EP2597409B1 - Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation - Google Patents

Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation Download PDF

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Publication number
EP2597409B1
EP2597409B1 EP11306552.8A EP11306552A EP2597409B1 EP 2597409 B1 EP2597409 B1 EP 2597409B1 EP 11306552 A EP11306552 A EP 11306552A EP 2597409 B1 EP2597409 B1 EP 2597409B1
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EP
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Prior art keywords
pressure column
column
liquid
sent
conduit
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EP11306552.8A
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English (en)
French (fr)
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EP2597409A1 (de
Inventor
Bao Ha
Jean-Renaud Brugerolle
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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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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
Priority to EP11306552.8A priority Critical patent/EP2597409B1/de
Priority to US14/359,176 priority patent/US20140318179A1/en
Priority to PCT/EP2012/068948 priority patent/WO2013075867A1/en
Priority to CN201280057446.7A priority patent/CN103988036B/zh
Publication of EP2597409A1 publication Critical patent/EP2597409A1/de
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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
    • F25J3/04006—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
    • 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
    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04248—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system

Definitions

  • the present invention relates to a process and apparatus for the separation of air by cryogenic distillation.
  • an intermediate pressure column can be added to the double column process to improve the distillation performance.
  • the main function of the intermediate pressure column is to distil the rich liquid bottom of the high pressure column to yield additional nitrogen rich liquid reflux for the low pressure column.
  • the intermediate pressure column is usually bottom heated or reboiled by condensing the nitrogen rich gas from the top of the high pressure column.
  • Double column process could have a side-arm column for argon extraction.
  • the reboil of the intermediate pressure column can be provided by feed gas to the argon side-arm column or by some gases derived from the argon column itself.
  • the intermediate pressure column operates at a pressure in between the pressures of the low pressure column and the high pressure column.
  • the argon and intermediate pressure columns can be used with the double column process, for example, to produce argon and to maximize the high pressure nitrogen extraction from the high pressure column. Good process efficiency can be achieved.
  • oxygen enriched liquid at the bottom of the high pressure column is fed to the intermediate pressure column and the resulting liquid extracted from the bottom of the intermediate pressure column is then partially vaporized in the top condensers of the intermediate and argon columns to provide the needed refluxes.
  • EP-A-0828123 utilizes the intermediate pressure column to improve the argon recovery when both liquid oxygen and liquid nitrogen are pumped and vaporized.
  • some liquid air is fed to the intermediate pressure column to produce additional bottom liquid of the intermediate pressure column.
  • Intermediate liquid with composition similar to air is mixed with intermediate pressure column's bottom liquid to provide cooling of the top condenser of the intermediate pressure column.
  • the top condenser of the argon column is also cooled by vaporizing bottom liquid of the intermediate pressure column.
  • Figure 2 discloses the use of the intermediate pressure column to enhance argon recovery.
  • the process is similar to that of EP-A-0828123 but more or almost all liquid air extracted from the high pressure column is sent to the intermediate pressure column to yield additional liquid nitrogen reflux.
  • the bottom stream of the intermediate pressure column is partially vaporized in its top condenser for cooling.
  • the liquid fraction is fed to the top condenser of the argon column and vaporized to supply the needed cooling.
  • the two top condensers of the intermediate and argon columns are in series in terms of receiving vaporizing liquid from the bottom of the intermediate pressure column.
  • a process for the separation of air by cryogenic distillation in a column system including a high pressure column, a low pressure column, the bottom of the low pressure column being thermally coupled with the top of the high pressure column, an intermediate pressure column, operating a pressure between that of the high pressure column and that of the low pressure column, and an argon column wherein:
  • an apparatus for the separation of air by cryogenic distillation comprising a column system including a high pressure column, a low pressure column, the bottom of the low pressure column being thermally coupled with the top of the high pressure column, an intermediate pressure column, operating a pressure between that of the high pressure column and that of the low pressure column, and an argon column a heat exchanger, means for sending purified compressed air to be cooled in the heat exchanger, means for sending cooled purified compressed air from the heat exchanger at least in part to the high pressure column, a conduit for sending nitrogen enriched liquid from the top of the high pressure column to the top of the low pressure column, a conduit for removing oxygen rich liquid from the low pressure column, said conduit being connected to first pressurization means, a conduit for sending pressurized oxygen rich liquid from the first pressurization means to the heat exchanger or another heat exchanger, a conduit for removing nitrogen rich liquid from the column system connected to second pressurization means, a conduit connecting the second pressurization means to the heat exchange
  • Purified air has been treated to remove the water and carbon dioxide which it contains.
  • Oxygen rich liquid contains at least 70% mol. oxygen, preferably at least 85% mol. oxygen. It contains less than 100% mol. oxygen.
  • Nitrogen rich liquid contains at least 85% mol. nitrogen, preferably at least 90% mol nitrogen. It contains less than 100% moll nitrogen.
  • Oxygen enriched liquid contains at least 25% mol oxygen, or at least 30% mol oxygen.
  • the high pressure column operates at between 4 and 8 bar, the intermediate pressure column at between 2 and 3 bar, the argon column at between 1 and 2 bar, the low pressure column at between 1 and 2 bar.
  • the gaseous oxygen produced by pumping and vaporizing can be as low as 2 bar and as high as 80 bar or even 100 bars.
  • the upper limit of the high pressure of pumped oxygen is usually dictated by the maximum allowable working pressure of the brazed heat exchanger.
  • the intermediate stream withdrawn from the high pressure column and sent to the intermediate pressure column top condenser contains between 18 and 25 mol% oxygen.
  • Figure 1 shows the column portion of a process operating according to the invention and Figures 2 and 3 show two alternative corresponding heat exchanger portions, to be used for oxygen pressures above 15 bars abs.
  • gaseous air 2 and liquid air 4 are fed to high pressure column 100.
  • Oxygen enriched liquid 10 formed at the bottom of the high pressure column 100 is divided in two. One portion 12 is expanded and sent to an intermediate level of the low pressure column 101. Another portion 11 is expanded and sent to top condenser 105 of the argon column where it vaporizes to form stream 13 which is sent to the low pressure column 101.
  • all the oxygen enriched liquid 10 can be sent to the condenser 105 and partially condensed. In this case, stream 12 is absent and liquid from condenser 105 is sent to the low pressure column 101.
  • the top of the high pressure column 100 is thermally coupled to the bottom of the low pressure column 101 via a condenser-reboiler 104.
  • Nitrogen enriched liquid 40 from the top of the high pressure column 100 is divided in two, one portion 41 being sent to the top of the low pressure column 101 as reflux. Nitrogen enriched gas is removed from the top of the low pressure column 101.
  • a side liquid stream 20 with composition similar to air, containing between 18 and 25% mol. oxygen is extracted from column 100.
  • the side liquid stream could be replaced or supplemented by a part of liquid air stream 4 or another liquid air stream.
  • a portion 22 of stream 20 (or stream 4, not illustrated) is partially vaporized in the top condenser 107 of intermediate pressure column 103.
  • Condenser 107 could be a falling film vaporizer.
  • the vapor 123 containing around 10% mol. oxygen) is sent to the low pressure column 101.
  • a portion 24 of the liquid fraction 26 of the partially vaporization is then fed to column 103.
  • Column 103 operates at about 2 bar and its condenser 107 at 1.4 bar.
  • Gravity feed or a pump 110 can be used to transfer this liquid from condenser 107 to a position between 2 and 5 theoretical trays above the bottom of intermediate pressure column 103.
  • Oxygen enriched liquid 60 from the bottom of column 103 containing preferably between 70 and 75 mol% oxygen is expanded and sent to the low pressure column. It is useful to note that a liquid air stream formed from the condensation of air for vaporizing liquid oxygen and liquid nitrogen products in the main heat exchanger can be sent to the top condenser of the intermediate column instead of using a part of the liquid stream 20 extracted from the high pressure column.
  • the average temperature difference for condensers 106, 107 should be between 0.8 and 0.9°C.
  • Column 103 produces additional reflux liquid 23 for the top of the low pressure column 101.
  • Column 102 is a typical side-arm argon column for a double column process. A portion 54 of argon enriched feed gas from the low pressure column 101 is separated in the argon column 102 to form argon product 80 in liquid form as shown or in gaseous form. The bottom liquid 52 from the argon column is sent back to the low pressure column 101.
  • a portion 51 of argon enriched feed gas 50 from the low pressure column 101 is condensed in the bottom reboiler 106, preferably of the falling film type, of column 103 to yield liquid 53 which is then fed to column 102 or 101 to be separated.
  • the argon column 102 is equipped with a top condenser 105 which vaporizes a portion 11 of oxygen enriched liquid 10 produced at the bottom of the high pressure column 100.
  • Another portion 45 of stream 40 is pumped by pump 121 to high pressure, vaporized and warmed to yield high pressure nitrogen product.
  • Liquid oxygen 30 produced at the bottom of column 101 is pumped by pump 120 to high pressure, vaporized and warmed to yield high pressure oxygen product.
  • the embodiment shown in Figure 2 can be used to vaporize efficiently the liquid products 31, 42.
  • the liquid products are vaporized in pumps 120,121, the oxygen being pressurized to a pressure between 15 and 80 bars abs.
  • the cold compression technique is utilized and is described as follows:
  • Feed air compressed by compressor 201 to an elevated pressure of about between 15 and 25 bar is dried and its CO 2 content is removed in the front end purification unit 208.
  • the resulting dried and CO 2 free stream 80 is divided into several portions.
  • Portion 83 is cooled in heat exchanger 200 to an intermediate temperature thereof, a portion 91 of portion 83 is expanded in turboexpander 204 into the high pressure column 100.
  • Second portion 84 of portion 83 is cold compressed, at a inlet temperature which is an intermediate temperature of the heat exchanger, in cold booster 202 to higher pressure to yield stream 85.
  • Stream 85 is next cooled in exchanger 200 and liquefied to form liquid air stream 4.
  • Another portion 79 of the cooled stream 83 is further cooled and liquefied to yield a second liquid air stream 6.
  • Streams 4 and 6 are fed at least in part to the high pressure column 100 as feeds.
  • a third portion 82 of feed air is further compressed in warm booster 207, cooled in exchanger 200 to yield cooled compressed stream 88 which is then expanded in turboexpander 203 into the high pressure column 100.
  • the power generated by turboexpanders 203 and 204 can be used to drive boosters 202 and 207.
  • turboexpanders 203 and 204 can be used to drive boosters 202 and 207.
  • the resulting liquid stream (not shown) is then fed to the column system.
  • By generating those auxiliary liquid streams less liquid, i.e. lower flow, needs to be compressed by the cold compressor to satisfy the refrigeration balance at the cold end of the exchanger. More efficient system can be achieved by reducing the required cold compression flow.
  • a multi stage booster compressor comprising several stages 209, 210 and 211 is added to further compress the fraction 82 feeding compressor 207.
  • Multiple pressurized streams 95 and 96 can be generated by the booster compressor to vaporize efficiently the liquid products to form liquid air streams 97 and 99.
  • a cold booster has an inlet temperature of below -20°C.

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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 (15)

  1. Verfahren zur Luftzerlegung durch Tieftemperaturdestillation in einem Kolonnensystem, umfassend eine Hochdruckkolonne (100), eine Niederdruckkolonne (101), wobei das untere Ende der Niederdruckkolonne thermisch mit dem oberen Ende der Hochdruckkolonne gekoppelt ist, eine Zwischendruckkolonne (103), die bei einem Druck betrieben wird, der zwischen dem der Hochdruckkolonne und dem der Niederdruckkolonne liegt, sowie eine Argonkolonne (102), wobei:
    i) gereinigte Druckluft in einem Wärmetauscher (200) abgekühlt und wenigstens zum Teil in die Hochdruckkolonne geleitet wird,
    ii) mit Stickstoff angereicherte Flüssigkeit (40, 41) aus dem oberen Ende der Hochdruckkolonne zum oberen Ende der Niederdruckkolonne geleitet wird,
    iii) sauerstoffreiche Flüssigkeit (30) aus der Niederdruckkolonne entnommen, mit Druck beaufschlagt und im Wärmetauscher oder in einem anderen Wärmetauscher verdampft wird,
    iv) stickstoffreiche Flüssigkeit (42) aus dem Kolonnensystem entnommen, mit Druck beaufschlagt und im Wärmetauscher oder in einem anderen Wärmetauscher verdampft wird,
    v) mit Argon angereichertes Gas aus der Niederdruckkolonne in die Argonkolonne geleitet wird, wobei die Argonkolonne einen oben angeordneten Kondensator (105) aufweist und argonreiches Fluid (80) aus dem oberen Ende der Argonkolonne entnommen wird,
    vi) mit Sauerstoff angereicherte Flüssigkeit (11) aus dem unteren Ende der Hochdruckkolonne im oben angeordneten Kondensator der Argonkolonne teilweise verdampft wird und das dabei gebildete Gas (13) in die Niederdruckkolonne geleitet wird,
    vii) ein Strom (4) aus flüssiger Luft oder ein Strom (20, 22) mit zwischen 18 und 25 Mol-% Sauerstoff, der an einem Punkt der Hochdruckkolonne entnommen wird, wenigstens zum Teil in einen oben angeordneten Kondensator (107) der Zwischendruckkolonne geleitet wird, wo er teilweise verdampft wird, um einen Dampf und eine Flüssigkeit zu erzeugen,
    viii) der im oben angeordneten Kondensator der Zwischendruckkolonne erzeugte Dampf (123) in die Niederdruckkolonne geleitet wird,
    ix) die im oben angeordneten Kondensator der Zwischendruckkolonne erzeugte Flüssigkeit (24) zum Trennen in die Zwischendruckkolonne geleitet wird,
    x) eine Flüssigkeit (60) aus dem unteren Ende der Zwischendruckkolonne in die Niederdruckkolonne geleitet wird, und
    xi) eine Flüssigkeit aus dem oberen Ende der Zwischendruckkolonne (23) zum oberen Ende der Niederdruckkolonne geleitet wird.
  2. Vorgang nach Anspruch 1, wobei die Zwischendruckkolonne einen unten angeordneten Verdampfer (106) aufweist und wobei mit Argon angereichertes Gas (51) aus der Niederdruckkolonne im unten angeordneten Verdampfer kondensiert wird.
  3. Vorgang nach Anspruch 1 oder 2, wobei die aus dem oben angeordneten Kondensator der Zwischendruckkolonne weitergeleitete Flüssigkeit (24) den einzigen in der Zwischendruckkolonne abgeschiedenen Strom ausmacht.
  4. Vorgang nach einem der vorhergehenden Ansprüche, wobei die gesamte mit Sauerstoff angereichte Flüssigkeit (10, 11, 12) aus der Hochdruckkolonne in den oben angeordneten Kondensator (105) der Argonkolonne oder in die Niederdruckkolonne und den oben angeordneten Kondensator der Argonkolonne geleitet wird, ohne den oben angeordneten Kondensator der Zwischendruckkolonne zu passieren.
  5. Vorgang nach einem der vorhergehenden Ansprüche, wobei die gesamte Flüssigkeit (60) aus dem unteren Ende der Zwischendruckkolonne in die Niederdruckkolonne geleitet wird, ohne den oben angeordneten Kondensator der Zwischendruckkolonne zu passieren.
  6. Vorgang nach einem der vorhergehenden Ansprüche, wobei ein Teil (25) der Flüssigkeit vom oben angeordneten Kondensator (107) der Zwischendruckkolonne in die Niederdruckkolonne geleitet wird.
  7. Vorgang nach einem der vorhergehenden Ansprüche, wobei die Flüssigkeit (24) aus dem oben angeordneten Kondensator in die Zwischendruckkolonne (103) an einem Punkt eingeleitet wird, der zwischen 2 und 5 gedachte Kolonnenböden über dem unteren Ende der Zwischendruckkolonne liegt.
  8. Verfahren nach einem der vorhergehenden Ansprüche, wobei wenigstens ein Teil der Luft auf eine Zwischentemperatur des Wärmetauschers (200) abgekühlt, in einem Kompressor (202) komprimiert, im Wärmetauscher weiter abgekühlt und wenigstens zur Hochdruckkolonne (100) geleitet wird.
  9. Verfahren nach einem der vorhergehenden Ansprüche, wobei die Flüssigkeit (60) aus dem unteren Ende der Zwischendruckkolonne (103) wenigstens 70 Mol-% Sauerstoff enthält.
  10. Vorgang nach einem der vorhergehenden Ansprüche, wobei der unten angeordnete Verdampfer (106) und/oder der oben angeordnete Kondensator (107) der Zwischendruckkolonne (103) ein Fallfilmverdampfer ist.
  11. Vorgang nach einem der vorhergehenden Ansprüche, wobei wenigstens ein Teil der Speiseluft in einem warmen Booster (207) von einem ersten Druck auf einen zweiten Druck komprimiert, bei dem zweiten Druck in den Wärmetauscher geleitet, abgekühlt, in einem ersten Turboexpander (203) expandiert und in die Hochdruckkolonne geleitet wird, und wenigstens ein weiterer Teil der Speiseluft beim ersten Druck in den Wärmetauscher geleitet und in drei Teile geteilt wird, wobei der erste Teil in einem kalten Booster (202) vom ersten Druck auf einen dritten Druck komprimiert, abgekühlt, expandiert und in die Hochdruckkolonne geleitet wird, der zweite Teil in einem zweiten Turboexpander (204) expandiert und in die Hochdruckkolonne geleitet wird, und der dritte Teil auf die Temperatur am kalten Ende des Wärmetauschers abgekühlt und in die Hochdruckkolonne geleitet wird.
  12. Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation, welche Folgendes umfasst: ein Kolonnensystem mit einer Hochdruckkolonne (100), einer Niederdruckkolonne (101), wobei das untere Ende der Niederdruckkolonne thermisch mit dem oberen Ende der Hochdruckkolonne gekoppelt ist, einer Zwischendruckkolonne (103), die bei einem Druck zwischen dem der Hochdruckkolonne und dem der Niederdruckkolonne betrieben wird, und einer Argonkolonne (102), einen Wärmetauscher (200), eine Leitung zum Leiten von gereinigter Druckluft zum Abkühlen in den Wärmetauscher, eine Leitung zum Leiten von abgekühlter gereinigter Druckluft aus dem Wärmetauscher wenigstens zum Teil in die Hochdruckkolonne, eine Leitung zum Leiten von mit Stickstoff angereicherter Flüssigkeit (40, 41) aus dem oberen Ende der Hochdruckkolonne zum oberen Ende der Niederdruckkolonne, eine Leitung zum Entnehmen von sauerstoffreicher Flüssigkeit (30) aus der Niederdruckkolonne, wobei die Leitung mit ersten Druckbeaufschlagungsmitteln (120) verbunden ist, eine Leitung zum Leiten von druckbeaufschlagter sauerstoffreicher Flüssigkeit aus den ersten Druckbeaufschlagungsmitteln zum Wärmetauscher oder zu einem anderen Wärmetauscher, eine Leitung zum Entnehmen von stickstoffreicher Flüssigkeit (40) aus dem Kolonnensystem, verbunden mit zweiten Druckbeaufschlagungsmitteln (121), eine Leitung zum Verbinden der zweiten Druckbeaufschlagungsmittel mit dem Wärmetauscher oder mit einem anderen Wärmetauscher, eine Leitung zum Leiten von mit Argon angereichertem Gas (50, 54) aus der Niederdruckkolonne zur Argonkolonne, wobei die Argonkolonne einen oben angeordneten Kondensator (105) aufweist, eine Leitung zum Entnehmen von argonreicher Flüssigkeit (80) aus dem oberen Ende der Argonkolonne, eine Leitung zum Leiten von mit Sauerstoff angereicherter Flüssigkeit (10, 11) aus dem unteren Ende der Hochdruckkolonne zum oben angeordneten Kondensator der Argonkolonne, um dort teilweise verdampft zu werden, eine Leitung, um das dabei erzeugte Gas (13) in die Niederdruckkolonne zu leiten, eine Leitung, um einen Strom (4) aus flüssiger Luft oder einen flüssigen Strom (20, 22) mit zwischen 18 und 25 % Sauerstoff, der an einem Punkt der Hochdruckkolonne entnommen wird, wenigstens zum Teil in einen oben angeordneten Kondensator (107) der Zwischendruckkolonne zu leiten, wo er teilweise verdampft wird, um einen Dampf und eine Flüssigkeit zu erzeugen, eine Leitung, um den im oben angeordneten Kondensator der Zwischendruckkolonne erzeugten Dampf (123) in die Niederdruckkolonne zu leiten, eine Leitung, um die Flüssigkeit (24) aus dem oben angeordneten Kondensator der Zwischendruckkolonne zum Trennen in die Zwischendruckkolonne zu leiten, eine Leitung, um eine Flüssigkeit (60) aus dem unteren Ende der Zwischendruckkolonne zur Niederdruckkolonne zu leiten, und eine Leitung, um eine Flüssigkeit (23) aus dem oberen Ende der Zwischendruckkolonne zum oberen Ende der Niederdruckkolonne zu leiten.
  13. Vorrichtung nach Anspruch 12, wobei die Zwischendruckkolonne (103) einen unten angeordneten Verdampfer (106) aufweist und eine Leitung umfasst, um mit Argon angereichertes Gas (51) aus der Niederdruckkolonne im unten angeordneten Verdampfer zu kondensieren.
  14. Vorrichtung nach Anspruch 12 oder 13, wobei die Flüssigkeit (24) aus dem oben angeordneten Kondensator in die Zwischendruckkolonne (103) an einem Punkt eingeleitet wird, der zwischen 2 und 5 gedachte Kolonnenböden über dem unteren Ende der Zwischendruckkolonne liegt.
  15. Vorrichtung nach einem der Ansprüche 12 bis 14, welche Folgendes umfasst: einen Kompressor, eine Leitung, um wenigstens einen Teil der auf eine Zwischentemperatur des Wärmetauschers abgekühlte Luft zum Kompressor (202) zu leiten, eine Leitung, um Luft aus dem Kompressor zu zum weiteren Abkühlen im Wärmetauscher leiten, und eine Leitung, um Luft aus dem Kompressor über den Wärmetauscher wenigstens zur Hochdruckkolonne zu leiten.
EP11306552.8A 2011-11-24 2011-11-24 Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation Not-in-force EP2597409B1 (de)

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US14/359,176 US20140318179A1 (en) 2011-11-24 2012-09-26 Process And Apparatus For The Separation Of Air By Cryogenic Distillation
PCT/EP2012/068948 WO2013075867A1 (en) 2011-11-24 2012-09-26 Process and apparatus for the separation of air by cryogenic distillation
CN201280057446.7A CN103988036B (zh) 2011-11-24 2012-09-26 用于通过低温蒸馏分离空气的方法和设备

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FR3010778B1 (fr) 2013-09-17 2019-05-24 Air Liquide Procede et appareil de production d'oxygene gazeux par distillation cryogenique de l'air
PL2963370T3 (pl) * 2014-07-05 2018-11-30 Linde Aktiengesellschaft Sposób i urządzenie do kriogenicznego rozdziału powietrza
US10401083B2 (en) * 2015-03-13 2019-09-03 Linde Aktiengesellschaft Plant for producing oxygen by cryogenic air separation
EP3067650B1 (de) * 2015-03-13 2018-04-25 Linde Aktiengesellschaft Anlage und verfahren zur erzeugung von sauerstoff durch tieftemperaturzerlegung von luft
KR101854623B1 (ko) 2016-06-15 2018-05-04 베니트엠 주식회사 중탄산암모늄 용액의 재생 방법
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