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EP0363861B1 - Verfahren zur Gewinnung von Rohargon - Google Patents

Verfahren zur Gewinnung von Rohargon Download PDF

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Publication number
EP0363861B1
EP0363861B1 EP89118671A EP89118671A EP0363861B1 EP 0363861 B1 EP0363861 B1 EP 0363861B1 EP 89118671 A EP89118671 A EP 89118671A EP 89118671 A EP89118671 A EP 89118671A EP 0363861 B1 EP0363861 B1 EP 0363861B1
Authority
EP
European Patent Office
Prior art keywords
air
stage
pressure
argon
raw argon
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 - Lifetime
Application number
EP89118671A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0363861A2 (de
EP0363861A3 (en
Inventor
Wilhelm Rohde
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 EP0363861A2 publication Critical patent/EP0363861A2/de
Publication of EP0363861A3 publication Critical patent/EP0363861A3/de
Application granted granted Critical
Publication of EP0363861B1 publication Critical patent/EP0363861B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/04096—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 argon or argon enriched stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • 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
    • 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 process for obtaining gaseous crude argon by low-temperature rectification of air, in which air is compressed, pre-cleaned, cooled and fed to the pressure stage of a two-stage rectification and in which crude argon is obtained in the liquid state after the two-stage rectification and evaporated under increased pressure is, with a partial stream of the air being branched off before cooling, post-compressed, cooled and then partially expanded to perform the work and fed to the low-pressure stage of the rectification, work obtained during the expansion of the post-compressed air being used for post-compression.
  • WO 88/01037 shows a method of the type described in the introduction, in which crude argon is obtained in liquid form and is compressed hydrostatically.
  • a coupled compressor / turbine unit is used, in which part of the separation air is post-compressed, all of the post-compressed air in the turbine is expanded and then fed to the low-pressure stage.
  • a large part of the separation air is introduced into the low-pressure stage without pre-separation, as a result of which its rectifying effect deteriorates. This is reflected in an incompletely satisfactory cost-effectiveness of the process, especially with regard to the argon yield.
  • a method with similar raw argon production is also known from DE-A 34 28 968, in which raw argon is removed from the top of a raw argon column in liquid form or liquefied after being removed from a raw argon column.
  • the liquid raw argon experiences an increase in pressure using its hydrostatic potential in order to bring the raw argon, which is generally obtained approximately under atmospheric pressure, to the pressure of approximately 3.5 to 5 bar required for further processing.
  • This procedure offers the advantage that a machine for compressing the raw argon, which is required, for example, in the case of gaseous extraction of the raw argon, can be saved.
  • the raw argon which is under increased pressure, must be evaporated to obtain pure argon.
  • the evaporation cold is removed in the process of DE-A 34 28 968 by heat exchange with nitrogen.
  • such a process stream is not available at such a high pressure in a low-pressure system in which the air is compressed to about 6 bar that it could be liquefied against the crude argon to be evaporated at elevated pressure, so that only the heat capacity of the gaseous one Nitrogen and not its latent heat is available to dissipate the evaporative cold of the raw argon.
  • the heat exchanger for crude argon evaporation must be made relatively large.
  • the rectification is supplied with an amount of liquid which is equivalent to the amount of crude argon removed, for which additional cold has to be generated elsewhere.
  • the object of the invention is to provide an improved process of the type mentioned at the outset for obtaining gaseous crude argons under increased pressure, in which in particular a high product yield is achieved with little expenditure on energy and apparatus.
  • the invention shows two solutions to this problem.
  • part of the post-compressed air is branched off before the expansion, brought into heat exchange with the crude argon obtained in liquid form and under increased pressure, and thereby liquefied.
  • the liquefied air is fed to the pressure stage of the rectification as the return liquid.
  • it is brought into heat exchange with gas in the head of a crude argon column from which the crude argon is removed.
  • the air under increased pressure is also used to give off heat to liquid raw argon and to evaporate it in the process. Since the post-compressed air is under increased pressure, it is liquefied during the heat exchange with the evaporating raw argon. The latent heat of the air is thus also available for absorbing the evaporative cold of the crude argon, whereby on the one hand a relatively small process stream is sufficient for the evaporation and on the other hand liquid is generated which is required for the cold balance of the rectification.
  • the peak cold transferred during the evaporation of the crude argon obtained in liquid form is particularly advantageously returned to the process; on the one hand as a return liquid for the pressure stage, on the other hand for the production of liquid during rectification, especially in the crude argon column.
  • the air evaporated during the heat exchange with gas at the top of the crude argon column can be introduced into the low-pressure column.
  • the invention is explained in more detail below with reference to an exemplary embodiment schematically illustrated in the drawing.
  • the figure shows a form of the method according to the invention from sucking in the air to be broken down to evaporating and heating the crude argon, the less essential and known method steps being shown in a highly simplified manner.
  • the work steps following the crude argon evaporation for the fine cleaning of the crude argon are not shown.
  • Air is drawn in via line 1, compressed in an air compressor 2, pre-cleaned in a cleaning stage 3 - for example a molecular sieve system - and introduced through line 4 into a main heat exchanger 5, in which it is cooled in counterflow to product streams.
  • the cold air becomes the Pressure stage 7 is fed to a two-stage rectification column 6, which is operated at a pressure of 5.0 to 7.0 bar and is in heat-exchanging connection with the low-pressure stage 8 via a condenser-evaporator 9.
  • Liquid enriched with oxygen is removed from the bottom of pressure stage 7 via line 10 and throttled at a suitable point in low pressure stage 8, which is under a pressure of 1.0 to 2.0 bar. From the low-pressure stage, nitrogen (line 11) and oxygen (line 12) are led out as product streams and then warmed to almost ambient temperature in the main heat exchanger 5. In addition, a further oxygen stream, which has a relatively high argon concentration, is led out via line 13 and introduced into a crude argon column 14. Liquid also flows back from the crude argon column 14 into the low-pressure stage 8 via the same line 13.
  • the crude argon column 14 is taken as liquid crude argon product (line 15).
  • the crude argon could also be taken in whole or in part in gaseous form and then liquefied, as proposed in DE-OS 34 28 968.
  • the hydrostatic potential of approx. 30 to 40 m along the line 15 the liquid raw argon experiences a pressure increase to 3.0 to 5.0 bar, preferably approx. 4.0 bar, is evaporated in a raw argon evaporator 16, in the main heat exchanger 5 warmed to about ambient temperature and fed via line 17 to a further cleaning stage.
  • part of the air is branched off via line 18 after the preliminary cleaning (3), further compressed in a post-compressor 19 to a pressure of 7.0 to 11.0 bar, preferably 9.0 bar, in the main heat exchanger 5 to a medium one Cooled temperature and largely relaxed in a turbine 20 work and introduced into the low pressure stage 8 (line 21).
  • the turbine 20 is mechanically coupled to the post-compressor 19.
  • part of the post-compressed air is branched off via line 22 before decompression (20), passed in countercurrent to the evaporating crude argon through the crude argon evaporator 16 and at least partially liquefied and then via line 23 and throttle valve 24 as a return to the pressure stage 7 initiated.

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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)
EP89118671A 1988-10-12 1989-10-07 Verfahren zur Gewinnung von Rohargon Expired - Lifetime EP0363861B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3834793A DE3834793A1 (de) 1988-10-12 1988-10-12 Verfahren zur gewinnung von rohargon
DE3834793 1988-10-12

Publications (3)

Publication Number Publication Date
EP0363861A2 EP0363861A2 (de) 1990-04-18
EP0363861A3 EP0363861A3 (en) 1990-06-20
EP0363861B1 true EP0363861B1 (de) 1992-06-03

Family

ID=6364973

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89118671A Expired - Lifetime EP0363861B1 (de) 1988-10-12 1989-10-07 Verfahren zur Gewinnung von Rohargon

Country Status (5)

Country Link
US (1) US4932212A (zh)
EP (1) EP0363861B1 (zh)
CN (1) CN1052940A (zh)
CA (1) CA2000595A1 (zh)
DE (2) DE3834793A1 (zh)

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Publication number Priority date Publication date Assignee Title
DE4126945A1 (de) * 1991-08-14 1993-02-18 Linde Ag Verfahren zur luftzerlegung durch rektifikation
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5245831A (en) * 1992-02-13 1993-09-21 Air Products And Chemicals, Inc. Single heat pump cycle for increased argon recovery
US5255522A (en) * 1992-02-13 1993-10-26 Air Products And Chemicals, Inc. Vaporization of liquid oxygen for increased argon recovery
US5255524A (en) * 1992-02-13 1993-10-26 Air Products & Chemicals, Inc. Dual heat pump cycles for increased argon recovery
US5365741A (en) * 1993-05-13 1994-11-22 Praxair Technology, Inc. Cryogenic rectification system with liquid oxygen boiler
FR2706195B1 (fr) † 1993-06-07 1995-07-28 Air Liquide Procédé et unité de fourniture d'un gaz sous pression à une installation consommatrice d'un constituant de l'air.
US5366239A (en) * 1993-09-27 1994-11-22 Trw Inc. Air bag inflator assembly
FR2787562B1 (fr) * 1998-12-22 2001-02-09 Air Liquide Procede et installation de distillation d'air avec production d'argon
JP2002511136A (ja) * 1998-04-21 2002-04-09 レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード アルゴンの製造を伴う空気精留プロセスおよびプラント
FR2777641B1 (fr) * 1998-04-21 2000-05-19 Air Liquide Procede et installation de distillation d'air avec production d'argon
US6397632B1 (en) 2001-07-11 2002-06-04 Praxair Technology, Inc. Gryogenic rectification method for increased argon production
DE102007051183A1 (de) * 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren zur Tieftemperatur-Luftzerlegung
FR2943773B1 (fr) * 2009-03-27 2012-07-20 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
CN113959179B (zh) * 2021-12-22 2022-05-03 杭州制氧机集团股份有限公司 一种用于液氩提纯的装置及方法

Citations (1)

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Publication number Priority date Publication date Assignee Title
WO1988001037A1 (en) * 1986-08-01 1988-02-11 Erickson Donald C Air distillation improvements for high purity oxygen

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DE1229561B (de) * 1962-12-21 1966-12-01 Linde Ag Verfahren und Vorrichtung zum Zerlegen von Luft durch Verfluessigung und Rektifikation mit Hilfe eines Inertgaskreislaufes
DE1667639A1 (de) * 1968-03-15 1971-07-08 Messer Griesheim Gmbh Verfahren zum Gewinnen eines Krypton-Xenon-Gemisches aus Luft
DE1922956B1 (de) * 1969-05-06 1970-11-26 Hoechst Ag Verfahren zur Erzeugung von argonfreiem Sauerstoff durch Rektifikation von Luft
US4615716A (en) * 1985-08-27 1986-10-07 Air Products And Chemicals, Inc. Process for producing ultra high purity oxygen
US4705548A (en) * 1986-04-25 1987-11-10 Air Products And Chemicals, Inc. Liquid products using an air and a nitrogen recycle liquefier
GB2198514B (en) * 1986-11-24 1990-09-19 Boc Group Plc Air separation
DE3643359C2 (de) * 1986-12-18 1993-11-18 Linde Ag Verfahren und Vorrichtung zur Luftzerlegung durch zweistufige Rektifikation
US4817394A (en) * 1988-02-02 1989-04-04 Erickson Donald C Optimized intermediate height reflux for multipressure air distillation

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988001037A1 (en) * 1986-08-01 1988-02-11 Erickson Donald C Air distillation improvements for high purity oxygen

Also Published As

Publication number Publication date
US4932212A (en) 1990-06-12
EP0363861A2 (de) 1990-04-18
DE58901598D1 (de) 1992-07-09
CN1052940A (zh) 1991-07-10
CA2000595A1 (en) 1990-04-12
DE3834793A1 (de) 1990-04-19
EP0363861A3 (en) 1990-06-20

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