DE2044363A1 - Process for the production of nitrogen and oxygen - Google Patents

Process for the production of nitrogen and oxygen

Info

Publication number
DE2044363A1
DE2044363A1 DE19702044363 DE2044363A DE2044363A1 DE 2044363 A1 DE2044363 A1 DE 2044363A1 DE 19702044363 DE19702044363 DE 19702044363 DE 2044363 A DE2044363 A DE 2044363A DE 2044363 A1 DE2044363 A1 DE 2044363A1
Authority
DE
Germany
Prior art keywords
nitrogen
fraction
pure
separation
liquid
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.)
Granted
Application number
DE19702044363
Other languages
German (de)
Other versions
DE2044363C2 (en
Inventor
Guy Sucy en-Bne; Anseimini Jean-Pierre Paris; Perrotin (Frank reich)
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of DE2044363A1 publication Critical patent/DE2044363A1/en
Application granted granted Critical
Publication of DE2044363C2 publication Critical patent/DE2044363C2/en
Expired legal-status Critical Current

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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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    • 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
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    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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    • 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
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    • 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
    • F25J3/04309—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 nitrogen
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    • 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
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    • 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
    • F25J3/04309—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 nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
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    • 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
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    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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    • F25J3/044—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 single pressure main column system only
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    • F17C2265/00—Effects achieved by gas storage or gas handling
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    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Description

Prankreich, Vo.' S.V. 69 50785France, Vo. ' S.V. 69 50785

Die Erfindung "betrifft ein Verfahren und eine Anlage zur Gewinnung von Sauerstoff und eines erheblichen Stickstoffantei-Ie8 einerseits in flüssiger Pore und andererseits in 9asiora bei einem oder mehreren Druokniveaus aus Luft und einer Quelle für verfügbare Kältekalorien, beispielsweise aue einem in Wjederverdampfung stehenden verflüssigten Naturgas. Beiner Sauerstoff und ein erheblicher Anteil reinen Stickstoffe in fltieei-•ger oder Sasform unter Druck gleichseitig «u gewinnen, gelingt mittels verschiedener bekannter Verfahren und Anlagen6 S® ist es Tsöglioh, in swei Stuft» au arbeiten, indtß «en ^ft auf einen Bsisek von beieyielswtiM 6 bar ko«priisitrt? die Init reinigtf abkühlt^ partiell kpadtnsiert und in einer DoppeIko- „. The invention "relates to a method and a system for the production of oxygen and a considerable amount of nitrogen on the one hand in liquid pores and on the other hand in 9asiora at one or more pressure levels from air and a source of available cold calories, for example aue liquefied natural gas which is in any evaporation. legged oxygen and a significant proportion pure nitrogens ger in fltieei- • or Sasform under pressure equilateral "u win, succeed by various known methods and equipment 6 S® is Tsöglioh in SWEi Scales" working au, indtß 's ^ ft on a Bsisek from beieyielswtiM 6 bar ko «priisitrt ? The init cleans f cools ^ partially kpadtnsiert and in a double box .

1O08ie/U381O08ie / U38

BAD ORIGINALBATH ORIGINAL

-2- 204A363-2-204A363

lonne destilliert, deren Niederdruckabteilienlg oberhalb Luftdruck steht· Die so erhaltenen Gase sind jedoch zum größten Seil Produkte von niedrigen Druck. Außerdem ist in allen Fällen die Menge des unmittelbar unter Brück oder iutlüssiger Porm erzeugten Gases äußerst beschränkt. Die Gase von niedrigem Druok müssen tatsächlich auf einen hohen Druck wieder verdichtet werden, und diejenigen, die man in flüssiger Porraeehalten will, müssen in einem Verflüssigungsgerät behandelt werden.lonne distilled, the Niederdruckabteilienlg above atmospheric pressure stands · The gases obtained in this way, however, are the greatest Rope products of low pressure. Also is in all Cases the amount of the immediately under bridge or iutlüssiger Porm generated gas is extremely limited. The gases of low Druok actually have to be recompressed to a high pressure, and those that are kept in liquid leek must be treated in a condensing unit.

Es ist auch möglich, unmittelbar bei hohem oder mittlerem Druck zu arbeiten« Die erforderliche Kälteisistung wird dann entweder durch «rbeitsleistenda Intgpsmmsg eines (Deils der »uvor behandelten Luft und auf sehr feeiien Druck von 100 bis 200 bar verdichteten Luft od®r mittels eines Eältezyklus mit äuSerer Arbeitsleistung unter Behandlung von gereinigter Luft, die nan rsicyeliert, eier vom Stickstoff erzielt.It is also possible to go straight to high or medium Pressure to work «The required refrigeration is then either through the work of an Intgpsmmsg (Deils der »Previously treated air and at a very low pressure of 100 to 200 bar compressed air or by means of a cold cycle external work performance with the treatment of purified air, the nan rsicyelized, eggs obtained from nitrogen.

wmn Sauerstoff wßä. einem starken Sticketeffanteil in öasfom unter Druok und/oder in flüssiger Fertg gewinnen will, •rweigSE sich die bekannten Terfatoreii βίε siebt Tüllig befriedigend. Sie erfordern nämlieb einen seißtiT bohen Bpezifieohes wmn oxygen wßä. A strong Sticketeff share in öasfom under Druok and / or in liquid Fertg wants to gain, • Tüllig sifts the well-known Terfatoreii βίε satisfactorily. They actually require a small body specific

und hQh& Auleg®kasten«and hQh & Aule g® box «

Sie lEfißÄua^et 9iob £ie Xuffabe gesll^y t-i#\< lifes^l su b^- beben lad «ußtjfde« fewi©s« s^sltßliefee ¥crttil*;; wit Hinfaob« heit dtr Birebftitessig «ai lsii«#»g«f!MiJE*it #a Alt- Btdiafunf ir. «reitltB$i!bts tine ^«ϋϊϊβ iiitses ^llt«l£ilsi*i#s au ver-Sie lEfissÄua ^ et 9iob £ ie Xuffabe gesll ^ y ti # \ <lifes ^ l su b ^ - quake lad «ußtjfde« fewi © s «s ^ sltßliefee ¥ crttil * ;; wit Hinfaob «means dtr Birebftitessig« ai lsii «#» g «f! MiJE * it #a Alt- Btdiafunf ir.« reitltB $ i! bts tine ^ «ϋϊϊβ iiitses ^ llt« l £ ilsi * i # s au ver

BAD ORiG/WAfBAD ORiG / WAf

109816/1430109816/1430

fügen.put.

Gegenstand der Erfindung ist ein Verfahren zur Gewinnung von Sauerstoff und eines starken Stickstoffanteiles, gegebenen* falls einerseits in flüssiger Form und andererseits in frasform, bei dem man einen Teil des reinen wiedererwärmten Stickstoffgases, das aus der Trennstufe stammt, verdichtet durch Austausch mit einem in der Verdampfung.'stehenden flüssigen Naturgas abkühlt und kondensiert, sowie entspannt, wobei mindestens A ein Teil der entspannten flüssigen Fraktion ausgenutzt wird, um den Rückfluß dieser Trennetufe sicherzustellen, und die verdampfte Fraktion mit dem zu verdichtenden Stickstoff vor dieser Verdichtung vereinigt wird, und das dadurch gekennzeichnet ist, daß der Stickstoff in flüssiger Form und in Gasform sowie der Sauerstoff auf mehreren Bruckniveaus erhalten werden und daß der Teil des reinen erwärmten Stickstoffgases, der mit einem Teil des vor dem Ende der Erwärmung abgezogenen Stickstoff gases vereinigt wird, nach Kondensation und vor seiner Entspannung durch Ge gens tr umführung zu der Fraktion unterkühlt wird, die im Verlauf der Entspannung gegebenenfalls schließlich durch Wärmeaustausch mit der reinen flüssigen Sauerstofffraktion, die man am Boden der Trennstufe erhält, wieder kondensiert» und nach Unterkühlung mit dem Stickstoff von Mittel druck vereinigt wird.The subject of the invention is a process for the production of oxygen and a high proportion of nitrogen, possibly in liquid form on the one hand and in milled form on the other hand, in which part of the pure re-heated nitrogen gas that comes from the separation stage is compressed by exchanging it with one in the Evaporation. 'Standing liquid natural gas cools and condenses, as well as expanded, with at least A part of the expanded liquid fraction is used to ensure the reflux of this separation stage, and the vaporized fraction is combined with the nitrogen to be compressed before this compression, and that as a result is characterized in that the nitrogen in liquid form and in gas form as well as the oxygen on several B r uckniveaus be obtained, and that the part of the pure heated nitrogen gas, the gas is combined with a part of the withdrawn before the end of heating nitrogen, after condensation and before he relaxes As opposed to bypassing, the fraction is supercooled, which in the course of the expansion is eventually condensed again by heat exchange with the pure liquid oxygen fraction obtained at the bottom of the separation stage and, after supercooling, is combined with the nitrogen of medium pressure.

Bei» Verfahren der Sj-fladung lassen sich die Gasverdichtungen auf ein Mindestmaß beschränken, diese Verdichtungen sich tauglichst häufig bei niederer Temperatur durchführest, die Anzahl und eingesetzte gesamte Maschinenleistung vezmdLndern und dieWith the »Sj-loading process, the gas compressions Limit the number to a minimum, these densifications are often carried out most suitably at a low temperature and total machine power used and the

109S16/H36109S16 / H36

Bemessung der Austauscher in erheblichem Maße begrenzen, well die Gase unter Brück oder im Zustand der Verflüssigung-Verdampfung in der Hauptaustauschleitung behandelt werden.Sizing the exchanger to a considerable extent, well the gases are treated under bridge or in the state of liquefaction-evaporation in the main exchange line.

Ferner gestattet die Erfindung den Betrieb einer Anlage zur Gewinnung von Sauerstoff und eines starken Stickstoffanteiles in Gasform und unter Durck und/oder in flüssiger Form zu vereinfachen, denn eine solche Anlage benötigt nur eine kleine Anzahl von Kompressoren und eine einzige Turbine, und diese Maschinen bestehen im allgemeinen aus Zentrifugen. Außerdem ist eine solche Anlage derart flexibel, daß die verschiedenen Produkte mit sehr veränderlichen Mengen äußerer Kältekalorien erhalten werden können, die im gegebenen Fall sogar fortfallen kSnnen· Außerdem lassen sich die Mengenverhältnisse zwischen den verschiedenen Produkten in sehr weiten Grenzen abwandeln.Furthermore, the invention allows the operation of a system for To simplify the extraction of oxygen and a high proportion of nitrogen in gas form and under pressure and / or in liquid form, because such a system only requires a small one Number of compressors and a single turbine, and these machines generally consist of centrifuges. aside from that Such a system is so flexible that the various products with very variable amounts of external cold calories can be obtained, which can even be omitted in the given case · In addition, the quantitative ratios between modify the various products within very wide limits.

Gemäß einer Ausführungeform der Erfindung wird mindestens ein Teil der so entspannten verflüssigten Fraktion zumindest teilweise zur Gewinnung einer entspannten, flüssigen, reinen Stickstoff fraktion benutzt; diese flüssige Fraktion wird zuvor im Gegenstrom mit einer im Verlauf dieser letzten Entspannung verdampften Fraktion unterkühlt.According to one embodiment of the invention, at least part of the so relaxed liquefied fraction is at least partially used to obtain a relaxed, liquid, pure nitrogen fraction; this liquid fraction is previously im Countercurrent with one in the course of this last relaxation evaporated fraction is supercooled.

Nach einem weiteren Merkmal der Erfindung wird ein Teil des aus dieser Trennung stammenden reinen flüssigen Sauerstoffs verdichtet, wiedererwärmt und verdampft, während der andere Teil im Gegenstom mit einer im Verlauf der letzten Entspannung verdampften Fraktion unterkühlt und teilweise im flüssigen Zustand entspannt erhalten wird.According to a further feature of the invention, some of the pure liquid oxygen resulting from this separation is used compressed, reheated and evaporated, while the other part is supercooled in the countercurrent with a fraction evaporated in the course of the last relaxation and is partly kept relaxed in the liquid state.

109816/U3S109816 / U3S

Gemäß einem Merkmal der Erfindung wird die Verdichtung des wiedererwärmten' Stickstoffgase· in einer einzigen Stufe oder in mehreren getrennten Stufen, vorzugsweise in zwei Stufen, durch Übergang auf einen Zwischendruck bewirkt.According to a feature of the invention, the compression of the reheated nitrogen gases in a single stage or in several separate stages, preferably in two stages, caused by transition to an intermediate pressure.

Gemäß einem anderen Merkmal der Erflndung wird das verdichtete, gekühlte und durch Wärmeaustausch mit einem in Wiederverdampfung stehenden flüssigen Naturgas kondensierte Stickstoffgas in mindestens zwei Stufen vor zwei aufeinanderfolgenden Entspannungen unterkühlt) die im Verlauf der ersten Entspannung verdampfte und für die erste Unterkühlung verwendete Fraktion wird mit einem*Teil des auf Mitteldruck verdichteten Stickstoffs vereinigt, dann vorzugsweise durch Austausch mit der bei der Trennung erhaltenen an Sauerstoff angereicherten flüssigen Fraktion verflüssigt, anschließend vorzugsweise durch Austausch mindestens mit dem aus der Trennung stammenden reinen Stickstoffgas unterkühlt und schließlich mit der flüssigen Fraktion vereinigt, die man nach der ersten Entspannung erhält, bevor diese der zweiten Entspannung unterzogen wird.According to another feature of the E r flndung is compressed, subcooled cooled and condensed by heat exchange with a standing in regasification liquid natural gas is nitrogen gas in at least two stages before two successive relaxations) the fraction evaporated in the course of the first relaxation and used for the first sub-cooling is combined with a part of the nitrogen compressed to medium pressure, then preferably liquefied by exchange with the oxygen-enriched liquid fraction obtained in the separation, then preferably subcooled by exchange with at least the pure nitrogen gas originating from the separation and finally combined with the liquid fraction, obtained after the first relaxation before it is subjected to the second relaxation.

Nach einem anderen Merkmal der Erfindung erfolgt diese Trennung durch Destillation unter einem einzigen Druck eder duroh Destillation unter zwei verschiedenen Drücken.According to another feature of the invention, this separation is carried out by distillation under a single pressure or duroh Distillation under two different pressures.

'Gemäß einem anderen Merkmal der Erfindung wird ver der Trennung duroh Destillation die Luft Auf ein erste· Druokniveau verdichtet, gereinigt, alsdann duroh Austausch alt einer Maturgasfraktien gekühlt und sohliefllioh auf eia hiheres Bruekniveau verdichtet·According to another feature of the invention, prior to the separation by distillation, the air is brought to a first pressure level compacted, cleaned, then by exchanging old one Matur gas fractions cooled and condensed to a higher bridge level

109816/U38109816 / U38

Gemäß einer Ausführungsform der Erfindung erhält man ein oder mehrere der folgenden Bestandteile: Reinen Stickstoff und reinen Sauerstoff in flüssigem Zustand bei verhältnismäßig niedrigem Druck (beispielsweise Luftdruck) reines Stlokstoffgas und reines Sauerstoffgas bei mittlerem Druck (beispielsweise in der GrSSesiordnung von 5 bar), reines Stickstoffgas und reines Sauerstoff gas bei hohen, gegebenenfalls verschiedenen Drücken (*. B. 15 bxw. kO bar)« Durch Entspannung eines Teils des aus der Trennung stammenden reinen flüssigen Sauerstoffes nach Unterkühlung durch die für die Entspannung vorgesehenen Gasfraktion; durch Entspannung eines Teiles des in Gasform aus der Trennung stammenden reinen verflüssigten Stickstoffs, dor in ein oder mehreren Stufen auf diesen hohen Druck verdichtet, dann gekühlt und durch Austausch mit in der Verdampfung stehendes flüssigen Naturgas verflüssigt und in ein oder mehreren Stufen nach ein oder mehreren Unterkühlungen mit der in Verlauf dieser Entspannungen erhaltenen Gasfraktlonen entspannt worden ist; durch Verdampfung und Wiedererwärmung eines Teil· des aus der Trennung stammenden reinen flüssigen Sauerstoffs} durch Erwärmung eines Teils des aus der Trennung stammenden reinen Stickstof f gases ι durch Verdichtung eines Teils des aus der Trennung mit anschließender Verdampfung und Wiedererwärmung stammenden flüssigen reinen Sauerstoff·) durch Verdichtung ein·· Teil· de· aus der Trennung stammenden reinen Stickstoff gases; das suver mindestens «um Teil vollständig «xitltxmt worden ist.According to one embodiment of the invention, one or more of the following components are obtained: pure nitrogen and pure oxygen in the liquid state at relatively low pressure (for example air pressure) pure nitrogen gas and pure oxygen gas at medium pressure (for example in the order of 5 bar), pure nitrogen gas and pure oxygen gas at high, possibly different pressures (*. B. 15 bxw. kO bar) «By expansion of part of the pure liquid oxygen from the separation after subcooling by the gas fraction intended for expansion; by expanding part of the pure liquefied nitrogen from the separation in gaseous form, which is compressed to this high pressure in one or more stages, then cooled and liquefied by exchanging it with liquid natural gas that is in the process of evaporation, and in one or more stages after one or more Undercooling with the gas fractions obtained in the course of these relaxations has been relaxed; by evaporation and reheating of part of the pure liquid oxygen originating from the separation by heating part of the pure nitrogen gas originating from the separation by compressing part of the pure liquid oxygen originating from the separation with subsequent evaporation and reheating) Compression of a ·· part · of the pure nitrogen gas from the separation; the suver has been at least partially completely xitltxmt.

Gegenstand der Erfindumg ist aueh ein· Anlage ier Durchführung d·· V«rfahr«it· aaeh der Erfindung.The subject of the invention is also an appendix to the implementation of the method of the invention.

109816/14-36109816 / 14-36

Andere Merkmale und Vorteile der Erfindung ergehen sich aus der nachstehenden Beschreibung bevorzugter Ausführungsformen der Erfindung anhand der Zeichnung.Other features and advantages of the invention will emerge the following description of preferred embodiments of the invention based on the drawing.

Fig. 1 Zeigt eine Ausführungsform einer Anlage nach der Erfindung mit einer doppelten Destillierkolonne und nur einer Verdichtung»stufe für reines Stickstoffgas.Fig. 1 shows an embodiment of a plant according to the invention with a double distillation column and only a compression stage for pure nitrogen gas.

Fig. 2 zeigt eine andere Ausführungsform einer Anlage nachFig. 2 shows another embodiment of a system according to

der Erfindung mit einer Destillierkolonne unter einem einfachen Druck und zwei Verdichtungsstufen des reinen Stickstoffgases.of the invention with a distillation column under one simple pressure and two stages of compression of the pure Nitrogen gas.

Fig. 1 erläutert eine Anwendung des Verfahrens für den Fall, wo man gleichzeitig Sauerstoffgas unter 5 und hO bar, Stickstoff gas unter 5 und 15'bar, flüssigen Sauerstoff und flüssigen Stickstoff unter Ausnutzung der Kältekalorien eines in Verdampfung stehenden verflüssigten Naturgases herstellen will· Die zu behandelnde Luft tritt nach Filtrierung in die Anlage durch Leitung 1 ein. In den ersten Stufen des isothermen Kompressor 2 wird sie auf 6 bar verdichtet und dann durch Adsorption von Wasser und Kohlendioxid in der Reinigungsstufe 3 gereinigt. Anschließend wird die in dem von einer Naturgasfraktion durchströmten Austauscher h auf etwa -100 C gekühlt und durch Leitung 5 iß die höheren Stufen des Verdichters 2 wieder eingeführt, von wo sie mit dem Druck von ungefähr 15 bar austritt· Anschließend wird sie durch Leitung 6 in die Austauscher 7 eingeführt, in denen sie gekühlt und teilweise verflüssigt wird. Durch Leitung 8 tritt sie in dieFig. 1 explains an application of the method for the case where you want to simultaneously produce oxygen gas below 5 and hO bar, nitrogen gas below 5 and 15 'bar, liquid oxygen and liquid nitrogen using the cold calories of a liquefied natural gas in evaporation Air to be treated enters the system through line 1 after filtration. In the first stage of the isothermal compressor 2 it is compressed to 6 bar and then cleaned by adsorption of water and carbon dioxide in the cleaning stage 3. Subsequently, the h in the perfused by a natural gas fraction exchanger cooled to about -100 C and i through conduit 5 ß the higher stages of the compressor 2 is introduced again from where it exits with the pressure of about 15 bar · Then it is passed through line 6 introduced into the exchanger 7, in which it is cooled and partially liquefied. Through line 8 it enters the

109816/U36109816 / U36

MitteldrucklcQloruae 9 ein, wo sie eine erste Rektifiaierung erfährt.Medium pressure lcQloruae 9 a, where they do a first rectification learns.

Aus dieser Kolonne sieht nsaa drei flüssige Fraktionen abs Blue aaueretoffreiob® Fraktion durch Leitung 10, «Int rein© Stickstof fraktion durcb Leitung 11 und eine Traktion τοη eiiior-wZwisohensuBaiBiaensetEung durch Leitung 12· Diese drei Iraktionon werden In den Austaueoltern 13 in Cegenstrora »it «üb der Solonno 14 koanen&en Produkten vor ihrer Einführung in dies»From this column nsaa sees three liquid fractions abs Blue aaueretoffreiob® fraction through line 10, «Int rein © Nitrogen fraction through line 11 and a traction τοη eiiior-wZwisohensuBaiBiaensetEung through line 12 Solonno 14 koanen & en products before their introduction to this »

unteren fell der Kolonne 14 Mebt »aiii abs Sine»-Denier β toff gas tmter 5 bar durob Leittmg 15» das dann Inlower head of column 14 Mebt »aiii abs Sine »-Denier β toff gas tmter 5 bar durob Leittmg 15» that then In

Austeueober 7 wiedorerwäiEfe wird,Austeueober 7 will be again

MBignn Saaerßtoff (Iu:eob Leitung 16: Hn Seil bierron wird den 3?oapen 17 auf 40 bar vordichtet und dan-η In den Auss^eokern 7 'rardeispft und wiedererwarat; ein «weiter Seil wird i des Untörkübler 19 geleitet* wo er sieb 1» Qegenetre* «it ->? PreTrtion abküblt, die In der auf diesen lueteueober fei- «adefr-iöitspennungBTaasobine verdaopft ist· MBignn Saaerßtoff (Iu: eob line 16: Hn rope bierron is pre-sealed the 3? Oapen 17 to 40 bar and then in the Aus ^ eokern 7 'rardeispft and reapplied; a «further rope is led into the Untörkübler 19 * where it sieve 1 "Qegenetre *" it ->? PreTrtion abküblt, which in the fei-

Tcrdanpfte fraktion wird durob Leitung 20 la da» Bobrbünfür unreinen Stickstoff «urüclcgebrecht· Xm »ittlean feil der Kolonne 14 Kleist »an den unreinen Stlokatoff ab, der im den Auvtaueoaern 15 und einem Seil der Austauscher 7 wlv» derexvÄrwt wird, bevor er In der !Turbine 21 entepennt und dann In leitung 20 vledererwgrat wird· in der Spitee siebt «an dia reine Stioketoffraktion duroh leitung 22 *b. Sie wirdRequired fraction is thrown from the line 20 la da "Bobrb5 for impure nitrogen". Xm "ittlean fil of the column 14 Kleist" from the impure Stlokatoff, which in the Auvtaueoaern 15 and a rope of the exchanger 7 wlv "derexvärwt, before it is in the ! Turbine 21 detached and then in line 20 vledererwgrat is · in the Spitee siebt «to the pure Stioketoff fraction duroh line 22 * b. she will daasi in dem Austausdarn 15 erwärat und verlÄBt »le unter eint»daasi heats up in the Ausausdarn 15 and leaves "le under one"

109816/U36109816 / U36

Druck von 5 Vsr In Leitung 25» Ein Teil dieser Fraktion viril durob-Leitung 24 innerhalb der Austauscher 7 vor ihrer vollständigen Erwärmung abgezogen und dann ait einem Seil dee an warmen -Ende der Austausober 7 erhaltenen Stickstoffe verwischt· Bach Vermischung «it kalten Stickstoff von 5 bar aus der XeI* tun®*25U(e£he nachstehend) wird diese Traktion in Kompressor 26 verdichtet, der bei tiefer Temperatur arbeitet· Während der Verdichtung in Kompressor 26 sieht man eine Stickstoffraktion von 15 bar ab, die durch leitung 27 unmittelbar aur VerbrauobssteHe geschickt wirdPressure of 5 Vsr In line 25 “Part of this fraction virile Durob line 24 within the exchanger 7 withdrawn before they are completely heated and then ait a rope dee on warm end of the exchange of 7 nitrogen obtained blurred Bach mixing "with cold nitrogen of 5 bar from the XeI * tun® * 25U (e £ he below) turns this traction into supercharger 26 compressed, which works at low temperature · During the Compression in compressor 26 shows a nitrogen fraction from 15 bar, which is sent directly to the consumption booth through line 27

Her Beat des Stickstoffβ wird auf 40 bar verdichtet und dann in Auetausoher23 in Gegenstron nit in Verdampfung stehenden naturgas von 70 bar gekühlt und kondensiert» Dieser ver/IUesigte Stickstoff wird in Austauscher 29 in eegenstronj&it der Traktion unterkühlt t die während der auf diesen Austauscher folgenden Entspannung auf 5 bar verdanpft worden ist· Sie ver» danpfte Traktion wird but Saugseit* des Xonprassors 26 duroh leitung 25 suxüokgebraoht·Her beat of Stickstoffβ is compacted bar to 40 and then in Auetausoher23 in Gegenstron nit in evaporation stationary natural gas 70 cooled bar and condensed "This ver / IUesigte nitrogen is in exchanger 29 in eegenstronj & ith the traction subcooled t during the exchanger on these following relaxation has been evaporated to 5 bar · The evaporated traction is but suction side * of the Xonprassors 26 duroh line 25 suxüokgebraoht ·

in Srenngefäß 30 erhaltene flüatge Stickstoff von 5 bar dient swtai Zweokeni Sin Soil wird durch Leitung 31 sun unter«* kühler 32 geleitet und dann entspannt· Die so in XrenngeffiS 33 aufgefangene flüssige S*raktion wird suv Verbrauohsstelle «•schickt, Si· während der Entspannung verdanpft· Traktion vereinigt sieh ait den unreinen Stickstoff durcb Leitung 20. 3Q*r aadar· Seil des flüssigen Stickstoffes au* den frtnagefaaFlüatge nitrogen of 5 bar obtained in separation vessel 30 serves swtai Zweokeni Sin Soil is served by line 31 sun under «* cooler 32 and then relaxed · The so in XrenngeffiS 33 liquid fraction collected becomes suv consumption point «• sends, you · owe traction during relaxation combined see the impure nitrogen through line 20. 3Q * r aadar · rope of liquid nitrogen au * den frtnagefaa

'bad'bath

- ίο - : ! 2U44363- ίο -: 2U44363

30 wird duroh Leitung 34 els Kückfluß zur Kolonne 14 geaohickt·30 is blocked through line 34 as the reflux to column 14

?ig* 2 zeigt eine abgewandelte Anlage» di« eicb von derjenigen nach S1Ig, 1 nur durch di® folgenden Hauptpunkte unterscheidet!? ig * 2 shows a modified system »di« eicb differs from that according to S 1 Ig, 1 only by the following main points!

Die Saft wird mm in eine» einteiligen Xosrpreeser auf 5 verdichtet und dann gereinigt, &a oh Abkühlung in den Austausahern 7 wird die Ιμ£Κ in teilweise verflüssigtes* Zustand unmittelbar in die Kolonne 14 eingeführt! der SeIX der Kälteproduktion» der durch die Verdichtung der behandelten loft von 5 auf 15 har geliefert wtsäe, wird durch einen Sticket offkroie Kwieohen 5 und 15 bar orsotst. Stickstoff von 1? bar wird elnerselte vom AusBtoß des ersten Abschnittes dee Kompressor β 26 und andererseits eua dem SrenngeffiB 30 alt 15 bar ahgessogen· Haoh Kühlung in &&n Austatiaohern 7 wird er in Sauer«—· atoffhad im Sumpf der Kolonne 14 verflüssigt und in AustauscherThe juice is compressed to 5 mm in a "one-piece Xosrpreeer" and then cleaned, & oh cooling in the exchangers 7, the Ιμ £ Κ in a partially liquefied * state is introduced directly into the column 14! the seIX of cold production »which would be delivered by compressing the treated loft from 5 to 15, is orsotst by a sticket offkroie Kwieohen 5 and 15 bar. Nitrogen from 1? bar is elnerselte dee AusBtoß from the first portion 26 and on the other hand β compressor EEA the old SrenngeffiB 30 15 bar ahgessogen · Haoh cooling it is in Sauer "in && n Austatiaohern 7 - · atoffhad the bottom of column 14 and condensed in exchanger

13 unterkühlt ·LItann wird er nach Verdampfung in der Kolonne13 supercooled · LItann it becomes after evaporation in the column

14 von den Bohrbündeln 23 und 24 sowie von den Bohrbündel 2514 from the drill bundles 23 and 24 and from the drill bundles 25

wieder aufgenonoen«resumed "

■·$$.:■■■
■r-:-". i ■ · $$ .: ■■■
■ r -: - ". I

Sa sei betont, &&& die Erfindung nicht auf die vorstehend beschriebene AuefOhrungsfon» beschränkt» sondern sahlreiohen Abwandlungen umgänglich ist» die eich für den laohnaui ohne Abweichung von Hrfindungsgedankon ergehen. So kam dar Stioketooffkreia nach Pig* 2 auch hei der 7ig· 1It should be emphasized that &&& the invention is not »restricted» to the execution form described above, but rather numerous modifications are accessible »which go through for the laohnaui without deviating from the idea of the invention. So the Stioketooffkreia came after Pig * 2 also called the 7ig · 1

werden· In diesen XaIl wird der Stickstoff von bar in die Kolonne 9 eingeführt und an Kopf la Berührung In this XaIl the nitrogen is introduced from bar into the column 9 and touched at head la

109816/U36 „109816 / U36 "

e* ORIGINALe * ORIGINAL

—> 11 - . . I --> 11 -. . I -

wit flüssiges Sauerstoff verflüssigt. Naoh einer Unterkühlung im Austauscher 13 kann si? auch naofe Entspannung auf 5 bar in äie Solonne 14 «lagefübst verdoa und so «a dar Sektiflelerung wit liquid oxygen liquefied. After hypothermia in exchanger 13 can you? Also, slight relaxation to 5 bar in the Solonne 14 "position, and so on, the champagne bottle

für die
:; ;soQßondere kann die/ITeräichtung des reinen erforderliobe Energie Sindostens zum Seil durch Sntopannung ©ines Strömungsmittel« erzeugt werden, das einen HilfstareIs. feireblSuft». einer vorherigen Kühlung und Kondensat lon durchfor the
:; In particular, the direction of the pure required energy Sindostens to the rope can be generated by tension © in a fluid, which is an auxiliary star. feireblSuft ». prior cooling and condensation

sit dieser Quelle für verfügbare Kältokalorien, durch eine Pi&spe und Verdampfung unterliegt Dieses, Ki Xf Biers Is durchlaufende Strömungsmittel kann ein einbit-sit this source of available cold calories, by a Pi & spe and evaporation is subject to this, Ki Xf Biers Is continuous fluid can be a one-bit

Bestandteil ,wie Xthylen, Ithan, Propan sein, es kann auch iBinde st ens iwei Bestandteile aufweisen» vie «in V ,uixa-Propan-Butnn-Seaisob· Die Entspannung in der Turbine Mim von ein^r teilweisen Terflüsslgung begleitet sein* Ui*It can be a component such as ethylene, ithane, propane Even in bindings, there are two constituents "much" in V, uixa-Propan-Butnn-Seaisob · The relaxation in the turbine Mim be accompanied by a partial discharge * Ui *

Anschluß an die Terdichtung des den Hilf »kreisConnection to the seal of the auxiliary circle

. irchleufenden StrSsungsailfeels srhält »an durch f tusob &lt einais Stros von höherer Temperatur und beeondere restlichen ibsug^sdSs^fen aus de» Energiekr«is dee. Any disturbance sentiment persists »on f tusob & lt a stros of higher temperature and special remaining ibsug ^ sdSs ^ fen from the "energy force" is dee

ftir dia Verdichtung dar luft vor ibrer trenn-For the compression of the air in front of the separating

BAD ORfGINALBAD ORfGINAL

109816/U36109816 / U36

Claims (1)

- 12 - 20U363- 12 - 20U363 PatentansprücheClaims I.y Verfahren zur Gewinnung von Sauerstoff und Stickstoff, gegebenenfalls einerseits in flüssiger und andererseits in Gasform, wobei ein Teil des aus der Trennstufe stammenden reinen erwärmten Stickstoffgases verdichtet, durch Wärmeaustausch in einem in Verdampfung stehenden flüssigen Naturgas gekühlt und kondensiert sowie entspannt wird und mindestens ein Teil der entspannten flüssigen Fraktion zur Herstellung des Rückflusses der Trennstufe benutzt wird, während die verdampfte Fraktion mit dem zu verdichtenden Stickstoff vor dessen Kompression vereinigt wird, dadurch gekennzeichnet, daß der Stickstoff in flüssiger und Gasform und der Sauerstoff auf mehreren Druckniveaus erhalten werden, und daß der Teil des erwärmten reinen Stickstoffgases, der mit einem Teil des vor Beendigung der Erwärmung abgezogenen Stickstoffgases wieder vereinigt wird, nach Kondensation und vor seiner Entspannung durch Gegenstvomführung mit der in Verlauf der Entspannung verdampften Fraktion unterkühlt, gegebenenfalls schließlich durch Wärmeaustausch mit der im Sumpf der Trennzone erhaltenen reinen flüssigen Sauerstofffraktion wieder kondensiert und nach Unterkühlung mit dem Stickstoff von Mitteldruck vereinigt wird·I.y processes for the production of oxygen and nitrogen, optionally on the one hand in liquid and on the other hand in gaseous form, part of which comes from the separation stage Pure heated nitrogen gas compressed by heat exchange in an evaporating liquid Natural gas is cooled and condensed and relaxed and at least part of the relaxed liquid fraction to produce the reflux of the separation stage is used, while the vaporized fraction with the to be compressed Nitrogen is combined before its compression, characterized in that the nitrogen in liquid and gaseous form and the oxygen are obtained at several pressure levels, and that the part of the heated pure Nitrogen gas which reunites with part of the nitrogen gas withdrawn before the end of the heating is evaporated after condensation and before its relaxation by counteracting with that in the course of the relaxation The fraction is supercooled, possibly finally by heat exchange with that obtained in the bottom of the separation zone pure liquid oxygen fraction condensed again and after subcooling with the nitrogen of Medium pressure is combined .2. Verfahren nach Anspruch 1, dadurch gekennzeichnet,, daß mindestens ein Teil dor so entspannten verflüssigten Fraktion zumindest teilweise xur Gewinnung einer entspannten flüssigen reinen Stickstofffraktion verwendet.2. Method according to claim 1, characterized in that at least part of the so relaxed liquefied Fraction at least partially used to obtain a relaxed liquid pure nitrogen fraction 109816/U36109816 / U36 wird, die zuvor im Gegenstrom mit einer im Verlauf der letzten Entspannung verdampften Fraktion unterkühlt worden ist. is that previously in countercurrent with one in the course of last relaxation evaporated fraction has been supercooled. 3» Verfahren nach einem der Ansprüche 1 und 2, dadurch gekennzeichnet, daß ein Teil des aus der Trennung stammenden reinen flüssigen Sauerstoffes verdichtet, wiedererwärmt und verdampft wird, während der andere Teil im Gegenstrom mit einer im Verlauf einer letzten Entspannung verdampften und teilweise auf den Flüssigkeitszustand entspannt erhaltenen Fraktion unterkühlt wird.3 »Method according to one of claims 1 and 2, characterized in that part of the resulting from the separation pure liquid oxygen compressed, reheated and is evaporated, while the other part is countercurrent with a vaporized in the course of a final relaxation and partially relaxed to the liquid state preserved Fraction is supercooled. k. Verfahren nach einem der Ansprüche 1 - 3» dadurch gekennzeichnet, daß die Verdichtung des wiedererwärmten Stickstoffgases in einer einzigen Stufe oder in mehreren getrennten Stufen und vorzugsweise in zwei Stufen mittels Durchleitung bei elnm Zwischendruck erfolgt. k. Process according to one of Claims 1 - 3 »characterized in that the compression of the reheated nitrogen gas takes place in a single stage or in several separate stages and preferably in two stages by means of passage at an intermediate pressure. 5* Verfahren nach einem der Ansprüche 1 - kt dadurch gekennzeichnet, daß das verdichtete, gekühlte und durch Wärmeaustausch mit einem in Verdampfung stehenden flüssigen Naturgas kondensierte Stickstoffgas in mindestens zwei Stufen vor zwei aufeinanderfolgenden Entspannungen unterkühlt wird, die im Verlauf der ersten Entspannung verdampfte und der ersten Unterkühlung unterzogene Fraktion mit einem Teil des auf Mitteldruck verdichteten Stickstoff· vereinigt und dann vorzugsweise durch Wärmeaustausch mit aus der Trennung stammendem flüssigen Sauerstoff verflüssigt, anschließend vorzugsweise duroh Austausch mit5 * Method according to one of claims 1 - k t characterized in that the compressed, cooled and through heat exchange with a liquid natural gas in evaporation condensed nitrogen gas is subcooled in at least two stages before two successive releases, which evaporated in the course of the first release and The fraction subjected to the first supercooling is combined with a part of the nitrogen compressed to medium pressure and then preferably liquefied by heat exchange with liquid oxygen originating from the separation, then preferably duroh exchange with 109816/U36109816 / U36 _ u . 2U44363_ u. 2U44363 mindestens dem aus der Trennung stammenden reinen Stickstoffgas unterkühlt und schließlich mit der flüssigen Fraktion vereinigt wird, die man nach der ersten Entspannung erhält, bevor diese der zweiten Entspannung unterzogen wird.at least the pure nitrogen gas originating from the separation is supercooled and finally with the liquid Fraction is combined, which is obtained after the first relaxation before this is subjected to the second relaxation. 6. Verfahren nach einem der Ansprüche 1 - 5i dadurch gekennzeichnet, daß die Trennung durch Destillation unter einem einheitlichen Druck oder durch Destillation unter zwei verschiedenen Drücken erfolgt.6. The method according to any one of claims 1-5i, characterized in that the separation by distillation under one uniform pressure or by distillation under two different pressures. 7» Verfahren nach einem der Ansprüche 1-6, dadurch gekennzeichnet, daß vor der Zerlegung durch Destillation die Luft auf ein erstes Druckniveau verdichtet, gereinigt, dann durch Austausch mit einer Naturgasfraktion gekühlt und schließlich auf ein höheres Druckniveau verdichtet wird.7 »The method according to any one of claims 1-6, characterized in that prior to the decomposition by distillation Air is compressed to a first pressure level, cleaned, then cooled by exchanging it with a natural gas fraction and finally it is compressed to a higher pressure level. 8. Verfahren nach einem der Ansprüche 1-7» dadurch gekennzeichnet, daß man einen oder mehrere der folgenden Bestandteile gewinntt Reinen flüssigen Stickstoff und Sauerstoff von relativ niedrigem Druck (beispielsweise Luftdruck), reine Stickstoff- und Sauerstoffgase von mittlerem Druck (beispielsweise der Größenordnung von 5 bar), reine Stickstoff- und Sauerstoffgase von hohen gegebenenfalls verschiedenen Drücken (wie 15 bsw* kO bar)ι durch Entspannung «Ines Teils des von der Trennung stammenden flüssigen reinen Sauerstoffs naoh Unterkühlung durch die Gasfraktion infolge Entspannung! durch Entspannung «Ines Teils8. The method according to any one of claims 1-7 »characterized in that one or more of the following components wins Pure liquid nitrogen and oxygen of relatively low pressure (for example air pressure), pure nitrogen and oxygen gases of medium pressure (for example of the order of 5 bar), pure nitrogen and oxygen gases of high, if necessary, different pressures (such as 15 bsw * kO bar) ι by relaxation "Ines part of the pure liquid oxygen originating from the separation after subcooling by the gas fraction as a result of relaxation! through relaxation «Ines Teil 109816/U36109816 / U36 ■'■■■■- 1.5 -■ '■■■■ - 1.5 - des aus der Trennung in Gasform entnommenen reinen verflüssigten Stickstoffs, der in ein oder mehreren Stufen auf diesen hohen Druck verdichtet, darauf gekühlt und durch Austausch mit einem in Verdampfung stehenden flüssigen Naturgas verflüssigt und in ein oder mehreren Stufen nach ein oder mehreren Unterkühlungen mit den im Verlauf der Entspannungen erhaltenen Grasfraktion entspannt worden ist; durch Verdampfung und Erwärmung eines Teils des aus der Trennung stammenden flüssigen reinen Sauerstoffs? durch Erwärmung eines Teils des aus der Trennung stammenden Stickstoffgases; durch Verdichtung eines Teils des aus der Trennung stammenden reinen flüssigen Sauerstoffs mit anschließender Verdampfung und Erwärmung; durch Verdichtung eines Teils des aus der Trennung stammenden reinen Stickstoff gases, bevor mindestens ein Teil vollständig wiedererwärmt ist.of the pure liquefied nitrogen removed from the separation in gaseous form, which is compressed in one or more stages to this high pressure, then cooled and liquefied by exchange with an evaporating liquid natural gas and in one or more stages after one or more subcooling with the im The grass fraction obtained has been relaxed in the course of the relaxations; by evaporation and heating a T e of the ils originating from the separation liquid of pure oxygen? by heating part of the nitrogen gas from the separation; by compressing part of the pure liquid oxygen resulting from the separation with subsequent evaporation and heating; by compressing a portion of the pure nitrogen gas resulting from the separation before at least a portion is fully reheated. 9» Verfahren nach einem der Ansprüche 1-8, dadurch gekennzeichnet, daß die für die Verdichtung des reinen Stickstoffgases erforderliche Energie mindestens zum Teil durch Entspannung eines einen Hilfekreis durchlaufenden Strömuhgsmittels erzeugt wird, das zuvor einer Kühlung und Kondensation durch Wärmeaustausch mit der Quelle verfügbarer Kältekalorien, Verdichtung durch Pumpen und Verdampfung unterzogen worden ist.9 »Method according to one of claims 1-8, characterized in that that the one for the compression of the pure nitrogen gas Required energy at least in part through the relaxation of a fluid flowing through an aid circuit is generated, which previously a cooling and condensation by heat exchange with the source available Cold calories, compression by pumping and evaporation has been subjected. to. Verfahren nach einem der Ansprüche 1 -9$ dadurch gekennzeichnet, daß die Verdampfung, die auf die Verdichtung to. Method according to one of claims 1 -9 $, characterized in that the evaporation, which affects the compression 109818/1436109818/1436 des den Hilfekreis durchlaufenden Strömungsmittels folgt» durch Wärmeaustausch mit einem Strom von einer höheren Temperatur und insbesondere mit Hilfe von restlichen Abzugsdämpfen des Dampfenergiegenerators für die Verdichtung der Luft vor deren Trennbehandlung erfolgt.of the fluid flowing through the aid circuit follows » by exchanging heat with a current from a higher one Temperature and in particular with the help of residual exhaust vapors from the steam energy generator for compression the air takes place before their separation treatment. 109816/U36109816 / U36 Lee rs e i teLee on the back
DE2044363A 1969-09-10 1970-09-08 Process for the production of oxygen and nitrogen Expired DE2044363C2 (en)

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CA (1) CA947636A (en)
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Also Published As

Publication number Publication date
FR2060184A1 (en) 1971-06-18
US3886758A (en) 1975-06-03
JPS501359B1 (en) 1975-01-17
CA947636A (en) 1974-05-21
DE2044363C2 (en) 1982-07-29
ES383502A1 (en) 1972-12-16
FR2060184B1 (en) 1973-11-16
GB1329861A (en) 1973-09-12

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