DE2044363C2 - Process for the production of oxygen and nitrogen - Google Patents

Process for the production of oxygen and nitrogen

Info

Publication number
DE2044363C2
DE2044363C2 DE2044363A DE2044363A DE2044363C2 DE 2044363 C2 DE2044363 C2 DE 2044363C2 DE 2044363 A DE2044363 A DE 2044363A DE 2044363 A DE2044363 A DE 2044363A DE 2044363 C2 DE2044363 C2 DE 2044363C2
Authority
DE
Germany
Prior art keywords
nitrogen
heat exchanger
main heat
compressor
gaseous
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.)
Expired
Application number
DE2044363A
Other languages
German (de)
Other versions
DE2044363A1 (en
Inventor
Jean-Pierre Paris Anselmini
Guy Sucy-en-Brie Perrotin
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of DE2044363A1 publication Critical patent/DE2044363A1/en
Application granted granted Critical
Publication of DE2044363C2 publication Critical patent/DE2044363C2/en
Expired legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—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
    • F25J3/04024—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 purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—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
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
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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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
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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
    • 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
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

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

Description

Die Erfindung betrifft ein Verfahren zur Erzeugung von flüssigem und/oder gasförmigem Sauerstoff sowie flüssigem und/oder gasförmigem Stickstoff durch Zerlegung von Luft in einer Destillationskolonne, mit einem Hauptwärmetauscher zur Abkühlung der zu zerlegenden Luft durch die abziehenden gasförmigen Produktströme, wobei aus dem abziehenden Stickstoffstrom ein noch nicht vollständig erwärmter Teil aus einem Zwischenbereich des Hauptwärmetauschers entnommen und einem Verdichter mit nachgeschaltetem Kühler, der durch ein externes Kühlmittel gekühlt wird, zugeführt und verflüssigt wird, wobei ein Teil des verflüssigten Stickstoffs als Rücklauf in die Kolonne zugeführt wird.The invention relates to a method for generating liquid and / or gaseous oxygen as well liquid and / or gaseous nitrogen by separating air in a distillation column with a main heat exchanger to cool the air to be separated by the evacuating gaseous air Product streams, with a not yet fully heated part of the nitrogen stream being withdrawn taken from an intermediate area of the main heat exchanger and a compressor with a downstream Cooler, which is cooled by an external coolant, is supplied and liquefied, with part of the Liquefied nitrogen is fed as reflux into the column.

Es ist schon bekannt, reinen Sauerstoff und einen erheblichen Anteil reinen Stickstoffs in flüssiger oder gasförmiger Form unter Druck gleichzeitig zu gewinnen. So ist es möglich, in zwei Stufen zu arbeiten, indem man Luft auf einen Druck von beispielsweise 6 bar komprimiert, die Luft reinigt, abkühlt, kondensiert und in einer Doppelkolonne destilliert, in deren Niederdruckteil etwas mehr als Luftdruck herrscht. Die so erhaltenen Gase sind jedoch zum größten Teil Produkte von niedrigem Druck. Außerdem ist in allen Fällen die Menge des unmittelbar unter Druck oder in flüssiger Form erzeugten Gases sehr gering. Die Gase von niedrigem Druck müssen tatsächlich auf einem hohen Druck wieder verdichtet werden, und diejenigen, die man in flüssiger Form erhalten will, müssen in einem Verflüssigungsgerät behandelt werden.It is already known to use pure oxygen and a significant proportion of pure nitrogen in liquid or to win gaseous form under pressure at the same time. So it is possible to work in two stages by air is compressed to a pressure of, for example, 6 bar, the air is cleaned, cooled, and condensed distilled in a double column, in the low pressure part of which there is a little more than air pressure. The so however, the gases obtained are for the most part products of low pressure. In addition, in all cases the The amount of gas generated directly under pressure or in liquid form is very small. The gases from low pressure actually need to be recompressed to a high pressure, and those that do one wants to get in liquid form, must be treated in a liquefaction device.

Weiterhin ist aus der deutschen Auslegeschrift 12 32174 ein Verfahren der eingangs genannten Art bekannt, bei welchem Luft in einer Destillationskolonne zerlegt wird. Das bekannte Verfahren ist nicht hinreichend flexibel und kann insbesondere nicht ohne Kälteverlust große Veränderungen der Produktströme vorsehen. Dies gelingt auch dann nicht, wenn der Hauptwärmeaustauscher in zwei Einheiten aufgeteilt wird und die in Abstromrichtung des Prodüktstromes des gasförmigen Stickstoffs liegende zweite Hälfte durch einen externen Kühlmittelhilfskreis zur Erreichung der gewünschten Temperatur gesteuert wird. Ein Eingriff in eine Anlage von außen ist zwar jederzeitFurthermore, from the German Auslegeschrift 12 32174 a method of the type mentioned above is known in which air is broken down in a distillation column. The known procedure is not sufficiently flexible and, in particular, cannot make major changes to the product flows without loss of cold provide. This does not work even if the main heat exchanger is split into two units and the second half lying in the downstream direction of the product stream of the gaseous nitrogen controlled by an external auxiliary coolant circuit to achieve the desired temperature. A External intervention in a system is possible at any time

ίο möglich, verbraucht aber zusätzliche Energie, auf die man möglichst nicht zurückgeifen wilL Außerdem ist die bekannte Anlage dadurch komplizierter herzustellen und zu betreiben.ίο possible, but uses additional energy on the you don't want to go back if possible known system thereby more complicated to manufacture and operate.

Der Erfindung liegt demgegenüber die Aufgabe zugrunde, das bekannte Verfahren dahingehend zu verbessern, daß der Betrieb, insbesondere bei Veränderung eines oder mehrerer Produktströme, auch ohne auftretende Kälteverluste ermöglicht wird.
Diese Aufgabe wird erfindungsgemäß dadurch gelöst, daß zur Anpassung des Wärmetausches im Hauptwärmetauscher an veränderte Produktströme bei Erzeugung mindestens eines Teiles des gasförmigen Sauerstoffs bei einem Druck, der höher ist als in der Kolonne, zumindest ein Teilstrom des abziehenden Stickstoffes nach Erwärmung auf Umgebungstemperatur dem aus dem Zwischenbereich des Hauptwärmetauschers entnommenen Stickstoffstrom bei seiner Entnahmetemperatur zugemischt wird und daß dieses Geniisch dem bei tiefer Temperatur arbeitenden Verdichter steuerbar zugeführt wird.In contrast, the invention is based on the object of improving the known method in such a way that operation, in particular when one or more product flows are changed, is also made possible without the occurrence of cold losses.
This object is achieved according to the invention in that in order to adapt the heat exchange in the main heat exchanger to changed product flows when generating at least part of the gaseous oxygen at a pressure that is higher than in the column, at least a partial flow of the nitrogen to be withdrawn after heating to ambient temperature is removed from the Nitrogen stream withdrawn between the main heat exchanger is admixed at its withdrawal temperature and that this geniisch is controllably fed to the compressor operating at low temperature.

Durch diese Maßnahme wird nicht nur, wie im bekannten Fall, lediglich die Temperatur im Hauptwärmetauscher oder am eingangsseitigen Ende des Verdichters gesteuert, sondern es wird durch die erfindungsgemäßen Maßnahmen die gesamte Wärmebilanz verbessert. Durch das steuerbare Zuführen einer mehr oder weniger großen Menge des auf Umgebungstemperatur erwärmten, abgezogenen Teilstromes an Stickstoff zu dem aus dem Zwischenbereich entnommenen Stickstcffstrom, die beide nach der Vereinigung dem Verdichter zugeführt werden, kann stets dafür gesorgt werden, daß am warmen Ende des Hauptwärmetauschers etwa Raumtemperatur bzw. Umgebungstemperatur vorherrscht, und zwar unbeachtlich der Tatsache, ob nun große Mengen flüssigen Stickstoffs und/oder Sauerstoffs und verschiedenste Mengen gasförmiger Produktströme Stickstoff und Sauerstoff abgezogen werden. Durch das steuerbare Zuführen des erwärmten Stickstoffteilstromes zu dem bereits im Zwischenbereich des Hauptwärmetauschers entnommenen Stickstoffstrom, der sich noch nicht ganz auf Umgebungstemperatur erwärmt hat, kann man etwaige Energieverluste in vorteilhafter Weise vermeiden, die nämlich z. B. auftreten können, wenn einer der Produktströme, z. B. der abgezogene Stickstoffteilstrom, eine weit unter der Umgebungstemperatur liegende Temperatur hat. Erfindungsgemäß kann diese Kälteenergie vollständig wieder in der Anlage zur Durchführung des Verfahrens gemäß der Erfindung verwendet werden.This measure not only, as in the known case, only the temperature in the main heat exchanger or at the input end of the compressor, but it is controlled by the Measures according to the invention improves the overall heat balance. The controllable feeding of a a more or less large amount of the withdrawn partial flow heated to ambient temperature Nitrogen to the nitrogen stream withdrawn from the intermediate area, both after the combination are fed to the compressor, it can always be ensured that at the warm end of the main heat exchanger about room temperature or ambient temperature prevails, regardless of the Fact, whether large amounts of liquid nitrogen and / or oxygen and various amounts gaseous product streams nitrogen and oxygen are withdrawn. The controllable feeding of the heated nitrogen partial flow to that already taken in the intermediate area of the main heat exchanger A stream of nitrogen that has not yet fully warmed to ambient temperature can be used Avoid energy losses in an advantageous manner, namely z. B. can occur if one of the Product streams, e.g. B. the withdrawn nitrogen partial flow, one well below the ambient temperature has a lying temperature. According to the invention, this cold energy can be completely returned to the system Implementation of the method according to the invention can be used.

Dabei ist es bevorzugt, daß gasförmiger Sauerstoff bei einem Druck erzeugt wird, der höher ist als der Druck in der Kolonne, wobei dieser Druck durch Komprimieren eines Teils des in der Destillationskolonne erzeugten flüssigen Sauerstoffs durch Pumpen erreicht wird. Dabei wird nicht ausgeschlossen, daß gegebenenfalls gleichzeitig von diesem Produktstrom flüssigen Sauerstoffes größere Mengen direkt bzw. nachIt is preferred that gaseous oxygen is generated at a pressure higher than that Pressure in the column, this pressure being obtained by compressing part of that in the distillation column generated liquid oxygen is achieved by pumping. It is not excluded that possibly at the same time larger amounts of this product stream of liquid oxygen directly or after

Entspannen und Unterkühlung zum Verbrauch abgeführt werden.Relaxation and hypothermia are dissipated for consumption.

Aus der DE-AS 11 99 293 ist zwar auch ein Verfahren zur Erzeugung von gasförmigem Sauerstoff und Stickstoff durch Zerlegung von Luft bekannt. Auch dort wird aus dem abzuziehenden Stickstoffsirom ein Teil entnommen und einem Verdichter zugeführt, um nach Verflüssigung als Rücklauf einer Destillationskolonne wieder zugeführt zu werden. Hier wird aber der Kreislauf-Stickstoff nicht nur unmittelbar nach Verlassen der Destillationskolonne abgezweigt, sondern er wird durch einen Wärmetauscher geführt, wo er sich offensichtlich auf Umgebungstemperatur erwärmt Da auch der andere Teilstrom des Stickstoffs auf Umgebungstemperatur erwärmt ist, wird dem Verdichter ein Gemisch aus auf Umgebungstemperatur befindlichen Stickstoffströmen zugeführt. Hierdurch könnte eine Steuerung der Zufuhr (bei entsprechendem öffnen des Abzugsventils) nur im Hinblick auf die Strömungsmenge des dem Verdichter zugeführten Stickstoffs, nicht aber eine Steuerung oder Änderung im Hinblick auf die Temperatur erreicht werden. Gerade dadurch kann der Betrieb aber nicht ohne Kälteverluste bei Veränderung der Produktslröme aufrecht erhalten werden.From DE-AS 11 99 293 there is also a method for generating gaseous oxygen and Nitrogen known from the decomposition of air. There, too, a part becomes part of the nitrogen syrup to be withdrawn taken and fed to a compressor to after liquefaction as a reflux of a distillation column to be fed back. Here, however, the cycle nitrogen is not only used immediately after leaving it the distillation column is branched off, but it is passed through a heat exchanger, where it is Obviously warmed up to ambient temperature Since the other partial flow of nitrogen has also been heated to ambient temperature is heated, the compressor is a mixture of at ambient temperature Nitrogen flows supplied. This could control the supply (when the Vent valve) only with regard to the flow rate of the nitrogen supplied to the compressor, not but control or change in temperature can be achieved. Precisely because of this, the However, operation cannot be maintained without loss of cold when the product flow changes.

Schließlich ist zwar auch noch aus der US-PS 29 82 108 ein Verfahren zur Lufttrennung bekannt. Dort wird kalter, gasförmiger, reiner Stickstoff in der Leitung zum Wärmetauscher geführt, wo er auf etwa —173° erwärmt wird. Dann fließt der Stickstoff durch Leitung zu einem Wärmeaustauscher, wo er nach Durchlaufen des kalten Endes ganz oder teilweise durch das Ventil bei — 1300C herausgenommen und durch Stickstoff unter Druck danach auf etwa +24°C erwärmt wird. Der restliche Stickstoffstrom durchläuft in der Leitung den Wärmetauscher vollständig, so daß er nach Austritt aus demselben ebenfalls auf Umgebungstemperatur erwärmt ist. Diese beiden erwärmten Ströme werden dann erst dem Verdichter zugeführt. Auch hier wird nicht ein warmer Stickstoffstrom mit einem kalten, nämlich vor seiner vollständigen Erwärmung, vereinigt, und der Verdichter arbeitet auch nicht bei tiefer Temperatur. Außerdem wird bei dieser bekannten Anlage auch nicht eine steuerbare Zuführung des Stickstoffstroms gewährleistet, denn vor Eintritt in den Verdichter wird die Gesamtheit der durch die Leitungen kommenden Stickstoffströme vereinigt.Finally, a method for air separation is also known from US Pat. No. 2,982,108. There, cold, gaseous, pure nitrogen is fed in the line to the heat exchanger, where it is heated to around -173 °. Then, the nitrogen flows through conduit to a heat exchanger where it completely or partly after passage through the cold end through the valve at - is taken out 130 0 C and under pressure with nitrogen then to about + 24 ° C heated. The remainder of the nitrogen stream runs completely through the heat exchanger in the line, so that it is likewise warmed to ambient temperature after exiting the same. Only then are these two heated streams fed to the compressor. Here, too, a warm nitrogen stream is not combined with a cold one, namely before it is completely heated, and the compressor does not work at a low temperature either. In addition, a controllable supply of the nitrogen flow is not guaranteed in this known system, because all of the nitrogen flows coming through the lines are combined before entering the compressor.

Durch das Abziehen des Stickstoffteilstromes einerseits nach Erwärmung auf Umgebungstemperatur und andererseits aus dem Zwischenbereich des Hauptwärmetauschers vor dieser Erwärmung und nachfolgende Vereinigung wird die Anlage zur Durchführung des erfindungsgemäßen Verfahrens in vorteilhafter Weise sehr flexibel, so daß man z. B. entweder nur den gasförmigen Sauerstoff mit dem höheren Druck als in der Kolonne oder gleichzeitig oder auch nut gasförmigen Sauerstoff mit einem niederen Druck erzeugt, wie er z. B. im Niederdruckteil einer doppelten Destillationskolonne oder bei einer anderen Ausführungsform in einer einheitlichen Destillationskolonne herrscht.By withdrawing the partial flow of nitrogen on the one hand after heating to ambient temperature and on the other hand from the intermediate area of the main heat exchanger before this heating and subsequent Combination is the system for carrying out the method according to the invention in an advantageous manner very flexible, so that you can z. B. either only the gaseous oxygen with the higher pressure than in the column or at the same time or also generated only gaseous oxygen at a low pressure, such as he z. B. in the low pressure part of a double distillation column or in another embodiment prevails in a uniform distillation column.

Durch die Maßnahmen der Erfindung kann man also aus der Vielzahl der durch die Anlage angebotenen Produktströme einige auswählen, auf einen anderen Betrieb durch große Veränderungen der Produktströme umschalten, und dennoch treten keine Kälteverluste auf.Through the measures of the invention, one can choose from the multitude of those offered by the system Select some product flows to operate another by making large changes in the product flows switch over, and yet there are no cold losses.

Dies alles erreicht man durch die erfindungsgemäßen Maßnahmen, wobei mit Vorteil ferner die Gasverdichtungen auf ein Mindestmaß beschränkt werden, diese Verdichtungen möglichst häufig bei niederer Temperatur erfolgen, die Anzahl der eingesetzten gesamten Maschinenleistung vermindert wird und die Bemessung der Austauscher in erheblichem Maß begrenzt ist, weil nämlich die Gase unter Druck oder im Zustand der Verflüssigung-Verdampfung im Hauptwärmeaustauscher behandelt werden.All of this is achieved by the measures according to the invention, the gas compressions also being advantageous be limited to a minimum, these densities as often as possible at low temperature take place, the number of total machine power used is reduced and the dimensioning the exchanger is limited to a considerable extent because the gases are under pressure or in the state of Liquefaction-evaporation are treated in the main heat exchanger.

Mit den erfindungsgemäßen Maßnahmen geht auch eine erhebliche Vereinfachung der Anlage einher, denn diese benötigt nur wenige Kompressoren und eine einzige Turbine, und diese Maschinen Gestehen im allgemeinen aus Zentrifugen.The measures according to the invention are also accompanied by a considerable simplification of the system, because this requires only a few compressors and a single turbine, and these machines confess general from centrifuges.

Die Lehre der Erfindung läßt sich sowohl bei einer doppelten als auch bei einer einfachen Destillation anwenden, d.h. wenn die Destillation unter einem mittleren und einem niedrigen Druck einerseits bzw. in nur einer Stufe bei niedrigem Druck erfolgt; und es ist auch für die erfindungsgemäßen Maßnahmen und Vorteile unbeachtlich, ob der Kreislaufstickstoff in einem einstufigen oder einem zweistufigen Verdichter komprimiert wird.The teaching of the invention can be applied both to a double and to a single distillation apply, i.e. if the distillation is carried out under medium and low pressure on the one hand or in only takes place in one stage at low pressure; and it is also for the measures according to the invention and Advantages irrespective of whether the circulating nitrogen is used in a single-stage or a two-stage compressor is compressed.

Als Beispiele für den niedrigen Druck kann man Anlagen mit 5 bar verwenden, bei denen dann der erwähnte mittlere Druck 15 bar und der hohe Druck, d. h. z. B. der Druck in der Kolonne ist, 40 bar ist. Weitere Vorteile, Merkmale und Anwendungsmöglichkeiten der vorliegenden Erfindung ergeben sich aus der folgenden Beschreibung anhand der einzigen Zeichnung. Systems with 5 bar can be used as examples of the low pressure, in which the aforementioned mean pressure is 15 bar and the high pressure, ie, for example, the pressure in the column, is 40 bar. Further advantages, features and possible applications of the present invention emerge from the following description with reference to the single drawing.

Diese zeigt eine bevorzugte Ausführungsform einer Anlage zur Durchführung des Verfahrens mit einer einfachen Destillationskolonne und mit einer Verdichtung des Stickstoffstromes in zwei Stufen.This shows a preferred embodiment of a system for performing the method with a simple distillation column and with a compression of the nitrogen stream in two stages.

Mit der in der Zeichnung gezeigten Anlage kann man gleichzeitig Sauerstoffgas unter 5 und 40 bar. Stickstoffgas unter 5 und 15 bar, flüssigen Sauerstoff und flüssigen Stickstoff unter Ausnutzung des Kälteinhaltes eines in Verdampfung stehenden flüssigen Naturgases herstellen. Die zu behandelnde Luft tritt nach Filtrierung in die Anlage durch Leitung 1 ein. In dem Kompressor 2 wird sie z. B. auf 5 bar verdichtet und dann durch Absorption von Wasser und Kohlendioxid in der Reinigungsstufe 3 gereinigt. Anschließend wird sie durch die Leitungen 5 und 6 in den Hauptwärmetauscher 7 eingeführt, in dem sie gekühlt und teilweise verflüssigt wird. Durch die Leitung 8 tritt sie in die Destillationskolonne 14 ein, wo sie eine Rektifizierung erfährt.With the system shown in the drawing, oxygen gas under 5 and 40 bar can be simultaneously produced. Nitrogen gas under 5 and 15 bar, liquid oxygen and liquid nitrogen using the cold content of an in Produce evaporation of standing liquid natural gas. The air to be treated enters the after filtration System through line 1. In the compressor 2 it is z. B. compressed to 5 bar and then by absorption cleaned of water and carbon dioxide in cleaning stage 3. It is then passed through the lines 5 and 6 introduced into the main heat exchanger 7, in which it is cooled and partially liquefied. Through the Line 8 it enters the distillation column 14, where it undergoes rectification.

Vom unteren Teil dieser Destillationskolonne 14 zieht man ab:From the lower part of this distillation column 14 one subtracts:

Reines Sauerstoffgas unter 5 bar durch die Leitung 15, das dann in dem Hauptwärmetauscher 7 wieder erwärmt wird, und flüssigen Sauerstoff durch Leitung 16:Pure oxygen gas under 5 bar through line 15, which is then returned to the main heat exchanger 7 is heated, and liquid oxygen through line 16:

Ein Teil hiervon wird in den Pumpen 17 auf 40 bar verdichtet und dann durch die Leitung 18 im Hauptwärmetauscher 7 verdampft und wieder erwärmt; ein zweiter Teil wird zu dem Unterkühler 19 geleitet, wo er sich im Gegenstrom mit derjenigen Fraktion abkühlt, die in der auf diesen Austauscher folgenden Entspannungsmaschine verdampft ist.A part of this is compressed in the pumps 17 to 40 bar and then through the line 18 in the Main heat exchanger 7 evaporates and reheated; a second part is sent to the subcooler 19, where it cools in countercurrent with that fraction that is in the expansion machine following this exchanger has evaporated.

Die verdampfte Fraktion wird durch Leitung 20 in das Rohrbündel für unreinen Stickstoff zurückgebracht. Im mittleren Teil der Destillationskolonne 14 zieht man bei 51 unreinen Stickstoff ab, der in den Austauschern 13 und danach in einem Teil des Hauptwärmetauschers 7 wiedererwärmt wird, bevor er in der Turbine 21 entspannt und dann in Leitung 20 wiedererwärmt wird. Man erkennt, daß der unreine Stickstoff im Hauptwärmetauscher 7 also zweimal unter unterschiedlichenThe vaporized fraction is returned through line 20 to the impure nitrogen tube bundle. in the middle part of the distillation column 14 is drawn off at 51 impure nitrogen, which in the exchangers 13 and is thereafter reheated in a part of the main heat exchanger 7 before being in the turbine 21 is relaxed and then reheated in line 20. It can be seen that the impure nitrogen is in the main heat exchanger 7 so twice under different ones

Drücken durchgeleitet wird. An der Spitze der Destillationskolonne zieht man die reine Stickstofffraktion durch Leitung 22 ab. Sie wird dann in den Austauschern 13 erwärmt und verläßt diese unter einem Druck von 5 bar in Leitung 23. Ein Teil dieser Fraktion wird durch die Leitung 24 aus dem Zwischenbereich des Hauptwärmetauschers 7 vor ihrer vollständigen Erwärmung abgezogen und dann mit einem Teil 50 des am warmen Ende des Hauptwärmetauschers 7 erhaltenen Stickstoffes vermischt. Nach Vermischen mit kaltem Stickstoff von 5 bar aus der Leitung 25 (wie nachfolgend noch erläutert wird) wird diese Fraktion im Verdichter, z. B. dem Kompressor 26a und danach in der zweiten Stufe im Kompressor 266 verdichtet, die beide bei tiefen Temperaturen arbeiten. Durch die Leitung 27 wird Stickstoff von 15 bar nach der ersten Stufe des Kompressors 26a abgezogen und unmittelbar zur Verbrauchsstelle geschickt.Press is passed through. The pure nitrogen fraction is drawn at the top of the distillation column through line 22. It is then heated in the exchangers 13 and leaves them under one Pressure of 5 bar in line 23. A part of this fraction is through line 24 from the intermediate area of the Main heat exchanger 7 withdrawn before they are fully heated and then with a part 50 of the am warm end of the main heat exchanger 7 mixed nitrogen obtained. After mixing with cold Nitrogen at 5 bar from line 25 (as will be explained below), this fraction is in the compressor, z. B. the compressor 26a and then in the second stage in the compressor 266, both of which are compressed at low Working temperatures. Through line 27, nitrogen at 15 bar after the first stage of the Compressor 26a withdrawn and sent immediately to the point of consumption.

Der Rest des Stickstoffs wird in der zweiten Kompressorstufe 26b auf 40 bar verdichtet und dann im Austauscher 28 im Gegenstrom mit in Verdampfung stehenden Naturgas von 70 bar gekühlt und kondensiert. Dieser verflüssigte Stickstoff wird im Austauscher 29 im Gegenstrom mit derjenigen Fraktion aus Leitung 42 unterkühlt, die während der auf diesen Austauscher 29 folgenden Entspannung im Ventil 49 auf 5 bar verdampft worden ist. Die verdampfte Fraktion wird durch Leitung 43 in einen Zwischenbereich 44 im Hauptwärmetauscher 7 geführt, wo sie mit einem Teilstrom 41 vereinigt wird, der von der Leitung 27 mit gasförmigem Stickstoff unter 15 bar nach dem Abziehen durch Leitung 40 hinter der ersten Kompressorstufe 26a herausgeführt ist. Nach der Vereinigung dieser beiden Ströme aus den Leitungen 41 und 43 an der Stelle 44 wird dieser Stickstoffstrom dann nach Kühlung im Hauptwärmetauscher 7 im Sauerstoffbad im Sumpf 45 der Destillationskolonne 40 verflüssigt und im Austauscher 13 unterkühlt. Dann wird er nach seiner Verdampfung bei 46 dem Stickstoffteilstrom zwischen der ersten Entspannung im Ventil 49 und der zweiten Entspannung im Ventil 48 zugemischt.The remainder of the nitrogen is compressed to 40 bar in the second compressor stage 26b and then cooled and condensed in the exchanger 28 in countercurrent with natural gas which is evaporating at 70 bar. This liquefied nitrogen is subcooled in exchanger 29 in countercurrent with that fraction from line 42 which has been evaporated to 5 bar during the expansion in valve 49 that follows this exchanger 29. The vaporized fraction is passed through line 43 into an intermediate area 44 in the main heat exchanger 7, where it is combined with a partial stream 41 which is led out from line 27 with gaseous nitrogen under 15 bar after being drawn off through line 40 downstream of the first compressor stage 26a. After the combination of these two streams from lines 41 and 43 at point 44, this nitrogen stream is then liquefied after cooling in the main heat exchanger 7 in the oxygen bath in the sump 45 of the distillation column 40 and subcooled in exchanger 13. Then, after its evaporation at 46, it is added to the nitrogen partial flow between the first expansion in valve 49 and the second expansion in valve 48.

Der im ersten Entspannungsventil 49 entspannte Teilstrom wird also im Trenngefäß 30 verflüssigt und danach in einem weiteren Austauscher 29a im *> Gegenstrom mit einer weiteren Fraktion unterkühlt, die während der auf diesem Austauscher 29a folgenden Entspannung (und nach der Vereinigung mit dem anderen Stickstoffteilstrom an der Stelle 46) auf 5 bar verdampft worden ist. Die verdampfte Fraktion wirdThe partial flow expanded in the first expansion valve 49 is therefore liquefied in the separation vessel 30 and then subcooled in a further exchanger 29a in *> countercurrent with a further fraction, which during the expansion following this exchanger 29a (and after the combination with the other nitrogen partial flow at the Point 46) has been evaporated to 5 bar. The vaporized fraction will

ίο schließlich durch die Leitung 25 zur Saugseite des ersten Kompressors 26a zurückgeführt.ίο finally through line 25 to the suction side of the first Compressor 26a returned.

Der in dem letzten Trenngefäß 30a erhaltene flüssige Stickstoff von 5 bar dient zwei Zwecken: Ein Teil wird durch Leitung 31 zum Unterkühler 32 geleitet und dannThe liquid nitrogen of 5 bar obtained in the last separation vessel 30a serves two purposes: One part becomes passed through line 31 to subcooler 32 and then

ίο entspannt. Die so im Trenngefäß 33 aufgefangene flüssige Fraktion wird zur Verbrauchsstelle geschickt. Die während der Entspannung verdampfte Fraktion vereinigt sich mit dem verunreinigten Stickstoff durch Leitung 20. Der andere Teil des flüssigen Stickstoffes aus dem Trenngefäß 30a wird durch Leitung 34 als Rückfluß zur Destillationskolonne 14 geschickt.ίο relaxed. The so collected in the separation vessel 33 liquid fraction is sent to the point of consumption. The fraction evaporated during the relaxation combines with the contaminated nitrogen through line 20. The other part of the liquid nitrogen from the separation vessel 30a is sent through line 34 as reflux to the distillation column 14.

Die für die Verdichtung des reinen Stickstoffgases erforderliche Energie kann mindestens zum Teil durch Entspannung eines Strömungsmittels erzeugt werden, das einen Hilfskreis durchläuft, einer vorherigen Kühlung und Kondensation durch Wärmeaustausch mit dieser Quelle für verfügbare Kälte, Verdichtung, durch eine Pumpe und Verdampfung unterliegt. Dieses, den Hilfskreis durchlaufende Strömungsmittel kann einThe energy required for the compression of the pure nitrogen gas can at least in part Relaxation of a fluid are generated, which passes through an auxiliary circuit, a previous one Cooling and condensation by exchanging heat with this source of available cold, compression, through a pump and subject to evaporation. This fluid passing through the auxiliary circuit can be a

einheitlicher Bestandteil, wie Äthylen, Äthan, Propan, sein, es kann aber auch mindestens zwei Bestandteile aufweisen, wie ein Äthan-Propan-Butan-Gemisch. Die Entspannung in der Turbine 21 kann von einer teilweisen Verflüssigung begleitet sein. Die Verdamp-uniform component, such as ethylene, ethane, propane, be, but it can also have at least two components, such as an ethane-propane-butane mixture. the Relaxation in the turbine 21 can be accompanied by a partial liquefaction. The evaporation

3^ fung im Anschluß an die Verdichtung des den Hilfskreis durchlaufenden Strömungsmittels erhält man durch Wärmeaustausch mit einem Strom von höherer Temperatur und besonders mittels restlichen Abzugsdämpfen aus dem Energiekreis des Dampferzeugers für die Verdichtung der Luft vor ihrer Zerlegung.3 ^ fung following the compression of the auxiliary circuit passing fluid is obtained by exchanging heat with a flow of higher Temperature and especially by means of remaining exhaust vapors from the energy circuit of the steam generator for the compression of the air before its decomposition.

Hierzu 1 Blatt Zeichnungen1 sheet of drawings

Claims (1)

Patentanspruch:Claim: Verfahren zur Erzeugung von flüssigem und/oder gasförmigem Sauerstoff sowie flüssigem und/oder gasförmigem Stickstoff durch Zerlegung von Luft in einer Destillationskolonne (14), mit einem Hauptwärmetauscher (7) zur Abkühlung der zu zerlegenden Luft durch die abziehenden gasförmigen Produktströme, wobei aus dem abziehenden Stickstoffstrom ein noch nicht vollständig erwärmter Teil (24) aus einem Zwischenbereich des Hauptwärmetauschers (7) entnommen und einem Verdichter (26) mit nachgeschaltetem Kühler (28), der durch ein externes Kühlmittel gekühlt wird, zugeführt und verflüssigt (33, 34) wird, wobei ein Teil des verflüssigten Stickstoffes (aus 34) als Rücklauf in die Kolonne (14) zugeführt wird, dadurch gekennzeichnet, daß zur Anpassung des Wärmetausches im Hauptwärmetauscher (7) an veränderte Produktströme bei Erzeugung mindestens eines Teiles des gasförmigen Sauerstoffs bei einem Druck, der höher ist als in der Kolonne (14), zumindest ein Teilstrom des abziehenden Stickstoffes (in 23) nach Erwärmung auf Umgebungstemperatur (bei 50) dem aus dem Zwischenbereich des Hauptwärmetauschers (7) entnommenen Stickstoffstrom (24) bei seiner Entnahmetemperatur zugemischt wird und daß dieses Gemisch dem bei tiefer Temperatur arbeitenden Verdichter (26) steuerbar zugeführt wird.Process for generating liquid and / or gaseous oxygen as well as liquid and / or gaseous nitrogen by separating air in a distillation column (14), with a main heat exchanger (7) for cooling the air to be separated by the withdrawing gaseous product streams, whereby from the withdrawing nitrogen stream a not yet fully heated part (24) from an intermediate area of the main heat exchanger (7) removed and a compressor (26) with a downstream cooler (28), which is through a external coolant is cooled, supplied and liquefied (33, 34), with part of the Liquefied nitrogen (from 34) is fed as reflux into the column (14), characterized in that that to adapt the heat exchange in the main heat exchanger (7) to changed product flows when generating at least one Part of the gaseous oxygen at a pressure which is higher than in the column (14), at least one Partial flow of the nitrogen to be withdrawn (in 23) after heating to ambient temperature (at 50) nitrogen stream (24) removed from the intermediate region of the main heat exchanger (7) its removal temperature is admixed and that this mixture is the one at low temperature working compressor (26) is controllably supplied.
DE2044363A 1969-09-10 1970-09-08 Process for the production of oxygen and nitrogen Expired DE2044363C2 (en)

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FR2060184A1 (en) 1971-06-18
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US3886758A (en) 1975-06-03
DE2044363A1 (en) 1971-04-15
JPS501359B1 (en) 1975-01-17
ES383502A1 (en) 1972-12-16

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