WO2013075867A1 - Procédé et dispositif pour séparer de l'air par distillation cryogénique - Google Patents

Procédé et dispositif pour séparer de l'air par distillation cryogénique Download PDF

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Publication number
WO2013075867A1
WO2013075867A1 PCT/EP2012/068948 EP2012068948W WO2013075867A1 WO 2013075867 A1 WO2013075867 A1 WO 2013075867A1 EP 2012068948 W EP2012068948 W EP 2012068948W WO 2013075867 A1 WO2013075867 A1 WO 2013075867A1
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WO
WIPO (PCT)
Prior art keywords
pressure column
column
liquid
conduit
argon
Prior art date
Application number
PCT/EP2012/068948
Other languages
English (en)
Inventor
Bao Ha
Jean-Renaud Brugerolle
Original Assignee
L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude filed Critical L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority to CN201280057446.7A priority Critical patent/CN103988036B/zh
Priority to US14/359,176 priority patent/US20140318179A1/en
Publication of WO2013075867A1 publication Critical patent/WO2013075867A1/fr

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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
    • 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
    • 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:
  • nitrogen enriched liquid is sent from the top of the high pressure column to the top of the low pressure column
  • oxygen rich liquid is removed from the low pressure column, pressurized and vaporized in the heat exchanger or another heat exchanger,
  • nitrogen rich liquid is removed from the column system, pressurized and vaporized in the heat exchanger or another heat exchanger, v) argon enriched gas is sent from the low pressure column to the argon column, said argon column having a top condenser, and argon rich fluid is removed from the top of the argon column,
  • oxygen enriched liquid from the bottom of the high pressure column is partially vaporized in the top condenser of the argon column and the gas thereby formed is sent to the low pressure column
  • an intermediate stream is removed at an intermediate point of the high pressure column and sent at least in part to a top condenser of the intermediate pressure column where it is partially vaporized to form a vapor and a liquid,
  • the intermediate pressure column has a bottom reboiler and wherein argon enriched gas from the low pressure column is condensed in the bottom reboiler.
  • the bottom liquid of the intermediate pressure column contains at least 70% mol. oxygen.
  • At least one of the bottom reboiler and the top condenser of the intermediate pressure column is a falling film reboiler.
  • At least one part of the feed air is compressed from a first pressure to a second pressure in a warm booster, fed to the heat exchanger at the second pressure, cooled, expanded in a first turboexpander and sent to the high pressure column and at least another part of the feed air is sent to the heat exchanger at the first pressure, divided into three portions, the first portion being compressed from the first pressure to a third pressure in a cold booster, cooled, expanded and sent to the high pressure column, the second portion being expanded in a second turboexpander and sent to the high pressure column and the third portion being cooled to the cold end of the heat exchanger and sent to the high pressure column.
  • 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
  • the intermediate pressure column has a bottom reboiler and the apparatus comprises a conduit for sending argon enriched gas from the low pressure column to be condensed in the bottom reboiler.
  • the liquid from the top condenser of the intermediate pressure column is sent to the intermediate pressure column between 2 and 5 theoretical trays above the bottom of the intermediate pressure column.
  • the apparatus comprises a compressor, a conduit for sending at least part of the air cooled to an intermediate temperature of the heat exchanger to the compressor, a conduit for sending air from the compressor to be further cooled in the heat exchanger and a conduit for sending the air from the compressor via the heat exchanger to at least the high pressure column.
  • the apparatus comprises a third pressurization means for pressurizing the liquid removed from the top condenser of the intermediate pressure column , before sending it to be separated in the intermediate pressure column.
  • 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 1 1 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 1 10 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 1 1 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)

Abstract

L'invention concerne un dispositif servant à séparer de l'air par distillation cryogénique et qui comprend un système de colonnes incluant une colonne double (100, 101), une colonne à pression intermédiaire (103), qui fonctionne à une pression comprise entre celle de la colonne à pression élevée et celle de la colonne à basse pression, et une colonne d'argon (102), un échangeur de chaleur (200), une conduite servant à envoyer de l'air comprimé purifié à refroidir dans l'échangeur de chaleur, une conduite pour envoyer l'air comprimé purifié refroidi provenant de l'échangeur de chaleur au moins partiellement vers la colonne à pression élevée, des moyens pour mettre sous pression et vaporiser le liquide riche en oxygène (30) provenant de la colonne à basse pression, des moyens pour mettre sous pression et vaporiser le liquide riche en azote (40), une conduite pour envoyer un gaz enrichi en argon (50,54) de la colonne à basse pression vers la colonne d'argon, ladite colonne d'argon comportant un condenseur supérieur (105), une conduite pour éliminer le fluide riche en argon (80) de la partie supérieure de la colonne d'argon, une conduite pour envoyer un écoulement d'air liquide (4, 20, 22) au moins partiellement vers un condenseur supérieur (107) de la colonne à pression intermédiaire, où ledit écoulement est partiellement vaporisé pour former une vapeur et un liquide, une conduite pour envoyer la vapeur (123) formée dans le condenseur supérieur de la colonne à pression intermédiaire vers la colonne à basse pression, et une conduite pour envoyer le liquide (24) provenant du condenseur supérieur de la colonne à pression intermédiaire vers la colonne à pression intermédiaire à des fins de séparation.
PCT/EP2012/068948 2011-11-24 2012-09-26 Procédé et dispositif pour séparer de l'air par distillation cryogénique WO2013075867A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
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
US14/359,176 US20140318179A1 (en) 2011-11-24 2012-09-26 Process And Apparatus For The Separation Of Air By Cryogenic Distillation

Applications Claiming Priority (2)

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EP11306552.8A EP2597409B1 (fr) 2011-11-24 2011-11-24 Procédé et installation pour la séparation de l'air par distillation cryogénique
EP11306552.8 2011-11-24

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WO2013075867A1 true WO2013075867A1 (fr) 2013-05-30

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US (1) US20140318179A1 (fr)
EP (1) EP2597409B1 (fr)
CN (1) CN103988036B (fr)
WO (1) WO2013075867A1 (fr)

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EP2634517B1 (fr) * 2012-02-29 2018-04-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil pour la séparation d'air par distillation cryogénique
FR3010778B1 (fr) * 2013-09-17 2019-05-24 Air Liquide Procede et appareil de production d'oxygene gazeux par distillation cryogenique de l'air
US10401083B2 (en) * 2015-03-13 2019-09-03 Linde Aktiengesellschaft Plant for producing oxygen by cryogenic air separation
EP3067650B1 (fr) * 2015-03-13 2018-04-25 Linde Aktiengesellschaft Installation et procede de production d'oxygene par separation cryogenique de l'air
KR101854623B1 (ko) 2016-06-15 2018-05-04 베니트엠 주식회사 중탄산암모늄 용액의 재생 방법
JP7355978B2 (ja) * 2019-04-08 2023-10-04 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 深冷空気分離装置
CN114174747A (zh) * 2019-07-26 2022-03-11 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的方法和设备
JP2021046961A (ja) * 2019-09-18 2021-03-25 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 高純度酸素製造システム
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US11193710B2 (en) * 2014-07-05 2021-12-07 Linde Aktiengesellschaft Method and apparatus for the cryogenic separation of air

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EP2597409B1 (fr) 2015-01-14
EP2597409A1 (fr) 2013-05-29
CN103988036B (zh) 2016-02-10
US20140318179A1 (en) 2014-10-30
CN103988036A (zh) 2014-08-13

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