EP0379435B1 - Verfahren und Vorrichtung zur Lufttrennung und Herstellung von ultrareinem Sauerstoff - Google Patents

Verfahren und Vorrichtung zur Lufttrennung und Herstellung von ultrareinem Sauerstoff Download PDF

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EP0379435B1
EP0379435B1 EP90400145A EP90400145A EP0379435B1 EP 0379435 B1 EP0379435 B1 EP 0379435B1 EP 90400145 A EP90400145 A EP 90400145A EP 90400145 A EP90400145 A EP 90400145A EP 0379435 B1 EP0379435 B1 EP 0379435B1
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Prior art keywords
column
vessel
additional
pressure column
medium pressure
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French (fr)
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EP0379435B2 (de
EP0379435A1 (de
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Maurice Grenier
Philippe Mazieres
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F25J3/04715—The auxiliary column system simultaneously produces 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
    • F25J3/04406—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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
    • 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
    • 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
    • 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
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream 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

Definitions

  • the present invention relates to a method and an installation for producing ultra-pure oxygen from a main double column air distillation apparatus according to the preamble of claims 1, 5, 9 and 13.
  • ultra-pure oxygen oxygen practically free of methane (and therefore of hydrocarbons) and argon, for example containing less than 0.1 ppm of hydrocarbons and less than 10 ppm of argon , these contents being fixed in advance and being able to vary according to the applications. Ultra-pure oxygen is especially intended for the electronics industries.
  • the invention aims to allow the production of ultra-pure oxygen at the cost of an inexpensive modification of the main distillation apparatus and, above all, without additional energy expenditure.
  • a preferential execution allows the production of high purity oxygen substantially free of hydrocarbons.
  • the installation shown in Figure 1 is intended to separate air into its constituents to produce: nitrogen gas under pressure of oxygen gas at about 99.5% purity; and ultra-pure oxygen having a predetermined maximum content of methane and argon, for example less than 0.1 ppm of methane and less than 10 ppm of argon.
  • the production of ultra-pure oxygen corresponds to a small fraction, preferably between 5 and 10%, of the oxygen production of the installation.
  • the installation comprises a main air distillation apparatus 1 itself comprising a double distillation column 2.
  • the double column comprises a medium pressure column 3 surmounted by a low pressure column 4.
  • a condenser-vaporizer 5 connects indirect heat exchange of the top nitrogen of column 3 and the tank liquid (oxygen at around 99.5% purity) of column 4.
  • the air to be treated, purified and cooled to its dew point is mainly introduced under medium pressure, ie approximately 6 bars absolute, at the bottom of column 3 via a pipe 6. Its condensation produces "rich liquid” LR , part of which is expanded in an expansion valve 7 and introduced at an intermediate level of the column 4, which operates at low pressure, ie slightly above atmospheric pressure. "Lean liquid” LP, consisting essentially of nitrogen, is taken off at the top of column 3 and then, after expansion in an expansion valve 8, is introduced at the top of column 4.
  • the double column 2 also includes a pipe 9 production of gaseous oxygen at 99.5% purity, at the bottom of column 4, a pipe 10 for producing nitrogen gas at 6 bars, at the top of column 3, and a pipe 11 for discharging a waste gas W (impure nitrogen) from the top of column 4.
  • a pipe 9 production of gaseous oxygen at 99.5% purity at the bottom of column 4
  • a pipe 10 for producing nitrogen gas at 6 bars at the top of column 3
  • a pipe 11 for discharging a waste gas W (impure nitrogen) from the top of column 4.
  • a first auxiliary column 12 having a small number of theoretical plates, with between 3 and 8, is connected to the tank of column 4 by lines 13 for the gas supply and 14 for the return of the liquid, and is equipped with a head condenser 15. The latter is supplied by a portion of the rich liquid LR, expanded in an expansion valve 16.
  • a second auxiliary column 17 is supplied at an intermediate location, via a pipe 18, by the head vapor of the column 12. It has + + nl theoretical plates below the pipe 18.
  • Its tank includes a vaporizer 19 and its at the top a condenser 20.
  • the vaporizer is heated by means of air at 6 bars, derived from line 6 by a line 21, and the condenser 20 is cooled by the rest of the rich liquid LR, expanded in an expansion valve 22.
  • the rich liquid vaporized in the condensers 15 and 20 is returned to column 4 via a common line 23.
  • the liquefied air leaving the vaporizer 19 can be returned to the corresponding level in column 4 or, as shown, be combined with the rich liquid withdrawn from the tank of column 4, since its flow rate is low compared to that of this rich liquid.
  • a pipe 24 connects the top of the column 17 to an intermediate point of the column 4.
  • the oxygen conveyed through line 13 contains argon and methane as impurities. Methane separates from oxygen and argon in column 12 with n theoretical plates, the more completely the greater the number. The calculation shows that a number less than or equal to 8 is sufficient for the usual applications of ultra-pure oxygen.
  • the invention applies in the same way to main air distillation apparatuses producing oxygen with a purity of less than 99.5%, for example 95 or 97%.
  • the gas drawn off through line 13 then contains nitrogen, which easily separates from the oxygen in the auxiliary column 17.
  • the vaporizer 19 it is possible to use the place of air, to heat the vaporizer 19, a gas depleted in oxygen taken from the lower or intermediate part of the column 3.
  • the oxygen content of the heating gas must however remain sufficient to allow to ensure, by condensation of this gas, the vaporization of ultra-pure oxygen. In fact, this vaporization takes place at a pressure higher than that of the tank of column 4 due to the presence of the nl additional plates of column 17.
  • FIG. 2 shows how the invention can be applied to a main air distillation apparatus 1A provided with an oxygen-argon separation column 26.
  • a main air distillation apparatus 1A provided with an oxygen-argon separation column 26.
  • a pipe 13A called "argon tapping" starts from an intermediate location of the column 4, N theoretical plates above the tank.
  • This pipe opens into the tank of column 26 and conveys a gas essentially consisting of oxygen and argon, and a return pipe 14A starts from the lowest point of column 26 and opens into column 4 at approximately the level 13A argon stitching.
  • the column 26 is equipped with a head condenser 15A supplied by the portion of the rich liquid LR which is not expanded in the valve 7, this liquid being expanded in an expansion valve 16A.
  • the rich liquid vaporized leaving the condenser 15A is returned to column 5, a little below the rich liquid coming from> valve 7.
  • the raw argon produced at the top of column 26 is discharged through a line 27.
  • the main distillation apparatus 1A is modified as follows to produce ultra-pure oxygen.
  • a vaporizer 19A is placed in the tank of the column 17A. This vaporizer is heated as before by air at 6 bars conveyed by line 21 and combined with the rich liquid LR after condensation.
  • the oxygen-argon gas mixture conveyed by line 13A contains methane as an impurity.
  • the methane separates from the oxygen and the argon in the lower section 12A with n theoretical plates of column 26, the more completely the greater the number.
  • the calculation shows that a number n less than or equal to 8 is sufficient for the usual applications of ultra-pure oxygen.
  • a line 29 for drawing off liquid oxygen at approximately 99.5% purity can, as shown, from an intermediate location of the column 17A Located substantially N + n trays Theories below the top of this column 17A.
  • This oxygen is practically free of hydrocarbons and can therefore be used for certain applications where hydrocarbons are undesirable, for example in the medical field.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Claims (16)

1. Verfahren zum Herstellen von ultrareinem Sauerstoff, ausgehend von einem Hauptdestillierapparat für Luft (1) mit zwei Kolonnen (2), mit einer Mitteldruckkolonne (3) und einer Niederdruckkolonne (4), welches die Stufen aufweist, um ein erstes Gas in die Wanne einer ersten Hilfskolonne (12) zu leiten, welches in der Niederdruckkolonne (4) hergestellt ist, in diese letztere die Flüssigkeit zurückzuleiten, die in der Wanne der ersten Hilfskolonne hergestellt ist, in einer zweiten Hilfskolonne (17) ein Fließmittel zu destillieren, welches in der ersten Hilfskolonne hergestellt ist, wobei der ultrareine Sauerstoff in der Wanne dieser zweiten Hilfskolonne hergestellt ist,
dadurch gekennzeichnet, daß das erste Gas in der Wanne der Niederdruckkolonne (4) abgenommen wird, man in der zweiten Hilfskolonne ein Fließmittel destilliert, welches am Kopf der ersten Hilfskolonne hergestellt ist, man die Wanne der zweiten Hilfskolonne (17) erwärmt, wobei man dort ein Heizgas kondensiert, welches unter dem Mitteldruck an dem unteren oder mittleren Teil der Mitteldruckkolonne (3) verfügbar ist, und man das Kondensat in den Hauptdestillationsapparat für Luft (1) zurückleitet.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die zweite Hilfskolonne (17) einen Kopfkondensator (20) aufweist und an einer Zwischenstelle durch den Dampf des Kopfes der ersten Hilfskolonne (12) versorgt wird, wobei der Dampf des Kopfes der zweiten Hilfskolonne in die Niederdruckkolonne (4) zurückgeleitet wird.
3. Verfahren nach einem der Ansprüche 1 und 2, dadurch gekennzeichnet, daß das Heizgas aus komprimierter Luft gebildet ist, die an der Versorgungsstelle (6) der Mitteldruckkolonne (3) abgenommen wird.
4. Verfahren nach einem der Ansprüche 1 und 2, dadurch gekennzeichnet, daß die in der Wanne der zweiten Hilfskolonne (17) kondensierte Luft der reichen Flüssigkeit (LR) zugeordnet wird, welche in der Wanne der Mitteldruckkolonne (3) hergestellt ist.
5. Anlage zum Trennen von Luft und zur Herstellung von ultrareinem Sauerstoff mit einem Hauptdestillierapparat (1) für Luft mit zwei Kolonnen (2), mit einer Mitteldruckkolonne (3) und einer Niederdruckkolonne (4), mit einer ersten Hilfskolonne (12), deren Wanne mit der Niederdruckkolonne (4) durch eine erste Gasleitung (13) und eine zweite Flüssigkeitsleitung (14) verbunden ist, und einer zweiten Hilfskolonne (17), welche durch eine dritte Leitung (18) mit der ersten Hilfskolonne verbunden ist und deren Wanne einen indirekten Wärmetauscher (19) aufweist,
dadurch gekennzeichnet, daß die erste Leitung (13) mit der Wanne der Niederdruckkolonne (4) verbunden ist, die dritte Leitung (18) mit dem Kopf der ersten Hilfskolonne verbunden ist und daß sie Mittel (21) aufweist, um an der Stelle des unteren oder mittleren Teils der Mitteldruckkolonne (3) ein Heizgas unter dem mittleren Druck abzunehmen und es in den Wärmetauscher der zweiten Hilfskolonne einzuführen, und Mittel, um das vom Wärmetauscher stammende Kondensat in den Hauptdestillierapparat für Luft (1) zurückzuleiten.
6. Anlage nach Anspruch 5, dadurch gekennzeichnet, daß die zweite Hilfskolonne (17) einen Kopfkondensator (20) aufweist und an einer Zwischenstelle durch den Dampf des Kopfes der ersten Hilfskolonne (12) versorgt wird, wobei der Dampf des Kopfes der zweiten Hilfskolonne in die Niederdruckkolonne (4) zurückgeleitet wird.
7. Anlage nach einem der Ansprüche 5 und 6, dadurch gekennzeichnet, daß das Heizgas durch komprimierte Luft gebildet ist, welche an der Versorgung (6) der Mitteldruckkolonne (3) abgenommen ist.
8. Anlage nach Anspruch 7, dadurch gekennzeichnet, daß sie Mittel aufweist, um der reichen Flüssigkeit (LR), die in der Mitteldruckkolonne (3) hergestellt ist, in dem Wärmetauscher (19) kondensierte Luft zuzuordnen.
9. Verfahren zur Herstellung von ultrareinem Sauerstoff, ausgehend von einem Hauptdestillierapparat für Luft (1A), mit zwei Kolonnen (2), mit einer Mitteldruckkolonne (3) und einer Niederdruckkolonne (4), mit Stufen, um ein erstes Gas in die Wanne einer ersten Hilfskolonne (12A) zu leiten, welches an der Argonabnahmestelle der Niederdruckkolonne (4) abgenommen ist, um die Flüssigkeit in diese letztere zurückzuleiten, die in der Wanne der ersten Hilfskolonne hergestellt ist, um ein Fließmittel in einer zweiten Hilfskolonne (17) zu destillieren, welches in der ersten Hilfskolonne hergestellt ist, wobei der ultrareine Sauerstoff in der Wanne dieser zweiten Hilfskolonne hergestellt ist,
dadurch gekennzeichnet, daß man die Wanne der zweiten Hilfskolonne (17A) erwärmt, wobei man dort ein Heizgas kondensiert, welches unter dem Mitteldruck an der Stelle des unteren oder mittleren Teils der Mitteldruckkolonne (3) zur Verfügung steht, und man das Kondensat in der Niederdruckkolonne (4) des Hauptdestillationsapparates (1A) für Luft zurückleitet.
10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, daß man flüssigen Sauerstoff, praktisch frei von Kohlenwasserstoffen, an einer Zwischenstelle (29) der zweiten Hilfskolonne (17A) abnimmt.
11. Verfahren nach einem der Ansprüche 9 und 10, dadurch gekennzeichnet, daß das Heizgas durch komprimierte Luft gebildet ist, die an der Versorgungsstelle (6) der Mitteldruckkolonne (3) abgenommen wird.
12. Verfahren nach Anspruch 11, dadurch gekennzeichnet, daß die in der Wanne der zweiten Hilfskolonne (17A) kondensierte Luft der reichen Flüssigkeit (LR) zugeordnet wird, die in der Wanne der Mitteldruckkolonne (3) hergestellt wird.
13. Anlage zurTrennung von Luft und Herstellung von ultrareinem Sauerstoff mit einem Hauptdestillationsapparat für Luft (1A) mit zwei Kolonnen (2) mit einer Mitteldruckkolonne (3) und einer Niederdruckkolonne (4), mit einer ersten Hilfskolonne (12A), deren Wanne mit derArgonabnahmezone der Niederdruckkolonne (4) durch eine erste Gasleitung (13A) und durch eine zweite Flüssigkeitsleitung (14A) verbunden ist, und mit einer zweiten Hilfskolonne (17A), die durch eine dritte Leitung (18A) mit der ersten Hilfskolonne verbunden ist und deren Wanne einen indirekten Wärmeaustauscher (19A) aufweist,
dadurch gekennzeichnet, daß sie Mittel (21A) aufweist zum Abnehmen eines Heizgases unter dem mittleren Druck an der Stelle des unteren oder mittleren Teils der Mitteldruckkolonne (3) und zum Einführen desselben in den Wärmetauscher (19A) der zweiten Hilfskolonne, und Mittel aufweist zum Zurückleiten des aus dem Wärmetauscher stammenden Kondensats in die Niederdruckkolonne (4) des Hauptdestillationsapparates für Luft (1A).
14. Anlage nach Anspruch 13, dadurch gekennzeichnet, daß die zweite Hilfskolonne (17A) an einer Zwischenstelle mit einer Leitung (29) für das Abziehen von praktisch kohlenwasserstofffreiem Sauerstoff ausgestattet ist.
15. Anlage nach einem der Ansprüche 9 und 14, dadurch gekennzeichnet, daß das Heizgas aus komprimierter Luft besteht, die an der Versorgungsstelle (6) der Mitteldruckkolonne (3) abgenommen ist.
16. Anlage nach Anspruch 15, dadurch gekennzeichnet, daß sie Mittel aufweist, um der reichen Flüssigkeit (LR), die in der Wanne der Mitteldruckkolonne (3) hergestellt ist, in dem Wärmetauscher (19A) kondensierte Luft zuzuordnen.
EP90400145A 1989-01-20 1990-01-19 Verfahren und Vorrichtung zur Lufttrennung und Herstellung von ultrareinem Sauerstoff Expired - Lifetime EP0379435B2 (de)

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Application Number Priority Date Filing Date Title
AT90400145T ATE74421T1 (de) 1989-01-20 1990-01-19 Verfahren und vorrichtung zur lufttrennung und herstellung von ultrareinem sauerstoff.

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FR8900670 1989-01-20
FR8900670 1989-01-20

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EP0379435A1 EP0379435A1 (de) 1990-07-25
EP0379435B1 true EP0379435B1 (de) 1992-04-01
EP0379435B2 EP0379435B2 (de) 1998-05-20

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US (1) US4977746A (de)
EP (1) EP0379435B2 (de)
JP (1) JPH0672740B2 (de)
AT (1) ATE74421T1 (de)
CA (1) CA2008187C (de)
DE (1) DE69000047D1 (de)
ES (1) ES2030311T5 (de)

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2693220B2 (ja) * 1989-04-24 1997-12-24 テイサン株式会社 超高純度酸素製造方法
US5049173A (en) * 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
US5129932A (en) * 1990-06-12 1992-07-14 Air Products And Chemicals, Inc. Cryogenic process for the separation of air to produce moderate pressure nitrogen
US5231837A (en) * 1991-10-15 1993-08-03 Liquid Air Engineering Corporation Cryogenic distillation process for the production of oxygen and nitrogen
FR2689223B1 (fr) * 1992-03-24 1994-05-06 Air Liquide Procede et installation de transfert de fluide en provenance d'une colonne de distillation, notamment d'air.
JP2966999B2 (ja) * 1992-04-13 1999-10-25 日本エア・リキード株式会社 超高純度窒素・酸素製造装置
US5528906A (en) * 1995-06-26 1996-06-25 The Boc Group, Inc. Method and apparatus for producing ultra-high purity oxygen
FR2739438B1 (fr) * 1995-09-29 1997-10-24 Air Liquide Procede et installation de production d'argon par distillation cryogenique
US5799508A (en) * 1996-03-21 1998-09-01 Praxair Technology, Inc. Cryogenic air separation system with split kettle liquid
GB9607200D0 (en) * 1996-04-04 1996-06-12 Boc Group Plc Air separation
US5628207A (en) * 1996-04-05 1997-05-13 Praxair Technology, Inc. Cryogenic Rectification system for producing lower purity gaseous oxygen and high purity oxygen
US5596886A (en) * 1996-04-05 1997-01-28 Praxair Technology, Inc. Cryogenic rectification system for producing gaseous oxygen and high purity nitrogen
US5682763A (en) * 1996-10-25 1997-11-04 Air Products And Chemicals, Inc. Ultra high purity oxygen distillation unit integrated with ultra high purity nitrogen purifier
DE19817794A1 (de) 1998-04-21 1999-10-28 Basf Ag Hochreine wässrige Wasserstoffperoxid-Lösungen, Verfahren zu ihrer Herstellung und ihre Verwendung
JP4242507B2 (ja) * 1999-04-05 2009-03-25 日本エア・リキード株式会社 超高純度ガスの製造方法及び製造装置
US6173586B1 (en) * 1999-08-31 2001-01-16 Praxair Technology, Inc. Cryogenic rectification system for producing very high purity oxygen
US6263701B1 (en) 1999-09-03 2001-07-24 Air Products And Chemicals, Inc. Process for the purification of a major component containing light and heavy impurities
JP5878310B2 (ja) * 2011-06-28 2016-03-08 大陽日酸株式会社 空気分離方法及び装置
CN103062991B (zh) * 2013-01-24 2015-07-08 成都深冷液化设备股份有限公司 深冷空分装置高纯氧生产系统及高纯氧制备工艺
DE102016011084A1 (de) 2016-09-13 2018-03-15 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines Hochreinsauerstoffproduktstroms durch Tieftemperaturzerlegung von Luft
EP3327393A1 (de) 2016-11-25 2018-05-30 Linde Aktiengesellschaft Verfahren und vorrichtung zur gewinnung eines hochreinsauerstoffproduktstroms durch tieftemperaturzerlegung von luft

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59150286A (ja) * 1983-02-15 1984-08-28 日本酸素株式会社 アルゴンの製造方法
US4615716A (en) * 1985-08-27 1986-10-07 Air Products And Chemicals, Inc. Process for producing ultra high purity oxygen
DE3600835A1 (de) * 1986-01-14 1989-01-05 Porsche Design Gmbh Telefonapparat
US4756731A (en) * 1986-02-20 1988-07-12 Erickson Donald C Oxygen and argon by back-pressured distillation
JPS62210386A (ja) * 1986-03-12 1987-09-16 株式会社日立製作所 空気分離装置
JPS61259077A (ja) * 1986-05-08 1986-11-17 株式会社神戸製鋼所 空気分離方法
US4715874A (en) * 1986-09-08 1987-12-29 Erickson Donald C Retrofittable argon recovery improvement to air separation
US4769055A (en) * 1987-02-03 1988-09-06 Erickson Donald C Companded total condensation reboil cryogenic air separation
US4762542A (en) * 1987-03-20 1988-08-09 The Boc Group, Inc. Process for the recovery of argon
DE3722746A1 (de) * 1987-07-09 1989-01-19 Linde Ag Verfahren und vorrichtung zur luftzerlegung durch rektifikation

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JPH02233984A (ja) 1990-09-17
ES2030311T5 (es) 1998-07-16
EP0379435B2 (de) 1998-05-20
EP0379435A1 (de) 1990-07-25
CA2008187A1 (fr) 1990-07-20
ES2030311T3 (es) 1992-10-16
ATE74421T1 (de) 1992-04-15
DE69000047D1 (de) 1992-05-07
CA2008187C (fr) 1999-12-07
JPH0672740B2 (ja) 1994-09-14
US4977746A (en) 1990-12-18

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