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DE10009977A1 - Process for the low temperature decomposition of air is carried out in a distillation system having a high pressure zone and a low pressure zone consisting of partial sections arranged in separate containers - Google Patents

Process for the low temperature decomposition of air is carried out in a distillation system having a high pressure zone and a low pressure zone consisting of partial sections arranged in separate containers

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Publication number
DE10009977A1
DE10009977A1 DE10009977A DE10009977A DE10009977A1 DE 10009977 A1 DE10009977 A1 DE 10009977A1 DE 10009977 A DE10009977 A DE 10009977A DE 10009977 A DE10009977 A DE 10009977A DE 10009977 A1 DE10009977 A1 DE 10009977A1
Authority
DE
Germany
Prior art keywords
low
fraction
distillation zone
pressure distillation
section
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
DE10009977A
Other languages
German (de)
Inventor
Horst Corduan
Christian Kunz
Dietrich Rottmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to DE10009977A priority Critical patent/DE10009977A1/en
Publication of DE10009977A1 publication Critical patent/DE10009977A1/en
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04084—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 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
    • 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
    • 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
    • F25J3/04309—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/42—Separating low boiling, i.e. more volatile components from nitrogen, e.g. He, H2, Ne
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/52—Separating high boiling, i.e. less volatile components from oxygen, e.g. Kr, Xe, Hydrocarbons, Nitrous oxides, O3
    • 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
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • 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
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid 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
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

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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

Process for the low temperature decomposition of air is carried out in a distillation system having a high pressure zone (4) and a low pressure zone. The low pressure zone has a first partial section (5) and a second partial section (6) arranged in separate containers. A gas fraction (13) is removed from the upper region of the first partial section of the low pressure zone and fed partially into the lower region of the second partial section of the low pressure zone. A liquid fraction (15, 17) is removed from the lower region of the second partial section and fed partially into the upper region of the first partial section. The first fraction is formed by a part of the gas fraction or a part of the liquid fraction. Process for the low temperature decomposition of air is carried out in a distillation system having a high pressure zone (4) and a low pressure zone. A first fraction (31) is removed from an intermediate region of the low pressure zone and fed to a condenser-vaporizer (28), in which a second fraction (32) is produced from the first fraction by indirect heat exchange with a hot or cooling fluid (27, 36). The second fraction is then fed to the low pressure zone. The low pressure zone has a first partial section (5) and a second partial section (6) arranged in separate containers. A gas fraction (13) is removed from the upper region of the first partial section of the low pressure zone and fed partially into the lower region of the second partial section of the low pressure zone. A liquid fraction (15, 17) is removed from the lower region of the second partial section and fed partially into the upper region of the first partial section. The first fraction is formed by a part of the gas fraction or a part of the liquid fraction. An independent claim is also included for an apparatus for carrying out the above process.

Description

Die Erfindung betrifft ein Verfahren zur Tieftemperaturzerlegung von Luft gemäß dem Oberbegriff von Patentanspruch 1, kurz gesagt ein Verfahren mit mindestens zwei Destillierstufen und einer Zwischenheizung oder einer Zwischenkühlung der Niederdruckstufe in Form eines Kondensator Verdampfers.The invention relates to a method for the low-temperature separation of air according to the Preamble of claim 1, in short a method with at least two Distillation stages and an intermediate heating or cooling of the Low pressure stage in the form of a condenser evaporator.

Der Erfindung liegt die Aufgabe zugrunde, ein derartiges Verfahren wirtschaftlich besonders günstig auszugestalten.The object of the invention is to make such a method economical to design particularly cheap.

Diese Aufgabe wird durch die Kombination der Merkmale von Oberbegriff und kennzeichnendem Teil des Patentanspruchs 1 gelöst.This task is accomplished by combining the features of generic term and characterizing part of claim 1 solved.

Die Niederdruckdestillierzone wird demnach in zwei Teilabschnitten realisiert. Diese sind in (mindestens) zwei voneinander getrennten Behältern untergebracht, werden aber im allgemeinen unter praktisch demselben Druck betrieben. In der Regel werden die beiden Teilabschnitte jeweils innerhalb eines einzigen Behälters realisiert, es ist jedoch im Rahmen der Erfindung auch möglich, die Teilabschnitte weiter aufzuteilen und in einer entsprechend höheren Zahl von Behältern anzuordnen.The low-pressure distillation zone is therefore implemented in two sections. This are housed in (at least) two separate containers but generally operated at virtually the same pressure. Usually will the two sections are each realized within a single container, it is however, within the scope of the invention it is also possible to further divide the sections and to be arranged in a correspondingly higher number of containers.

Die Gasfraktion aus dem oberen Bereich der ersten Teilabschnitts der Niederdruckdestillierzone wird vorzugsweise ohne druckverändernde Maßnahmen und Vorrichtungen in den zweiten Teilabschnitt geführt. Sie kann beispielsweise am Kopf des ersten Teilabschnitts abgezogen werden. Der zweite Teilabschnitt ist vorzugsweise neben dem ersten Teilabschnitt (oder neben einer Kombination aus Hochdrucksäule, die die Hochdruckdestillierzone enthält, und erstem Teilabschnitt der Niederdruckdestillierzone) angeordnet. Damit ist es - wegen des in etwa gleichen Betriebsdrucks der beiden Teilabschnitte - häufig notwendig, die Flüssigfraktion gegen den hydrostatischen Druck in den ersten Teilabschnitt zu fördern, beispielsweise mittels einer Pumpe. The gas fraction from the upper area of the first section of the Low pressure distillation zone is preferably without pressure-changing measures and Devices performed in the second section. For example, on the head of the first section. The second section is preferred next to the first section (or next to a combination of high pressure column, which contains the high pressure distillation zone, and the first section of the Low pressure distillation zone) arranged. So that's it - because of the roughly the same Operating pressure of the two sections - often necessary to counter the liquid fraction promote the hydrostatic pressure in the first section, for example by means of a pump.  

Im Rahmen der Erfindung werden die zweiteilige Anordnung der Niederdruckdestillierzone und der Kondensator-Verdampfer auf besonders günstige Weise miteinander verknüpft.In the context of the invention, the two-part arrangement of Low pressure distillation zone and the condenser-evaporator on particularly cheap Way linked together.

Der Kondensator-Verdampfer kann entweder als Zwischenkühlung (Patentanspruch 2) oder als Zwischenheizung (Patentanspruch 3) der Niederdruckdestillierzone ausgebildet sein.The condenser-evaporator can either be used as intermediate cooling (claim 2) or as an intermediate heater (claim 3) of the low pressure distillation zone be trained.

Im ersteren Fall ist es günstig, wenn das Kühlfluid durch flüssigen Stickstoff gebildet wird, der in dem Kondensator-Verdampfer mindestens teilweise verdampft. Dieser Stickstoff kann beispielsweise aus einer der erwähnten Destillierzonen, aus einem Speichertank oder aus einer weiteren Säule zur Stickstoffgewinnung stammen.In the former case, it is favorable if the cooling fluid is formed by liquid nitrogen that evaporates at least partially in the condenser-evaporator. This Nitrogen can, for example, from one of the distillation zones mentioned, from a Storage tank or come from another column for nitrogen production.

Vorzugsweise wird er jedoch aus der Niederdruckdestillierzone entnommen, beispielsweise aus dem Verflüssigungsraum eines Kopfkondensators des zweiten Teilabschnitts, vom Kopf des zweiten Teilabschnitts oder von einer Zwischenstelle einige theoretische oder praktische Böden darunter. Der Druck des flüssigen Stickstoffs kann beispielsweise mittels einer Pumpe stromaufwärts des Kondensator- Verdampfers auf den benötigten Druck erhöht werden. Eine derartige Druckerhöhung im flüssigen Stickstoff, der aus einer Niederdruckdestillierzone abgezogen wird, ist beispielsweise in WO 9819122 im Detail erläutert.However, it is preferably removed from the low-pressure distillation zone, for example from the liquefaction space of a top condenser of the second Section, from the head of the second section or from an intermediate point some theoretical or practical floors underneath. The pressure of the liquid Nitrogen can be pumped upstream of the condenser Evaporator can be increased to the required pressure. Such an increase in pressure in liquid nitrogen withdrawn from a low pressure distillation zone for example, explained in detail in WO 9819122.

Der in dem Kondensator-Verdampfer aus dem flüssigen Stickstoff gebildete gasförmige Stickstoff kann als Produkt abgezogen werden, insbesondere nach Anwärmung auf etwa Umgebungstemperatur. Dabei kann ein Produktdruck erreicht werden, der deutlich über dem Betriebsdruck der Niederdruckdestillierzone liegt (siehe auch WO 9819122), auch ohne daß weitere Maßnahmen zur Druckerhöhung stromabwärts des Kondensator-Verdampfers ergriffen werden. Selbstverständlich ist eine weitere Verdichtung in gasförmigen Zustand möglich, um den Produktstickstoff auf noch höhere Drücke zu bringen als denjenigen, unter dem der Verdampfungsraum des Kondensator-Verdampfers steht.The gaseous formed from the liquid nitrogen in the condenser-evaporator Nitrogen can be withdrawn as a product, especially after heating up about ambient temperature. A product pressure can be achieved that is significantly above the operating pressure of the low pressure distillation zone (see also WO 9819122), even without further measures for increasing the pressure downstream of the condenser-evaporator. Of course there is another one Compression in gaseous state possible to keep the product nitrogen on bring higher pressures than the one under which the evaporation space of the Condenser-evaporator stands.

Besonders große Vorteile zeitigt das erfindungsgemäße Verfahren, wenn der Kondensator-Verdampfer zur Erzeugung von flüssigem Rücklauf für eine Seitenkolonne des ersten Teilabschnitts eingesetzt wird, indem der erste Teilabschnitt der Niederdruckdestillierzone in seinem unteren Bereich mit der Seitenkolonne verbunden ist und ein Gasstrom aus dem oberen Bereich der Seitenkolonne in dem Kondensator-Verdampfer mindestens teilweise verflüssigt wird. Eine solche Seitenkolonne kann insbesondere zur Erzeugung eines an schwererflüchtigen Komponenten abgereicherten Sauerstoffprodukts dienen.The method according to the invention has particularly great advantages if the Condenser-evaporator for the generation of liquid return for a Side column of the first section is used by the first section  the low pressure distillation zone in its lower area with the side column is connected and a gas stream from the upper region of the side column in the Condenser-evaporator is at least partially liquefied. Such Side column can be used in particular to produce a more volatile Components depleted oxygen product serve.

In dem Verfahren muß außerdem flüssiger Rücklauf für die Hochdruckdestillierzone und aufsteigender Dampf für den ersten Teilabschnitt der Niederdruckdestillierzone erzeugt werden. Hierzu ist es günstig, wenn Sumpfflüssigkeit des ersten Teilabschnitts der Niederdruckdestillierzone in einem Hauptkondensator mindestens teilweise verdampft wird, insbesondere durch indirekten Wärmeaustausch mit einem kondensierenden Gasstrom aus dem oberen Bereich der Hochdruckdestillierzone.The process also requires liquid reflux for the high pressure distillation zone and rising steam for the first section of the low pressure distillation zone be generated. For this purpose, it is favorable if the bottom liquid of the first section the low pressure distillation zone in a main condenser at least partially is evaporated, in particular by indirect heat exchange with a condensing gas stream from the upper area of the high pressure distillation zone.

Bei dem erfindungsgemäßen Verfahren wird die Niederdrucksäule vorzugsweise deutlich über Atmosphärendruck betrieben. Dabei ist es vorteilhaft, wenn Kopfgas des zweiten Teilabschnitts der Niederdruckdestillierzone mindestens teilweise verflüssigt wird, beispielsweise durch indirekten Wärmeaustausch mit einem verdampfenden Flüssigstrom aus der Niederdruckdestillierzone. Einzelheiten über die Betriebsweisen einer derartigen Kopfkühlung der Niederdruckdestillierzone sind der bereits genannten Anmeldung WO 9819122 zu entnehmen, deren Offenbarung insoweit in diese Anmeldung einbezogen wird.In the method according to the invention, the low pressure column is preferred operated well above atmospheric pressure. It is advantageous if the top gas second section of the low pressure distillation zone at least partially liquefied is, for example, by indirect heat exchange with an evaporating Liquid flow from the low pressure distillation zone. Details of the modes of operation such a head cooling of the low pressure distillation zone are those already mentioned Application WO 9819122 can be found, the disclosure of which in this respect Registration is involved.

Außerdem betrifft die Erfindung eine Vorrichtung gemäß Patentanspruch 10.The invention also relates to a device according to claim 10.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand des in der Zeichnung dargestellten Ausführungsbeispiels näher erläutert.The invention and further details of the invention are described below of the embodiment shown in the drawing.

Verdichtete und gereinigte Einsatzluft 1 wird in einem Hauptwärmetauscher 2 auf etwa Taupunkt abgekühlt und über Leitung 3 dem Destilliersystem zugeführt. Die Hochdruckdestillierzone ist in dem Beispiel in einer Hochdrucksäule 4 angeordnet. Die Niederdruckdestillierzone weist zwei Teilabschnitte auf, die in einer ersten Niederdrucksäule 5 beziehungsweise in einer zweiten Niederdrucksäule 6 angeordnet sind. Erste Niederdrucksäule 5 und Hochdrucksäule 4 stehen über einen Hauptkondensator 7 in wärmetauschender Verbindung und bilden eine Doppelsäulen- Konfiguration. Flüssiger Rohsauerstoff 8 aus dem Sumpf der Hochdrucksäule 4 wird in einem Unterkühlungs-Gegenströmer 9 unterkühlt und über Leitung 10 einer Zwischenstelle der zweiten Niederdrucksäule 6 zugeleitet.Compressed and cleaned feed air 1 is cooled in a main heat exchanger 2 to about dew point and fed to the distillation system via line 3 . The high-pressure distillation zone is arranged in a high-pressure column 4 in the example. The low-pressure distillation zone has two sections which are arranged in a first low-pressure column 5 or in a second low-pressure column 6 . The first low-pressure column 5 and high-pressure column 4 are in heat-exchanging connection via a main condenser 7 and form a double-column configuration. Liquid raw oxygen 8 from the bottom of the high pressure column 4 is subcooled in a subcooling countercurrent 9 and fed via line 10 to an intermediate point of the second low pressure column 6 .

Flüssiger Stickstoff, der vom Hauptkondensator 7 stammen kann oder - wie in der Zeichnung dargestellt - einige Böden unterhalb des Kopfs der Hochdrucksäule 4 abgezogen wird, strömt über Leitung 11 ebenfalls dem Unterkühlungs-Gegenströmer 9 zu und wird über Leitung 12 auf den Kopf der zweiten Niederdrucksäule 6 aufgegeben. Eine Gasfraktion 13 wird am Kopf der ersten Niederdrucksäule 5 abgenommen und fließt zu einem ersten Teil 14 zur zweiten Niederdrucksäule 6, wo sie unmittelbar oberhalb des Sumpf eingespeist wird. Die mit 13 und 14 bezeichneten Leitungen weisen vorzugsweise keine druckverändernden Vorrichtungen auf, so daß der Betriebsdruck am Kopf der ersten und über dem Sumpf der zweiten Niederdrucksäule bis auf die Leitungsverluste in der Gasfraktion identisch sind.Liquid nitrogen, which can originate from the main condenser 7 or, as shown in the drawing, is drawn off some trays below the head of the high-pressure column 4 , likewise flows to the supercooling countercurrent flow 9 via line 11 and is passed via line 12 to the top of the second low-pressure column 6 abandoned. A gas fraction 13 is taken from the top of the first low-pressure column 5 and flows to a first part 14 to the second low-pressure column 6 , where it is fed directly above the sump. The lines designated 13 and 14 preferably have no pressure-changing devices, so that the operating pressure at the top of the first and above the sump of the second low-pressure column are identical except for the line losses in the gas fraction.

In gegenläufiger Richtung wird eine Flüssigfraktion 15 aus dem Sumpf der zweiten Niederdrucksäule 6 mittels einer Pumpe 16 über die Leitung 17 zum Kopf der ersten Niederdrucksäule 5 geführt. Die zweite Niederdrucksäule 6 weist einen Kopfkondensator 18 auf, der in dem Beispiel durch eine Zwischenflüssigkeit 19 der zweiten Niederdrucksäule 6 gekühlt wird. (Alternativ oder zusätzlich können auch eine oder mehrere andere Flüssigkeiten aus der Hochdruckdestillierzone oder aus der Niederdruckdestillierzone zur Kühlung des Kopfkondensators 18 eingesetzt werden, insbesondere die in WO 9819122 genannten Arten der Kopfkühlung der Niederdruckdestillierzone sind auch bei der Erfindung anwendbar.) Restdampf 20 vom Verdampfungsraum des Kopfkondensators 18 wird in den Wärmetauschern 9 und 2 auf etwa Umgebungstemperatur angewärmt und über die Leitungen 21 und 22 abgezogen. Er kann beispielsweise zur Regenerierung einer nicht dargestellten Reinigungseinrichtung für die Einsatzluft 1 verwendet werden.In the opposite direction, a liquid fraction 15 is led from the bottom of the second low-pressure column 6 by means of a pump 16 via line 17 to the top of the first low-pressure column 5 . The second low-pressure column 6 has a top condenser 18 , which in the example is cooled by an intermediate liquid 19 of the second low-pressure column 6 . (Alternatively or additionally, one or more other liquids from the high-pressure distillation zone or from the low-pressure distillation zone can be used to cool the top condenser 18 , in particular the types of head cooling of the low-pressure distillation zone mentioned in WO 9819122 can also be used in the invention.) Residual steam 20 from the evaporation chamber of the Top condenser 18 is heated to approximately ambient temperature in heat exchangers 9 and 2 and drawn off via lines 21 and 22 . It can be used, for example, to regenerate a cleaning device (not shown) for the feed air 1 .

Das Stickstoffprodukt nimmt bei dem Beispiel folgenden Weg: Flüssiger Stickstoff wird. Über Leitung 23 einige Böden unterhalb des Kopfs der zweiten Niederdrucksäule 6 und in einer Pumpe 24 auf einen Produktdruck gebracht, der deutlich über dem Betriebsdruck der Niederdruckdestillierzone liegt. Falls Stickstoff auch als Flüssigprodukt (MPLIN) benötigt wird, kann dieses über Leitung 25 abgezogen werden. Der Rest 26 des flüssigen Stickstoffs wird in dem Unterkühlungs-Gegenströmer 9 angewärmt, über Leitung 27 zu einem Kondensator Verdampfer 28 geführt und dort verdampft. Der in dem Kondensator-Verdampfer 28 gebildete gasförmige Stickstoff 29 wird im Hauptwärmetauscher 2 angewärmt und bei 30 als Druckstickstoffprodukt (MPGAN) abgeführt.In the example, the nitrogen product takes the following route: Liquid nitrogen becomes. Via line 23, some trays below the top of the second low-pressure column 6 and brought to a product pressure in a pump 24 which is significantly above the operating pressure of the low-pressure distillation zone. If nitrogen is also required as a liquid product (MPLIN), this can be drawn off via line 25 . The remainder 26 of the liquid nitrogen is warmed in the subcooling countercurrent 9 , led via line 27 to a condenser evaporator 28 and evaporated there. The gaseous nitrogen 29 formed in the condenser-evaporator 28 is heated in the main heat exchanger 2 and removed at 30 as a pressure nitrogen product (MPGAN).

Auf der Verflüssigungsseite des Kondensator-Verdampfers 28 kondensiert ein zweiter Teil 31 der Gasfraktion 13 vom Kopf der ersten Niederdrucksäule 5. Das Kondensat 32 wird in die erste Niederdrucksäule 5 zurückgespeist. Damit erfüllt der Kondensator- Verdampfer 28 die Funktion einer Zwischenheizung der Niederdruckdestillierzone.On the liquefaction side of the condenser-evaporator 28, a second part 31 of the gas fraction 13 condenses from the top of the first low-pressure column 5 . The condensate 32 is fed back into the first low-pressure column 5 . The condenser-evaporator 28 thus fulfills the function of intermediate heating of the low-pressure distillation zone.

Über die Leitungen 33 und 34 ist der Sumpfbereich der ersten Niederdrucksäule 5 mit dem unteren Ende einer Seitenkolonne 35 verbunden. Kopfgas 36 der Seitenkolonne 35 wird in dem Kondensator-Verdampfer 28 kondensiert. Die dabei gewonnene Flüssigkeit 37 dient mindestens zu einem ersten Teil 38 als Rücklauf für die Seitenkolonne 35. Der Rest 39 kann flüssig als hochreines Sauerstoffprodukt abgezogen und in einer Pumpe 40 auf den gewünschten Produktdruck gebracht werden. In dem Beispiel wird ein Teil 41 als Flüssigsauerstoffprodukt (MPLOX) gewonnen. Der restliche Hochdrucksauerstoff 42 wird unter dem Produktdruck im Hauptwärmetauscher 2 verdampft und angewärmt und schließlich über Leitung 43 als gasförmiges Drucksauerstoffprodukt (MPGOX) abgezogen.The bottom region of the first low-pressure column 5 is connected to the lower end of a side column 35 via lines 33 and 34 . Top gas 36 of the side column 35 is condensed in the condenser-evaporator 28 . The liquid 37 obtained in this way serves at least for a first part 38 as a return for the side column 35 . The rest 39 can be drawn off in liquid form as a high-purity oxygen product and brought to the desired product pressure in a pump 40 . In the example, part 41 is obtained as a liquid oxygen product (MPLOX). The remaining high-pressure oxygen 42 is evaporated and heated under the product pressure in the main heat exchanger 2 and finally drawn off via line 43 as a gaseous pressurized oxygen product (MPGOX).

Zur Kälteerzeugung wird eine gasförmige Zwischenfraktion 44, die aus unreinem Stickstoff besteht, aus der zweiten Niederdrucksäule 6 abgezogen, im Unterkühlungs- Gegenströmer 9 angewärmt, über Leitung 45 zum Hauptwärmetauscher 2 geführt und mindestens zum Teil 46 von einer Zwischentemperatur aus arbeitsleistend entspannt (47). Die entspannte Zwischenfraktion 48 wird mit dem Restdampf 20 vom Kopfkondensator 18 vereinigt.To generate cold, a gaseous intermediate fraction 44 , which consists of impure nitrogen, is drawn off from the second low-pressure column 6 , heated in the subcooling countercurrent 9 , led via line 45 to the main heat exchanger 2 and, at least in part 46, relaxed from an intermediate temperature ( 47 ). The relaxed intermediate fraction 48 is combined with the residual steam 20 from the top condenser 18 .

Claims (10)

1. Verfahren zur Tieftemperaturzerlegung von Luft in einem Destilliersystem, das eine Hochdruckdestillierzone (4) und eine Niederdruckdestilierzone aufweist, wobei die Niederdruckdestillierzone unter niedrigerem Druck als die Hochdruckdestillierzone betrieben wird, und wobei bei dem Verfahren
  • - eine erste Fraktion (31) aus einem Zwischenbereich der Niederdruckdestillierzone entnommen und in einen Kondensator-Verdampfer (28) eingeleitet wird,
  • - in dem Kondensator-Verdampfer (28) durch indirekten Wärmeaustausch mit einem Heiz- oder Kühlfluid (27, 36) aus der ersten Fraktion (31) eine zweite Fraktion (32) erzeugt wird und
  • - die zweite Fraktion (32) in die Niederdruckdestillierzone eingeleitet wird
dadurch gekennzeichnet, daß
  • - die Niederdruckdestillierzone einen ersten Teilabschnitt (5) und einen zweiten Teilabschnitt (6) aufweist, die in voneinander getrennten Behältern angeordnet sind, wobei
  • - eine Gasfraktion (13) aus dem oberen Bereich des ersten Teilabschnitts (5) der Niederdruckdestillierzone entnommen und mindestens teilweise in den unteren Bereich des zweiten Teilabschnitts (6) der Niederdruckdestillierzone eingeleitet (14) wird und
  • - eine Flüssigfraktion (15, 17) aus dem unteren Bereich des zweiten Teilabschnitts (6) der Niederdruckdestillierzone entnommen und mindestens teilweise in den oberen Bereich des ersten Teilabschnitts (5) der Niederdruckdestillierzone eingeleitet wird, und daß
  • - die erste Fraktion (31) durch einen Teil der Gasfraktion (13) oder einen Teil der Flüssigfraktion gebildet wird.
1. A method of cryogenic air separation in a distillation system having a high pressure distillation zone ( 4 ) and a low pressure distillation zone, the low pressure distillation zone being operated at a lower pressure than the high pressure distillation zone, and wherein the method
  • a first fraction ( 31 ) is removed from an intermediate region of the low-pressure distillation zone and introduced into a condenser-evaporator ( 28 ),
  • - In the condenser-evaporator ( 28 ) by indirect heat exchange with a heating or cooling fluid ( 27 , 36 ) from the first fraction ( 31 ), a second fraction ( 32 ) is generated and
  • - The second fraction ( 32 ) is introduced into the low pressure distillation zone
characterized in that
  • - The low pressure distillation zone has a first section ( 5 ) and a second section ( 6 ), which are arranged in separate containers, wherein
  • - A gas fraction ( 13 ) is removed from the upper area of the first section ( 5 ) of the low-pressure distillation zone and at least partially introduced ( 14 ) into the lower area of the second section ( 6 ) of the low-pressure distillation zone and
  • - A liquid fraction ( 15 , 17 ) is removed from the lower region of the second section ( 6 ) of the low-pressure distillation zone and at least partially introduced into the upper region of the first section ( 5 ) of the low-pressure distillation zone, and that
  • - The first fraction ( 31 ) is formed by part of the gas fraction ( 13 ) or part of the liquid fraction.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die erste Fraktion (31) durch einen Teil der Gasfraktion (13) gebildet, in dem Kondensator-Verdampfer (28) durch indirekten Wärmeaustausch mit einem Kühlfluid (27, 36) mindestens teilweise verflüssigt wird, wobei die zweite Fraktion (32) gebildet wird, und daß die zweite Fraktion (32) in den oberen Bereich des ersten Teilabschnitts (5) der Niederdruckdestillierzone eingeleitet wird. 2. The method according to claim 1, characterized in that the first fraction ( 31 ) is formed by part of the gas fraction ( 13 ) in the condenser-evaporator ( 28 ) by indirect heat exchange with a cooling fluid ( 27 , 36 ) is at least partially liquefied , wherein the second fraction ( 32 ) is formed, and that the second fraction ( 32 ) is introduced into the upper region of the first section ( 5 ) of the low-pressure distillation zone. 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß die erste Fraktion durch einen Teil der Flüssigfraktion gebildet, in dem Kondensator- Verdampfer durch indirekten Wärmeaustausch mit einem Heizfluid mindestens teilweise verdampft wird, wobei die zweite Fraktion gebildet wird, und daß die zweite Fraktion in den unteren Bereich des zweiten Teilabschnitts der Niederdruckdestillierzone eingeleitet wird.3. The method according to claim 1 or 2, characterized in that the first Fraction formed by part of the liquid fraction in which condenser Evaporator by indirect heat exchange with a heating fluid at least is partially evaporated, forming the second fraction, and that the second fraction in the lower part of the second section of the Low pressure distillation zone is initiated. 4. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß das Kühlfluid mindestens teilweise durch flüssigen Stickstoff (27) gebildet wird, der in dem Kondensator-Verdampfer (28) mindestens teilweise verdampft.4. The method according to claim 2, characterized in that the cooling fluid is at least partially formed by liquid nitrogen ( 27 ) which evaporates at least partially in the condenser-evaporator ( 28 ). 5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß der als Kühlfluid verwendete Stickstoff (27) aus der Niederdruckdestillierzone entnommen (23, 24, 26) wird.5. The method according to claim 4, characterized in that the nitrogen ( 27 ) used as the cooling fluid is removed from the low-pressure distillation zone ( 23 , 24 , 26 ). 6. Verfahren nach Anspruch 4 oder 5, dadurch gekennzeichnet, daß der in dem Kondensator-Verdampfer (28) aus dem flüssigen Stickstoff (27) gebildete gasförmige Stickstoff (29) als Produkt (30) abgezogen wird.6. The method according to claim 4 or 5, characterized in that in the condenser-evaporator ( 28 ) from the liquid nitrogen ( 27 ) formed gaseous nitrogen ( 29 ) is withdrawn as a product ( 30 ). 7. Verfahren nach Anspruch 2 oder nach einem der Ansprüche 4 bis 6, dadurch gekennzeichnet, daß erste Teilabschnitt (5) der Niederdruckdestillierzone in seinem unteren Bereich mit einer Seitenkolonne (35) verbunden (33, 34) ist und ein Gasstrom (36) aus dem oberen Bereich der Seitenkolonne (35) in dem Kondensator-Verdampfer (28) mindestens teilweise verflüssigt wird.7. The method according to claim 2 or according to one of claims 4 to 6, characterized in that the first section ( 5 ) of the low-pressure distillation zone is connected in its lower region to a side column ( 35 ) ( 33 , 34 ) and a gas stream ( 36 ) the upper region of the side column ( 35 ) in the condenser-evaporator ( 28 ) is at least partially liquefied. 8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß Sumpfflüssigkeit des ersten Teilabschnitts (5) der Niederdruckdestillierzone in einem Hauptkondensator (7) mindestens teilweise verdampft wird, insbesondere durch indirekten Wärmeaustausch mit einem kondensierenden Gasstrom aus dem oberen Bereich der Hochdruckdestillierzone (4).8. The method according to any one of claims 1 to 7, characterized in that bottom liquid of the first section ( 5 ) of the low pressure distillation zone in a main condenser ( 7 ) is at least partially evaporated, in particular by indirect heat exchange with a condensing gas stream from the upper region of the high pressure distillation zone ( 4 ). 9. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß Kopfgas des zweiten Teilabschnitts (6) der Niederdruckdestillierzone mindestens teilweise verflüssigt wird, insbesondere durch indirekten Wärmeaustausch (18) mit einer verdampfenden Flüssigstrom (19) aus der Niederdruckdestillierzone. 9. The method according to any one of claims 1 to 8, characterized in that overhead gas of the second section ( 6 ) of the low-pressure distillation zone is at least partially liquefied, in particular by indirect heat exchange ( 18 ) with an evaporating liquid stream ( 19 ) from the low-pressure distillation zone. 10. Vorrichtung zur Tieftemperaturzerlegung von Luft mit einem Destilliersystem, das eine Hochdruckdestillierzone (4) und eine Niederdruckdestillierzone aufweist, und mit
  • - eine Zuleitung (31) für eine erste Fraktion, die aus einem Zwischenbereich der Niederdruckdestillierzone in einen Kondensator-Verdampfer (28) führt und mit
  • - einer Rückleitung (32) für eine zweite Fraktion, die aus dem Kondensator- Verdampfer (28) in die Niederdruckdestillierzone führt,
dadurch gekennzeichnet, daß
  • - die Niederdruckdestillierzone einen ersten Teilabschnitt (5) und einen zweiten Teilabschnitt (6) aufweist, die in voneinander getrennten Behältern angeordnet sind, wobei
  • - der obere Bereich des ersten Teilabschnitts (5) und der untere Teil des zweiten Teilabschnitts (6) der Niederdruckdestillierzone über eine Gasleitung (13, 14) und eine Flüssigleitung (15, 17) verbunden sind, und daß
  • - die Zuleitung (31) in Strömungsverbindung mit der Gasleitung (13, 14) oder der Flüssigleitung steht.
10. Device for low-temperature separation of air with a distillation system which has a high-pressure distillation zone ( 4 ) and a low-pressure distillation zone, and with
  • - A feed line ( 31 ) for a first fraction, which leads from an intermediate region of the low-pressure distillation zone into a condenser-evaporator ( 28 ) and with
  • a return line ( 32 ) for a second fraction, which leads from the condenser-evaporator ( 28 ) into the low-pressure distillation zone,
characterized in that
  • - The low pressure distillation zone has a first section ( 5 ) and a second section ( 6 ), which are arranged in separate containers, wherein
  • - The upper region of the first section ( 5 ) and the lower part of the second section ( 6 ) of the low pressure distillation zone are connected via a gas line ( 13 , 14 ) and a liquid line ( 15 , 17 ), and that
  • - The supply line ( 31 ) is in flow connection with the gas line ( 13 , 14 ) or the liquid line.
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011113668A1 (en) 2011-09-20 2013-03-21 Linde Aktiengesellschaft Method and apparatus for the cryogenic separation of air
WO2013041229A1 (en) 2011-09-20 2013-03-28 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
DE202014002220U1 (en) 2013-10-31 2014-04-14 Linde Aktiengesellschaft Apparatus for the cryogenic separation of air

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011113668A1 (en) 2011-09-20 2013-03-21 Linde Aktiengesellschaft Method and apparatus for the cryogenic separation of air
EP2573492A1 (en) 2011-09-20 2013-03-27 Linde Aktiengesellschaft Method and device for cryogenic decomposition of air
WO2013041229A1 (en) 2011-09-20 2013-03-28 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
AU2012311959B2 (en) * 2011-09-20 2016-09-08 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
US10443931B2 (en) 2011-09-20 2019-10-15 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
DE202014002220U1 (en) 2013-10-31 2014-04-14 Linde Aktiengesellschaft Apparatus for the cryogenic separation of air

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