EP0377117B2 - Procédé et dispositif de séparation de l'air - Google Patents

Procédé et dispositif de séparation de l'air Download PDF

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Publication number
EP0377117B2
EP0377117B2 EP89122047A EP89122047A EP0377117B2 EP 0377117 B2 EP0377117 B2 EP 0377117B2 EP 89122047 A EP89122047 A EP 89122047A EP 89122047 A EP89122047 A EP 89122047A EP 0377117 B2 EP0377117 B2 EP 0377117B2
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EP
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Prior art keywords
column
argon
rectification
pressure
crude argon
Prior art date
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Expired - Lifetime
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EP89122047A
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German (de)
English (en)
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EP0377117A1 (fr
EP0377117B1 (fr
Inventor
Wilhelm Rohde
Horst Dipl.-Ing. Corduan
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2250/58—One fluid being argon or crude argon
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the invention relates to a method and a device for air separation by low-temperature rectification of air, in which air is compressed, pre-cleaned, cooled, fed to a two-stage rectification and is broken down into an oxygen-rich and a nitrogen-rich fraction, with another from the low-pressure stage of the rectification Oxygen-enriched argon fraction is removed and broken down into crude argon in a crude argon rectification and into a heavier-boiling residual fraction, and the head cooling of the crude argon rectification is effected by indirect heat exchange with evaporating liquid from the sump of the pressure column, which is relaxed to about the pressure of the low-pressure stage.
  • the main products of air separation, oxygen and nitrogen, can be taken directly from the two-stage rectification.
  • Argon on the other hand, whose boiling temperature lies between the boiling temperatures of oxygen and nitrogen. accumulates in the middle area of the low-pressure stage of the rectification.
  • a fraction consisting essentially of oxygen is removed, with which a large part of the argon contained in the feed air is drawn off.
  • This fraction is broken down into crude argon and into a liquid residual fraction by rectification in a crude argon column. The remaining fraction is returned to the low pressure stage.
  • a method of the type mentioned is known from DE-OS-34 36 897. There, after a two-stage air rectification in a crude argon column, gaseous crude argon is obtained, which consists of approximately 95% argon and is mainly contaminated by approximately 3% oxygen and 2% nitrogen (all percentages relate to the volume).
  • the oxygen can be rectified in the crude argon column. which usually contains about 60 rectification trays, can only be removed incompletely because the boiling points of argon and oxygen are extremely close together. The difference in boiling temperatures is, for example, 2.9 K at a pressure of 1 bar.
  • the oxygen is separated from the crude argon in a so-called deoxo device by burning the oxygen with added hydrogen and separating the water formed in a dryer.
  • a deoxo device by burning the oxygen with added hydrogen and separating the water formed in a dryer.
  • Such a deoxo device is a complex apparatus and, above all, causes high operating costs due to the not inconsiderable consumption of hydrogen.
  • the provision of hydrogen is particularly complex if it does not occur in chemical processes that are carried out at the location of the air separation plant.
  • the invention has for its object to develop a method and an apparatus of the type mentioned, which are characterized by a low level of equipment and low operating costs.
  • the head of the rectification column in which such separation is to be carried out must be cooled in order to produce reflux.
  • An indirect heat exchange with the bottom fraction from the pressure stage comes into question, as is usually also used in the crude argon rectification.
  • the bottom fraction is expanded in a top condenser and evaporated there. Indirect heat exchange absorbs heat from the condensing gas in the top of the crude argon column.
  • the evaporated bottom fraction is introduced into the low pressure column.
  • a prerequisite for the fact that return can be generated in this way is, however, that the condensation temperature of the gas at the top of the column to be cooled is higher than the evaporation temperature of the evaporating bottom liquid. These temperatures are determined by the pressures of the respective fractions.
  • an exclusively rectifying separation of the oxygen is nevertheless maintained.
  • rectification trays are dispensed with in the device according to the invention and instead structured packings or fillers are used which bring about a substantially lower pressure drop within the rectification column. Since there was no empirical data on the effect of structured packings or packing elements in air rectification, it was only with the experience gained in a larger test facility that the possible implementations of packs in this area and especially in the raw argon column could be assessed. The tests showed that with a theoretical number of trays between 150 and 200, preferably about 180, an oxygen content of less than 1 ppm in the raw argon is possible with an economical argon yield.
  • the invention is explained in more detail below on the basis of an exemplary embodiment shown schematically in the drawing.
  • the figure shows in simplified form a process for air separation with subsequent argon extraction, which is carried out purely by rectification according to the invention.
  • Air is drawn from the compressor 2 via line 1 and freed of water vapor and carbon dioxide in a cleaning stage 3.
  • the air is then cooled in a heat exchanger 4 in counterflow to product gases and some of it is introduced via line 5 into the pressure column 10 of a two-stage rectification column 9.
  • Another part of the air is branched off in the heat exchanger 4 at an average temperature (line 6), expanded in a turbine 7 while performing work, and fed to the low-pressure column 11 via line 8.
  • a condenser-evaporator 12 gas is condensed from the top of the pressure column against evaporating bottom liquid of the low-pressure column, and is fed as a return to the pressure column.
  • Nitrogen gaseous (line 15) and liquid (line 14) are removed from the pressure column.
  • a portion of the liquid nitrogen is fed as a return liquid into the low pressure column via line 18.
  • Sump liquid is fed out of the pressure column via line 13 and partly fed via line 16 to the central region of the low pressure column.
  • Gaseous nitrogen (line 20) and gaseous oxygen (line 21) are taken from the low-pressure column as product streams and then heated in the heat exchanger 4 to almost ambient temperature.
  • Another fraction leaves the low-pressure column via line 22.
  • This fraction contains 87-92%, preferably 90% oxygen, 8-13%, preferably 10% argon and also approximately 0.05% nitrogen and is fed into the lower region of a crude argon column 24.
  • the top condenser 26 of the crude argon column 24 is cooled by vaporizing liquid which is fed from the bottom of the pressure column 10 via line 17.
  • the bottom liquid in line 17 contains 35-40% oxygen and is expanded to approximately the pressure of the low-pressure column before being introduced into the top condenser 26.
  • the evaporated portion is introduced via line 19 into the low pressure column.
  • the raw argon column 24 is equipped with structured packings which correspond to a theoretical number of plates of 170-200, preferably approximately 180, and is operated under the pressure of the low pressure column from 1.2 to 1.6, preferably approximately 1.3 bar.
  • packings fillers with a similarly low pressure drop could also be used.
  • Raw argon which contains only about 1 ppm oxygen, is removed via line 25. A part of this raw argon is liquefied in the top condenser 26 and returned to the raw argon column as a return. The remaining raw argon is condensed in a raw argon liquefier 28 by heat exchange with evaporating nitrogen 29, which comes from the pressure column.
  • the nitrogen remaining in the crude argon is separated off.
  • the bottom of the column is heated by nitrogen gas which is fed from the pressure column via line 15.
  • the condensed nitrogen 31 is used together with nitrogen 32 which has been removed from the pressure column to cool the head of the pure argon column.
  • gas is withdrawn via line 34 and partly liquefied in the top condenser 33 and returned to the pure argon column 30.
  • the remaining part is discharged via line 37 as residual gas, which consists essentially of nitrogen.
  • Liquid pure argon is removed via line 39 and contains a total of 1-10 ppm, preferably 3 ppm, of impurities.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Removal Of Specific Substances (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)
  • Motor Or Generator Cooling System (AREA)

Claims (3)

  1. Procédé de fractionnement de l'air par rectification de l'air à très basse température, procédé dans lequel
    a) l'air est condensé, prépurifié, refroidi,
    b) est soumis à rectification en deux étages,
    c) puis divisé en une fraction riche en oxygène et en une fraction riche en azote, et dans lequel
    d) une autre fraction d'oxygène enrichie en argon est prélevée dans l'étage basse-pression de la rectification,
    e) et est séparée dans une rectification de l'argon brut en une fraction d'argon brut et en une fraction résiduelle dont l'évaporation est plus difficile, et dans lequel
    f) le refroidissement effectué en tête de la rectification de l'argon brut est réalisé par échange de chaleur indirect avec la phase liquide, en train de s'évaporer et ramenée par détente à la pression de l'étage basse-pression, provenant de la cuve de la colonne sous pression,
    caractérisé en ce que la rectification d'argon brut est mise en oeuvre:
    g) sur au moins 150 plateaux théoriques,
    h) en présence de garnitures structurées ou corps de remplissage.
  2. Procédé selon la revendication 1, caractérisé en ce que l'argon brut provenant de la rectification d'argon brut est fractionné dans une zone de rectification d'argon pur, en une fraction d'argon pur et en une fraction résiduelle de point d'ébullition moins élevé.
  3. Dispositif d'exécution du procédé selon la revendication 1, comportant une colonne de rectification à deux étages, comprenant une colonne sous pression et une colonne basse-pression, ainsi qu'une colonne d'argon brut, qui comporte un condenseur de tête qui est relié par une conduite d'amenée de liquide à la cuve de la colonne sous pression, caractérisé en ce que la colonne d'argon brut, est mise en oeuvre sur au moins 150 plateaux théoriques et en présence de garnitures structurées ou corps de remplissage.
EP89122047A 1988-12-01 1989-11-29 Procédé et dispositif de séparation de l'air Expired - Lifetime EP0377117B2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3840506 1988-12-01
DE3840506A DE3840506A1 (de) 1988-12-01 1988-12-01 Verfahren und vorrichtung zur luftzerlegung

Publications (3)

Publication Number Publication Date
EP0377117A1 EP0377117A1 (fr) 1990-07-11
EP0377117B1 EP0377117B1 (fr) 1992-03-25
EP0377117B2 true EP0377117B2 (fr) 1995-05-17

Family

ID=6368245

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89122047A Expired - Lifetime EP0377117B2 (fr) 1988-12-01 1989-11-29 Procédé et dispositif de séparation de l'air

Country Status (11)

Country Link
US (1) US5019145A (fr)
EP (1) EP0377117B2 (fr)
JP (1) JPH0781781B2 (fr)
KR (1) KR950014009B1 (fr)
CN (1) CN1019690B (fr)
AT (1) ATE74199T1 (fr)
AU (1) AU617226B2 (fr)
CA (1) CA2004263C (fr)
DE (2) DE3840506A1 (fr)
ES (1) ES2031677T5 (fr)
ZA (1) ZA899186B (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007035619A1 (de) 2007-07-30 2009-02-05 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft
EP2026024A1 (fr) 2007-07-30 2009-02-18 Linde Aktiengesellschaft Procédé et dispositif pour la production d'argon par séparation cryogénique d'air
DE102009016043A1 (de) 2009-04-02 2010-10-07 Linde Ag Verfahren zum Betreiben einer Reinargonsäule und Vorrichtung zur Reinargongewinnung
DE102012006484A1 (de) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Transportables Paket mit einer Coldbox und Verfahren zum Herstellen einer Tieftemperatur-Luftzerlegungsanlage
DE102013003417A1 (de) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Trennsäule für eine Tieftemperatur-Luftzerlegungsanlage, Tieftemperatur-Luftzerlegungsanlage und Verfahren zur Tieftemperaturzerlegung von Luft
DE102012006479A1 (de) 2012-03-29 2013-10-02 Linde Ag Transportables Paket mit einer Coldbox und Verfahren zum Herstellen einer Tieftemperatur-Luftzerlegungsanlage
DE102012008415A1 (de) 2012-04-27 2013-10-31 Linde Aktiengesellschaft Transportables Paket mit einer Coldbox, Tieftemperatur-Luftzerlegungsanlage und Verfahren zum Herstellen einer Tieftemperatur-Luftzerlegungsanlage
DE102013018664A1 (de) 2013-10-25 2015-04-30 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Tieftemperatur-Luftzerlegungsanlage

Families Citing this family (52)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4983194A (en) * 1990-02-02 1991-01-08 Air Products And Chemicals, Inc. Production of high purity argon
US4994098A (en) * 1990-02-02 1991-02-19 Air Products And Chemicals, Inc. Production of oxygen-lean argon from air
US5133790A (en) * 1991-06-24 1992-07-28 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification method for producing refined argon
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EP0377117A1 (fr) 1990-07-11
CA2004263C (fr) 1994-02-01
JPH0781781B2 (ja) 1995-09-06
CN1043196A (zh) 1990-06-20
AU4582189A (en) 1990-06-07
ATE74199T1 (de) 1992-04-15
US5019145A (en) 1991-05-28
KR950014009B1 (ko) 1995-11-20
ZA899186B (en) 1990-08-29
KR900009433A (ko) 1990-07-04
CN1019690B (zh) 1992-12-30
ES2031677T3 (es) 1992-12-16
DE3840506A1 (de) 1990-06-07
EP0377117B1 (fr) 1992-03-25
JPH02247484A (ja) 1990-10-03
DE58901041D1 (de) 1992-04-30
AU617226B2 (en) 1991-11-21
ES2031677T5 (es) 1995-09-16
CA2004263A1 (fr) 1990-06-01
DE3840506C2 (fr) 1992-01-16

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