EP2758734A1 - Verfahren und vorrichtung zur tieftemperaturzerlegung von luft - Google Patents
Verfahren und vorrichtung zur tieftemperaturzerlegung von luftInfo
- Publication number
- EP2758734A1 EP2758734A1 EP12762536.6A EP12762536A EP2758734A1 EP 2758734 A1 EP2758734 A1 EP 2758734A1 EP 12762536 A EP12762536 A EP 12762536A EP 2758734 A1 EP2758734 A1 EP 2758734A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- pressure column
- low
- pressure
- column
- evaporator
- 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.)
- Granted
Links
Classifications
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- 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
- F25J3/04454—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 a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
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- 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
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- 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
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- 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
- F25J3/04103—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 using solely hydrostatic liquid head
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- 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
- F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
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- 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
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
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- 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
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
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- 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
- F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
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- 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
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- 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
- F25J3/04212—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 and simultaneously condensing vapor from a column serving as reflux within the or another column
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- 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
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- 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
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- 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
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- 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
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- 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
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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- 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.
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- 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
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- 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
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- 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
- F25J2200/10—Processes or apparatus using separation by rectification in a quadruple, or more, column or pressure system
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
- F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
- F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/62—Purifying more than one feed stream in multiple adsorption vessels, e.g. for two feed streams at different pressures
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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/54—Oxygen production with multiple pressure O2
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- 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
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
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- 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
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- 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
- F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude oxygen")
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
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- 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
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- 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
- F25J2250/10—Boiler-condenser with superposed stages
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- 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
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- 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
Definitions
- the invention relates to a method for the cryogenic separation of air according to the preamble of patent claim 1.
- the method is carried out in a distillation column system for nitrogen-oxygen separation, which is a first
- High-pressure column and a low pressure column and three condenser evaporator namely a high-pressure column head capacitor, a
- Low-pressure column bottom evaporator and a secondary condenser The invention particularly relates to a low pressure process.
- low pressure process is meant here a process in which the
- Operating pressure at the top of the low-pressure column is less than 2.0 bar, in particular less than 1, 8 bar, in particular less than 1, 5 bar.
- condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream. Each condenser evaporator has a
- Condensing passages or evaporation passages exist.
- the condensation (liquefaction) of a first fluid flow is performed, in the evaporation space the evaporation of a second fluid flow.
- Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
- a condenser-evaporator may be formed, for example, as a falling film or bath evaporator.
- the fluid to be evaporated flows from top to bottom through the evaporation space and is partially evaporated.
- a bath evaporator (sometimes called “circulation evaporator” or “thermosiphon evaporator”) is the heat exchanger block in one
- Liquid bath of the fluid to be evaporated This flows by means of
- the remaining liquid flows outside the heat exchanger block back into the liquid bath.
- the evaporation chamber may include both the evaporation passages and the outer space around the heat exchanger block.
- the condenser evaporators for the low-pressure column (the high-pressure column head condenser, if it is designed as a low-pressure column intermediate evaporator, and the low-pressure column bottom evaporator) can inside the
- the high-pressure column top condenser can also be arranged at the top of the first high-pressure column.
- mass transfer elements are understood here all column internals, which cause the decisive for the distillation (rectification) intensive mass transfer between rising steam and trickling down liquid.
- the term includes in particular conventional mass transfer trays, ordered packing and packed beds (disordered packing). Basically, at the
- the high-pressure column and the low-pressure column each form a separation column in the process engineering sense. They are regularly arranged in a container. Alternatively, the mass transfer elements of each column may be distributed over two or more containers connected in correspondence.
- the insert for the auxiliary capacitor is either by a part of the
- Bath evaporator is formed.
- the bottom liquid of the low-pressure column which runs from the bottom mass transfer element, into the evaporation space of the
- Low-pressure column bottom evaporator introduced, and the unevaporated portion of Low pressure column bottoms liquid exiting the bottom of the low pressure column is at least partially fed to the side condenser.
- air or a nitrogen-enriched fraction from a high-pressure column can be used as the heating medium.
- the low-pressure column sump evaporator is heated together with the secondary condenser with a stream of air; this is unfavorable for the
- High pressure column brought in a cold compressor to an elevated pressure and used as a heating medium in the low-pressure column bottom evaporator (and in the secondary condenser).
- the use of a cold compressor is expensive and is also associated with heat input at a low temperature level, which is fundamentally unfavorable in terms of energy.
- the invention has for its object to make such a method and a corresponding device so that a relatively low expenditure on equipment is operated and they are energetically particularly favorable to operate.
- the method of the invention can be dispensed with a cold compressor and it is also no air in the low-pressure column bottom evaporator pre-liquefied.
- the liquefaction chamber of the low-pressure column bottom evaporator is operated at about the pressure of the head of the second high-pressure column; in any case, the top gas of the second high-pressure column is not compressed before being introduced into the low-pressure column bottom evaporator, but preferably enters its liquefaction space under its natural pressure.
- cold can be obtained by a pressurized nitrogen turbine by performing a nitrogen-enriched stream from a high-pressure column of the distillation column nitrogen-oxygen separation system and warming the work-expanded nitrogen-enriched stream in the main heat exchanger.
- the nitrogen-enriched stream may originate from the second high-pressure column, but is preferably from the first
- Inlet pressure is therefore equal to the operating pressure of the corresponding high-pressure column (minus line losses). It is beneficial if at least a part of the after work
- Relaxation warmed nitrogen-enriched stream is used as a regeneration gas in a cleaning device for feed air. This not only constitutes a beneficial use of the work-stream decompressed stream, but also decouples the low pressure column pressure from the pressure loss that the
- Regeneriergas in the cleaning device learns. Because the regeneration gas is not taken as usual from the low pressure column, the regeneration gas is not taken as usual from the low pressure column, the
- Low pressure column pressure to be correspondingly lower, for example, lower than 1, 30 bar, and thus the entire pressure level can be lowered. This further increases the energy efficiency of the process.
- the high-pressure column head condenser is operated as a low-pressure column intermediate evaporator by evaporating there a liquid intermediate fraction from the low pressure column and at least a portion of the vaporized in the low-pressure column intermediate evaporator intermediate fraction introduced as ascending gas in the low pressure column becomes.
- the reflux liquid for the first high-pressure column is produced in a particularly advantageous manner and at the same time improves the separation efficiency of the low-pressure column.
- the low-pressure column is formed by at least two sections, wherein a first section and a second section are each arranged in a separate container containing mass transfer elements, and the second section of the low-pressure column is arranged adjacent to the first high-pressure column.
- the low pressure column is divided, that is their
- Mass transfer elements are distributed to more than one container, in particular to exactly two containers. These containers are connected by piping, that overall the procedural effect of a low-pressure column is realized. As a result, the columns and condenser-evaporator can be arranged so that the liquids flow as far as possible due to natural gradient in the corresponding vessels.
- the second section of the low-pressure column is arranged next to the first high-pressure column. "By” here means that the two columns are arranged in normal operation of the plant so that the projections of their cross sections on a horizontal plane do not overlap.
- the first contains
- the Low-pressure column intermediate evaporator and low-pressure column bottom evaporator and the second section, the mass transfer elements of the low-pressure column, over which the top product of this column is withdrawn.
- the Low-pressure column can also be divided into three or more sections. Preferably, exactly two sections are used.
- the first section of the low-pressure column is also arranged next to the first high-pressure column, in particular between the first high-pressure column and the second section of the low-pressure column. If the first high pressure column in one piece and the low pressure column are formed in two parts, in this case, all
- first section of the low-pressure column is not on the ground, but slightly elevated, so that the liquid nitrogen, which is required as reflux in the low-pressure column, does not need to be pumped.
- the first section of the low-pressure column may be arranged above the first high-pressure column.
- the first section of the low pressure column may be above the first
- the low-pressure column intermediate evaporator is preferably arranged above or within the first section of the low-pressure column.
- the first case relates to the construction in which the low-pressure column intermediate evaporator is accommodated in an external container separate from the low-pressure column, the second to an internal low-pressure column intermediate evaporator installed in the top of the first section of the low-pressure column. It is also advantageous if the low-pressure column bottom evaporator is arranged below or within the first section of the low-pressure column.
- the first case relates to the design in which the low-pressure column bottom evaporator is housed in an external, separate from the low-pressure column container, the second to an internal, built into the bottom of the low-pressure column low-pressure column evaporator.
- Sub-condenser is arranged below the low-pressure column bottom evaporator.
- the first and the second high-pressure column are arranged one above the other and the first high-pressure column is arranged below the second high-pressure column.
- none of the usual arrangements is used, that is, neither the low-pressure column over a
- High-pressure columns arranged one above the other, in particular the second high-pressure column over the first.
- Low-pressure column is preferably arranged next to the high-pressure columns.
- the two high-pressure columns can be accommodated in a common coldbox.
- This common coldbox can be prefabricated cost-effectively in the factory. Then it is transported as a whole lying on the site, there erected and connected to the other parts of the system.
- the low-pressure column is preferably accommodated in a second, separate coldbox, which can be prefabricated and transported in an analogous manner.
- An arrangement of two columns “above one another” is understood here to mean that the upper end of the lower of the two columns is at a lower geodetic height than the lower end of the upper of the two columns and the projections of the two columns overlap in a horizontal plane.
- the two columns are arranged exactly one above the other, that is, the axes of the two columns run on the same vertical line. This definition applies analogously to similar terms such as “above” and "below”.
- the sub-capacitor is between the first and the second
- High-pressure column arranged, in particular over the first high pressure column and under the second high pressure column. This seems illogical at first, because the secondary capacitor is functionally not connected to any of these columns. Overall, however, results in a very compact
- this common coldbox can be inexpensively prefabricated in the factory without the need for a separate coldbox for the secondary condenser or the usually quite high cold box of the low-pressure column must be further increased.
- air is used as the heating medium in the secondary condenser by at least partially condensing a third feed air stream in the secondary condenser, which is in particular below a third pressure which is higher than the first pressure.
- the third pressure is equal to the second pressure and the second and the third feed air stream are diverted from a common partial air flow, which has previously been brought to a correspondingly increased pressure.
- Pressures are referred to herein as "equal" when the pressure differential between the respective locations is not greater than the natural conduction losses due to pressure losses in piping, heat exchangers, coolers, adsorbers, etc.
- the feed air streams can be common and the lower
- Pressure level of a common air purification are supplied. In many cases, however, it is better to provide two separate cleaning devices, which are operated under the two different pressures, as is known per se from EP 342436. It is favorable if the third feed air stream is formed by at least part of the cooled second partial air stream. Second and third feed air flow are thus brought together to an increased pressure (for example, the second or third pressure plus line losses) and then separated from each other in the second high-pressure column or the
- the entire second partial air stream can be passed as a second feed air stream through the secondary condenser, there partially condensed only to a small extent and then passed as the first feed air stream into the second high-pressure column.
- the third pressure in
- Einblaseturbine be recovered by a fourth feed air stream is working expanded and introduced into the low pressure column.
- the fourth feed air stream can, for example, be compressed to the same pressure level as the first feed air stream for the first high-pressure column and fed to the corresponding expansion machine at approximately the first pressure.
- the secondary condenser is designed as a bath evaporator.
- all condenser evaporators of the process are designed as bath evaporators. This results - especially in superimposed high-pressure columns - a particularly cost-effective design and a particularly reliable operation.
- the low-pressure column evaporator at the top of the second high-pressure column that is, the low-pressure column sump evaporator sits above the second high-pressure column and the return liquid generated there can due to the natural gradient (ie without Liquid nitrogen pump) into the head of the second high-pressure column.
- the low-pressure column bottom evaporator is preferably arranged directly above the top of the second high-pressure column, like a conventional top condenser.
- the second high-pressure column and the low-pressure column bottom evaporator can be accommodated in a common container, wherein between the evaporation space of the low-pressure column bottom evaporator and the head region of the second
- High pressure column is arranged a partition wall.
- the low-pressure column intermediate evaporator and / or low-pressure column bottom evaporator can be designed as a falling film evaporator.
- the secondary condenser can be designed as a bath evaporator or alternatively also as a falling-film evaporator.
- a third high-pressure column can be used in the method of the invention. It is preferably under higher pressure than the second
- Sub-condenser can be used. Accordingly, the lower is the
- the invention also relates to a device according to claims 22 and 23.
- the device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.
- Figure 1 shows a first embodiment of the invention with pressure nitrogen turbine and two cleaning devices under different pressure level
- Figure 2 shows a second embodiment with injection turbine and a
- FIG. 3 shows a third exemplary embodiment with three high-pressure columns
- Figure 4 shows an embodiment with arrangement of the first portion of
- Figure 5 shows an embodiment with arrangement of the first portion of
- FIG. 6 shows a further exemplary embodiment with the arrangement of a secondary condenser between two separating columns
- FIG. 7 shows a first embodiment of the variant of the invention, in which the
- High-pressure columns are arranged one above the other, with arrangement of the
- Figure 8 shows a second embodiment of this variant of the invention with
- Figure 9 shows a third embodiment of this variant of the invention
- Atmospheric air 1 is sucked in Figure 1 by a main air compressor 3 with aftercooler 4 via a filter 2 and there compressed to a first total air pressure of 3, 1 bar.
- the main air compressor may have two or more stages with intercooling; it is preferably designed for redundancy reasons two-stranded (both not shown in the drawing).
- the total air flow 5 is under the first total air pressure and a temperature of 295 K a first
- Direct contact cooler 6 fed and cooled there in direct heat exchange with cooling water 7 from an evaporative cooler 8 further to 283 K.
- the cooled total air flow 9 is divided into a first partial air flow 10 and a second partial air flow 11.
- the second partial air stream 1 1 is in a secondary compressor 12 with aftercooler 13 from the first total air pressure (minus pressure drops) to a second
- the booster may have two or more intermediate cooling stages; it is preferred for redundancy reasons formed two-stranded (both not shown in the drawing).
- the main air compressor and the Nachverêtrs may be designed as a machine with a common drive, in particular as a transmission compressor.
- the second partial air stream 14 is then cooled in a second direct-contact cooler 15 of 295 K to 290 K, in direct heat exchange with a warmer cooling water stream sixteenth
- the first partial air stream is cleaned in a first cleaning device 18, which is operated under the first total air pressure, and then fed via line 19 under this pressure to the warm end of a main heat exchanger, which is formed in the embodiment by two blocks 20, 21 connected in parallel.
- the cooled to about dew point air forms a "first feed air stream" 22, which is a first high-pressure column 23 is supplied.
- the first high-pressure column 23 is part of a distillation column system for nitrogen-oxygen separation, which also has a second high-pressure column 24, a
- Low-pressure column intermediate evaporator 27 is formed, a low-pressure column bottom evaporator 28 and a secondary capacitor 29 has.
- Low-pressure column intermediate evaporator 27 and the low-pressure column bottom evaporator 28 are formed as a falling film evaporator, the secondary condenser 29 as a bath evaporator.
- the pre-cooled second partial air stream 17 is cleaned in a second cleaning device 30, which is operated under the second total air pressure. From the purified second partial air stream, a small part can be removed via line 32, which is used as instrument air or for purposes outside the air separation. The remainder flows via line 33 to the main heat exchanger 20 and is cooled there.
- the cooled second partial air stream 34 is divided into a "second feed air stream" 35, which is introduced into the second high-pressure column 24, and into a "third
- Feed air stream "36 which is fed to the liquefaction space of the secondary condenser 29.
- the at least partially, preferably substantially completely condensed, third substream 37 is introduced into a separator (phase separator) 38.
- the liquid portion 39 is supplied to a first part 40 of the first high-pressure column 23.
- To a second part 41 it is fed via a supercooling countercurrent 42 and line 43 in the low-pressure column 26.
- Nitrogen-rich overhead gas 44 of the first high-pressure column 23 is condensed to a first part in the low-pressure column intermediate evaporator 27.
- recovered liquid nitrogen 46 is fed to a first part 47 as reflux to the top of the first high-pressure column 23.
- a second part 48 is cooled in the supercooling countercurrent 42 and fed via line 49 as reflux to the top of the low-pressure column 26.
- a portion 50 of the supercooled liquid can be recovered as needed as a liquid product (LIN).
- a second portion 51 of the nitrogen-rich overhead gas 44 of the first high-pressure column 23 is introduced into the main heat exchanger 20. At least a part of it 52 warmed only to an intermediate temperature, and then in a
- the outlet pressure of the turbine is just enough to the work-performing relaxed flow 54 through the main heat exchanger 20 and via the lines 55, 56, 57 as a regeneration gas through the first and the second
- Another part of the stream 51 is in the main heat exchanger 20 up to
- Nitrogen-rich head gas 58 of the second high-pressure column 24 is in the
- Low-pressure column bottom evaporator 28 condenses.
- recovered liquid nitrogen 59 is given to a first part 60 as reflux to the head of the second high-pressure column 24.
- a second part 61 is cooled in the supercooling countercurrent 42 and fed via line 62 as reflux to the top of the low-pressure column 26.
- the bottom liquids 63, 64 of the two high-pressure columns 23, 24 become
- Sub-condenser 29 and is partially evaporated there.
- the fraction 68 evaporated in the secondary condenser is conducted to the cold end of the main heat exchanger block 20, warmed to approximately ambient temperature and finally recovered via line 69 as gaseous oxygen product (GOX) of a purity of 95 mol%.
- the liquid remaining fraction is evaporated to a part 70 in a pump 71 to a pressure of 6 bar, in the main heat exchanger block 21 and warmed and finally admixed with the gaseous oxygen product 69.
- Another part 72 may be via the subcooling countercurrent 42, pump 73 and line 74 as
- Liquid oxygen product (LOX) are recovered.
- Low-pressure column section 26 is obtained by means of a pump 76 in the
- nitrogen-rich residual gas 80 is withdrawn under a pressure of 1, 26 bar and fed after warming in supercooling countercurrent 42 and main heat exchanger 20 via line 81 virtually pressureless as dry gas into the evaporative cooler 8 and used there for cooling of cooling water 82 ,
- FIG. 2 differs with regard to two process sections of FIG. 1, namely the generation of cooling and the air compression with precooling and cleaning. In the following, only the deviating aspects are explained in more detail, both can be combined independently with the other sections of the procedure.
- Blow-in turbine 153 generated. This is operated with a "fourth feed air stream" 151, 152, which consists of the first partial air flow 119 under the lower first
- Feed air stream 154 is supplied to the low pressure column 26 at a suitable intermediate point.
- the air compression is carried out here simpler than in Figure and in particular has only a single cleaning device 1 18, in which the total air 105, 10 is cleaned under the first total air pressure. Only a direct contact cooler 106 is used.
- the division into the first partial air flow 119 and the second partial air flow 111 is carried out downstream of the cleaning device 18 here.
- the after-compressor 112 is constructed as in FIG. 1, but has only one conventional after-cooler 113 and the air is not further cooled in a direct-contact cooler. Via line 119 then the second HeilteNstrom is performed analogously to line 19 in Figure 1.
- FIG. 3 largely corresponds to FIG. 1.
- the warm section of the method is not shown and may be designed as in FIG. 1 or as in FIG.
- Partial air flow a high-pressure feed air stream 233 is introduced into the main heat exchanger 20.
- the cold high pressure feed air stream 235 enters a third high pressure column 224 at a third pressure of 5.3 bar.
- the nitrogen-rich overhead gas 258 is used as heating medium in the secondary condenser 228 and condensed there substantially completely.
- liquid nitrogen 259 obtained is fed to a first part 260 as reflux to the top of the second high-pressure column 24.
- a second portion 261 is cooled in the subcooling countercurrent 42 and fed via line 262 as reflux to the top of the low pressure column 26.
- the secondary condenser 228 is embodied in this embodiment as a multi-storey bath evaporator, in particular as a cascade evaporator, in which the individual floors are connected in parallel on the evaporation side in series and on the liquefaction side.
- a multi-storey bath evaporator in particular as a cascade evaporator, in which the individual floors are connected in parallel on the evaporation side in series and on the liquefaction side.
- an injection turbine can also be used in the method of FIG. 3, as well as in the following FIGS. 4 to 6.
- the third high pressure column 224 is, as shown in Figure 3, preferably below the secondary capacitor 228 or the combination of
- the spatial arrangement of the remaining columns corresponds to that of Figures 1 and 2.
- FIG. 4 differs from FIG. 1 in that the first section 25 of the low-pressure column with the two evaporators 27, 28 is above the second
- High pressure column 24 is arranged.
- the first section 25 of the low-pressure column with the two evaporators 27, 28 is arranged above the first high-pressure column 23.
- the secondary condenser 29 of Figure 6 is disposed between the second high pressure column 24 and the first portion 25 of the low pressure column. Otherwise, Figure 6 corresponds to the embodiment of Figure 4.
- the arrangement of the secondary capacitor 29 between two columns according to Figure 6 can also be transferred to the embodiment of Figure 5.
- the compression and cleaning of the feed air and any diversion of instrument air is not shown in Figures 7 to 9.
- the required for the process two air streams with different pressures are supplied with only one two-section air compressor.
- the entire feed air is brought in the first, two-stage section to a pressure of about 3.8 bara and passed exclusively into the precooling system. After the pre-cooling and
- a first partial air flow 19 is fed in FIG. 7 at a first pressure of approximately 3.6 bar to the warm end of a main heat exchanger 20.
- the cooled to about dew point air forms a "first feed air stream" 22, the first
- High-pressure column 23 is supplied.
- the first high-pressure column 23 is part of a distillation column system for nitrogen-oxygen separation, which also has a second high-pressure column 24, a
- Low-pressure column bottom evaporator 28 and a secondary capacitor 29 has. All these capacitors are formed in the embodiment as a bath evaporator.
- the low-pressure column is integrally formed - that is, her two sections 25, 26 below and above the low-pressure column intermediate evaporator 27 are arranged in a common container - and stands on the floor. The combination of the two
- High pressure columns and the low pressure column are arranged side by side.
- a second partial air stream 33 flows under a second pressure of about 5.25 bar to the main heat exchanger 20 and is cooled there.
- the cooled second partial air stream 34 is divided into a "second feed air stream" 35, which in the second High pressure column 24 is introduced, and in a "third feed air stream” 36, which is fed to the liquefaction space of the secondary condenser 29.
- the at least partially, preferably substantially completely condensed, third substream 37 is fed to a first part 40 of the first high-pressure column 23. To a second part 41 it is fed via a supercooling countercurrent 42 and line 43 in the low-pressure column 26.
- Nitrogen-rich overhead gas of the first high-pressure column 23 is condensed to a first part 44 in the low-pressure column intermediate evaporator 27.
- recovered liquid nitrogen 46 is fed to a first part 47 as reflux to the top of the first high-pressure column 23.
- a second part 48 is cooled in the supercooling countercurrent 42 and fed via line 49 as reflux to the top of the low-pressure column 26.
- a portion of the supercooled liquid may be recovered as needed as a liquid product (not shown).
- a second portion 51 of the nitrogen-rich overhead gas of the first high-pressure column 23 is heated in the main heat exchanger 20 to an intermediate temperature.
- the warmed pressurized nitrogen 52 is recovered as gaseous pressure nitrogen product (PGAN).
- Nitrogen-rich head gas 58 of the second high-pressure column 24 is in the
- Low-pressure column bottom evaporator 28 condenses.
- liquid nitrogen 59 obtained is fed to a first part 60 by means of a pump 57 as reflux to the head of the second high-pressure column 24.
- a second part 61 is in the
- Subcooling countercurrent 42 cooled and abandoned via line 62 as reflux to the head of the low pressure column 26.
- the bottom liquid 64 of the second high pressure column 24 is in the first
- High-pressure column 23 introduced, namely at the bottom and / or something above it.
- the bottom liquid 63 of the first high-pressure column 23 is fed via the supercooling countercurrent 42 and line 65 into the low-pressure column 26.
- the bottom liquid of the low-pressure column 25 is introduced into the evaporation space of the low-pressure column bottom evaporator 28 and partially evaporated there.
- the fraction 68 evaporated in the secondary condenser is conducted to the cold end of the main heat exchanger 20, warmed to approximately ambient temperature and finally recovered via line 69 as gaseous oxygen product (GOX), in this particular case with a purity of approximately 93 mol%.
- the liquid remaining portion 86 is brought to a part 70 in a pump 71 to higher pressure and evaporated in the main heat exchanger 20 (or pseudo-evaporated, if the pressure is supercritical) and warmed.
- Purge stream is then admixed via line 88 to the gaseous oxygen product 69 or alternatively discharged as a separate product.
- a portion of the oxygen product is recovered as internally compressed product ICGOX (for example, 15% of the total amount of oxygen under a pressure of 7 bar).
- ICGOX for example, 15% of the total amount of oxygen under a pressure of 7 bar.
- the secondary capacitor 29 is also rinsed very well. In this case, it suffices if the pump 71 brings the liquid oxygen to the desired product pressure (plus line losses).
- a further portion 72 of liquid remaining portion 86 from the secondary condenser 29 can via the supercooling countercurrent 42 and line 74 as
- Liquid oxygen product (LOX) are recovered.
- nitrogen-rich residual gas 80 is withdrawn under a pressure of about 1, 33 bar and withdrawn after heating in supercooling countercurrent 42 and main heat exchanger 20 via line 81 and is available as a dry gas for an evaporative cooler (not shown) 8 for cooling of cooling water available or can be used as a regeneration gas in a facility for cleaning
- Feed air (also not shown) can be used.
- Cold is generated by an injection turbine 153 in the process. This is operated with a "fourth feed air flow" 151, which - like the first partial air flow 19 - is below the lower first pressure and has been cooled in the main heat exchanger 20 to an intermediate temperature.
- Feed air stream 154 is supplied to the low pressure column 26 at a suitable intermediate point.
- FIG. 8 differs from FIG. 7 in that the secondary capacitor 29 is arranged next to the columns.
- liquid oxygen product 74 is recovered under pressure by the corresponding stream 72 is branched off downstream of the pump 71 and separated in a separator 201 into a gaseous portion 202 and a liquid portion 272.
- a separator 201 is installed relatively high in the cold box and the liquid product 272 flows by means of hydrostatic pressure from this separator into the storage tank.
- FIG. 9 largely corresponds to FIG. 8.
- the low-pressure column bottom evaporator 28 is arranged at the top of the second high-pressure column 24 instead of in the bottom of the lower low-pressure column section 25, ie above the second high-pressure column. This allows the system to operate without a liquid nitrogen pump.
- the return liquid 60 flows solely to the head of the second high-pressure column 24 due to the gradient.
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Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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EP12762536.6A EP2758734B1 (de) | 2011-09-20 | 2012-09-20 | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
PL12762536T PL2758734T3 (pl) | 2011-09-20 | 2012-09-20 | Sposób i urządzenie do niskotemperaturowego rozkładu powietrza |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE201110113671 DE102011113671A1 (de) | 2011-09-20 | 2011-09-20 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE201110113668 DE102011113668A1 (de) | 2011-09-20 | 2011-09-20 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
EP11008534A EP2573492A1 (de) | 2011-09-20 | 2011-10-25 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
EP12004193 | 2012-05-31 | ||
PCT/EP2012/003944 WO2013041229A1 (de) | 2011-09-20 | 2012-09-20 | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
EP12762536.6A EP2758734B1 (de) | 2011-09-20 | 2012-09-20 | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
Publications (2)
Publication Number | Publication Date |
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EP2758734A1 true EP2758734A1 (de) | 2014-07-30 |
EP2758734B1 EP2758734B1 (de) | 2018-07-18 |
Family
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EP12762536.6A Not-in-force EP2758734B1 (de) | 2011-09-20 | 2012-09-20 | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
Country Status (6)
Country | Link |
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US (1) | US10443931B2 (de) |
EP (1) | EP2758734B1 (de) |
CN (1) | CN103998883B (de) |
AU (1) | AU2012311959B2 (de) |
PL (1) | PL2758734T3 (de) |
WO (1) | WO2013041229A1 (de) |
Families Citing this family (6)
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JP5997105B2 (ja) * | 2013-06-05 | 2016-09-28 | 神鋼エア・ウォーター・クライオプラント株式会社 | 空気分離方法 |
FR3013105B1 (fr) * | 2013-11-14 | 2016-01-01 | Air Liquide | Procede et appareil de separation d’air par distillation cryogenique |
CN109520207B (zh) * | 2017-09-18 | 2022-04-08 | 乔治洛德方法研究和开发液化空气有限公司 | 用于通过低温蒸馏分离空气的方法和单元 |
CN111406191B (zh) * | 2017-12-25 | 2021-12-21 | 乔治洛德方法研究和开发液化空气有限公司 | 具有反向主热交换器的单封装空气分离设备 |
CN113924452A (zh) * | 2019-11-26 | 2022-01-11 | 林德有限责任公司 | 用于低温分离空气的方法和设备 |
FR3116586B1 (fr) * | 2020-11-26 | 2023-05-12 | Air Liquide | Procédé et appareil de vaporisation de liquide de purge d’un vaporiseur de liquide cryogénique |
Family Cites Families (25)
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DE3817244A1 (de) | 1988-05-20 | 1989-11-23 | Linde Ag | Verfahren zur tieftemperaturzerlegung von luft |
GB9325648D0 (en) * | 1993-12-15 | 1994-02-16 | Boc Group Plc | Air separation |
US5469710A (en) * | 1994-10-26 | 1995-11-28 | Praxair Technology, Inc. | Cryogenic rectification system with enhanced argon recovery |
US5669237A (en) * | 1995-03-10 | 1997-09-23 | Linde Aktiengesellschaft | Method and apparatus for the low-temperature fractionation of air |
DE19605500C1 (de) * | 1996-02-14 | 1997-04-17 | Linde Ag | Vorrichtung und Verfahren zum Verdampfen einer Flüssigkeit |
US5682762A (en) * | 1996-10-01 | 1997-11-04 | Air Products And Chemicals, Inc. | Process to produce high pressure nitrogen using a high pressure column and one or more lower pressure columns |
US5730003A (en) * | 1997-03-26 | 1998-03-24 | Praxair Technology, Inc. | Cryogenic hybrid system for producing high purity argon |
US5966967A (en) * | 1998-01-22 | 1999-10-19 | Air Products And Chemicals, Inc. | Efficient process to produce oxygen |
DE19939294A1 (de) | 1999-08-19 | 2001-02-22 | Linde Ag | Mehrstöckiger Umlaufkondensator |
DE10009977A1 (de) | 2000-03-03 | 2001-09-06 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE10027139A1 (de) | 2000-05-31 | 2001-12-06 | Linde Ag | Mehrstöckiger Badkondensator |
DE10027140A1 (de) | 2000-05-31 | 2001-12-06 | Linde Ag | Mehrstöckiger Badkondensator |
DE10103968A1 (de) | 2001-01-30 | 2002-08-01 | Linde Ag | Drei-Säulen-System zur Tieftemperaturzerlegung von Luft |
DE10137103A1 (de) | 2001-07-30 | 2003-02-13 | Linde Ag | Mehrstöckiger Kondensator-Verdampfer |
US6536234B1 (en) * | 2002-02-05 | 2003-03-25 | Praxair Technology, Inc. | Three column cryogenic air separation system with dual pressure air feeds |
DE10205878A1 (de) * | 2002-02-13 | 2003-08-21 | Linde Ag | Tieftemperatur-Luftzerlegungsverfahren |
DE10249383A1 (de) | 2002-10-23 | 2004-05-06 | Linde Ag | Verfahren und Vorrichtung zur variablen Erzeugung von Sauerstoff durch Tieftemperatur-Zerlegung von Luft |
US6662593B1 (en) * | 2002-12-12 | 2003-12-16 | Air Products And Chemicals, Inc. | Process and apparatus for the cryogenic separation of air |
DE102006012241A1 (de) * | 2006-03-15 | 2007-09-20 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
US20080115531A1 (en) | 2006-11-16 | 2008-05-22 | Bao Ha | Cryogenic Air Separation Process and Apparatus |
DE102007003437A1 (de) | 2007-01-23 | 2007-09-20 | Linde Ag | Mehrstöckiger Badkondensator im Flüssigkeitsbad |
JP5425100B2 (ja) * | 2008-01-28 | 2014-02-26 | リンデ アクチエンゲゼルシャフト | 低温空気分離方法及び装置 |
FR2930330B1 (fr) * | 2008-04-22 | 2013-09-13 | Air Liquide | Procede et appareil de separation d'air par distillation cryogenique |
US20100024478A1 (en) * | 2008-07-29 | 2010-02-04 | Horst Corduan | Process and device for recovering argon by low-temperature separation of air |
DE102009048456A1 (de) * | 2009-09-21 | 2011-03-31 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
-
2012
- 2012-09-20 US US14/345,840 patent/US10443931B2/en not_active Expired - Fee Related
- 2012-09-20 WO PCT/EP2012/003944 patent/WO2013041229A1/de active Application Filing
- 2012-09-20 CN CN201280046019.9A patent/CN103998883B/zh not_active Expired - Fee Related
- 2012-09-20 EP EP12762536.6A patent/EP2758734B1/de not_active Not-in-force
- 2012-09-20 AU AU2012311959A patent/AU2012311959B2/en not_active Ceased
- 2012-09-20 PL PL12762536T patent/PL2758734T3/pl unknown
Non-Patent Citations (2)
Title |
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None * |
See also references of WO2013041229A1 * |
Also Published As
Publication number | Publication date |
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PL2758734T3 (pl) | 2018-12-31 |
AU2012311959B2 (en) | 2016-09-08 |
US10443931B2 (en) | 2019-10-15 |
US20140223959A1 (en) | 2014-08-14 |
AU2012311959A1 (en) | 2014-03-20 |
EP2758734B1 (de) | 2018-07-18 |
CN103998883B (zh) | 2016-12-14 |
WO2013041229A1 (de) | 2013-03-28 |
CN103998883A (zh) | 2014-08-20 |
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