EP2895811B1 - Verfahren und vorrichtung zur lufttrennung durch kryogene destillation - Google Patents

Verfahren und vorrichtung zur lufttrennung durch kryogene destillation Download PDF

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Publication number
EP2895811B1
EP2895811B1 EP13767026.1A EP13767026A EP2895811B1 EP 2895811 B1 EP2895811 B1 EP 2895811B1 EP 13767026 A EP13767026 A EP 13767026A EP 2895811 B1 EP2895811 B1 EP 2895811B1
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Prior art keywords
exchanger
column
pressure
nitrogen
air
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English (en)
French (fr)
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EP2895811A1 (de
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Marie Cognard
Richard Dubettier-Grenier
Sylvain Gerard
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • 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
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • 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
    • F25J3/04151—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
    • 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
    • F25J3/0429—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 feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or 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
    • 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
    • F25J3/04406—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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet

Definitions

  • the present invention relates to a method and apparatus for air separation by cryogenic distillation.
  • the invention proposes in particular a method and describes an apparatus for the transient production of a gas from an apparatus producing, in normal operation, oxygen and nitrogen gas and liquid oxygen and nitrogen.
  • the apparatus comprises a double column having a first column operating at a first so-called medium pressure (MP) and a second column operating at a second so-called low pressure (BP), lower than the first pressure.
  • MP medium pressure
  • BP low pressure
  • This gas, produced in transient mode may for example be pure nitrogen and under pressure and used during inerting phases of petrochemical processes requiring continuous large amounts of nitrogen over several days before requiring the gas requirements of normal walking.
  • the present invention proposes an arrangement of dedicated body heat exchangers making it possible to specifically produce the gaseous requirement during the transient phase, and also produce the need for the other gas (s) (eg oxygen); the production of liquid nitrogen and oxygen can be reduced or even zero during the transient phase.
  • the arrangement of the exchange bodies then makes it possible to produce in normal operation the gas and liquid requirements.
  • the flexibility required of the main exchanger of the separating apparatus is all the greater as the productions required (in terms of pressure and flow) between different operating modes are remote.
  • the dimensioning of the heat exchanger resulting from the different operating steps thus departs from a technico-economic optimum for a given step.
  • an air separation apparatus producing industrial gases for a petrochemical complex will be required to produce very different amounts, at different pressures, depending on the specific operations of the consuming units.
  • the storage of liquids nitrogen, oxygen, argon
  • the use of liquid storage is however limited by the storage capacity.
  • unusual steps of the consuming units require large volumes over several days, it may be preferable to produce directly from the air separation apparatus rather than sizing the storage for this transient step.
  • the production flexibility of the air separation apparatus required by this step can then be provided by the present invention, without degrading the efficiency of normal steps.
  • An alternative solution is the production of medium pressure nitrogen gas from a medium pressure (MP) column and compressor compression. If the gas withdrawal from the MP column is insufficient, vaporization of stored liquid nitrogen will then be necessary.
  • MP medium pressure
  • the nitrogen can be produced by the upper stages of a low pressure column and then compressed by a compressor.
  • the present invention provides an arrangement of dedicated body heat exchangers comprising a dedicated transient exchange line for specifically producing the gaseous requirement during the transient phase.
  • the transient gas considered in this example is nitrogen but the invention is also applicable to other gases produced by the air separation apparatus.
  • the transient nitrogen is pumped from the first column (MP column) and vaporized through a dedicated line of exchanger (called here exchange line transient) against high pressure air (HP) coming from the discharge of a booster possibly driven by a turbine; simultaneously, the pumped oxygen is vaporized through another dedicated line of exchangers against HP air from the discharge of the same booster or a second booster.
  • the production of nitrogen gas which is normally produced from the MP column and heated against MP air from the air purification unit in a dedicated third exchange line, is stopped.
  • the transient nitrogen production is stopped while the normal production of nitrogen gas from the MP column is established.
  • the production of gaseous oxygen is maintained, and the liquid productions are adjusted to their normal instructions.
  • the exchange line dedicated to the production of transient nitrogen gas only involves fluids that will change state as it passes: liquid nitrogen (LIN) vaporises into high pressure nitrogen (HP GAN) against HP air that liquefies.
  • LIN liquid nitrogen
  • HP GAN high pressure nitrogen
  • the expected gain in compactness is substantial because, for the same 'charge' exchanged, the exchange volume can be less than half the volume usually required in the presence of a third fluid without change of state. That is, (Volume / Charge) transient exchanger ⁇ 0.5 x (Volume / Charge) conventional exchanger .
  • a cryogenic distillation air separation installation comprising a double column comprising a first column and a second column, the second column operating at a lower pressure than the first column, a first column heat exchanger, a second heat exchanger.
  • a third heat exchanger capable of, and connected to, supply lines for, allowing indirect heat exchange between only two fluids, a third heat exchanger, means for sending a flow of air to a first pressure substantially equal to the operating pressure of the first column at the first exchanger and the first exchanger at the first column, means for dividing air at a second pressure greater than the first pressure into a first and a second fractions, means for sending the first fraction to the second pressure at the second exchanger through a first era of the supply lines, a valve to prevent the sending of the first fraction to the second exchanger, means to send the second fraction to the second pressure to the third exchanger, possibly other means to send an air flow at a pressure greater than the first pressure at the third exchanger, means for sending a pressurized liquid from the double column to vaporize in the third exchanger, means for sending a liquid required punctually from the double column to vaporize in the second exchanger through a second of the supply lines, a valve to prevent the liquid from being sent occasionally from the double column to the second
  • At least the first and third heat exchangers are brazed aluminum plate and fin exchangers.
  • the apparatus used comprises three heat exchangers 1, 2, 3 which can be brazed aluminum plate and fin heat exchangers. It also comprises a system of distillation columns 25, comprising at least one double distillation column.
  • the double column comprises a first column operating at a first pressure and a second column operating at a second pressure, lower than the first pressure.
  • the apparatus comprises three air compressors, a main compressor, a first booster for supercharging a portion 13 of the air from the main compressor, a portion of the air of the first booster supplying a turbine and a second booster to boost a compressor. part 7 of the air from the first booster, this second booster being driven by the turbine. An air flow 5 at the first pressure is sent from the main compressor to the first column without being overpressed. Part 7 of the air is at least partially condensed before being sent to the column system.
  • the apparatus has at least two operating steps. According to a first of these steps, which is the normal operation of the process, the air flow 5 at the first pressure is cooled in the exchanger 1 and sent to the first column where it is separated. A flow of nitrogen gas 23 from the first column and a flow of residual nitrogen 21 from the second column are heated in this first exchanger 1: the heat exchanger 1 allows the exchange between three fluids.
  • the second heat exchanger 2 receives no fluid to cool or to heat.
  • the third exchanger 3 cools air 7, 11 from the second booster driven by the turbine.
  • the air partially condensed 11 is sent to the system of columns 25.
  • the air 13 of the first booster is cooled and is sent to an intermediate temperature thereof to the turbine and then to the first or second column.
  • the third exchanger heats residual nitrogen 17 from the second column and liquid oxygen from the second column after a pressurization step.
  • the liquid oxygen can be replaced by gaseous oxygen from the second column.
  • cryogenic liquid as final product 27 which may be liquid nitrogen and / or liquid oxygen.
  • a second step called a transient step
  • the air flow 5 at the first pressure is cooled in the exchanger 1 and sent to the first column where it is separated.
  • a flow of residual nitrogen 21 from the second column is heated in this first exchanger 1: the heat exchanger 1 exchanges between two fluids only, the flow 23 is no longer sent to the exchanger 1, the valve V1 being closed.
  • the second exchanger 2 receives air 9 through a valve V2 from the second booster and pump-pressurized liquid nitrogen 19 from the first column through the valve V3.
  • the third exchanger 3 cools air 7, 11 from the second booster driven by the turbine.
  • the partially condensed air 11 is sent to the column system 25.
  • the air 13 of the first booster is cooled and is sent to an intermediate temperature thereof to the turbine, thus driving the second booster, and then to the first or second column.
  • the third exchanger heats residual nitrogen 17 from the second column and liquid oxygen from the second column after a pressurization step.
  • the liquid oxygen can be replaced by gaseous oxygen from the second column.
  • cryogenic liquid 27 as final product which may be liquid nitrogen and / or liquid oxygen, the total amount of liquid produced as final product being lower than that produced during normal operation.

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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)

Claims (10)

  1. Verfahren zur Herstellung eines ersten unter Druck stehenden Gases, sowie im Einzelfall eines zweiten Gases durch kryogene Destillation der Luft in einer Doppelsäule, eine erste Säule und eine zweite Säule umfassend, wobei die zweite Säule mit einem geringeren Druck arbeitet, als die erste Säule, wobei:
    i) sich in einem ersten Schritt Luft (5) mit einem ersten Druck, der im Wesentlichen der Betriebsdruck der ersten Säule ist, in einem ersten Wärmetauscher (1) abkühlt, und in die erste Säule geschickt wird, sich zwei stickstoffreiche Gasströme (21, 23) aus der ersten und der zweiten Säule im ersten Tauscher erwärmen, sich zumindest ein Luftstrom (11, 13) mit einem zweiten Druck, der größer ist, als der erste Druck, in einem dritten Wärmetauscher (3) abkühlt, eine mit Druck beaufschlagte Flüssigkeit (15) im dritten Tauscher verdampft und sich ein stickstoffreicher Gasstrom (17) aus der zweiten Säule im dritten Tauscher erwärmt, und
    ii) sich in einem zweiten Schritt Luft (5) mit dem ersten Druck im ersten Tauscher abkühlt und in die erste Säule geschickt wird, sich ein stickstoffreicher Gasstrom (21) aus der zweiten Säule im ersten Tauscher erwärmt, sich ein mit Druck beaufschlagter Flüssigkeitsstrom (19) aus der Doppelsäule erwärmt und in einem zweiten Tauscher verdampft, um ein im Einzelfall benötigtes Gas zu bilden, sich ein Luftstrom (9) mit dem zweiten Druck abkühlt und eventuell im zweiten Tauscher kondensiert, wobei dieser Luftstrom und der mit Druck beaufschlagte Flüssigkeitsstrom die einzigen Fluide sind, die im zweiten Tauscher Wärme austauschen, sich ein Luftstrom (11, 13) mit dem zweiten Druck im dritten Tauscher abkühlt, sich eventuell ein anderer Luftstrom mit einem Druck, der größer ist, als der erste, oder gar als der zweite Druck im dritten Tauscher abkühlt, eine mit Druck beaufschlagte Flüssigkeit (15) im dritten Tauscher verdampft und sich ein stickstoffreicher Gasstrom (17) aus der zweiten Säule im dritten Tauscher erwärmt, dadurch gekennzeichnet, dass sich im ersten Schritt kein Fluid im zweiten Wärmetauscher (2) erwärmt oder abkühlt.
  2. Verfahren nach Anspruch 1, wobei sich im zweiten Schritt ein einziger stickstoffreicher Gasstrom (21) aus der zweiten Säule im ersten Tauscher erwärmt.
  3. Verfahren nach einem der vorherigen Ansprüche, wobei sich einer der Luftströme (13) mit dem Druck, der größer ist, als der Betriebsdruck der ersten Säule, im ersten und zweiten Schritt im dritten Tauscher (3) teilweise abkühlt, in einer Turbine entspannt wird und in die erste oder die zweite Säule geschickt wird.
  4. Verfahren nach Anspruch 3, wobei der in die Turbine geschickte Strom aus einer ersten Druckerhöhungsanlage stammt.
  5. Verfahren nach Anspruch 3 oder 4, wobei der andere (7, 11) der Luftströme mit dem Druck, der größer ist, als der Betriebsdruck der ersten Säule, aus einer zweiten Druckerhöhungsanlage stammt, die von der Turbine angetrieben wird.
  6. Verfahren nach einem der vorherigen Ansprüche, wobei man eine Menge an Flüssigkeit (27) als Endprodukt im ersten Schritt erzeugt und man keine Flüssigkeit als Endprodukt im zweiten Schritt erzeugt.
  7. Verfahren nach einem der Ansprüche 1 bis 5, wobei man eine Menge an Flüssigkeit (27) als Endprodukt im ersten Schritt erzeugt und man eine Menge an Flüssigkeit kleiner als jene, die im ersten Schritt erzeugt wird, als Endprodukt im zweiten Schritt erzeugt.
  8. Verfahren nach einem der Ansprüche 1 bis 7, wobei der mit Druck beaufschlagte Flüssigkeitsstrom (17) reich an Stickstoff ist.
  9. Installation zur Lufttrennung durch kryogene Destillation, die geeignet ist, um das Verfahren nach Anspruch 1 auszuführen, eine Doppelsäule umfassend, die erste Säule und eine zweite Säule umfasst, wobei die zweite Säule mit einem geringeren Druck arbeitet, als die erste Säule, einen ersten Wärmetauscher (1), einen zweiten Wärmetauscher (2), der dazu fähig ist, und mit Zuführleitungen verbunden ist, um einen indirekten Wärmetausch zwischen nur zwei Fluiden zu ermöglichen, einen dritten Wärmetauscher (3), Mittel (5), um einen Luftstrom mit einem ersten Druck im Wesentlichen gleich dem Betriebsdruck der ersten Säule zum ersten Tauscher zu schicken, und vom ersten Tauscher zur ersten Säule, Mittel zum Teilen der Luft (7) mit einem zweiten Druck, der größer ist, als der erste Druck, in eine erste (9) und eine zweite Fraktion (11), Mittel, um die erste Fraktion (9) mit dem zweiten Druck durch eine erste der Zuführleitungen zum zweiten Tauscher zu schicken, ein Ventil (V2), um das Schicken der ersten Fraktion zum zweiten Tauscher zu verhindern, Mittel, um die zweite Fraktion (11) mit dem zweiten Druck zum dritten Tauscher zu schicken, eventuell weitere Mittel, um einen Luftstrom mit einem Druck, der größer ist, als der erste Druck, zum dritten Tauscher zu schicken, Mittel, um eine mit Druck beaufschlagte Flüssigkeit (15) aus der Doppelsäule zum Verdampfen in den dritten Tauscher zu schicken, Mittel, um eine im Einzelfall benötigte Flüssigkeit aus der Doppelsäule durch eine zweite (19) der Zuführleitungen zum Verdampfen in den zweiten Tauscher zu schicken, indem Wärme mit der ersten Fraktion ausgetauscht wird, ein Ventil (V3), um das Schicken der im Einzelfall benötigten Flüssigkeit aus der Doppelsäule zum zweiten Tauscher zu verhindern, Mittel, um ein stickstoffreiches Gas aus der ersten Säule zum Erwärmen in den ersten Tauscher zu schicken, ein Ventil (V1), um das Schicken von stickstoffreichem Gas aus der ersten Säule in den ersten Tauscher zu verhindern, Mittel, um ein mit Stickstoff angereichertes Gas aus der Doppelsäule zum ersten Tauscher zu schicken, und Mittel, um ein mit Stickstoff angereichertes Gas aus der Doppelsäule zum dritten Tauscher zu schicken.
  10. Installation nach Anspruch 9, wobei zumindest der erste und der dritte Wärmetauscher (1, 3) Plattenwärmetauscher und mit Rippen aus hartgelötetem Aluminium versehene Wärmetauscher sind.
EP13767026.1A 2012-09-12 2013-08-28 Verfahren und vorrichtung zur lufttrennung durch kryogene destillation Active EP2895811B1 (de)

Applications Claiming Priority (2)

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FR1258549A FR2995393B1 (fr) 2012-09-12 2012-09-12 Procede et appareil de separation d'air par distillation cryogenique.
PCT/FR2013/051985 WO2014041274A1 (fr) 2012-09-12 2013-08-28 Procédé et appareil de séparation d'air par distillation cryogénique.

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EP2963367A1 (de) * 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch
FR3062197B3 (fr) * 2017-05-24 2019-05-10 Air Liquide Procede et appareil pour la separation de l'air par distillation cryogenique
EP3438584B1 (de) * 2017-08-03 2020-03-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Verfahren und gerät zur trennung von luft durch kryogene destillation

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EP0093448B1 (de) * 1982-05-03 1986-10-15 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von gasförmigem Sauerstoff unter erhöhtem Druck
US5355682A (en) * 1993-09-15 1994-10-18 Air Products And Chemicals, Inc. Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen
EP2185879A1 (de) * 2007-08-10 2010-05-19 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und vorrichtung zur trennung von luft durch kryogene destillation
US20120125044A1 (en) * 2010-11-19 2012-05-24 Neil Mark Prosser Feed compression method and apparatus for air separation process

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CN104620067B (zh) 2017-03-08
WO2014041274A1 (fr) 2014-03-20
FR2995393A1 (fr) 2014-03-14
US20150241121A1 (en) 2015-08-27
US10012435B2 (en) 2018-07-03
FR2995393B1 (fr) 2014-10-03
CN104620067A (zh) 2015-05-13
EP2895811A1 (de) 2015-07-22

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