EP1306633A1 - Procédé et dispositif de séparation cryogénique pour la production d'argon et d'oxygène à haute pureté - Google Patents

Procédé et dispositif de séparation cryogénique pour la production d'argon et d'oxygène à haute pureté Download PDF

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Publication number
EP1306633A1
EP1306633A1 EP02001357A EP02001357A EP1306633A1 EP 1306633 A1 EP1306633 A1 EP 1306633A1 EP 02001357 A EP02001357 A EP 02001357A EP 02001357 A EP02001357 A EP 02001357A EP 1306633 A1 EP1306633 A1 EP 1306633A1
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EP
European Patent Office
Prior art keywords
argon
container
oxygen
column
rectification section
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Withdrawn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
EP02001357A
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German (de)
English (en)
Inventor
Dietrich Rottmann
Christian Kunz
Horst Corduan
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Linde GmbH
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Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1306633A1 publication Critical patent/EP1306633A1/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Withdrawn legal-status Critical Current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
    • F25J3/04642—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
    • F25J3/04642—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
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same 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
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • 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

Definitions

  • the invention relates to a process for the production of argon by low-temperature decomposition in which an argon-enriched oxygen fraction into a Raw argon rectification is initiated and from the raw argon rectification crude argon is removed, the crude argon rectification at least a first Rectification section and the argon-enriched oxygen fraction in the first rectification section is initiated, the first rectification section contains at least partially pack.
  • Rectification section here means an area in which countercurrent mass transfer takes place takes place, which means in particular mass transfer elements such as has ordered and / or disordered packing and / or mass transfer trays.
  • Rectification section can be in one container or in several gas and liquid side be arranged in series interconnected containers. It can be about a distillation column, but in particular also a pure reinforcement column and / or act purely a power column. Is a rectification section in more than arranged in a container, preferably prevails essentially in all containers the same pressure. This is achieved in that in the gas line between the No pressure-changing measures are carried out on containers.
  • EP 377117 B2 US 5019145
  • EP 628777 B1 US 5426946
  • the invention is based on the object, in such a system additionally to obtain highly pure oxygen.
  • This object is achieved in that from an intermediate point of the first Rectification section a depleted in less volatile constituents Oxygen fraction is removed and introduced into a pure oxygen column, and that highly pure oxygen is taken from the pure oxygen column.
  • EP 299364 B1 US 4824453
  • their teaching cannot be easily compared with that of Connect EP 628777 B1 or EP 377117 B2 because the latter refer to one Obtain crude argon rectification, that with packing, especially ordered packing, Is provided.
  • EP 299364 B1 US 4824453 requires the deduction of one Intermediate fraction a few soils above the bottom of the crude argon rectification. On however, such a deduction is not acceptable for a packed column Effort. Contrary to these concerns, the invention is nevertheless a Combination of the teachings of the two documents mentioned.
  • the oxygen product is placed in a separate container by the first one Rectification section in a first container and in at least a second container is arranged, the argon-enriched oxygen fraction in the first container introduced and gas from the top of the first container into the second Container is introduced, further a liquid fraction from the lower part of the taken from the second container, a first partial flow of the liquid fraction as Return liquid is fed into the upper area of the first container and the on less volatile constituents depleted oxygen fraction, which in the Pure oxygen column is introduced through a second partial flow of liquid Fraction from the second container is formed.
  • the first container can be as efficient as possible Depletion of less volatile components are designed, the second Container on the oxygen-argon separation.
  • the first container is a mass transfer tray and the second Containers pack, especially ordered pack, has.
  • the first container Preferably contains the first container only floors, for example three to 15, preferably about ten practical floors.
  • the second container can also be combinations of pack and have floors; it preferably contains only an ordered pack.
  • the first container at least partially higher than the pure oxygen column.
  • the first container immediately above the pure oxygen column or the second Be placed container.
  • This allows the residual fraction from the first container, the usually liquid in the swamp, without additional conveyors such as Example, a pump removed from the first rectification section and, for example one step for further processing.
  • the liquid fraction flows solely due to the geodetic Slope back into the low pressure column. In this case, it is advantageous if the first container is placed higher than the intermediate point of the low pressure column to which the liquid fraction flows back.
  • the first and the second partial flow of the liquid fraction from the lower area of the second container can be transported by means of a common conveyor become.
  • the - which is required anyway in the case of a divided crude argon column - Pump at the same time for transporting or lifting the depleted oxygen-depleted components.
  • the first rectification section is in one single container arranged below the intermediate point at which the depleted oxygen fraction depleted of less volatile constituents, Mass transfer trays and packing above this intermediate point, in particular orderly pack. In this way it is also possible to part of the first rectification section, which is used to hold back the less volatile Components can be realized in a particularly cost-effective manner without the Influence argon-oxygen significantly.
  • Both variants of the invention are basically independent of the source of the argon enriched oxygen fraction. They are preferably related applied with a low temperature air separation plant.
  • feed air is in disassembled a two-column system that has at least one high-pressure column and one Has low pressure column, at least part of the feed air in the High pressure column is introduced and the argon-enriched oxygen fraction, which is introduced into a first rectification section, from the low pressure column is subtracted.
  • the crude argon rectification is preferably designed as a "divided crude argon column, by the crude argon rectification having a second rectification section, wherein a oxygen-depleted gas from the first rectification section to the second Rectification section is initiated in which it is further depleted of oxygen.
  • the "first" and the “second” rectification section in the sense of the invention are in arranged in different containers.
  • the invention also relates to an apparatus for the production of argon claims 10 and 11 respectively.
  • a first part 6 of the gaseous top nitrogen 5 of the high pressure column 2 is in the Main condenser 4 against evaporating bottom liquid of the low pressure column 3 liquefied.
  • the condensate 7 obtained in this way is fed into the high-pressure column and used there for the first part as a return.
  • a second part of the liquid Nitrogen 7 from the main condenser 4 is via line 8, a supercooling countercurrent 9, line 10 and throttle valve 11 as a return to the Low pressure column 3 abandoned or via line 12 as a liquid Nitrogen product withdrawn.
  • Liquid crude oxygen is obtained in the sump of the high-pressure column 2. This is about Line 13 also led to the supercooling counterflow 9.
  • the hypothermic Part of crude oxygen 14 is throttled directly into the low-pressure column 3 (16).
  • gaseous nitrogen 17, 18, Impure nitrogen 19, 20, gaseous oxygen 21 and liquid oxygen 22, 23 as Products withdrawn from the low pressure column 3, if necessary after passage by the supercooling counterflow 9.
  • the purity of the oxygen products 21, 23 is, for example, 99.5 to 99.6 mol%. If necessary, part 24 of the Head nitrogen 5 of the high pressure column 2 directly obtained as a gaseous pressure product become.
  • the sieve tray column contains only Soils as mass transfer elements, for example three to 15, preferably about ten practical floors. These floors hold less volatile components like Hydrocarbon, krypton, xenon and carbon dioxide from the rising steam back.
  • the crude argon rectification has two in the exemplary embodiments Rectification sections.
  • the sieve plate column 26 forms together with a first one Crude argon column 28 the "first rectification section" in the sense of the invention ("first Container “26 and” second container “28.
  • The” second rectification section is through realized a second raw argon column 29.
  • These three containers form the Raw argon rectification by removing gas 30 from the top of the sieve plate column 26 via line 31 is led to the bottom of the first crude argon column 28 and the top gas 32 of the first Crude argon column 28 continues to flow to the bottom of the second crude argon column 29 in each case without measures to change the pressure in lines 30, 31 and 32.
  • the return liquid for is in the top condenser 40 of the second crude argon column 29 the entire crude argon rectification (29, 28, 26) is generated.
  • part 41 of the supercooled raw oxygen 14 from the high pressure column 2 in the evaporation chamber of the Head condenser 40 evaporates.
  • Raw argon is gaseous from line 43 from second raw argon column 29 or the top condenser and a pure argon column 44 forwarded to an intermediate point.
  • a nitrogen-rich residual gas 55 deducted, liquid pure argon 45 is obtained in the sump.
  • a top capacitor 46 and a sump evaporator 47 are return liquid in the known manner or rising steam generated.
  • the sieve plate column 26 is arranged so that its sump is on a larger one Height are as the mouth of the lines 25 and 27 in the Low pressure column 3 are. In the example it is above the pure oxygen column 49 built. The pure oxygen column 49 is placed so that it can also be used for its operation no additional pumps are required. For the introduction of the return liquid in both columns 26, 49 - anyway with a divided crude argon column required - pump 37 shared. The residual liquid 27 of the Sieve tray column 26 flows just like the liquid generated in the bottom evaporator 52 54 back to the two-pillar system due to the geodetic gradient alone.
  • the number of trays in the sieve tray column can be easily attributed to the contamination of the Adapt ambient air with less volatile components without this Influence on the other rectification steps.
  • FIG. 1 The heating of the pure oxygen column 49 with nitrogen shown in FIG. 1 is preferred in terms of separation efficiency.
  • Figures 2 and 3 show alternatives for the choice of heating means for the bottom evaporator 52; otherwise differentiate it does not differ from Figure 1.
  • a gaseous fraction which has approximately the composition of the feed air 1, is drawn off from the lower region of the high-pressure column 2 via line 253 and passed into the evaporation space of the bottom evaporator 52.
  • FIG. 3 differs from this in that a partial flow 353 of the feed air 1 is used as heating means for the bottom evaporator 52, which is branched off from the high-pressure column air upstream of the high-pressure column 2.
  • the liquefied air 354 flows back to the high pressure column 2.
  • FIG. 4 The second variant of the invention is shown in FIG. 4 . Only the differences from the system of FIG. 1 are described below.
  • the mass transfer trays 426 which are accommodated in the sieve tray column 26 in FIG are in addition to the packing section 455 in Figure 4 in the first Crude argon column 428.
  • the "first rectification section” is thus in one Containers arranged.
  • Two pumps are necessary here.
  • One (437) encourages them less volatile constituents depleted oxygen fraction 436, the above the sieve trays 426 are removed in liquid form, onto the top of the pure oxygen column 49; a second pump (456) lifts the residual liquid 427 to flow into the To feed low pressure column 3.
  • the bottom evaporator 52 of the pure oxygen column 49 is shown in FIG. 4 as in FIG High pressure column nitrogen 53 heated.
  • the invention can also be applied to systems with crude argon rectification which have only a single (the "first") rectification section.
  • the head condenser 40 is on the liquefaction side with the head of the first Raw argon column 28 connected.
  • Line 32 then leads - in deviation from the Representation in Figure 1 - in the liquefaction space of the top condenser 40; management 33 is connected to the liquefaction space of the top condenser 40 in such a way that the Liquid generated there flows back to the top of the (first) crude argon column 28.
  • a suitable arrangement of the head condenser 40 can dispense with a pump 34 become.
  • the second crude argon column 29 (below the head condenser tank 40) does not apply.

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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)
EP02001357A 2001-10-24 2002-01-18 Procédé et dispositif de séparation cryogénique pour la production d'argon et d'oxygène à haute pureté Withdrawn EP1306633A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10152356 2001-10-24
DE10152356A DE10152356A1 (de) 2001-10-24 2001-10-24 Verfahren und Vorrichtung zur Gewinnung von Argon und hoch reinem Sauerstoff durch Tieftemperatur-Zerlegung

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EP1306633A1 true EP1306633A1 (fr) 2003-05-02

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1211061A2 (fr) 2000-11-30 2002-06-05 Illinois Tool Works Inc. Procédé de formation de sachets à soufflets
EP1211060A2 (fr) 2000-11-29 2002-06-05 Illinois Tool Works Inc. Préparation de fermeture à glissière pour sachet à soufflets

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3327393A1 (fr) * 2016-11-25 2018-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de produit d'oxygène ultrapur par cryogénie de séparation d'air
EP3870915A1 (fr) 2018-10-23 2021-09-01 Linde GmbH Procédé et installation de séparation d'air à basse température
WO2020169257A1 (fr) 2019-02-22 2020-08-27 Linde Gmbh Procédé et installation de décomposition d'air à basse température
WO2023030683A1 (fr) * 2021-09-01 2023-03-09 Linde Gmbh Installation et procédé de fractionnement à basse température de l'air

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5019144A (en) * 1990-01-23 1991-05-28 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with hybrid argon column
EP0446004A1 (fr) * 1990-03-06 1991-09-11 Air Products And Chemicals, Inc. Production d'oxygène ultra-pur par separation d'air cryogénique
US5425241A (en) * 1994-05-10 1995-06-20 Air Products And Chemicals, Inc. Process for the cryogenic distillation of an air feed to produce an ultra-high purity oxygen product
EP0752565A2 (fr) * 1995-07-06 1997-01-08 The BOC Group plc Production d'argon
US5768914A (en) * 1997-07-28 1998-06-23 Air Products And Chemicals, Inc. Process to produce oxygen and argon using divided argon column
EP1103772A1 (fr) * 1999-11-26 2001-05-30 Linde Aktiengesellschaft Dispositif de production d'argon

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5019144A (en) * 1990-01-23 1991-05-28 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with hybrid argon column
EP0446004A1 (fr) * 1990-03-06 1991-09-11 Air Products And Chemicals, Inc. Production d'oxygène ultra-pur par separation d'air cryogénique
US5425241A (en) * 1994-05-10 1995-06-20 Air Products And Chemicals, Inc. Process for the cryogenic distillation of an air feed to produce an ultra-high purity oxygen product
EP0752565A2 (fr) * 1995-07-06 1997-01-08 The BOC Group plc Production d'argon
US5768914A (en) * 1997-07-28 1998-06-23 Air Products And Chemicals, Inc. Process to produce oxygen and argon using divided argon column
EP1103772A1 (fr) * 1999-11-26 2001-05-30 Linde Aktiengesellschaft Dispositif de production d'argon

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1211060A2 (fr) 2000-11-29 2002-06-05 Illinois Tool Works Inc. Préparation de fermeture à glissière pour sachet à soufflets
EP1211061A2 (fr) 2000-11-30 2002-06-05 Illinois Tool Works Inc. Procédé de formation de sachets à soufflets

Also Published As

Publication number Publication date
DE10152356A1 (de) 2002-12-12

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