EP1387136A1 - Procédé et appareil de production d'oxygène impur par distillation cryogénique de l'air - Google Patents

Procédé et appareil de production d'oxygène impur par distillation cryogénique de l'air Download PDF

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Publication number
EP1387136A1
EP1387136A1 EP02018727A EP02018727A EP1387136A1 EP 1387136 A1 EP1387136 A1 EP 1387136A1 EP 02018727 A EP02018727 A EP 02018727A EP 02018727 A EP02018727 A EP 02018727A EP 1387136 A1 EP1387136 A1 EP 1387136A1
Authority
EP
European Patent Office
Prior art keywords
oxygen
column
nitrogen
feed air
impure
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.)
Withdrawn
Application number
EP02018727A
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German (de)
English (en)
Inventor
Ralph Spöri
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1387136A1 publication Critical patent/EP1387136A1/fr
Withdrawn legal-status Critical Current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
    • F25J3/0446—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases
    • F25J3/04466—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid 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
    • F25J3/04078—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Definitions

  • the invention relates to a method for producing impure oxygen by Cryogenic air separation according to the preamble of patent claim 1.
  • the rectification system of the invention can be a two-pillar system, for example as classic double-column system, be designed, but also as a three- or multi-column system. It can be used in addition to the columns for nitrogen-oxygen separation other devices for extracting other air components, especially noble gases (e.g. krypton, xenon and / or argon) exhibit.
  • noble gases e.g. krypton, xenon and / or argon
  • the oxygen-rich fraction used as the insert for the mixing column points an oxygen concentration higher than that of air and for example 70 to 99.5 mol%, preferably 90 to 98 mol%.
  • Under Mixing column is understood to be a countercurrent contact column in which a more volatile gaseous fraction of a less volatile liquid is sent to.
  • the method according to the invention is particularly suitable for the extraction of gaseous impure oxygen.
  • a mixture with is used here as impure oxygen an oxygen content of 99.5 mol% or less, in particular from 70 to Designated 99.5 mol%.
  • the product pressure is usually below the Operating pressure of the high pressure column (when using a two or more column process as a distillation column system for nitrogen-oxygen separation), for example at 2 to 4 bar, preferably at about 3 bar. Of course you can the printed product can be further compressed in the gaseous state if necessary.
  • the invention can also at mixing column pressures above the High pressure column pressure are used, for example at 4.5 to 16 bar, especially at 5 to 12 bar.
  • the invention has for its object a method of the type mentioned and specify a corresponding device that is particularly economical are.
  • the mixing column is operated under a pressure which is higher than that The discharge pressure of the impure oxygen product is.
  • Further compression of the product is not excluded; the advantages of the method according to the invention, however, come at relatively low Product pressures of, for example, 2 to 4 bar, preferably about 3 bar particularly clearly to bear, where generally no further compaction is required is.
  • the pressure difference between the mixing column and the discharge pressure is determined by the work-related relaxation of the impure oxygen fraction to generate cold used. Any known type of relaxation machine can be used come, for example a booster turbine; preferably an oil-braked one Turbine or a generator turbine used.
  • a liquid from the lower and / or middle area of the Mixing column in the distillation column system for nitrogen-oxygen separation introduced.
  • the distillation column system for nitrogen-oxygen separation is preferably as Two or more column system is formed and has a high pressure column and one Low pressure column, the first feed air flow into the high pressure column is introduced and the oxygen-rich fraction is removed from the low pressure column becomes.
  • the first feed air stream is used for the distillation column system Nitrogen-oxygen separation and the second feed air flow, which as Heat transfer stream for the mixing column serves, together to about the operating pressure the high pressure column are compressed.
  • the second feed airflow downstream of the compression to approximately the operating pressure of the high pressure column preferably not recompressed. In this way, a single machine is sufficient Compression of separation and mixing column air.
  • any another method known for the low temperature separation of air Refrigeration can also be used.
  • a combination with one is more favorable Blow-in turbine, with a third stream of feed air relaxing and into the work Low pressure column is initiated. All three feed air flows can be combined in one single machine can be compressed together to a uniform pressure.
  • the third feed air flow can be directed directly into the blowing turbine or before be post-compressed, preferably driven in one by a turbine Post-compressor (turbine booster).
  • the invention also relates to a device for producing impure Oxygen by low-temperature decomposition of air according to claim 8.
  • a first feed air stream 1 is in a main heat exchanger, which in the example consists of two serially connected blocks 2a, 2b, cooled to about dew point.
  • the cold air 3 is in the high pressure column 4 of a distillation column system for Nitrogen-oxygen separation initiated.
  • the operating pressure of the high pressure column 4 is, for example, 4.3 to 6.9 bar, preferably about 5.6 bar.
  • the distillation column system for nitrogen-oxygen separation also has a low pressure column 5 on, which is operated under, for example, 1.3 to 1.7 bar, preferably about 1.5 bar.
  • the head of the high pressure column and the bottom of the low pressure column 5 protrude a common condenser-evaporator, the main condenser 6 in heat exchanging connection.
  • the first feed air stream 1 Before entering the main heat exchanger 2a the first feed air stream 1 is compressed to a pressure (not shown) that is the same the operating pressure of the high pressure column plus line losses.
  • Oxygen-enriched bottom liquid 7 of the high pressure column 4 is in a first Subcooling countercurrent 8 cooled, in a throttle valve 9 to about Low pressure column pressure is released and via line 10 of the low pressure column 5 fed to a first intermediate point.
  • Gaseous nitrogen 11 from the top of the High-pressure column 4 is at least a first part via line 12 Main capacitor 6 supplied and condensed substantially completely there.
  • the liquid nitrogen 13 from the main condenser serves as a return for High pressure column and low pressure column and optionally as a liquid product.
  • To is a first part via lines 14 and 16 by a second supercooling counterflow 15 introduced into a first separator (phase separator) 17. On second part flows via line 18 into the high pressure column 4 and is there as a return used.
  • Another part also flows via line 18 into the high pressure column, but is removed again via line 19 and through the second subcooling countercurrent 15 and through line 20 into a second separator (phase separator) 21 fed.
  • the liquid 22 from the first separator 17 becomes at least too a part via the lines 23 and 24 as a return to the low pressure column 5 given up.
  • the remaining liquid 25 can - like the liquid fraction 26 from the second separator 21 - can be obtained as a liquid nitrogen product.
  • Gaseous pure nitrogen 27 from the top of the low pressure column 5 is shared with the flash gases 28 and 29 from the two separators 17, 26 via line 30 deducted, in the two supercooling countercurrent 15, 16 and in Main heat exchanger 2b, 2a warmed up and via line 31 under about Ambient temperature obtained as a pressureless gaseous nitrogen product.
  • impure nitrogen 32 is removed in gaseous form, also in the two Subcooling countercurrents 15, 16 and heated in the main heat exchanger 2b, 2a and discharged via line 33 as residual or regeneration gas.
  • an oxygen-rich fraction 34 is drawn off in liquid form in a pump 35 Brought pressure and flows under one opposite the trigger from the Low pressure column 5 increased pressure (usually equal to the mixing column pressure plus Line losses and static pressure) is via lines 36, 37 and 38 after Subcooling in the first subcooling countercurrent 8 and at the cold end of the Main heat exchanger 2b placed on the head of a mixing column 39.
  • the Mixing column can be operated under the same pressure as the high pressure column 4, that is to say the same applies to at least one point within the mixing column Pressure as at at least one point on the high pressure column.
  • a second feed air stream 40, 41 is injected, which is preferably is under the same pressure as the first feed air stream 1 and together with this was compressed (not shown).
  • the bottom liquid 42 - 43 and one Intermediate liquid 44-45 of the mixing column 39 are each in the first Supercooling countercurrent 8 and supercooled on their composition corresponding places throttled in the low pressure column 5.
  • An impure oxygen fraction 46 is drawn off from the top of the mixing column 39 and warmed to a first intermediate temperature in the main heat exchanger 2b. Under this first intermediate temperature, it becomes a work-performing line 47 Relaxation 48 fed. There it occurs under a pressure of, for example, 2 to 4 bar, preferably about 3 bar and under a second, lower Intermediate temperature off again and is the line 49 again Main heat exchanger 2b supplied. After complete heating in the It is the main heat exchanger 2b, 2a via line 50 as an impure oxygen product won.
  • a purer gaseous is also Oxygen product 53 obtained by liquid oxygen 51 from the bottom of the Low pressure column 5 withdrawn, brought to pressure by means of a pump 52 (Internal compression) and finally evaporated in the main heat exchanger 2b, 2a and is warmed up.
  • gaseous pressurized nitrogen 55, 56 can be taken directly from the top of the High pressure column 4 are withdrawn.

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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)
EP02018727A 2002-08-02 2002-08-21 Procédé et appareil de production d'oxygène impur par distillation cryogénique de l'air Withdrawn EP1387136A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10235483 2002-08-02
DE10235483 2002-08-02

Publications (1)

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EP1387136A1 true EP1387136A1 (fr) 2004-02-04

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011116871A2 (fr) 2010-03-26 2011-09-29 Linde Aktiengesellschaft Dispositif pour le fractionnement cryogénique de l'air
WO2011116981A2 (fr) 2010-03-26 2011-09-29 Linde Aktiengesellschaft Dispositif pour la décomposition à basse température d'air
EP2503269A1 (fr) 2011-03-25 2012-09-26 Linde Aktiengesellschaft Dispositif de décomposition à basse température de l'air
EP2505947A1 (fr) 2011-03-29 2012-10-03 Linde Aktiengesellschaft Procédé et dispositif destinés à la production de verre flotté
DE102011015429A1 (de) 2011-03-29 2012-10-04 Linde Ag Verfahren und Vorrichtung zum Betreiben eines Rebox-Brenners
DE102012021694A1 (de) 2012-11-02 2014-05-08 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft in einer Luftzerlegungsanlage und Luftzerlegungsanlage
DE102013002094A1 (de) 2013-02-05 2014-08-07 Linde Aktiengesellschaft Verfahren zur Produktion von Luftprodukten und Luftzerlegungsanlage
DE102015015684A1 (de) 2015-12-03 2016-07-21 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage
EP3179186A1 (fr) 2015-12-07 2017-06-14 Linde Aktiengesellschaft Procede de production d'un produit comprime riche en oxygene, gazeux et liquide dans une installation de decomposition de l'air et installation de decomposition de l'air

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0229803A1 (fr) * 1985-07-15 1987-07-29 Air Liquide Procede et installation de distillation d'air.
EP0531182A1 (fr) * 1991-08-07 1993-03-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de distillation d'air, et application a l'alimentation en gaz d'une aciérie
DE19951521A1 (de) * 1999-10-26 2001-05-03 Linde Ag Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0229803A1 (fr) * 1985-07-15 1987-07-29 Air Liquide Procede et installation de distillation d'air.
EP0531182A1 (fr) * 1991-08-07 1993-03-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de distillation d'air, et application a l'alimentation en gaz d'une aciérie
DE19951521A1 (de) * 1999-10-26 2001-05-03 Linde Ag Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011116871A2 (fr) 2010-03-26 2011-09-29 Linde Aktiengesellschaft Dispositif pour le fractionnement cryogénique de l'air
DE102010012920A1 (de) 2010-03-26 2011-09-29 Linde Aktiengesellschaft Vorrichtung zur Tieftemperaturzerlegung von Luft
WO2011116981A2 (fr) 2010-03-26 2011-09-29 Linde Aktiengesellschaft Dispositif pour la décomposition à basse température d'air
EP2503269A1 (fr) 2011-03-25 2012-09-26 Linde Aktiengesellschaft Dispositif de décomposition à basse température de l'air
DE102011015233A1 (de) 2011-03-25 2012-09-27 Linde Ag Vorrichtung zur Tieftemperaturzerlegung von Luft
US9228778B2 (en) 2011-03-25 2016-01-05 Linde Aktiengesellschaft Device for the low-temperature separation of air
DE102011015430A1 (de) 2011-03-29 2012-10-04 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von Flachgas
DE102011015429A1 (de) 2011-03-29 2012-10-04 Linde Ag Verfahren und Vorrichtung zum Betreiben eines Rebox-Brenners
EP2505947A1 (fr) 2011-03-29 2012-10-03 Linde Aktiengesellschaft Procédé et dispositif destinés à la production de verre flotté
DE102012021694A1 (de) 2012-11-02 2014-05-08 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft in einer Luftzerlegungsanlage und Luftzerlegungsanlage
WO2014067662A2 (fr) 2012-11-02 2014-05-08 Linde Aktiengesellschaft Procédé de séparation d'air à basse température dans une installation de séparation d'air et installation de séparation d'air
DE102013002094A1 (de) 2013-02-05 2014-08-07 Linde Aktiengesellschaft Verfahren zur Produktion von Luftprodukten und Luftzerlegungsanlage
DE102015015684A1 (de) 2015-12-03 2016-07-21 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage
EP3179186A1 (fr) 2015-12-07 2017-06-14 Linde Aktiengesellschaft Procede de production d'un produit comprime riche en oxygene, gazeux et liquide dans une installation de decomposition de l'air et installation de decomposition de l'air
EP3179187A1 (fr) 2015-12-07 2017-06-14 Linde Aktiengesellschaft Procédé de production d'un produit comprime riche en oxygène, gazeux et liquide dans une installation de décomposition de l'air et installation de décomposition de l'air

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