US20070204652A1 - Process and apparatus for producing ultrapure oxygen - Google Patents

Process and apparatus for producing ultrapure oxygen Download PDF

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US20070204652A1
US20070204652A1 US11/676,773 US67677307A US2007204652A1 US 20070204652 A1 US20070204652 A1 US 20070204652A1 US 67677307 A US67677307 A US 67677307A US 2007204652 A1 US2007204652 A1 US 2007204652A1
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oxygen
column
stream
purity oxygen
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Paul MUSICUS
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Linde Process Plants Inc
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Linde Process Plants Inc
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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
    • 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
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • 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
    • F25J3/04406—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a process and an apparatus for producing ultrapure oxygen incorporating a single distillation column for nitrogen production and a high-purity oxygen column.
  • the process and the apparatus do not exhibit any further separation column.
  • the invention comprises a process and an apparatus for producing ultrapure oxygen, the process comprising the following steps:
  • “Ultrapure” oxygen means an oxygen fraction with a total molar content of impurities of 1000 ppb or less, preferably 100 ppb or less, more preferably 10 ppb or less.
  • the “oxygen-containing stream” used as feed mixture for the high-purity oxygen has an oxygen content of 5% or more, preferably 10% or more, more preferably 15% or more. (All percentage values are on a molar basis.)
  • the single drawing shows an embodiment of the invention.
  • atmospheric air 1 flows through a filter 2 and is compressed by an air compressor 3 to a pressure of 8 to 13 bars, preferably about 11 bars (all pressure values in this document are gauge, i.e. above atmospheric).
  • the compressed air 6 is introduced into a purification device 7 comprising a pair of vessels filled with adsorptive material.
  • the purified air 8 is cooled in main heat exchanger 9 to about its dewpoint.
  • a first portion 11 of the cold air feed air stream 10 is introduced in gaseous (or slightly wet) form into a single distillation column 12 for producing nitrogen, preferably some theoretical or practical trays above the bottom.
  • the single column 12 is operated at a pressure of 7 to 12 bars, preferably about 10 bars. Its head condenser 13 operated by vaporizing bottom liquid 14 and a nitrogen-richer liquid 18 withdrawn from an intermediate stage some theoretical or practical trays above the gaseous air inlet. As its main product, gaseous pressurized nitrogen is withdrawn via lines 15 , 16 , warmed to about ambient temperature in main heat exchanger 9 . It leaves the plant via line 17 as pressurized gaseous nitrogen product (PGAN).
  • GPN pressurized gaseous nitrogen product
  • a first waste gas 19 produced by evaporation of the bottom liquid 14 is warmed to an intermediate temperature in the main heat exchanger 9 , withdrawn via line 20 and work-expanded in one turbine (not shown) or in two parallel turbines 21 , 22 from a pressure of 4 to 8 bars, preferably about 6 bars to a pressure of pressure of 0.25 to 1 bars, preferably about 0.5 bars.
  • the work-expanded stream 23 is warmed to about ambient temperature in main heat exchanger 9 .
  • the warm first waste gas stream 24 is released to the atmosphere (line 25 ), and/or used as regeneration gas 26 , 27 in purification device 7 , eventually after heating in heating device 28 .
  • a second waste gas 29 produced by evaporation of the intermediate liquid 18 is compressed from a pressure of 4 to 8 bars, preferably about 6 bars to a pressure of 7 to 12 bars, preferably about 10 bars in a cold compressor 30 driven by turbine 21 , cooled in main heat exchanger 9 and reintroduced via line 31 into the single column 12 at its bottom.
  • a portion of the nitrogen product of the single column may be withdrawn as a liquid product LIN from the head condenser 13 via line 32 , after being subcooled in subcooler 33 .
  • a portion 35 of the subcooled liquid nitrogen 34 is expanded and used for delivering refrigeration to the subcooler 33 and admixed to the work-expanded waste gas afterwards.
  • An oxygen-containing stream 36 is withdrawn in liquid form from an intermediate section of the single column 12 , which is at least 5 to 25 practical or theoretical trays above any feed air inlet.
  • the liquid oxygen-containing stream is eventually subcooled in a bottom reboiler 37 of a high-purity oxygen column 38 and fed via line 39 to the top of the high-purity oxygen column 38 after having been expanded through valve 40 to a pressure of 0.25 to 1 bars, preferably about 0.5 bars.
  • the liquid refluxing column 38 is further enriched in oxygen.
  • a portion 44 is withdrawn as liquid ultrapure oxygen product UHPLOX from 1 to 5 trays, preferably about 3 practical or theoretical trays above the bottom.
  • the remainder is reboiled in bottom reboiler 37 for producing rising vapour in the high-purity oxygen column.
  • Some purge liquid 41 is withdrawn from time to time or continuously from the bottom, i.e. from the evaporation space of bottom reboiler 37 .
  • reboiler 37 is driven at least in part by a second portion 42 of the feed air stream 10 .
  • Such air portion is at least partially, e.g. totally condensed and subcooled in bottom reboiler 37 .
  • the liquefied air 43 is introduced into the single column 12 at an intermediate section somewhat above the gaseous air introduction.
  • At least a portion of the process refrigeration is delivered in form of an external cryogenic liquid, e.g. by liquid nitrogen from a tank, which is injected into single column 12 or into the evaporation space of head condenser 13 .
  • an external cryogenic liquid e.g. by liquid nitrogen from a tank
  • Such liquid injection may partially or totally replace the work expansion 21 and 22 of process streams as shown in the drawing.
  • the nitrogen subcooler 33 may be omitted and/or a subcooler for liquid ultrapure oxygen product 44 may be added.
  • the nitrogen products 17 , 34 can be either ultra-high-purity (ppb impurity) or normal commercial grade (ppm impurity).
  • the ultrapure oxygen product 44 can also be recovered as commercial grade LOX (95 to 99.9%); in this case, the safety purge 41 may be omitted.
  • the ultrapure oxygen product can also be withdrawn as a gas and warmed up in the main exchanger 9 .
  • At least a portion compressed recycled second waste gas 31 may be used as heating medium in the botttom reboiler 37 instead of feed air 42 .
  • the condensed recycle fluid produced in the botteom reboiler 37 would flow either to the single column 12 or directly to the head condenser 13 , eventually after being combined with stream 18 after its valve.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

For the production of ultrapure oxygen, conduct the followig steps: introduce a feed air stream (10, 11, 42, 43) into a single distillation column (12) for producing nitrogen; withdraw an oxygen-containing stream (36, 39) from an intermediate stage of the single distillation column (12), introduce the oxygen-containing stream (36, 39) into an upper section of a high-purity oxygen column (38), and withdraw an ultrapure oxygen product stream (44) from the high-purity oxygen column (38), with the caveat that rising vapour for the high-purity oxygen column (38) is produced by indirect heat exchange in a reboiler (37) between a liquid fraction from a lower section of the high-purity oxygen column and a gaseous heating stream (42), so that the heating stream (42) is at least partially condensed during such indirect heat exchange.

Description

  • This application claims the benefit of the filing date of U.S. Provisional Application Ser. No. 60/774,662 filed Feb. 21, 2006.
  • The invention relates to a process and an apparatus for producing ultrapure oxygen incorporating a single distillation column for nitrogen production and a high-purity oxygen column. Preferably, the process and the apparatus do not exhibit any further separation column.
    • BACKGROUND OF THE INVENTION
  • Such process is known from U.S. Pat. No. 5,689,973 where rising vapour for the high-purity oxygen column is produced by condensing and subcooling a portion of the oxygen-containing feed mixture for the high-purity oxygen column in a bottom reboiler.
    • SUMMARY OF THE INVENTION
  • It is an object of the invention to provide a process and apparatus which is economically advantageous.
  • It is a further object of the invention to provide a process and an apparatus with optimized reboiling of the high-purity oxygen column.
  • Upon further study of the specification and appended claims, other aspects of the invention will become apparent.
  • In brief, the invention comprises a process and an apparatus for producing ultrapure oxygen, the process comprising the following steps:
      • introducing a feed air stream into a single distillation column for producing nitrogen,
      • withdrawing an oxygen-containing stream from an intermediate stage of the single distillation column,
      • introducing the oxygen-containing stream into an upper section of a high-purity oxygen column, and
      • withdrawing an ultrapure oxygen product stream from the high-purity oxygen column,
        whereby
      • rising vapour for the high-purity oxygen column is produced by indirect heat exchange in a reboiler between a liquid fraction from a lower section of the high-purity oxygen column and a gaseous heating stream,
      • whereby the heating stream is at least partially condensed during such indirect heat exchange.
  • By providing reboil for the high-purity oxygen column by a gaseous heating stream, which is at least partially condensed in a reboiler of the high-purity oxygen column, the following advantages are achieved:
      • Increased yield of either ultrapure oxygen, gaseous or liquid nitrogen product, or both.
      • Reduced feed air requirement for fixed ultrapure oxygen or nitrogen production.
      • Reduced length of high-purity oxygen column.
  • “Ultrapure” oxygen means an oxygen fraction with a total molar content of impurities of 1000 ppb or less, preferably 100 ppb or less, more preferably 10 ppb or less.
  • The “oxygen-containing stream” used as feed mixture for the high-purity oxygen has an oxygen content of 5% or more, preferably 10% or more, more preferably 15% or more. (All percentage values are on a molar basis.)
  • Additional preferred features of the invention are listed in the dependent claims.
    • BRIEF DESCRIPTION OF THE DRAWING
  • The single drawing shows an embodiment of the invention.
    • DETAILED DESCRIPTION OF THE DRAWING
  • In the embodiment of the drawing, atmospheric air 1 flows through a filter 2 and is compressed by an air compressor 3 to a pressure of 8 to 13 bars, preferably about 11 bars (all pressure values in this document are gauge, i.e. above atmospheric). After an aftercooler 4 and a water separator 5, the compressed air 6 is introduced into a purification device 7 comprising a pair of vessels filled with adsorptive material. The purified air 8 is cooled in main heat exchanger 9 to about its dewpoint. A first portion 11 of the cold air feed air stream 10 is introduced in gaseous (or slightly wet) form into a single distillation column 12 for producing nitrogen, preferably some theoretical or practical trays above the bottom.
  • The single column 12 is operated at a pressure of 7 to 12 bars, preferably about 10 bars. Its head condenser 13 operated by vaporizing bottom liquid 14 and a nitrogen-richer liquid 18 withdrawn from an intermediate stage some theoretical or practical trays above the gaseous air inlet. As its main product, gaseous pressurized nitrogen is withdrawn via lines 15,16, warmed to about ambient temperature in main heat exchanger 9. It leaves the plant via line 17 as pressurized gaseous nitrogen product (PGAN).
  • A first waste gas 19 produced by evaporation of the bottom liquid 14 is warmed to an intermediate temperature in the main heat exchanger 9, withdrawn via line 20 and work-expanded in one turbine (not shown) or in two parallel turbines 21, 22 from a pressure of 4 to 8 bars, preferably about 6 bars to a pressure of pressure of 0.25 to 1 bars, preferably about 0.5 bars. The work-expanded stream 23 is warmed to about ambient temperature in main heat exchanger 9. The warm first waste gas stream 24 is released to the atmosphere (line 25), and/or used as regeneration gas 26, 27 in purification device 7, eventually after heating in heating device 28.
  • A second waste gas 29 produced by evaporation of the intermediate liquid 18 is compressed from a pressure of 4 to 8 bars, preferably about 6 bars to a pressure of 7 to 12 bars, preferably about 10 bars in a cold compressor 30 driven by turbine 21, cooled in main heat exchanger 9 and reintroduced via line 31 into the single column 12 at its bottom.
  • A portion of the nitrogen product of the single column may be withdrawn as a liquid product LIN from the head condenser 13 via line 32, after being subcooled in subcooler 33. A portion 35 of the subcooled liquid nitrogen 34 is expanded and used for delivering refrigeration to the subcooler 33 and admixed to the work-expanded waste gas afterwards.
  • An oxygen-containing stream 36, being essentially free of lower-boiling impurities, is withdrawn in liquid form from an intermediate section of the single column 12, which is at least 5 to 25 practical or theoretical trays above any feed air inlet. The liquid oxygen-containing stream is eventually subcooled in a bottom reboiler 37 of a high-purity oxygen column 38 and fed via line 39 to the top of the high-purity oxygen column 38 after having been expanded through valve 40 to a pressure of 0.25 to 1 bars, preferably about 0.5 bars.
  • The liquid refluxing column 38 is further enriched in oxygen. A portion 44 is withdrawn as liquid ultrapure oxygen product UHPLOX from 1 to 5 trays, preferably about 3 practical or theoretical trays above the bottom. The remainder is reboiled in bottom reboiler 37 for producing rising vapour in the high-purity oxygen column. Some purge liquid 41 is withdrawn from time to time or continuously from the bottom, i.e. from the evaporation space of bottom reboiler 37.
  • According to the invention, reboiler 37 is driven at least in part by a second portion 42 of the feed air stream 10. Such air portion is at least partially, e.g. totally condensed and subcooled in bottom reboiler 37. The liquefied air 43 is introduced into the single column 12 at an intermediate section somewhat above the gaseous air introduction.
  • There are many variations of the process within the scope of the invention. In a first variation of the embodiment, at least a portion of the process refrigeration is delivered in form of an external cryogenic liquid, e.g. by liquid nitrogen from a tank, which is injected into single column 12 or into the evaporation space of head condenser 13. Such liquid injection may partially or totally replace the work expansion 21 and 22 of process streams as shown in the drawing. As another variant, the nitrogen subcooler 33 may be omitted and/or a subcooler for liquid ultrapure oxygen product 44 may be added.
  • The nitrogen products 17, 34 can be either ultra-high-purity (ppb impurity) or normal commercial grade (ppm impurity). The ultrapure oxygen product 44 can also be recovered as commercial grade LOX (95 to 99.9%); in this case, the safety purge 41 may be omitted. The ultrapure oxygen product can also be withdrawn as a gas and warmed up in the main exchanger 9.
  • In a further variation, at least a portion compressed recycled second waste gas 31 may be used as heating medium in the botttom reboiler 37 instead of feed air 42. The condensed recycle fluid produced in the botteom reboiler 37 would flow either to the single column 12 or directly to the head condenser 13, eventually after being combined with stream 18 after its valve.
  • Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent. The preceding preferred specific embodiments are, therefore, to be construed as merely illustrative, and not limitative of the remainder of the disclosure in any way whatsoever.
  • In the foregoing and in the examples, all temperatures are set forth uncorrected in degrees Celsius and, all parts and percentages are by weight, unless otherwise indicated.
  • The entire disclosures of all applications, patents and publications, cited herein and of corresponding U.S. Provisional Application Ser. No. 60/774,552, filed Feb. 21, 2006, are incorporated by reference herein.
  • The preceding examples can be repeated with similar success by substituting the generically or specifically described reactants and/or operating conditions of this invention for those used in the preceding examples.
  • From the foregoing description, one skilled in the art can easily ascertain the essential characteristics of this invention and, without departing from the spirit and scope thereof, can make various changes and modifications of the invention to adapt it to various usages and conditions.

Claims (17)

1. A process for producing ultrapure oxygen, the process comprising the following steps:
introducing a feed air stream (10, 11, 42, 43) into a single distillation column (12) for producing nitrogen,
withdrawing an oxygen-containing stream (36, 39) from an intermediate stage of the single distillation column (12),
introducing the oxygen-containing stream (36, 39) into an upper section of a high-purity oxygen column (38), and
withdrawing an ultrapure oxygen product stream (44) from the high-purity oxygen column (38), wherein
rising vapour for the high-purity oxygen column (38) is produced by indirect heat exchange in a reboiler (37) between a liquid fraction from a lower section of the high-purity oxygen column and a gaseous heating stream (42),
whereby the gaseous heating stream (42) is at least partially condensed during such indirect heat exchange.
2. A according to claim 1, whereby the gaseous heating stream (42) comprises at least a portion of the feed air stream (10).
3. A process according to claim 1, wherein or the gaseous heating stream (42) downstream of the indirect heat exchange (37) is introduced into the single distillation column (12).
4. A process according to claim 1, wherein the oxygen-containing stream (36, 39) is introduced into the top of the high-purity oxygen column (38).
5. A process according to claim 1, wherein at least a portion of the oxygen-containing stream (36) is subcooled in the reboiler (37) before being introduced (39) into the high-purity oxygen column (38).
6. A process according claim 1, wherein the ultrapure oxygen product stream (44) is withdrawn from an intermediate section of the high-purity oxygen column (38).
7. A process according to claim 1, wherein the ultrapure oxygen product stream (44) is withdrawn from the high-purity oxygen column (38) in a liquid state.
8. A process according to claim 7, wherein the ultrapure oxygen product stream is withdrawn as a final liquid product.
9. Apparatus for producing ultrapure oxygen the process comprising
means for introducing a feed air stream (10, 11, 42, 43) into a single distillation column (12) for producing nitrogen,
means for withdrawing an oxygen-containing stream (36, 39) from an intermediate stage of the single distillation column (12),
means for introducing the oxygen-containing stream (36, 39) into an upper section of a high-purity oxygen column (38), and
means for withdrawing an ultrapure oxygen product stream (44) from the high-purity oxygen column (38),
the apparatus further comprising
a reboiler (37) for producing rising vapour for the high-purity oxygen column (38) by indirect heat exchange in a reboiler (37) between a liquid fraction from a lower section of the high-purity oxygen column and a gaseous heating stream (42).
10. A process according to claim 2, wherein the heating stream (42) downstream of the indirect heat exchange (37) is introduced into the single distillation column (12).
11. A process according to claim 10, wherein the oxygen-containing stream (36, 39) is introduced into the top of the high-purity oxygen column (38).
12. A process according to claim 2, wherein at least a portion of the oxygen-containing stream (36) is subcooled in the reboiler (37) before being introduced (39) into the high-purity oxygen column (38).
13. A process according to claim 3, wherein at least a portion of the oxygen-containing stream (36) is subcooled in the reboiler (37) before being introduced (39) into the high-purity oxygen column (38).
14. A process according to claim 10, wherein at least a portion of the oxygen-containing stream (36) is subcooled in the reboiler (37) before being introduced (39) into the high-purity oxygen column (38).
15. A process according to claim 12, wherein at least a portion of the oxygen-containing stream (36) is subcooled in the reboiler (37) before being introduced (39) into the high-purity oxygen column (38).
16. A process according to claim 15, wherein the ultrapure oxygen product stream (44) is withdrawn from the high-purity oxygen column (38) in a liquid state.
17. A process according to claim 16, wherein the ultrapure product stream is withdrawn as a final liquid product.
US11/676,773 2006-02-21 2007-02-20 Process and apparatus for producing ultrapure oxygen Abandoned US20070204652A1 (en)

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WO2015003785A1 (en) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Method and device for generating a compressed gas flow and method and device for separating air at a low-temperature
US20230050296A1 (en) * 2021-08-11 2023-02-16 Zhengrong Xu Cryogenic air separation unit with argon condenser vapor recycle
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