high-pressure tower operating pressure.
No matter which kind of situation, at least one gaseous state pressurized stream all can extract from distillation column system by one with first pressure water for this Put down the stream of the destilling tower (i.e. lower pressure column, medium pressure column, then be also optionally medium pressure column if it exists) for operating pressure operation At least part is formed.It, can at least one gaseous state pressurized stream be at least partly sent into stress level by this after cold compressor is compressed Relatively high destilling tower is (if extracting from lower pressure column, for medium pressure column or high-pressure tower, if extracting from medium pressure column, for high pressure Tower).
As an alternative, this at least one gaseous state pressurized stream also can by one by main air compressor provide and through it is main heat hand over The cooling stream of parallel operation (being for example partially fed to the medium pressure column of distillation column system and " middle pressure stream " in relevant pressure) is extremely Few a part is formed.After after cold compressor is compressed, which can be fed in and to be run in relevant pressure level Destilling tower.
Before being admitted to corresponding destilling tower, this at least one gaseous state pressurized stream also can in second pressure level at least One other streams converge.If the second pressure level is for example equal to high-pressure tower operating pressure, the gaseous state pressurized stream through accordingly compressing is just The corresponding compressed air stream that can be provided in the second pressure level by main air compressor and be cooled down through main heat exchanger to one Converge.
If the compressed gaseous pressurized stream is not yet in nominal temperature, at least one gaseous state pressurized stream can be through cold compression for this It is cooled after machine compression at least partially in main heat exchanger.This is also one beneficial to measure, can by selective thermal input come Reply leads to the changed unfavorable situation of main heat exchanger Temperature Distribution because feeding liquid air product.
It arbitrarily can facilitate to obtain on good cooling effect and/or the position for influencing Temperature Distribution as needed in the case of this Heat exchanger feeding, for example, see Fig. 9 and Figure 10.Can by this at least one gaseous state pressurized stream after cold compressor is compressed in Hot side or on the temperature levels of another hot side temperature lower than main heat exchanger be sent into main heat exchanger cooled down.
If a part of the gaseous state pressurized stream compressed through cold compressor is heated in main heat exchanger and/or at least portion Divide and be exported air separation equipment, then this method can also obtain beneficial effect.Corresponding stream can for example include contactor It is used as regeneration gas in purification device, and thus in particularly advantageous pressure and temperature levels.
About the features and advantages of air separation equipment of the invention, aforementioned advantages are please referred to.Such air separation equipment With main air compressor, main heat exchanger and distillation column system and it is suitable in aforementioned first operational mode and aforementioned second operation It is run under mode, is provided with and results from liquid in the distillation column system to store at least one under first operational mode State air products and at least one liquid air that stores under first operational mode is produced under second operational mode Product and/or at least one other liquid air products are sent into the device of the distillation column system.Related device for example may include turning manually The bridgeware for changing part or being constructed using control technology.The air separation equipment has cold compressor.Furthermore be provided with to Under second operational mode by least one gaseous state pressurized stream on the temperature levels of the hot side temperature lower than main heat exchanger It is sent into the cold compressor, at least one gaseous state pressurized stream from the first superpressure stress level is compressed in the cold compressor Two superpressure stress levels, then by this, at least one gaseous state pressurized stream is at least partly sent into the distillation in second pressure level The device of at least one destilling tower of Tower System.
About the features and advantages of the method for the present invention and apparatus of the present invention for producing electricl energy, foregoing teachings are also please referred to.It should Method and the device especially can be oxygen-rich combustion method or IGCC method and related device.
The present invention is elaborated referring to institute's accompanying drawings.
Detailed description of the invention
The air separation equipment that Fig. 1 show non-present invention is in equipment schematic diagram when the first operational mode；
Fig. 2 show equipment schematic diagram when air separation equipment shown in FIG. 1 is in the second operational mode；
The air separation equipment that Fig. 3 show an embodiment according to the present invention is in equipment when the second operational mode Schematic diagram；
The air separation equipment that Fig. 4 show an embodiment according to the present invention is in equipment when the second operational mode Schematic diagram；
The air separation equipment that Fig. 5 show an embodiment according to the present invention is in equipment when the second operational mode Schematic diagram；
The air separation equipment that Fig. 6 show an embodiment according to the present invention is in equipment when the second operational mode Schematic diagram；
The air separation equipment that Fig. 7 show an embodiment according to the present invention is in equipment when the second operational mode Schematic diagram；
The air separation equipment that Fig. 8 show an embodiment according to the present invention is in equipment when the second operational mode Schematic diagram；
When the air separation equipment that Fig. 9 show an embodiment according to the present invention is in the second operational mode, at this The partial schematic diagram of the feasible program of cold compressor is set in air separation equipment；And
When the air separation equipment that Figure 10 show an embodiment according to the present invention is in the second operational mode, at this The partial schematic diagram of the feasible program of cold compressor is set in air separation equipment.
Specific embodiment
Peer component have in the drawings the same symbol and not repeated explanation in the hope of concise.
Fig. 1 to Figure 10 show the icon of the identical equipment in part and its component under different operational modes, the equal operation Mode discrimination essentially consists in position of multiple valves in respective lines, therefore liquid stream and gaseous flow pass through distinct device component. Valve is unillustrated.But blocking tube is online by cross (- x-).
Fig. 1 is the equipment schematic diagram of the air separation equipment 110 of non-present invention.Air separation equipment 110 is in Fig. 1 First operational mode is produced without the liquid air largely from " external source " (such as storage tank or air liquefaction plant) under this operational mode Product are admitted to the air separation equipment.The first operational mode of icon is for example for electricity price is cheap or electric energy superfluous period generates liquid State air products, wherein the grade liquid air product is stored in corresponding storage tank and prepares under the second operational mode shown in Fig. 2 It is admitted to air separation equipment 110.Other operational modes also may include only providing or mainly providing gaseous air product.
The core component of air separation equipment 110 includes the main air compressor 10 being shown schematically in the figure, main heat exchange Device 20 and distillation column system 30, the distillation column system be configured in illustrated embodiment comprising high-pressure tower 31, medium pressure column 32 with it is low The many tower systems of tower are pressed, wherein the lower pressure column has the first section 38 and the second section 33.This two section is not taken by one appoints The gas line k of what transformation measure is connected, to form unified distillery, the distillery is in separating effect, pressure and temperature Degree aspect is no different with integral type lower pressure column.
The top operating pressure of high-pressure tower 31 is, for example, 5.0 to 5.5 bars, and the top operating pressure of lower pressure column 33 is, for example, 1.3 to 1.4 bars.The operating pressure of medium pressure column 32 is between the operating pressure of high-pressure tower 31 and the operating pressure of lower pressure column 33.
In order to provide corresponding compressed air to distillation column system 30 or each tower, main air compressor 10 is configured to mention For at least one first compressed air stream a and one second compressed air stream l.In the case, the pressure water of the first compressed air stream a The operating pressure (therefore being also known as " pressure-air ", HPAIR) for high-pressure tower 31 is put down, the stress level of the second compressed air stream l is then The operating pressure (therefore being also known as " middle pressure air ", MPAIR) of medium pressure column 32.
The presentation mode of corresponding compressed air stream a and l are substantially known, and details are not described herein again.For example, primary air pressure Contracting machine 10 can be sucked atmospheric air by filter and by its multi-stage compression to above-mentioned pressure.Such as it can be in multi-stage compression terminal point The first compressed air stream a is extracted, extracts the second compressed air stream l in a middle position.The air can be after compression direct It is cooled down in contact cooler by indirect heat exchange is carried out with cooling water.The cooling water can be by vaporization chamber cooler and/or outer Source provides.The compression cooling air can be then cleaned in purification device.The purification device can have a pair of equipped with suitable The container of adsorbent material.Purification device is regenerated with rich nitrogen regeneration gas (referred to stream v, associated description are seen below).
In the illustrated embodiment, the first compressed air stream a is in aforementioned pressure level across the channel of main heat exchanger 20 It 21 and is cooled at this close to dew point.The cooling compressed air stream for continuing to be indicated with a is in 20 downstream one of main heat exchanger Part enters high-pressure tower 31, and another part is in bath evaporator or bath condenser equipped with oxygen enriched liquid (see below) (Badkondensator) 34 interior liquefaction.A part in the liquefaction portion is sent into medium pressure column 32 by liquid, and another part passes through Subcooler 35 is simultaneously expanded into lower pressure column 33.
Second compressed air stream l a part passes through the channel 24 of main heat exchanger 20 and is cooled at this close to dew Point.Another part then passes through the heat exchanger assemblies 44 that one can also be integrated in main heat exchanger 20 and is used to evaporate at this oxygen-enriched Liquid stream n (see below).Two parts then converge once again is combined into medium pressure column 32.
Oxygen coalescence liquid stream is extracted from high-pressure tower 31 and 32 tower bottom of medium pressure column respectively, passes through subcooler 35 simultaneously as stream h It is expanded into lower pressure column 33.
Oxygen-rich liquid stream i is extracted from lower pressure column tower bottom, which increases pressure by pump 36, and expanded valve is (not Symbol) lower pressure column central evaporator 37 is imported, with nitrogen-enriched stream r (see below) contrary part evaporates and is imported into low pressure herein First section 38 of tower is provided with lower pressure column tower bottom evaporator 39 in its tower bottom.In embodiment, two condenser/evaporator (low pressure Tower central evaporator 37 and lower pressure column tower bottom evaporator 39) it is configured to falling film evaporator.The liquid that is obtained from the top of oxygen column 38 and Gaseous parts are partially fed back to lower pressure column 33 as stream k.Flow out the another of the liquid of the vaporization chamber of lower pressure column central evaporator 37 A part is sent to the first section of lower pressure column 38 as withdrawing fluid.
Liquid oxygen-enriched stream is extracted from 38 tower bottom of lower pressure column and is conducted into auxiliary condenser 34, which is configured to Condenser/evaporator (bath evaporator) comprising liquid bath.Gaseous state oxygen-rich stream m, the gaseous state oxygen-rich stream are extracted from the top of auxiliary condenser 34 Be heated in main heat exchanger 20 and be used to gaseous oxygen pressurized product (Sauerstoff- Druckprodukt it) (is indicated herein with GOX).Liquid oxygen-enriched stream is extracted from 34 tower bottom of auxiliary condenser, one shunts n in liquid Under be enhanced pressure, in heat exchanger assemblies 44 evaporate and be equally used to gaseous oxygen pressurized product.Shunt the then part o It is too cold in subcooler 35 and is used to liquid oxygen-enriched air products (being indicated herein with LOX).It can be by the liquid air Product imports suitable reservoir 61 and is stored in this.
Richness nitrogen gaseous flow p is extracted from the top of high-pressure tower 31 and it is made to liquefy in falling film evaporator or falling film condenser 39. One shunting is fed back to high-pressure tower 31, and another shunting (referring to bound symbol A) passes through subcooler 35, is then expanded into lower pressure column 33。
Rich nitrogen gaseous flow r, part of it liquid in falling film evaporator or falling film condenser 37 are extracted from the top of medium pressure column 32 Change.One shunting is fed back to medium pressure column 32, and another shunting s passes through subcooler 35, and then demi-inflation enters lower pressure column 33, part It is provided in the form of liquid nitrogen-rich air product (being indicated herein with LIN).Also the liquid nitrogen-rich air product can be stored in conjunction Suitable storage tank 62.
Another (larger) shunting t of stream r is got around after cold compressor 45 under the first operational mode of icon in main heat exchanger It is heated in 20.Autonomous heat exchanger 20 it can extract another part at intermediate temperatures (the stream u) i.e. in figure, this part then may be used In " cold " expansion turbine 46 (so-called pressurization nitrogen turbine) interior swell refrigeration, which can for example couple power generation Machine.The part not expanded in expansion turbine 45 is provided in the form of gaseous state nitrogen-rich air product (being indicated herein with MPGAN). After expanding in expansion turbine 45, stream u passes through main heat exchanger 20 from cold end to hot end and once again in main heat exchanger 20 Hot side, which is divided into, shunts v and w.V is shunted to be used as in main air compressor 10 or the purification device for distributing to the main air compressor Regeneration gas (REGGAS) (see on).It shunts w then to be heated by the heat exchanger 51 run using hot water stream, then equally can coupling Expansion in another expansion turbine 52 of sending and receiving motor.
Nitrogen-enriched stream y is extracted from the top of lower pressure column 33, and the nitrogen-enriched stream is heated in main heat exchanger 20 and is exported air Separation equipment 110.
Because of insulation and main heat exchanger internal loss (the hot side temperature difference) reason, heat leak is inevitable, and as previously mentioned, using Expansion turbine 46 is to provide for the cooling capacity therefore needed alwaysIf working as air separation equipment 110 When in the second operational mode shown in Fig. 2, this cooling capacityIt is provided, can be broken by the liquid air product fed Open expansion turbine 46.In the illustrated embodiment, as a result a large amount of corresponding pressurization nitrogen-rich air products are available, therefrom Recoverable energy.In other configurations, if such as " direct " is provided by main air compressor and the cooling in main heat exchanger Pressurized stream expansion in corresponding expansion turbine (being similar to expansion turbine 46), then can reduce in main air compressor 10 Driving power.
Fig. 2 shows corresponding second operational modes of air separation equipment 110.It in this operating mode, on the one hand will be oxygen-enriched Liquid air product (LOX) imports bath evaporator or bath condenser 34 (referring to bound symbol B) from storage tank 61, on the other hand by liquid State air products (such as liquefied air from External liquefying device, indicated herein with LAIR) are sent into lower pressure column from another storage tank 63 33.Since the chilling requirement of air separation equipment 110 has been more than to be met with needing at this time, expansion turbine 46 can be disconnected. In this way, according to the extracted amount that gaseous state nitrogen-rich air product (MPGAN) can be adjusted by valve (non-symbol), Have a large amount of corresponding pressurization nitrogen-rich air products (being also denoted as stream x herein) available, therefrom can in expansion turbine 52 or It recovers energy in its generator.But it must preheated air.However, being more troublesome using corresponding preheating device.
Cold compressor 45 is also run in the second operating mode.As previously mentioned, liquid air product (herein for LOX and LAIR it will be more than) ice chest of the cooling capacity input air separation equipment 110 needed, cause the Temperature Distribution " deformation " in heat exchanger And the temperature of the stream of one or more outflow heat exchangers is lower and lower.It just can not ensure air separation again from a certain limit value Equipment reliability service.This problem is resolved in air separation equipment 110 by cold compressor 45 is run as heat source. However, cold compressor 45 is not only system heat supply, but predetermined substance stream (herein for stream t) is compressed by selectivity to influence And overall procedure is improved, this is other heat-producing units such as air hot type, vapor heating type, gas hot type, electric power hot type Heat exchanger or the heat exchanger otherwise heated cannot reach.Boost effect caused by cold compressor 45 can be swollen It is utilized in swollen turbine 52.
Compared with the air separation equipment 110 of non-present invention, following air separation equipments 100 of the invention have and particularly have Beneficial effect, wherein cold compressor 45 is used as so-called feed compressor (Feedverdichter) and is integrated in distillation column system 30.In other words, in the second operating mode, at least one gaseous state pressurized stream (is being lower than main heat exchange referring to following each stream b to g) Cold compressor 45 is admitted on the temperature levels of the hot side temperature of device 20, from the first superpressure stress level quilt in cold compressor 45 It is compressed to the second superpressure stress level and is admitted at least one distillation of distillation column system 30 on the second superpressure stress level Tower 31,32.In other words, such as a corresponding gaseous state pressurized stream is (such as from main air compressor 10 and form is following stream e Air, or from one of destilling tower and rich nitrogen state pressurized streams that form is following stream b to d, f and g) in cold compressor From one for lower pressure column or medium pressure column 32 or 33 or for using lower pressure as the stress level pressure of the tower of operating pressure in 45 One is reduced to for medium pressure column or high-pressure tower 31 or 32 or for using elevated pressures as the stress level of the tower of operating pressure.In master Accordingly cooled down in heat exchanger 20 (if it is necessary to) after, which is sent into corresponding destilling tower 31,32 at suitable position.
Method such as this method of the pressurized stream a and l of two different stress levels are provided particularly with utilization main compressor 10, this Rectification effect can be improved.In three-tower system, high-pressure tower 31 should be imported into and the share of the air of high pressure must be compressed into before this Become smaller, medium pressure column should be imported into and the share that must be compressed into the air of middle pressure before this then becomes larger.As a result, respective air point Total energy consumption from equipment 100 significantly reduces.In this case, it is preferable to thus and thus switch cold compressor 45, so that in the case of this The connector (pipe fitting) for the cold compressor 45 being disconnected obtain using.Equipment cost and line cost can be greatly reduced in this.
Referring to shown in Fig. 3, the respective air separation equipment 100 of an embodiment according to the present invention is in the second operation mould Formula.First operational mode with it is unanimous on the whole shown in Fig. 1, therefore not again illustrate: in the first operating mode, one flows through accordingly It crosses expansion turbine 46 and gets around cold compressor 45.Under the second operational mode as shown in Figure 2, on the one hand by oxygen-rich liquid sky Gas product (LOX) imports bath evaporator or bath condenser 34 (referring to bound symbol B) from storage tank 61, on the other hand by liquid air Product (such as liquefied air from External liquefying device, indicated herein with LAIR) is sent into lower pressure column 33 from another storage tank 63.
Cold compressor 45 is herein charging with the shunting b for extracting from the nitrogen-enriched stream y of lower pressure column 33, therefore the shunting is in low pressure On the aforementioned superpressure stress level at 33 top of tower, such as 1.3 to 1.4 bars.This shunts b and is somebody's turn to do (" first ") certainly in cold compressor 45 Superpressure stress level is compressed into higher (" second ") the superpressure stress level equal to the operating pressure of medium pressure column 32.Then in Between at a temperature of by the compression shunt b be sent into main heat exchanger 20 channel 25 and accordingly cool down.Stream b is sent to middle pressure after cooling 32 top of tower.Equally other can be shunted to j (MPGAN) when needing and z (is partially used as regeneration gas REGGAS, is optionally only used for First operational mode) export air separation equipment.The configuration formed by heat exchanger 51 and expansion turbine 52 is unused.
Referring to shown in Fig. 4, another air separation equipment of an embodiment according to the present invention is in the second operational mode. Cold compressor 45 also splits into charging herein with the nitrogen-enriched stream y for extracting from lower pressure column 33, which is indicated and be in c herein On the aforementioned superpressure stress level at 33 top of lower pressure column, such as 1.3 to 1.4 bars.This shunts c in cold compressor 45 from should (" the One ") superpressure stress level is compressed into higher (" second ") the superpressure stress level equal to the operating pressure of high-pressure tower 31.Then At intermediate temperatures by the compression shunt c be sent into main heat exchanger 20 channel 27 and accordingly cool down.Stream c is sent to after cooling 31 top of high-pressure tower.Equally can other streams j (MPGAN) and z (be partially used as regeneration gas REGGAS when needing, optionally only used In the first operational mode) and rich nitrogen high-pressure spray (HPGAN) export air separation equipment.
Referring to Figure 5, another air separation equipment of an embodiment according to the present invention is in the second operational mode. Cold compressor 45 is herein to flow d for charging, which is to extract from the top of medium pressure column 32, so in the aforementioned of 32 top of medium pressure column On the temperature levels of superpressure stress level and medium pressure column.This shunts d certainly should (" first ") superpressure pressure water in cold compressor 45 Flat higher (" second ") the superpressure stress level for being compressed into the operating pressure for being still equal to high-pressure tower 31.Then at intermediate temperatures By the compression shunt d be sent into main heat exchanger 20 respective channel 27 and accordingly cool down.Stream d is sent to high-pressure tower 31 after cooling Top.Equally can other streams j (MPGAN) and z (be partially used as regeneration gas REGGAS when needing, optionally be only used for the first fortune Row mode) and rich nitrogen high-pressure spray (HPGAN) export air separation equipment.
Referring to shown in Fig. 6, another air separation equipment of an embodiment according to the present invention is in the second operational mode. Cold compressor 45 from the shunting e of the pressurized stream l of main air compressor 10 has been charging since herein, which, which is in, is equal to medium pressure column On the aforementioned superpressure stress level of 32 operating pressure.The cold end of autonomous heat exchanger 20, which is extracted, shunts e, therefore its temperature levels is low It is horizontal in the hot side temperature of main heat exchanger 20.This shunts e certainly should (" first ") superpressure stress level quilt in cold compressor 45 It is compressed to higher (" second ") the superpressure stress level for the operating pressure for being still equal to high-pressure tower 31.Compression shunting e is then in Between at a temperature of be admitted to the channel 21 of main heat exchanger 20, to converge with stream a.This continues accordingly to be cooled down with the stream that a is indicated. Stream a is sent into high-pressure tower 31 after cooling.As described above, equally other streams j (MPGAN) and z (partially can be used as regeneration when needing Gas REGGAS is optionally only used for the first operational mode) export air separation equipment.
Referring to shown in Fig. 7, another air separation equipment of an embodiment according to the present invention is in the second operational mode. Cold compressor 45 herein with flow f for charging, the stream be extract from lower pressure column 33, so be in lower pressure column 33 aforementioned superpressure pressure On horizontal (such as 1.3 to 1.4 bars) and its temperature levels.This shunts f certainly should (" first ") superpressure pressure in cold compressor 45 Level is compressed into higher (" second ") the superpressure stress level for the operating pressure for being still equal to medium pressure column 32.The compression shunt f and The channel 24 of main heat exchanger 20 is admitted at intermediate temperatures afterwards, to converge with stream l.The stream for continuing to be indicated with l is by phase It should cool down.Stream l is sent into medium pressure column 32 after cooling.As described above, equally can be by other streams j (MPGAN) and (part z when needing As regeneration gas REGGAS, it is optionally only used for the first operational mode) export air separation equipment.
Referring to shown in Fig. 8, another air separation equipment of an embodiment according to the present invention is in the second operational mode. Cold compressor 45 herein also with flow g for charging, the stream be extract from lower pressure column 33, so be in lower pressure column 33 aforementioned superpressure pressure In power level (such as 1.3 to 1.4 bars) and its temperature levels.This shunts g certainly should (" first ") superpressure pressure in cold compressor 45 Power level is compressed into higher (" second ") the superpressure pressure for the operating pressure (such as 5.0 to 5.5 bars) for being still equal to high-pressure tower 31 It is horizontal.The compression shunts the channel 21 that g is then admitted to main heat exchanger 20 at intermediate temperatures, to converge with stream a.It should be after The continuous stream indicated with a is accordingly cooled down.Stream a is mainly sent into high-pressure tower 31 after cooling.Equally other can be flowed j when needing (MPGAN) and z (being partially used as regeneration gas REGGAS, be optionally only used for the first operational mode) exports air separation equipment.
Fig. 9 and Figure 10 is the partial schematic diagram that the optinal plan of cold compressor 45 is arranged.Corresponding stream is no longer with symbol mark Show.The feasible side such as this is all able to achieve in Fig. 3 to all devices shown in Fig. 8 and other embodiments (not shown) of the invention Case.
According to Fig. 9, the stream compressed through cold compressor 45 is admitted to main heat exchanger 20 in hot side.Referring to Fig.1 shown in 0, Autonomous heat exchanger 20 extracts one stream under first medium temperature, then compresses the stream and gives it once again under the second medium temperature Enter main heat exchanger 20.

Claims (16)

1. the method for producing at least one air products, wherein using air separation equipment (100), which has Main air compressor (10), main heat exchanger (20) and distillation column system (30), the distillation column system include high-pressure tower (31), in Tower (32), lower pressure column (33), lower pressure column tower bottom evaporator (39) and lower pressure column central evaporator (37) are pressed, wherein the high-pressure tower (31) it is run with the operating pressure for being higher than the lower pressure column (33), the medium pressure column (32) is between the high-pressure tower (31) and the lower pressure column (33) the operating pressure operation between operating pressure, and evaporation among the lower pressure column tower bottom evaporator (39) and the lower pressure column Device (37) is configured to condenser/evaporator, which is characterized in that and this method includes the first operational mode and the second operational mode, wherein
In the first operating mode, storage it is at least one generated in the distillation column system (30) liquid air product (LIN, LOX), and
In the second operating mode,
By at least one liquid air product stored in the first operating mode and/or at least one not in the second operation The other liquid air products generated under mode are sent into the distillation column system (30), and
It will at least one gaseous state pressurized stream (b-g) be sent into the temperature levels of the hot side temperature lower than the main heat exchanger (20) Cold compressor (45) is compressed to the second superpressure stress level by the first superpressure stress level in the cold compressor (45), and The second superpressure stress level is at least partly sent at least one destilling tower of the distillation column system (30).
2. the method according to claim 1, wherein in the first operating mode, at least one pressurized stream and/or at least one its His gaseous state pressurized stream (b-g) swell refrigeration in expansion turbine (46).
3. method according to claim 1 or 2, wherein the oxygen coalescence stream of the tower bottom from the lower pressure column is in auxiliary condenser (34) In be evaporated to provide gaseous oxygen pressurized product (GOX), wherein the auxiliary condenser (34) is configured to condenser/evaporator.
4. method according to claim 1 or 2, wherein the air-flow (r) of the tower top discharge nitrogen enrichment by medium pressure column (32), and portion Divide ground liquefaction in lower pressure column central evaporator (37).
5. method according to claim 1 or 2, wherein the first superpressure stress level is equivalent to the operation pressure of the lower pressure column (33) Power and/or the second superpressure stress level are equivalent to the operating pressure of the high-pressure tower (31).
6. method according to claim 1 or 2, wherein the first superpressure stress level is equivalent to the operation pressure of the lower pressure column (33) Power and the second superpressure stress level be equivalent to the medium pressure column (32) or the high-pressure tower (31) operating pressure or this first Superpressure stress level is equivalent to the operating pressure of the medium pressure column (32) and the second superpressure stress level is equivalent to the high-pressure tower (31) operating pressure.
7. method according to claim 1 or 2, wherein at least one gaseous state pressurized stream are by the distillation column system (30) with this What at least part of the stream for the destilling tower discharge that the first superpressure stress level is run as operating pressure was formed.
8. method according to claim 1 or 2, wherein this at least one gaseous state pressurized stream is by utilizing the main air compressor (10) provide and utilize at least part of the stream of the main heat exchanger (20) cooling to be formed.
9. method according to claim 1 or 2, wherein this at least one gaseous state pressurized stream is being admitted to the distillation column system (30) At least one destilling tower before converge in the second superpressure stress level and at least one other flow (a).
10. method according to claim 1 or 2, wherein at least one gaseous state pressurized stream compression in the cold compressor (45) It is at least partly cooling in the main heat exchanger (20) later.
11. method according to claim 10, wherein at least one gaseous state pressurized stream compression in the cold compressor (45) The main heat exchanger is sent into hot side or in the temperature levels of other hot side temperatures lower than the main heat exchanger (20) afterwards (20) to be cooled down.
12. method according to claim 1 or 2, wherein a part of the gaseous state pressurized stream compressed in the cold compressor (45) It heats in the main heat exchanger (20) and/or is at least partly exported by the air separation equipment (100).
13. air separation equipment (100), with main air compressor (10), main heat exchanger (20) and distillation column system (30) it and is set up to be run under the first operational mode and the second operational mode, is provided in order to first At least one liquid air product (LIN, LOX) generated in the distillation column system (30) is stored under operational mode and the By at least one liquid air product stored in the first operating mode and/or at least one not the under two operational modes The other liquid air products generated under two operational modes are sent into the distillation column system (30) and the device (61- that sets up 63), which is characterized in that the air separation equipment (100) includes cold compressor (45), and is provided with to run mould second It will at least one gaseous state pressurized stream (b-g) be somebody's turn to do in the temperature levels feeding of the hot side temperature lower than the main heat exchanger (20) under formula Cold compressor (45), in the cold compressor (45) by the first superpressure stress level be compressed to the second superpressure stress level and then It is set up at least one destilling tower that the second superpressure stress level is at least partly sent into the distillation column system (30) Device.
14. the method produced electricl energy, wherein by according to claim 1 to one of 12 method at least in the second operational mode phase Between at least one air products are provided, and be used for generating and/or converting at least one fuel.
15. the equipment set up to implement method according to claim 14.
16. equipment according to claim 15, the equipment is for implementing oxygen-rich combustion method and/or integrated gasification combined cycle plants Method.
CN201480039508.0A 2013-07-11 2014-07-10 Produce method, the air separation plant, the method and apparatus produced electricl energy of at least one air products Active CN105378411B (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP13003510.8 2013-07-11
EP13003510 2013-07-11
PCT/EP2014/001891 WO2015003808A2 (en) 2013-07-11 2014-07-10 Method for producing at least one air product, air separation system, method and device for producing electrical energy

Publications (2)

Publication Number Publication Date
CN105378411A CN105378411A (en) 2016-03-02
CN105378411B true CN105378411B (en) 2019-01-22

Family

ID=48792938

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201480039508.0A Active CN105378411B (en) 2013-07-11 2014-07-10 Produce method, the air separation plant, the method and apparatus produced electricl energy of at least one air products

Country Status (7)

Country Link
US (1) US20160370111A1 (en)
EP (1) EP3019804A2 (en)
KR (1) KR20160032160A (en)
CN (1) CN105378411B (en)
AU (1) AU2014289591A1 (en)
TW (1) TW201518664A (en)
WO (1) WO2015003808A2 (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10337792B2 (en) 2014-05-01 2019-07-02 Praxair Technology, Inc. System and method for production of argon by cryogenic rectification of air
US10082333B2 (en) 2014-07-02 2018-09-25 Praxair Technology, Inc. Argon condensation system and method
EP3557166A1 (en) * 2018-04-19 2019-10-23 Linde Aktiengesellschaft Method for the low-temperature decomposition of air and air separation plant
CN109357475B (en) * 2018-08-30 2020-05-19 华中科技大学 System for cascade utilization LNG cold energy prepares liquid oxygen liquid nitrogen

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2819046A1 (en) * 2001-01-03 2002-07-05 Air Liquide Cryogenic distillation air separation plant uses compressor to compress nitrogen-rich flow with inlet temperature below that of heat exchanger
CN1918444A (en) * 2003-12-23 2007-02-21 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 Cryogenic air separation process and apparatus
WO2008059399A2 (en) * 2006-11-16 2008-05-22 L'air Liquide-Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
CN201265997Y (en) * 2008-09-05 2009-07-01 苏州制氧机有限责任公司 Liquid air separation plant

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5682764A (en) * 1996-10-25 1997-11-04 Air Products And Chemicals, Inc. Three column cryogenic cycle for the production of impure oxygen and pure nitrogen
US6626008B1 (en) * 2002-12-11 2003-09-30 Praxair Technology, Inc. Cold compression cryogenic rectification system for producing low purity oxygen
DE102006027650A1 (en) * 2006-06-14 2007-02-01 Linde Ag Method for cryogenic air separation, involves discharging of deep frozen liquid from external source into single column or into head condenser and feed air is condensed and discharged in single column
FR2930331B1 (en) * 2008-04-22 2013-09-13 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
US8443625B2 (en) * 2008-08-14 2013-05-21 Praxair Technology, Inc. Krypton and xenon recovery method

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2819046A1 (en) * 2001-01-03 2002-07-05 Air Liquide Cryogenic distillation air separation plant uses compressor to compress nitrogen-rich flow with inlet temperature below that of heat exchanger
CN1918444A (en) * 2003-12-23 2007-02-21 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 Cryogenic air separation process and apparatus
WO2008059399A2 (en) * 2006-11-16 2008-05-22 L'air Liquide-Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
CN201265997Y (en) * 2008-09-05 2009-07-01 苏州制氧机有限责任公司 Liquid air separation plant

Also Published As

Publication number Publication date
AU2014289591A1 (en) 2015-12-24
US20160370111A1 (en) 2016-12-22
CN105378411A (en) 2016-03-02
TW201518664A (en) 2015-05-16
WO2015003808A2 (en) 2015-01-15
WO2015003808A3 (en) 2015-09-24
EP3019804A2 (en) 2016-05-18
KR20160032160A (en) 2016-03-23

Similar Documents

Publication Publication Date Title
JP4733124B2 (en) Cryogenic air separation method for producing pressurized gas products
CN101097112B (en) Method for air feeding in low temperature separation process
CN104755360B (en) Method and apparatus for carrying out air separation by low temperature distillation
US20090078001A1 (en) Cryogenic Distillation Method and System for Air Separation
JP2009509120A (en) Method and apparatus for separating air by cryogenic distillation.
US9810103B2 (en) Method and device for generating electrical energy
CN111406192B (en) Cryogenic rectification method and apparatus for producing pressurized air by expander booster braked in conjunction with nitrogen expander
JPH09228852A (en) Air separation method for incorporating combustion turbine
JPH11509615A (en) Method and apparatus for variably generating pressurized product gas
US20200149808A1 (en) Air separation method and apparatus
EP2634517B1 (en) Process and apparatus for the separation of air by cryogenic distillation
CN105378411B (en) Produce method, the air separation plant, the method and apparatus produced electricl energy of at least one air products
US20150192330A1 (en) Method and device for generating electrical energy
CN105579801A (en) Process and apparatus for producing gaseous oxygen by cryogenic distillation of air
US20170211880A1 (en) Method for obtaining an air product, and air separation plant
CN104185767B (en) For the method and apparatus producing two strands of partial air flow purified
JP2005134036A (en) Air separator, and its operating method
US20160153711A1 (en) Method and system for air separation using a supplemental refrigeration cycle
EP1726900A1 (en) Process and apparatus for the separation of air by cryogenic distillation
CN103453731B (en) Method and device for generating electrical energy
US20040244416A1 (en) Method for separating air by cryogenic distillation and installation therefor
US20120174625A1 (en) Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air
JP2003021457A (en) Internal pressurization type low-temperature air separation equipment

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant