EP1387136A1 - Process and device for producing impure oxygen by cryogenic air distillation - Google Patents

Process and device for producing impure oxygen by cryogenic air distillation Download PDF

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Publication number
EP1387136A1
EP1387136A1 EP02018727A EP02018727A EP1387136A1 EP 1387136 A1 EP1387136 A1 EP 1387136A1 EP 02018727 A EP02018727 A EP 02018727A EP 02018727 A EP02018727 A EP 02018727A EP 1387136 A1 EP1387136 A1 EP 1387136A1
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EP
European Patent Office
Prior art keywords
oxygen
column
nitrogen
feed air
impure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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EP02018727A
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German (de)
French (fr)
Inventor
Ralph Spöri
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Linde GmbH
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Linde GmbH
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Publication of EP1387136A1 publication Critical patent/EP1387136A1/en
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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
    • F25J3/0446—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases
    • F25J3/04466—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Definitions

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

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Production of impure oxygen by the low temperature decomposition of air in a distillation system for nitrogen-oxygen separation comprises feeding a first process stream into the distillation system, placing an oxygen-rich fraction from the distillation system under pressure and feeding to a mixing column, introducing a heat carrier stream into the mixing column and contacting with the oxygen-rich fraction and removing an impure oxygen fraction. Production of impure oxygen by the low temperature decomposition of air in a distillation system for nitrogen-oxygen separation comprises feeding a first process stream (1, 3) into the distillation system, placing an oxygen-rich fraction (34) from the distillation system under pressure and feeding to a mixing column (39), introducing a heat carrier stream into the lower region of the mixing column and contacting with the oxygen-rich fraction in a counter-current manner, and removing an impure oxygen fraction (46, 47, 49) from the upper region of the mixing column as impure oxygen product. The impure oxygen fraction is expanded. An independent claim is also included for a device for carrying out the production of impure oxygen by the low temperature decomposition of air in a distillation system for nitrogen-oxygen separation.

Description

Die Erfindung betrifft ein Verfahren zur Erzeugung von unreinem Sauerstoff durch Tieftemperaturzerlegung von Luft gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to a method for producing impure oxygen by Cryogenic air separation according to the preamble of patent claim 1.

Das Rektifiziersystem der Erfindung kann als Zwei-Säulen-System, beispielsweise als klassisches Doppelsäulen-System, ausgebildet sein, aber auch als Drei- oder Mehr-Säulen-System. Es kann zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung weitere Vorrichtungen zur Gewinnung anderer Luftkomponenten, insbesondere von Edelgasen (beispielsweise Krypton, Xenon und/oder Argon) aufweisen.The rectification system of the invention can be a two-pillar system, for example as classic double-column system, be designed, but also as a three- or multi-column system. It can be used in addition to the columns for nitrogen-oxygen separation other devices for extracting other air components, especially noble gases (e.g. krypton, xenon and / or argon) exhibit.

Die sauerstoffreiche Fraktion, die als Einsatz für die Mischsäule verwendet wird, weist eine Sauerstoffkonzentration auf, die höher als diejenige von Luft ist und beispielsweise bei 70 bis 99,5 mol-%, vorzugsweise bei 90 bis 98 mol-% liegt. Unter Mischsäule wird eine Gegenstromkontaktkolonne verstanden, in der eine leichterflüchtige gasförmige Fraktion einer schwererflüchtigen Flüssigkeit entgegengeschickt wird.The oxygen-rich fraction used as the insert for the mixing column points an oxygen concentration higher than that of air and for example 70 to 99.5 mol%, preferably 90 to 98 mol%. Under Mixing column is understood to be a countercurrent contact column in which a more volatile gaseous fraction of a less volatile liquid is sent to.

Das erfindungsgemäße Verfahren eignet sich insbesondere zur Gewinnung von gasförmigem unreinen Sauerstoff. Als unreiner Sauerstoff wird hier ein Gemisch mit einem Sauerstoffgehalt von 99,5 mol-% oder weniger, insbesondere von 70 bis 99,5 mol-% bezeichnet. Der Produktdruck liegt in der Regel unterhalb des Betriebsdrucks der Hochdrucksäule (bei Einsatz eines Zwei- oder Mehr-Säulen-Prozesses als Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung), beispielsweise bei 2 bis 4 bar, vorzugsweise bei etwa 3 bar. Selbstverständlich kann das Druckprodukt bei Bedarf in gasförmigem Zustand weiter verdichtet werden. Grundsätzlich kann die Erfindung auch bei Mischsäulendrücken oberhalb des Hochdrucksäulendrucks angewendet werden, zum Beispiel bei 4,5 bis 16 bar, insbesondere bei 5 bis 12 bar. The method according to the invention is particularly suitable for the extraction of gaseous impure oxygen. A mixture with is used here as impure oxygen an oxygen content of 99.5 mol% or less, in particular from 70 to Designated 99.5 mol%. The product pressure is usually below the Operating pressure of the high pressure column (when using a two or more column process as a distillation column system for nitrogen-oxygen separation), for example at 2 to 4 bar, preferably at about 3 bar. Of course you can the printed product can be further compressed in the gaseous state if necessary. Basically, the invention can also at mixing column pressures above the High pressure column pressure are used, for example at 4.5 to 16 bar, especially at 5 to 12 bar.

Mischsäulen-Verfahren und -Vorrichtungen sind in EP 697576 A1 und EP 698772 A1 gezeigt. Bei diesen Systemen wird Kälte mindestens zum Teil durch arbeitsleistende Entspannung von Mischsäulenluft (des "zweiten Einsatzluftstroms") gewonnen.Mixing column methods and devices are described in EP 697576 A1 and EP 698772 A1 shown. In these systems, cold is at least partly caused by work Relaxation of mixing column air (of the "second feed air stream") gained.

Verfahren der eingangs genannten Art sind auch aus EP 531182 A1, DE 19951521 A1 und EP 1139046 A1 bekannt (siehe auch nicht vorveröffentlichte deutsche Patentanmeldungen 10228111 und 10139727, sowie dazu korrespondierende Anmeldungen in weiteren Ländern). Hier wird Verfahrenskälte durch arbeitsleistende Entspannung von Luft in einer Einblaseturbine erzeugt; die Turbinenluft wird anschließend in die Niederdrucksäule eingeführt. Die nicht vorveröffentlichte deutsche Patentanmeldung 10209421 und die und dazu korrespondierenden Anmeldungen in weiteren Ländern offenbaren die Kombination einer Einblase- und einer Mischsäulen-Turbine.Methods of the type mentioned at the outset are also known from EP 531182 A1, DE 19951521 A1 and EP 1139046 A1 known (see also unpublished German Patent applications 10228111 and 10139727, and corresponding ones Registrations in other countries). Here process cold becomes work-performing Relaxation of air generated in a blowing turbine; the turbine air will then inserted into the low pressure column. The unpublished German Patent application 10209421 and the corresponding applications in other countries disclose the combination of a single-bladed and a mixing column turbine.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die wirtschaftlich besonders günstig sind.The invention has for its object a method of the type mentioned and specify a corresponding device that is particularly economical are.

Diese Aufgabe wird dadurch gelöst, dass die Unrein-Sauerstoff-Fraktion arbeitsleistend entspannt wird. Hierbei wird Kälte gewonnen, welche die arbeitsleistende Entspannung von Luft in die Niederdrucksäule (Einblaseturbine) ganz oder teilweise ersetzt. Dadurch wird die Produktausbeute verbessert (verringerter Luftfaktor). Auch beim kostengünstigen Einsatz von Rektifizierböden (zum Beispiel Siebböden) in der oder den Säulen des Destilliersäulen-Systems zur Stickstoff-Sauerstoff-Trennung an Stelle von Packungen kann bei der Erfindung noch ein akzeptabler Energieverbrauch trotz höheren Luftdrucks erreicht werden. Der erhöhte Luftdruck vermindert wiederum den Aufwand bei der Luftreinigung; es kann beispielsweise eine kleinere Molekularsieb-Station eingesetzt werden.This object is achieved in that the impure oxygen fraction does the work is relaxed. Here, cold is gained, which is the work-related relaxation completely or partially replaced by air in the low pressure column (blowing turbine). Thereby the product yield is improved (reduced air factor). Also at inexpensive use of rectification trays (for example sieve trays) in the or the columns of the distillation column system for nitrogen-oxygen separation in place of packs can still be acceptable energy consumption despite the invention higher air pressure can be achieved. The increased air pressure in turn reduces the Effort in air purification; for example, it can be a smaller molecular sieve station be used.

Bei der Erfindung wird die Mischsäule unter einem Druck betrieben, der höher als der Abgabedruck des unreinen Sauerstoffprodukts ist. Dabei ist eine anschließende Weiterverdichtung des Produkts (Außenverdichtung) nicht ausgeschlossen; die Vorteile des erfindungsgemäßen Verfahrens kommen jedoch bei relativ niedrigen Produktdrücken von beispielsweise 2 bis 4 bar, vorzugsweise etwa 3 bar besonders deutlich zum Tragen, bei denen im Allgemeinen keine Weiterverdichtung erforderlich ist. Die Druckdifferenz zwischen Mischsäule und Abgabedruck wird durch die arbeitsleistende Entspannung der Unrein-Sauerstoff-Fraktion zur Erzeugung von Kälte genutzt. Dabei kann jeder bekannte Typ von Entspannungsmaschine zum Einsatz kommen, beispielsweise eine Booster-Turbine; vorzugsweise wird eine ölgebremste Turbine oder eine Generator-Turbine eingesetzt.In the invention, the mixing column is operated under a pressure which is higher than that The discharge pressure of the impure oxygen product is. There is a subsequent one Further compression of the product (external compression) is not excluded; the advantages of the method according to the invention, however, come at relatively low Product pressures of, for example, 2 to 4 bar, preferably about 3 bar particularly clearly to bear, where generally no further compaction is required is. The pressure difference between the mixing column and the discharge pressure is determined by the work-related relaxation of the impure oxygen fraction to generate cold used. Any known type of relaxation machine can be used come, for example a booster turbine; preferably an oil-braked one Turbine or a generator turbine used.

Vorzugsweise wird eine Flüssigkeit aus dem unteren und/oder mittleren Bereich der Mischsäule in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eingeführt.Preferably, a liquid from the lower and / or middle area of the Mixing column in the distillation column system for nitrogen-oxygen separation introduced.

Das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung ist vorzugsweise als Zwei- oder Mehr-Säulen-System ausgebildet und weist eine Hochdrucksäule und eine Niederdrucksäule auf, wobei der erste Einsatzluftstrom in die Hochdrucksäule eingeführt wird und die sauerstoffreiche Fraktion aus der Niederdrucksäule entnommen wird.The distillation column system for nitrogen-oxygen separation is preferably as Two or more column system is formed and has a high pressure column and one Low pressure column, the first feed air flow into the high pressure column is introduced and the oxygen-rich fraction is removed from the low pressure column becomes.

Es ist günstig, wenn der erste Einsatzluftstrom für das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung und der zweite Einsatzluftstrom, der als Wärmeträgerstrom für die Mischsäule dient, gemeinsam auf etwa den Betriebsdruck der Hochdrucksäule verdichtet werden. Dabei wird der zweite Einsatzluftstrom stromabwärts der Verdichtung auf etwa den Betriebsdruck der Hochdrucksäule vorzugsweise nicht nachverdichtet. Auf diese Weise genügt eine einzige Maschine zur Verdichtung von Zerlegungs- und Mischsäulen-Luft.It is favorable if the first feed air stream is used for the distillation column system Nitrogen-oxygen separation and the second feed air flow, which as Heat transfer stream for the mixing column serves, together to about the operating pressure the high pressure column are compressed. The second feed airflow downstream of the compression to approximately the operating pressure of the high pressure column preferably not recompressed. In this way, a single machine is sufficient Compression of separation and mixing column air.

Falls die Kälte, die bei der arbeitleistenden Entspannung der Unrein-Sauerstoff-Fraktion erzeugt wird, nicht für das Verfahren ausreicht, kann selbstverständlich jede andere für die Tieftemperaturzerlegung von Luft bekannte Methode der Kälteerzeugung zusätzlich angewendet werden. Beispielsweise kann Luft auf über Mischsäulen- beziehungsweise Hochdrucksäulen-Druck gebracht und anschließend arbeitsleistend in die Mischsäule oder in die Hochdrucksäule entspannt werden. Günstiger ist im Rahmen der Erfindung jedoch eine Kombination mit einer Einblaseturbine, wobei ein dritter Einsatzluftstrom arbeitsleistend entspannt und in die Niederdrucksäule eingeleitet wird. Hierbei können alle drei Einsatzluftströme in einer einzigen Maschine gemeinsam auf einen einheitlichen Druck verdichtet werden. Der dritte Einsatzluftstrom kann direkt in die Einblaseturbine geleitet oder vorher nachverdichtet werden, vorzugsweise in einem von einer Turbine angetrieben Nachverdichter (Turbinen-Booster).If the cold, the relaxation of the impure oxygen fraction is not sufficient for the process, of course, any another method known for the low temperature separation of air Refrigeration can also be used. For example, air on over Mixing column or high pressure column pressure brought and then can be relaxed while working in the mixing column or in the high pressure column. In the context of the invention, however, a combination with one is more favorable Blow-in turbine, with a third stream of feed air relaxing and into the work Low pressure column is initiated. All three feed air flows can be combined in one single machine can be compressed together to a uniform pressure. The third feed air flow can be directed directly into the blowing turbine or before be post-compressed, preferably driven in one by a turbine Post-compressor (turbine booster).

Die Erfindung betrifft außerdem eine Vorrichtung zur Erzeugung von unreinem Sauerstoff durch Tieftemperaturzerlegung von Luft gemäß Patentanspruch 8.The invention also relates to a device for producing impure Oxygen by low-temperature decomposition of air according to claim 8.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand eines in der Zeichnung schematisch dargestellten Ausführungsbeispiels näher erläutert.The invention and further details of the invention are described below an embodiment shown schematically in the drawing explained.

Ein erster Einsatzluftstrom 1 wird in einem Hauptwärmetauscher, der in dem Beispiel aus zwei seriell verbundenen Blöcken 2a, 2b besteht, auf etwa Taupunkt abgekühlt. Die kalte Luft 3 wird in die Hochdrucksäule 4 eines Destilliersäulen-Systems zur Stickstoff-Sauerstoff-Trennung eingeleitet. Der Betriebsdruck der Hochdrucksäule 4 beträgt beispielsweise 4,3 bis 6,9 bar, vorzugsweise etwa 5,6 bar. Das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung weist außerdem eine Niederdrucksäule 5 auf, die unter beispielsweise 1,3 bis 1,7 bar, vorzugsweise etwa 1,5 bar betrieben wird. Der Kopf der Hochdrucksäule und der Sumpf der Niederdrucksäule 5 stehen über einen gemeinsamen Kondensator-Verdampfer, den Hauptkondensator 6 in wärmetauschender Verbindung. Vor dem Eintritt in den Hauptwärmetauscher 2a wird der erste Einsatzluftstrom 1 auf einen Druck verdichtet (nicht dargestellt), der gleich dem Betriebsdruck der Hochdrucksäule plus Leitungsverlusten ist.A first feed air stream 1 is in a main heat exchanger, which in the example consists of two serially connected blocks 2a, 2b, cooled to about dew point. The cold air 3 is in the high pressure column 4 of a distillation column system for Nitrogen-oxygen separation initiated. The operating pressure of the high pressure column 4 is, for example, 4.3 to 6.9 bar, preferably about 5.6 bar. The distillation column system for nitrogen-oxygen separation also has a low pressure column 5 on, which is operated under, for example, 1.3 to 1.7 bar, preferably about 1.5 bar. The head of the high pressure column and the bottom of the low pressure column 5 protrude a common condenser-evaporator, the main condenser 6 in heat exchanging connection. Before entering the main heat exchanger 2a the first feed air stream 1 is compressed to a pressure (not shown) that is the same the operating pressure of the high pressure column plus line losses.

Sauerstoffangereicherte Sumpfflüssigkeit 7 der Hochdrucksäule 4 wird in einem ersten Unterkühlungs-Gegenströmer 8 abgekühlt, in einem Drosselventil 9 auf etwa Niederdrucksäulen-Druck entspannt und über Leitung 10 der Niederdrucksäule 5 an einer ersten Zwischenstelle zugeführt. Gasförmiger Stickstoff 11 vom Kopf der Hochdrucksäule 4 wird mindestens zu einem ersten Teil über Leitung 12 dem Hauptkondensator 6 zugeführt und dort im Wesentlichen vollständig kondensiert. Der flüssige Stickstoff 13 aus dem Hauptkondensator dient als Rücklauf für Hochdrucksäule und Niederdrucksäule und gegebenenfalls als Flüssigprodukt. Dazu wird ein erster Teil über die Leitungen 14 und 16 durch einen zweiten Unterkühlungs-Gegenströmer 15 in einen ersten Abscheider (Phasentrenner) 17 eingeleitet. Ein zweiter Teil fließt über Leitung 18 in die Hochdrucksäule 4 und wird dort als Rücklauf eingesetzt. Ein weiterer Teil strömt ebenfalls über Leitung 18 in die Hochdrucksäule, wird aber über Leitung 19 wieder entnommen und durch den zweiten Unterkühlungs-Gegenströmer 15 und durch Leitung 20 in einen zweiten Abscheider (Phasentrenner) 21 eingespeist. Die Flüssigkeit 22 aus dem ersten Abscheider 17 wird mindestens zu einem Teil über die Leitungen 23 und 24 als Rücklauf auf die Niederdrucksäule 5 aufgegeben. Die restliche Flüssigkeit 25 kann - wie die flüssige Fraktion 26 aus dem zweiten Abscheider 21 - als flüssiges Stickstoffprodukt gewonnen werden.Oxygen-enriched bottom liquid 7 of the high pressure column 4 is in a first Subcooling countercurrent 8 cooled, in a throttle valve 9 to about Low pressure column pressure is released and via line 10 of the low pressure column 5 fed to a first intermediate point. Gaseous nitrogen 11 from the top of the High-pressure column 4 is at least a first part via line 12 Main capacitor 6 supplied and condensed substantially completely there. The liquid nitrogen 13 from the main condenser serves as a return for High pressure column and low pressure column and optionally as a liquid product. To is a first part via lines 14 and 16 by a second supercooling counterflow 15 introduced into a first separator (phase separator) 17. On second part flows via line 18 into the high pressure column 4 and is there as a return used. Another part also flows via line 18 into the high pressure column, but is removed again via line 19 and through the second subcooling countercurrent 15 and through line 20 into a second separator (phase separator) 21 fed. The liquid 22 from the first separator 17 becomes at least too a part via the lines 23 and 24 as a return to the low pressure column 5 given up. The remaining liquid 25 can - like the liquid fraction 26 from the second separator 21 - can be obtained as a liquid nitrogen product.

Gasförmiger Reinstickstoff 27 vom Kopf der Niederdrucksäule 5 wird gemeinsam mit den Flashgasen 28 und 29 aus den beiden Abscheidem 17, 26 über Leitung 30 abgezogen, in den beiden Unterkühlungs-Gegenströmem 15, 16 und im Hauptwärmetauscher 2b, 2a angewärmt und über Leitung 31 unter etwa Umgebungstemperatur als druckloses gasförmiges Stickstoffprodukt gewonnen. Einige Böden tiefer wird Unrein-Stickstoff 32 gasförmig entnommen, ebenfalls in den beiden Unterkühlungs-Gegenströmern 15, 16 und im Hauptwärmetauscher 2b, 2a angewärmt und über Leitung 33 als Rest- oder Regeneriergas abgeführt.Gaseous pure nitrogen 27 from the top of the low pressure column 5 is shared with the flash gases 28 and 29 from the two separators 17, 26 via line 30 deducted, in the two supercooling countercurrent 15, 16 and in Main heat exchanger 2b, 2a warmed up and via line 31 under about Ambient temperature obtained as a pressureless gaseous nitrogen product. Some Bottom deeper, impure nitrogen 32 is removed in gaseous form, also in the two Subcooling countercurrents 15, 16 and heated in the main heat exchanger 2b, 2a and discharged via line 33 as residual or regeneration gas.

Aus dem Sumpf oder von etwas oberhalb des Sumpfs der Niederdrucksäule 5 wird eine sauerstoffreiche Fraktion 34 flüssig abgezogen, in einer Pumpe 35 flüssig auf Druck gebracht und strömt unter einem gegenüber dem Abzug aus der Niederdrucksäule 5 erhöhten Druck (in der Regel gleich dem Mischsäulen-Druck plus Leitungsverlusten und statischem Druck) wird über die Leitungen 36, 37 und 38 nach Unterkühlung im ersten Unterkühlungs-Gegenströmer 8 und am kalten Ende des Hauptwärmetauschers 2b auf den Kopf einer Mischsäule 39 aufgegeben. Die Mischsäule kann unter demselben Druck wie die Hochdrucksäule 4 betrieben werden, das heißt an mindestens einer Stelle innerhalb der Mischsäule herrscht der gleiche Druck wie an mindestens einer Stelle der Hochdrucksäule. In den Sumpf der Mischsäule wird ein zweiter Einsatzluftstrom 40, 41 eingeblasen, der vorzugsweise unter demselben Druck wie der erste Einsatzluftstrom 1 steht und gemeinsam mit diesem verdichtet wurde (nicht dargestellt). Die Sumpfflüssigkeit 42 - 43 und eine Zwischenflüssigkeit 44 - 45 der Mischsäule 39 werden jeweils in dem ersten Unterkühlungs-Gegenströmer 8 unterkühlt und an den ihrer Zusammensetzung entsprechenden Stellen in die Niederdrucksäule 5 eingedrosselt.From the sump or from slightly above the sump of the low pressure column 5 an oxygen-rich fraction 34 is drawn off in liquid form in a pump 35 Brought pressure and flows under one opposite the trigger from the Low pressure column 5 increased pressure (usually equal to the mixing column pressure plus Line losses and static pressure) is via lines 36, 37 and 38 after Subcooling in the first subcooling countercurrent 8 and at the cold end of the Main heat exchanger 2b placed on the head of a mixing column 39. The Mixing column can be operated under the same pressure as the high pressure column 4, that is to say the same applies to at least one point within the mixing column Pressure as at at least one point on the high pressure column. In the swamp of the Mixing column, a second feed air stream 40, 41 is injected, which is preferably is under the same pressure as the first feed air stream 1 and together with this was compressed (not shown). The bottom liquid 42 - 43 and one Intermediate liquid 44-45 of the mixing column 39 are each in the first Supercooling countercurrent 8 and supercooled on their composition corresponding places throttled in the low pressure column 5.

Vom Kopf der Mischsäule 39 wird eine Unrein-Sauerstoff-Fraktion 46 abgezogen und im Hauptwärmetauscher 2b auf eine erste Zwischentemperatur angewärmt. Unter dieser ersten Zwischentemperatur wird sie über Leitung 47 einer arbeitsleistenden Entspannung 48 zugeführt. Dort tritt sie unter einem Druck von beispielsweise 2 bis 4 bar, vorzugsweise etwa 3 bar und unter einer zweiten, niedrigeren Zwischentemperatur wieder aus und wird über Leitung 49 wieder dem Hauptwärmetauscher 2b zugeführt. Nach vollständiger Erwärmung im Hauptwärmetauscher 2b, 2a wird sie über Leitung 50 als unreines Sauerstoffprodukt gewonnen.An impure oxygen fraction 46 is drawn off from the top of the mixing column 39 and warmed to a first intermediate temperature in the main heat exchanger 2b. Under this first intermediate temperature, it becomes a work-performing line 47 Relaxation 48 fed. There it occurs under a pressure of, for example, 2 to 4 bar, preferably about 3 bar and under a second, lower Intermediate temperature off again and is the line 49 again Main heat exchanger 2b supplied. After complete heating in the It is the main heat exchanger 2b, 2a via line 50 as an impure oxygen product won.

In dem Ausführungsbeispiel wird außerdem ein reineres gasförmiges Sauerstoffprodukt 53 gewonnen, indem flüssiger Sauerstoff 51 vom Sumpf der Niederdrucksäule 5 abgezogen, mittels einer Pumpe 52 auf Druck gebracht (Innenverdichtung) und schließlich im Hauptwärmetauscher 2b, 2a verdampft und angewärmt wird.In the embodiment, a purer gaseous is also Oxygen product 53 obtained by liquid oxygen 51 from the bottom of the Low pressure column 5 withdrawn, brought to pressure by means of a pump 52 (Internal compression) and finally evaporated in the main heat exchanger 2b, 2a and is warmed up.

Wenn auf die Reinsauerstoff-Erzeugung verzichtet wird, kann die sauerstoffreiche Fraktion 34 entgegen der Darstellung in der Zeichnung unmittelbar vom Sumpf der Niederdrucksäule 5 abgezogen werden. In diesem Fall können über eine kontinuierlich oder intermittierend betriebene Spülleitung 54 schwererflüchtige Komponenten ausgeschleust werden. Dabei wird ein kleiner Teil der sauerstoffreichen Fraktion 34 stromabwärts der Pumpe 35 abgezweigt und über die Spülleitung 54 und ein Drosselventil in die Unrein-Sauerstoff-Fraktion 49 stromabwärts der arbeitsleistenden Entspannung 48 eingeführt.If the pure oxygen generation is dispensed with, the oxygen-rich can Fraction 34 contrary to the representation in the drawing directly from the swamp of the Low pressure column 5 are deducted. In this case, you can continuously or intermittently operated flush line 54 less volatile components be removed. A small part of the oxygen-rich fraction 34 branched downstream of the pump 35 and via the flush line 54 and a Throttle valve in the impure oxygen fraction 49 downstream of the work Relaxation 48 introduced.

Als weiteres Produkt kann gasförmiger Druckstickstoff 55, 56 direkt vom Kopf der Hochdrucksäule 4 abgezogen werden.As a further product, gaseous pressurized nitrogen 55, 56 can be taken directly from the top of the High pressure column 4 are withdrawn.

Claims (8)

Verfahren zur Erzeugung von unreinem Sauerstoff durch Tieftemperaturzerlegung von Luft in einem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (4, 5), bei dem ein erster Einsatzluftstrom (1, 3) in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eingeführt wird, eine sauerstoffreiche Fraktion (34) aus dem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung flüssig auf Druck gebracht (35) und auf eine Mischsäule (39) aufgegeben (36, 37, 38) wird, ein Wärmeträgerstrom, insbesondere ein zweiter Einsatzluftstrom (40, 41), in den unteren Bereich der Mischsäule (39) eingeleitet und in Gegenstromkontakt mit der sauerstoffreichen Fraktion (34, 36, 37, 38) gebracht wird und bei dem aus dem oberen Bereich der Mischsäule (39) eine Unrein-Sauerstoff-Fraktion (46, 47, 49) entnommen und als unreines Sauerstoffprodukt (50) abgeführt wird, dadurch gekennzeichnet, dass dass die Unrein-Sauerstoff-Fraktion (46) arbeitsleistend entspannt (48) wird. Process for the production of impure oxygen by low-temperature separation of air in a distillation column system for nitrogen-oxygen separation (4, 5), in which a first feed air stream (1, 3) is introduced into the distillation column system for nitrogen-oxygen separation, an oxygen-rich fraction (34) from the distillation column system for nitrogen-oxygen separation is pressurized liquid (35) and applied to a mixing column (39) (36, 37, 38), a heat transfer stream, in particular a second feed air stream (40, 41), is introduced into the lower region of the mixing column (39) and brought into countercurrent contact with the oxygen-rich fraction (34, 36, 37, 38) and in which an impure oxygen fraction (46, 47, 49) is removed from the upper region of the mixing column (39) and discharged as an impure oxygen product (50), characterized in that that the impure oxygen fraction (46) is relaxed during work (48). Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass eine Flüssigkeit (42, 43, 44, 45) aus dem unteren und/oder mittleren Bereich der Mischsäule (39) in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eingeführt wird.A method according to claim 1, characterized in that a liquid (42, 43, 44, 45) from the lower and / or middle region of the mixing column (39) is introduced into the distillation column system for nitrogen-oxygen separation. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eine Hochdrucksäule (4) und eine Niederdrucksäule (5) aufweist, wobei der erste Einsatzluftstrom (1, 3) in die Hochdrucksäule (4) eingeführt wird und die sauerstoffreiche Fraktion (34) aus der Niederdrucksäule (5) entnommen wird.Method according to claim 1 or 2, characterized in that the distillation column system for nitrogen-oxygen separation has a high-pressure column (4) and a low-pressure column (5), the first feed air stream (1, 3) being introduced into the high-pressure column (4) and the oxygen-rich fraction (34) is removed from the low pressure column (5). Verfahren nach Anspruch 3, dadurch gekennzeichnet, dass der erste Einsatzluftstrom (1, 3) für das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung und der zweite Einsatzluftstrom (40, 41), der als Wärmeträgerstrom für die Mischsäule (39) dient, gemeinsam auf etwa den Betriebsdruck der Hochdrucksäule (4) verdichtet werden. A method according to claim 3, characterized in that the first feed air stream (1, 3) for the distillation column system for nitrogen-oxygen separation and the second feed air stream (40, 41), which serves as a heat transfer stream for the mixing column (39), together be compressed to approximately the operating pressure of the high pressure column (4). Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass der zweite Einsatzluftstrom (40, 41) stromabwärts der Verdichtung auf etwa den Betriebsdruck der Hochdrucksäule (4) nicht nachverdichtet wird.A method according to claim 4, characterized in that the second feed air stream (40, 41) downstream of the compression to about the operating pressure of the high pressure column (4) is not post-compressed. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass ein dritter Einsatzluftstrom arbeitsleistend entspannt und in die Niederdrucksäule eingeleitet wird.Method according to one of claims 1 to 5, characterized in that a third stream of feed air is expanded to perform work and is introduced into the low pressure column. Verfahren nach Anspruch 4 und 6, dadurch gekennzeichnet, dass der dritte Einsatzluftstrom gemeinsam mit dem ersten und dem zweiten Einsatzluftstrom auf etwa den Betriebsdruck der Hochdrucksäule verdichtet wird.A method according to claim 4 and 6, characterized in that the third feed air stream is compressed together with the first and second feed air stream to approximately the operating pressure of the high pressure column. Vorrichtung zur Erzeugung von unreinem Sauerstoff durch Tieftemperaturzerlegung von Luft mit einem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (4, 5) und einer Mischsäule (39) mit einer ersten Einsatzluftleitung (1, 3) zur Einleitung eines ersten Einsatzluftstroms in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung, einer Flüssigkeitsleitung (34, 36, 37, 38) zur Entnahme einer sauerstoffreichen Fraktion aus dem Destilliersäulen-System, die durch Mittel zur Druckerhöhung im flüssigen Zustand, insbesondere durch eine Flüssigpumpe (35), führt und mit dem oberen Bereich der Mischsäule (39) verbunden ist, eine Wärmeträgerleitung (40, 41) zur Einleitung eines Wärmeträgerstroms, insbesondere eines zweiten Einsatzluftstroms, in den unteren Bereich der Mischsäule (39) und mit einer Produktleitung (46, 47, 49, 50) zur Entnahme einer Unrein-Sauerstoff-Fraktion aus dem oberen Bereich der Mischsäule (39) und zum Abführen der Unrein-Sauerstoff-Fraktion als unreines Sauerstoffprodukt, gekennzeichnet durch eine Entspannungsmaschine (48) zur arbeitsleistenden Entspannung der Unrein-Sauerstoff-Fraktion. Device for generating impure oxygen by low-temperature separation of air with a distillation column system for nitrogen-oxygen separation (4, 5) and a mixing column (39) with a first feed air line (1, 3) for introducing a first feed air flow into the distillation column system for nitrogen-oxygen separation, a liquid line (34, 36, 37, 38) for removing an oxygen-rich fraction from the distillation column system, which leads through means for increasing the pressure in the liquid state, in particular through a liquid pump (35), and with the upper region of the mixing column (39) connected is, a heat transfer line (40, 41) for introducing a heat transfer stream, in particular a second feed air stream, into the lower region of the mixing column (39) and with a product line (46, 47, 49, 50) for removing an impure oxygen fraction from the upper area of the mixing column (39) and for removing the impure oxygen fraction as an impure oxygen product, marked by a relaxation machine (48) for work-relieving the impure oxygen fraction.
EP02018727A 2002-08-02 2002-08-21 Process and device for producing impure oxygen by cryogenic air distillation Withdrawn EP1387136A1 (en)

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DE102011015429A1 (en) 2011-03-29 2012-10-04 Linde Ag Method involves for operating rebox burner, involves removing gaseous oxygen stream from upper region of mixing column and leading out oxygen product used for production of gas mixture
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WO2014067662A2 (en) 2012-11-02 2014-05-08 Linde Aktiengesellschaft Process for the low-temperature separation of air in an air separation plant and air separation plant
DE102013002094A1 (en) 2013-02-05 2014-08-07 Linde Aktiengesellschaft Method for producing liquid and gaseous oxygen by low temperature separation of air in air separation system in industrial application, involves feeding feed air flow to portion in mixed column and to another portion in separating column
DE102015015684A1 (en) 2015-12-03 2016-07-21 Linde Aktiengesellschaft Process for the cryogenic separation of air and air separation plant
EP3179187A1 (en) 2015-12-07 2017-06-14 Linde Aktiengesellschaft Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus
EP3179186A1 (en) 2015-12-07 2017-06-14 Linde Aktiengesellschaft Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus

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