EP0948730B1 - Procede et dispositif de production d'azote comprime - Google Patents

Procede et dispositif de production d'azote comprime Download PDF

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Publication number
EP0948730B1
EP0948730B1 EP97948844A EP97948844A EP0948730B1 EP 0948730 B1 EP0948730 B1 EP 0948730B1 EP 97948844 A EP97948844 A EP 97948844A EP 97948844 A EP97948844 A EP 97948844A EP 0948730 B1 EP0948730 B1 EP 0948730B1
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EP
European Patent Office
Prior art keywords
pressure column
low
nitrogen
product
liquid
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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.)
Expired - Lifetime
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EP97948844A
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German (de)
English (en)
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EP0948730A1 (fr
Inventor
Horst Corduan
Dietrich Rottmann
Jürgen Voit
Christian Kunz
Wolfgang Haag
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Linde GmbH
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Linde GmbH
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • F25J3/0403—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
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    • 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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    • 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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    • 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
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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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    • 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
    • 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
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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.
    • 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
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • 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
    • 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
    • F25J2250/10—Boiler-condenser with superposed stages
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing 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
    • 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
    • F25J2250/42—One fluid 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
    • F25J2250/30—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
    • 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
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"

Definitions

  • the invention is based, relative to nitrogen under high pressure with the task to gain little effort.
  • the pressure increase in the nitrogen product from the low pressure column is therefore at least partially carried out in the liquid state.
  • the pressure increase in the Liquid can be carried out by any known measure for example by means of a pump, using a hydrostatic potential and / or the pressure build-up evaporation on a tank. It means one less expenditure on equipment than a gas compressor. It will also be a indirect heat exchange is required in which the liquid is pressurized Low pressure column nitrogen is evaporated. Nevertheless, there is an overall economically particularly favorable process.
  • the inventive method Compared to a removal of the pressure nitrogen product directly from the pressure column the inventive method also has the advantage of higher product purity on.
  • the pressure column reduced concentration of volatile components such as Helium, neon and / or hydrogen can be achieved.
  • the entire nitrogen product of the low pressure column liquid from the Low pressure column or their top condenser removed.
  • the operating pressures of the double column can be in the method according to the invention for example 6 to 20, preferably 7 to 16 bar in the pressure column and for example 3 to 8, preferably 3 to 6 bar in the low pressure column.
  • the top condenser of the low pressure column is, for example, with a liquid from the low pressure column such as the low pressure column sump liquid as Refrigerant operated. Return for the pressure column is usually through a Condenser-evaporator is generated over the top of the pressure column and the sump the low-pressure column are in heat-exchanging connection.
  • a gas from the pressure column preferably a nitrogenous one Fraction from an upper or middle area of the pressure column, as a heat transfer medium be used. It can be the top fraction of the pressure column or act a gas that is withdrawn at an intermediate point of the pressure column. This The intermediate point is below the number of theoretical floors Pressure column head, which up to 5/6, preferably 1/3 to 5/6 of the total number theoretical plates within the pressure column. That with the indirect Heat exchange in the product evaporator is condensate at least partially, preferably completely back into the pressure column returned and used there as a return.
  • the liquid nitrogen is used for indirect heat exchange only partially evaporated in the product evaporator and the liquid portion of the Nitrogen is returned to the low pressure column.
  • the product evaporator will preferably operated as a falling film evaporator. That kind of evaporation enables a particularly low temperature difference and thus one correspondingly high evaporation pressure, which is also pure when used Nitrogen from the top of the pressure column as a heat transfer medium only slightly (about 0.3 to 0.8 bar) is below the pressure column pressure.
  • the low pressure column serves as Flash gas separator when recycling the remaining liquid portion.
  • the bottom liquid of the low pressure column is used as a refrigerant Condensation of the gaseous nitrogen from the low pressure column in the Top condenser of the low pressure column used.
  • the method according to the invention is also relatively pure or pure oxygen (purity higher than 40 mol%, in particular higher than 80 mol% or higher than 90 mol%, preferably between 99.5 and 99.999 mol%) it is particularly beneficial if a liquid fraction, its oxygen content between that of the oxygen-containing liquid fraction from the pressure column and that of the bottom liquid of the low pressure column for condensation of the gaseous nitrogen from the low pressure column in the top condenser is used.
  • compressed and cleaned air 1 is combined in one Main heat exchanger 2 cooled and a pressure column 4 under a pressure of 14 bar supplied (3).
  • the rectification system also has a low pressure column 5 on, which is operated at a pressure of 5 bar and with the pressure column via a common condenser-evaporator (main condenser) 6 in heat-exchanging Connection is established.
  • Part 8 of the nitrogen removed at the top of the pressure column is liquefied in the main condenser 6 and via lines 9 and 10 as a return placed on the pressure column.
  • Bottom liquid 11 of the pressure column is after Hypothermia 15 as an oxygen-rich liquid fraction in the low pressure column 5 throttled (12).
  • FIG. 1 Another part 20 of the liquid nitrogen 19 from the top condenser 17 is either as shown in Figure 1 taken from the low pressure column or directly branched off from line 19.
  • This liquid nitrogen 20 is according to the invention in liquid state brought to pressure (in the example 14 bar) (pump 21) and over Line 22 through the subcooler 15 to a product evaporator 23.
  • the method of FIG. 2 differs from this mainly in that Use of another heat transfer medium in the product evaporator.
  • Top gas 7 of the pressure column 4 becomes a gas 35 'from an intermediate point here Pressure column passed into the liquefaction chamber of the product evaporator 23.
  • the gas 35 'still has an oxygen content of about 2 mol% and thus a higher one Condensation temperature as the pure nitrogen from the top of the pressure column 6 (10 ppb Oxygen).
  • the pressure on the evaporation side of the Product evaporator 23 (14 bar instead of 13.4 bar in the case of Figure 1).
  • indirect heat exchange condensate 36 ' is on one of its Returned composition corresponding point in the pressure column 4, especially in the place of the extraction (line 35 'or something above).
  • the double column is operated at a sufficiently high pressure (For example 8 to 15 bar), the entire feed air 3 ′ can be fed into the pressure column 4 be directed.
  • a sufficiently high pressure For example 8 to 15 bar
  • the operating pressures in pressure column 4 and low pressure column 5 are 15 bar in this example or 5 bar.
  • Process cold is here due to work relaxation of steam 31, 31 'from the evaporation side of the overhead condenser 17 Low pressure column 5 generated.
  • the relaxation machine 33 ' can also as in Figure 1 coupled to a compressor 26 for nitrogen product.
  • a method according to FIG. 5 is used if in addition to pressure nitrogen pure oxygen (in the example: 99.5 mol%) is to be obtained.
  • the refrigerant 13 'for the Top condenser 17 of the low pressure column 5 not from the sump, but from one Intermediate point is withdrawn, preferably from a liquid reservoir within the low pressure column 5, which is immediately below the feed of the oxygen-containing liquid fraction 11 from the pressure column 4 is arranged.
  • the oxygen product can be liquid (42) and / or gaseous (43) are withdrawn.
  • part 44 of the Liquid 42 are led into the top condenser 17. If the oxygen is below Pressure is required, oxygen 42 can be used according to the known method of Internal compression in the liquid state brought to pressure and then are evaporated, for example against part of the feed air.
  • the method of FIG. 6 differs from that in several points Figure 1. For example, it shows a slightly different hypothermia Process streams represented by only one heat exchanger block 15 for this purpose is.
  • a part of the bottom product 13 of the low pressure column 5 can be used as a liquid product (LOX) can be won.
  • the nitrogen 9 liquefied in the main condenser 6 can partly subcooled 160 (15) and throttled into the low-pressure column 5 (161) become.
  • the bottom liquid 11 of the pressure column can partially (162) in the Evaporation chamber of the top condenser 17 of the low pressure column passed (163) become.
  • the pressure nitrogen product 24 is made from the Product evaporator 23 not post-compressed, but under the evaporation pressure deducted (29).
  • the turbine exhaust gas 151 is warmed up again in the heat exchanger 2 and as residual gas 152 discharged or for the regeneration of a device for the Purification of the feed air used.
  • the one in the relaxation machine 133 Mechanical energy obtained can be given to a generator or used for Compaction of a process fraction can be used, preferably by direct mechanical coupling of the relaxation machine 133 with a not shown Compressor.
  • the main difference compared to Figure 1 lies in the product evaporator 23.
  • This is operated on the liquefaction side with steam from the low pressure column. This is done on the Liquefaction side of the product evaporator 23 a part of the above the sump Low pressure column condensed gas. The resulting liquid 136 flows back into the low pressure column.
  • the product evaporator 23 is in the Example arranged within the low pressure column. It can be used as a falling film evaporator be formed in which only partial evaporation takes place. Liquid remaining nitrogen can be returned to the low pressure column 5.
  • the product evaporator 23 is similar to that in FIG 6 built into the double column. He sits here in the upper area of the pressure column 4. Die The liquefaction side of the product evaporator 23 is similar to that in FIGS. 1 to 5 with a portion 35 of the gaseous nitrogen 7 from the top of the pressure column 4 acted upon.
  • FIG 8 there are subcoolers and product evaporators in a heat exchanger block 223 integrated.
  • a portion 246 of the bottom liquid 11 of the Pressure column for additional head cooling of the pressure column (via valve 248) or Low pressure column (via valve 247) can be used.
  • Process cold becomes like in figure 1 obtained by work-relaxation 33 of a part 32 of the feed air.
  • the product evaporator 323 from FIG. 9 is a countercurrent heat exchanger, preferably realized as an aluminum plate heat exchanger. in the However, it differs from FIG. 8 from the subcooling heat exchanger 15 Cut.
  • the liquid nitrogen 20, which is the Pump 21 is supplied instead of removal at the top of the low pressure column at least one theoretical or practical floor below the head of the Low pressure column are withdrawn.
  • the liquid nitrogen 20 which is the Pump 21 is supplied instead of removal at the top of the low pressure column at least one theoretical or practical floor below the head of the Low pressure column are withdrawn.
  • these floors preferably carried out as conventional rectification trays.
  • FIGS. 6 to 9 a further modification can be made to the methods of FIGS. 6 to 9 be made in which a produced in the pressure column 4 Liquid nitrogen stream (160 in Figures 6 and 7) as a return to the top of the Low pressure column 5 is abandoned (via valve 161).
  • This stream can also be removed from an intermediate point, the one to ten, preferably three up to five theoretical or practical floors below the head of the pressure column 4 is arranged.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (10)

  1. Procédé pour l'extraction d'azote comprimé par fractionnement d'air à basse température dans un système de rectification, qui présente une colonne de pression (4) et une colonne de basse pression (5), dans lequel, lors du procédé, l'air d'alimentation (1, 3; 1, 3') est introduit dans la colonne de pression (4), une fraction liquide oxygénée (11) est prélevée de la colonne de pression (4) et introduite dans la colonne de basse pression (5), de l'azote gazeux (18) de la colonne de basse pression (5) est au moins partiellement condensé dans un condenseur de tête (17) par échange indirect de chaleur avec un liquide s'évaporant (13; 13', 44) et de l'azote de la colonne de basse pression est extrait sous forme de produit d'azote gazeux comprimé (24, 24', 25, 29) à une pression qui est plus élevée que la pression de fonctionnement de la colonne de basse pression (5), au moins une partie de l'azote liquide obtenu par l'échange indirect de chaleur dans le condenseur de tête (17) ou de l'azote liquide (20) soutiré de la colonne de basse pression étant amené à l'état liquide à une pression (21) qui dépasse la pression de la colonne de basse pression (5), étant évaporé dans un évaporateur de produit (23) par échange indirect de chaleur avec un agent caloporteur (35; 35') et étant extrait sous forme de produit d'azote comprimé (24, 24', 25, 29).
  2. Procédé suivant la revendication 1, dans lequel on utilise comme agent caloporteur un gaz de la colonne de pression (4), de préférence une fraction contenant de l'azote (35; 35') d'une zone supérieure ou centrale de la colonne de pression (4), et/ou un gaz de la colonne de basse pression (5), de préférence une fraction contenant de l'oxygène d'une zone inférieure ou centrale de la colonne de basse pression (5).
  3. Procédé suivant la revendication 1 ou 2, dans lequel l'azote liquide (22) n'est que partiellement évaporé lors de l'échange indirect de chaleur dans l'évaporateur de produit (23) et la proportion restée liquide (45) de l'azote est ramenée dans la colonne de basse pression (5).
  4. Procédé suivant l'une des revendications 1 à 3, dans lequel une fraction de processus (32, 31', 38) est détendue de manière à fournir un travail (33, 33', 33") et l'énergie obtenue lors de la détente fournissant un travail (33, 33', 33") est utilisée pour recomprimer (26) le produit d'azote comprimé (24) en aval de l'évaporateur de produit (23).
  5. Procédé suivant l'une des revendications 1 à 4, dans lequel une fraction liquide (13'), dont la teneur en oxygène se situe entre celle de la fraction liquide oxygénée (11) de la colonne de pression (4) et celle du liquide de bas de colonne (42) de la colonne de basse pression (5), est utilisée pour la condensation de l'azote gazeux (18) en provenance de la colonne de basse pression (5) dans le condenseur de tête (17).
  6. Dispositif pour l'extraction d'azote comprimé par fractionnement d'air à basse température dans un système de rectification qui présente une colonne de pression (4) et une colonne de basse pression (5), avec une conduite d'air d'alimentation (1, 3; 1, 3') qui mène à la colonne de pression (4), avec une conduite (11) pour une fraction liquide oxygénée qui mène de la colonne de pression (4) à la colonne de basse pression (5), avec un condenseur de tête (17) dont le côté liquéfaction est raccordé (18) à une zone supérieure de la colonne de basse pression (5), et avec une conduite de produit comprimé (24, 24', 25, 29) pour le prélèvement d'azote de la colonne de basse pression (5) en tant que produit comprimé gazeux, le côté liquéfaction du condenseur de tête (17) de la colonne de basse pression (5) ou la zone supérieure de la colonne de basse pression (5) étant en liaison d'écoulement par l'intermédiaire d'une conduite d'azote liquide (20, 22) avec des moyens (21) pour augmenter la pression d'un liquide et avec un évaporateur de produit (23) pour évaporer par échange indirect de chaleur, l'évaporateur de produit (23) étant raccordé quant à lui à la conduite de produit comprimé (24, 24', 25, 29).
  7. Dispositif suivant la revendication 6, dans lequel le côté liquéfaction de l'évaporateur de produit (23) est raccordé à une zone supérieure ou centrale de la colonne de pression et/ou à une zone inférieure ou centrale de la colonne de basse pression (7, 8; 35').
  8. Dispositif suivant la revendication 6 ou 7, avec une conduite de retour de liquide (45), qui mène de l'évaporateur de produit (23) à la colonne de basse pression (5).
  9. Dispositif suivant l'une des revendications 6 à 8, avec une machine de détente (33, 33', 33") pour la détente fournissant un travail, d'une fraction de processus (32, 31', 38), qui est accouplée à un compresseur (26) pour recomprimer le produit d'azote comprimé (24) en aval de l'évaporateur de produit (23).
  10. Dispositif suivant l'une des revendications 6 à 9, avec une conduite de liquide (13) pour un agent réfrigérant, qui, d'un côté, est raccordée à une zone centrale de la colonne de basse pression (5) ou à une zone inférieure de la colonne de pression et, de l'autre côté, au côté évaporation du condenseur de tête (17) de la colonne de basse pression (5).
EP97948844A 1996-10-30 1997-10-30 Procede et dispositif de production d'azote comprime Expired - Lifetime EP0948730B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP97948844A EP0948730B1 (fr) 1996-10-30 1997-10-30 Procede et dispositif de production d'azote comprime

Applications Claiming Priority (10)

Application Number Priority Date Filing Date Title
DE19643916 1996-10-30
DE19643916 1996-10-30
EP97102533 1997-02-17
EP97102533 1997-02-17
DE19717124 1997-04-23
DE19717124 1997-04-23
DE19735154 1997-08-13
DE19735154A DE19735154A1 (de) 1996-10-30 1997-08-13 Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff
EP97948844A EP0948730B1 (fr) 1996-10-30 1997-10-30 Procede et dispositif de production d'azote comprime
PCT/EP1997/006010 WO1998019122A1 (fr) 1996-10-30 1997-10-30 Procede et dispositif de production d'azote comprime

Publications (2)

Publication Number Publication Date
EP0948730A1 EP0948730A1 (fr) 1999-10-13
EP0948730B1 true EP0948730B1 (fr) 2000-08-30

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EP97948844A Expired - Lifetime EP0948730B1 (fr) 1996-10-30 1997-10-30 Procede et dispositif de production d'azote comprime

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US (1) US6196023B1 (fr)
EP (1) EP0948730B1 (fr)
JP (1) JP2001509246A (fr)
KR (1) KR20000052974A (fr)
CN (1) CN1235666A (fr)
CA (1) CA2277838A1 (fr)
DE (2) DE19735154A1 (fr)
DK (1) DK0948730T3 (fr)
ES (1) ES2150291T3 (fr)
PT (1) PT948730E (fr)
WO (1) WO1998019122A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19819263C2 (de) * 1998-04-30 2003-08-21 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff
EP0955509B1 (fr) 1998-04-30 2004-12-22 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté
DE10018200A1 (de) * 2000-04-12 2001-10-18 Linde Gas Ag Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft
DE10058332A1 (de) * 2000-11-24 2002-05-29 Linde Ag Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff
US6397631B1 (en) 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
EP1300640A1 (fr) 2001-10-04 2003-04-09 Linde Aktiengesellschaft Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air
US6499312B1 (en) 2001-12-04 2002-12-31 Praxair Technology, Inc. Cryogenic rectification system for producing high purity nitrogen
US6494060B1 (en) 2001-12-04 2002-12-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity nitrogen using high pressure turboexpansion
GB0422635D0 (en) * 2004-10-12 2004-11-10 Air Prod & Chem Process for the cryogenic distillation of air
CN102003865A (zh) * 2010-11-09 2011-04-06 苏州制氧机有限责任公司 一种制氮装置及其制氮方法
US8991209B2 (en) * 2010-12-13 2015-03-31 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for producing high-pressure nitrogen
EP2662654A1 (fr) * 2012-05-07 2013-11-13 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Processus et appareil pour la séparation de lýair par distillation cryogénique
MX2016001221A (es) * 2013-08-02 2016-05-24 Linde Ag Metodo y dispositivo para producir nitrogeno comprimido.
CN103776239B (zh) * 2014-01-13 2016-03-30 浙江海天气体有限公司 多功能制氮装置
US9366476B2 (en) 2014-01-29 2016-06-14 Praxair Technology, Inc. Condenser-reboiler system and method with perforated vent tubes
US9488408B2 (en) 2014-01-29 2016-11-08 Praxair Technology, Inc. Condenser-reboiler system and method
EP3059536A1 (fr) * 2015-02-19 2016-08-24 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'un produit d'azote pressurisé
EP3290843A3 (fr) * 2016-07-12 2018-06-13 Linde Aktiengesellschaft Procédé et dispositif destiné à fabriquer de l'azote pressurisé et liquide par décomposition à basse température de l'air
WO2021242309A1 (fr) * 2020-05-26 2021-12-02 Praxair Technology, Inc. Améliorations apportées à une unité de séparation d'air cryogénique à double colonne produisant de l'azote
WO2021242307A1 (fr) * 2020-05-28 2021-12-02 Praxair Technology, Inc. Améliorations apportées à une unité de séparation d'air cryogénique à double colonne produisant de l'azote

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FR2578532B1 (fr) * 1985-03-11 1990-05-04 Air Liquide Procede et installation de production d'azote
DE3528374A1 (de) 1985-08-07 1987-02-12 Linde Ag Verfahren und vorrichtung zur erzeugung von stickstoff mit ueberatmosphaerischem druck
US5098457A (en) 1991-01-22 1992-03-24 Union Carbide Industrial Gases Technology Corporation Method and apparatus for producing elevated pressure nitrogen
US5303556A (en) * 1993-01-21 1994-04-19 Praxair Technology, Inc. Single column cryogenic rectification system for producing nitrogen gas at elevated pressure and high purity
US5402647A (en) * 1994-03-25 1995-04-04 Praxair Technology, Inc. Cryogenic rectification system for producing elevated pressure nitrogen

Also Published As

Publication number Publication date
CN1235666A (zh) 1999-11-17
KR20000052974A (ko) 2000-08-25
US6196023B1 (en) 2001-03-06
DK0948730T3 (da) 2000-10-16
PT948730E (pt) 2000-12-29
DE19735154A1 (de) 1998-05-07
ES2150291T3 (es) 2000-11-16
WO1998019122A1 (fr) 1998-05-07
DE59702301D1 (de) 2000-10-05
JP2001509246A (ja) 2001-07-10
EP0948730A1 (fr) 1999-10-13
CA2277838A1 (fr) 1998-05-07

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