EP4163576A1 - Apparatus and process for the separation of air by cryogenic distillation - Google Patents

Apparatus and process for the separation of air by cryogenic distillation Download PDF

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Publication number
EP4163576A1
EP4163576A1 EP22199455.1A EP22199455A EP4163576A1 EP 4163576 A1 EP4163576 A1 EP 4163576A1 EP 22199455 A EP22199455 A EP 22199455A EP 4163576 A1 EP4163576 A1 EP 4163576A1
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EP
European Patent Office
Prior art keywords
stream
pressure
heat exchanger
air
column
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP22199455.1A
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German (de)
French (fr)
Inventor
Michael A. Turney
Lindsey TURNEY
Alain Guillard
Baptiste FARA
Jean-Pierre Tranier
Alain Briglia
Eric Day
Feng-jie XUE
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication date
Priority claimed from US17/495,456 external-priority patent/US20230103843A1/en
Priority claimed from EP22192944.1A external-priority patent/EP4215856A1/en
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP4163576A1 publication Critical patent/EP4163576A1/en
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04006—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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • 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.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages 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
    • 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
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • a main air compressor compresses air to provide feed air stream 101 which is split into main feed air stream 102 and secondary feed air stream 103.
  • Main feed air stream 102 is introduced into main heat exchanger 104 wherein it is cooled, thereby producing cold feed air stream 105.
  • Secondary feed air stream 103 is introduced into first booster air compressor 106 thereby producing boosted air feed stream 107.
  • Secondary feed air stream 103 has a first inlet pressure, and boosted air feed stream 107 has a first outlet pressure.
  • Boosted air feed stream 107 is introduced into aftercooler 108, thereby producing cooled compressed air feed stream 109.
  • Cold feed air stream 105 is introduced into HP column 201.
  • Cool boosted feed air stream 110 is introduced into first heat exchanger 203, wherein it exchanges heat with liquid oxygen stream 214, thereby producing at least partially condensed cold boosted feed air stream 204.
  • Second heat exchanger 203 vaporizes liquid oxygen stream 214 against at least partially condensing air stream 110 at a pressure provided by first booster air compressor 106.
  • the pressure of liquid oxygen stream 214 vaporized in second heat exchanger 203 is boosted by static head by positioning second heat exchanger 203 at a lower elevation than the liquid oxygen supply sump 217 of LP column 202.
  • the pressure of liquid oxygen stream 214 may be boosted by a liquid oxygen pump. (not shown).
  • the gaseous oxygen product pressure is in the range of 1.1 bara to 3 bara and preferably in the range of 1.2 bara and 2 bara.
  • LP column 202 produces at least three output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, and cold gaseous nitrogen stream 216.
  • Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115.
  • Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara.
  • Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113.
  • Cold gaseous nitrogen stream 216 passes through second heat exchanger 207, thereby producing gaseous nitrogen product stream 111.
  • LP column 202 produces at least two output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115.
  • Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara.
  • Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113.
  • Waste nitrogen product stream 113 is introduced into main heat exchanger 104, thereby producing warmed waste nitrogen product 114.
  • Gaseous oxygen product stream 115 is introduced into main heat exchanger 104, thereby producing warmed gaseous oxygen product 116.
  • a main air compressor compresses air to provide feed air stream 101 which is split into main feed air stream 102 and secondary feed air stream 103, and tertiary feed air stream 301.
  • Main feed air stream 102 is introduced into main heat exchanger 104 wherein it is cooled, thereby producing cold feed air stream 105.
  • Secondary feed air stream 103 is introduced into first booster air compressor 106 thereby producing boosted air feed stream 107.
  • Secondary feed air stream 103 has a first inlet pressure, and boosted air feed stream 107 has a first outlet pressure.
  • Tertiary feed air stream 301 is introduced into second booster air compressor 302, thereby producing compressed tertiary feed air stream 304.
  • First booster air compressor 106 may control this common discharge pressure, in order to fully vaporize the oxygen stream.
  • the load on turboexpander 119 will determine the relative flowrates between first booster air compressor 106 and second booster air compressor 302.
  • Combined boosted feed air stream 305 is introduced into aftercooler 108, thereby producing cooled compressed air feed stream 109.
  • Cooled compressed air feed stream 109 is then introduced into main heat exchanger 104 wherein it is cooled, thereby producing cool boosted feed air stream 110.
  • HP column 201 produces at least 3 output streams rich liquid stream 208, nitrogen reflux stream 212, and HP gaseous nitrogen stream 117.
  • Rich liquid stream 208 passes through second heat exchanger 207, thereby producing cold rich liquid stream 209, which is introduced into LP column 202.
  • Nitrogen reflux stream 212 passes through second heat exchanger 207, thereby producing cold reflux stream 213, which is introduced into LP column 202.
  • LP column 202 produces at least two output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115.
  • Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara.
  • Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113.
  • Waste nitrogen product stream 113 is introduced into main heat exchanger 104, thereby producing warmed waste nitrogen product 114.
  • Gaseous oxygen product stream 115 is introduced into main heat exchanger 104, thereby producing warmed gaseous oxygen product 116.
  • Gaseous nitrogen 13 is removed from the top of the first column, warmed in heat exchanger E01LP to an intermediate temperature thereof and then expanded in a turbine T03 to the pressure of the second column K02. It is then mixed with the nitrogen from the minaret K03 of the second column and removed as waste or as a low pressure product.
  • the heat exchangers E01HP and LP may be combined in a single heat exchanger.
  • the first column may be thermally linked to the second column via a double stage vaporiser or a film type vaporiser.

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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

An air separation process having a first booster air compressor comprising a first outlet stream and a second booster air compressor comprising a second outlet stream,wherein the first booster air compressor and the second booster air compressor are in parallel, and the second booster air compressor is driven by a nitrogen turboexpander, the first outlet stream and the second outlet stream being at least partially condensed by heat exchange with a vaporizing oxygen stream.

Description

  • The present invention relates to an apparatus and a process for the separation of air by cryogenic distillation.
  • Processes as known in the art are presented in Figures 1 through 4. A main air compressor (not shown) compresses air to provide feed air stream 101 which is split into main feed air stream 102 and secondary feed air stream 103. Main feed air stream 102 is introduced into main heat exchanger 104 wherein it is cooled, thereby producing cold feed air stream 105. Secondary feed air stream 103 is introduced into first booster air compressor 106 thereby producing boosted air feed stream 107. Secondary feed air stream 103 has a first inlet pressure, and boosted air feed stream 107 has a first outlet pressure. Boosted air feed stream 107 is introduced into aftercooler 108, thereby producing cooled compressed air feed stream 109. The pressure of cooled compressed air feed stream 109 is determined by the oxygen vaporizing pressure in first heat exchanger 203. For efficient heat transfer the air condensing temperature in first heat exchanger 203 must be only slightly (~2C to 3C) warmer than the temperature of the vaporizing oxygen. Cooled compressed air feed stream 109 is then introduced into main heat exchanger 104 wherein it is cooled, thereby producing cool boosted feed air stream 110.
  • Cold feed air stream 105 is introduced into HP column 201. Cool boosted feed air stream 110 is introduced into first heat exchanger 203, wherein it exchanges heat with liquid oxygen stream 214, thereby producing at least partially condensed cold boosted feed air stream 204. Second heat exchanger 203 vaporizes liquid oxygen stream 214 against at least partially condensing air stream 110 at a pressure provided by first booster air compressor 106. The pressure of liquid oxygen stream 214 vaporized in second heat exchanger 203 is boosted by static head by positioning second heat exchanger 203 at a lower elevation than the liquid oxygen supply sump 217 of LP column 202. Alternatively, the pressure of liquid oxygen stream 214 may be boosted by a liquid oxygen pump. (not shown). For this process the gaseous oxygen product pressure is in the range of 1.1 bara to 3 bara and preferably in the range of 1.2 bara and 2 bara.
  • Cold boosted feed air stream 204 may be split into two portions, primary cold boosted feed air stream 205 and secondary cold boosted fed air stream 206. Primary cold boosted feed air stream 205 is introduced into HP column 201. Secondary cold boosted fed air stream 206 is introduced into LP column 202.
  • In one embodiment, as illustrated in Figure 1 and Figure 2, HP column 201 produces at least four output streams, rich liquid stream 208, first nitrogen reflux stream 210, second nitrogen reflux stream 212, and HP gaseous nitrogen stream 117. Rich liquid stream 208 passes through second heat exchanger 207, thereby producing cold rich liquid stream 209, which is introduced into LP column 202. First nitrogen reflux stream 210 passes through second heat exchanger 207, thereby producing cold first reflux stream 211, which is introduced into LP column 202. Second nitrogen reflux stream 212 passes through second heat exchanger 207, thereby producing cold second reflux stream 213, which is introduced into LP column 202.
  • LP column 202 produces at least three output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, and cold gaseous nitrogen stream 216. Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115. Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara. Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113. Cold gaseous nitrogen stream 216 passes through second heat exchanger 207, thereby producing gaseous nitrogen product stream 111.
  • Gaseous nitrogen product stream 111 is introduced into main heat exchanger 104, thereby producing warmed gaseous nitrogen product 112. Waste nitrogen product stream 113 is introduced into main heat exchanger 104, thereby producing warmed waste nitrogen product 114. Gaseous oxygen product stream 115 is introduced into main heat exchanger 104, thereby producing warmed gaseous oxygen product 116.
  • HP gaseous nitrogen stream 117 is introduced into main heat exchanger 104, thereby producing warmed HP gaseous nitrogen stream 118. Warmed HP gaseous nitrogen stream 118 is then introduced into turboexpander 119, thereby producing LP gaseous nitrogen stream 120. Turboexpander 119 may have an inlet pressure of between 4 and 10 bara, and an outlet pressure of between atmospheric pressure and 2 bara. Turboexpander 119 may have a loading or braking device to act as a sink for the expander's energy. As a brake, turboexpander 119 may utilize a booster, a generator or oil (not shown). Typically, a booster brake is preferred to put as much energy back into the system as possible, with less overall losses and equipment cost. LP gaseous nitrogen stream 120 is then introduced into main heat exchanger 104 thereby producing warmed LP gaseous nitrogen stream 121.
  • In another embodiment, as illustrated in Figure 3 and Figure 4, HP column 201 produces at least 3 output streams rich liquid stream 208, nitrogen reflux stream 212, and HP gaseous nitrogen stream 117. Rich liquid stream 208 passes through second heat exchanger 207, thereby producing cold rich liquid stream 209, which is introduced into LP column 202. Nitrogen reflux stream 212 passes through second heat exchanger 207, thereby producing cold reflux stream 213, which is introduced into LP column 202.
  • LP column 202 produces at least two output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115. Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara. Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113. Waste nitrogen product stream 113 is introduced into main heat exchanger 104, thereby producing warmed waste nitrogen product 114. Gaseous oxygen product stream 115 is introduced into main heat exchanger 104, thereby producing warmed gaseous oxygen product 116.
  • HP gaseous nitrogen stream 117 is introduced into main heat exchanger 104, thereby producing warmed HP gaseous nitrogen stream 118. Warmed HP gaseous nitrogen stream 118 is then introduced into turboexpander 119, thereby producing LP gaseous nitrogen stream 120. Turboexpander 119 may have an inlet pressure of between 4 and 10 bara, and an outlet pressure of between atmospheric pressure and 2 bara. Turboexpander 119 may have a loading or braking device to act as a sink for the expander's energy. As a brake, turboexpander 119 may utilize a booster, a generator or oil (not shown). Typically, a booster brake is preferred to put as much energy back into the system as possible, with less overall losses and equipment cost. LP gaseous nitrogen stream 120 is then introduced into main heat exchanger 104 thereby producing warmed LP gaseous nitrogen stream 121.
  • An air separation process having a first booster air compressor comprising a first outlet stream and a second booster air compressor comprising a second outlet stream. Wherein the first booster air compressor and the second booster air compressor are in parallel, and the second booster air compressor is driven by a nitrogen turboexpander. The first outlet stream and/or the second outlet stream may be at least partially condensed by heat exchange with a vaporizing low pressure oxygen stream, and the low-pressure gaseous oxygen pressure is in the range of 1.1 bara to 3 bara.
  • According to an object of the invention, there is provided a process for the separation of air by cryogenic distillation comprising:
    1. i) Cooling compressed air in a heat exchanger
    2. ii) Sending cooled and compressed air from the heat exchanger to a distillation column system comprising a first column operating at a first pressure and a second column operating at a second pressure lower than the first pressure, including sending at least part of the air to first column
    3. iii) Removing a liquid oxygen stream from the second column, vaporizing it against feed air to produce a gaseous stream
    4. iv) Removing a gaseous nitrogen stream from the first column, warming it in the heat exchanger and expanding it in a turbine
    5. v) Dividing a portion of the compressed air into first and second parts
    6. vi) Compressing the first part of the compressed air portion at a first inlet pressure in a first booster air compressor to form a first outlet stream at a first outlet pressure,
    7. vii) Compressing the second part of the compressed air at the first inlet pressure in a second booster air compressor to form a second outlet stream at the first outlet pressure, wherein the second booster air compressor is driven by the turbine and the first outlet stream and the second outlet stream are combined to form a combined stream and sent to the heat exchanger to be cooled before being sent to the distillation column system .
  • According to optional aspects of the invention:
    • the combined stream is introduced into a common after-cooler upstream of the heat exchanger.
    • the turbine has an inlet pressure in the range of 4 to 10 bara
    • the turbine has outlet pressure in the range of atmospheric pressure to 2 bara.
    • the combined stream is at least partially condensed by heat exchange with the liquid oxygen stream.
    • the low-pressure gaseous oxygen pressure of the vaporised stream formed by vaporizing the liquid oxygen stream is in the range of 1.1 bara to 3 bara, preferably in the range of 1.2 bara and 2 bara .
    • a stream of air at the inlet pressure of the first and second booster compressors is cooled in the heat exchanger at that pressure and sent to the first column.
    • the liquid oxygen is pressurized by a pump before being vaporised.
    • the inlet and outlet temperatures of the first and second booster compressors are higher than the inlet temperature of the heat exchanger.
    • the first booster compressor is not coupled to the turbine.
    • the first booster compressor is driven by a motor.
  • According to another aspect of the invention, there is provided an apparatus for the separation of air by cryogenic distillation comprising: a heat exchanger, a distillation column system comprising a first column operating at a first pressure and a second column operating at a second pressure lower than the first pressure, means for cooling compressed air in the heat exchanger, means for sending cooled and compressed air from the heat exchanger to the distillation column system, including sending at least part of the air to first column, means for removing a liquid oxygen stream from the second column, means for vaporizing the liquid oxygen stream against feed air to produce a gaseous stream, a turbine, means for removing a gaseous nitrogen stream from the first column, warming it in the heat exchanger and expanding it in the turbine, means for dividing a portion of the compressed air into first and second parts, first and second booster air compressors, means for sending the first part of the compressed air portion at a first inlet pressure to be compressed in the first booster air compressor to form a first outlet stream at a first outlet pressure, means for sending the second part of the compressed air at the first inlet pressure to be compressed in the second booster air compressor to form a second outlet stream at the first outlet pressure, wherein the second booster air compressor is driven by the turbine and means for combining the first outlet stream and the second outlet stream to form a combined stream and means for sending the combined stream to the heat exchanger to be cooled before being sent to the distillation column system .
  • The apparatus may include:
    • the means for vaporizing the liquid oxygen Is a dedicated heat exchanger.
    • the means for vaporizing the liquid oxygen is the heat exchanger.
    • Figure 1 is a schematic representation of the main heat exchanger with a low-pressure nitrogen stream, as utilized in one system as known in the art.
    • Figure 2 is a schematic representation of an overall system with a low-pressure nitrogen stream, as utilized in one system as known in the art.
    • Figure 3 is a schematic representation of the main heat exchanger without a low-pressure nitrogen stream, as utilized in one system as known in the art.
    • Figure 4 is a schematic representation of an overall system without a low-pressure nitrogen stream, as utilized in one system as known in the art.
    • Figure 5 is a schematic representation of the main heat exchanger with a low-pressure nitrogen stream, in accordance with the present invention.
    • Figure 6 is a schematic representation of an overall system with a low-pressure nitrogen stream, in accordance with the present invention.
    • Figure 7 is a schematic representation of the main heat exchanger without a low-pressure nitrogen stream, in accordance with the present invention.
    • Figure 8 is a schematic representation of an overall system without a low-pressure nitrogen stream, in accordance with the present invention.
    • Figure 9 is a schematic representation of the compressor and booster set-up of a process in accordance with the present invention
    • Figure 10 is a schematic representation of an overall system with a low-pressure nitrogen stream, in accordance with the present invention.
    Element Numbers
    • 101 = feed air stream
    • 102 = main feed air stream (first portion)
    • 103 = secondary feed air stream (second portion)
    • 104 = main heat exchanger
    • 105 = cold feed air stream
    • 106 = first booster air compressor
    • 107 = boosted air feed stream
    • 108 = aftercooler
    • 109 = cooled compressed air feed stream
    • 110 = cool boosted feed air stream
    • 111 = gaseous nitrogen product
    • 112 = warmed gaseous nitrogen product
    • 113 = waste nitrogen
    • 114 = warmed waste nitrogen
    • 115 = gaseous oxygen product
    • 116 = warmed gaseous oxygen product
    • 117 = HP gaseous nitrogen
    • 118 = warmed HP gaseous nitrogen
    • 119 = turboexpander
    • 120 = LP gaseous nitrogen
    • 121 = warmed LP gaseous nitrogen
    • 201 = HP column
    • 202 = LP column
    • 203 = first heat exchanger
    • 204 = cold boosted feed air stream
    • 205 = primary cold boosted feed air stream (first portion)
    • 206 = secondary cold boosted feed air stream (second portion)
    • 207 = second heat exchanger
    • 208 = rich liquid (rich in oxygen)
    • 209 = cold rich liquid
    • 210 = first (nitrogen) reflux stream
    • 211 = cold first reflux stream
    • 212 = second (nitrogen) reflux stream
    • 213 = cold second reflux stream
    • 214 = gaseous oxygen stream
    • 215 = cold waste nitrogen stream
    • 216 = cold gaseous nitrogen
    • 301 = tertiary feed air stream (third portion)
    • 302 = second booster air compressor
    • 303 = drive connection (between turboexpander and secondary feed air compressor)
    • 304 = compressed tertiary feed air stream
    • 305 = combined boosted feed air stream
    Description of Embodiments
  • Illustrative embodiments of the invention are described below. While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and are herein described in detail. It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
  • It will of course be appreciated that in the development of any such actual embodiment, numerous implementation-specific decisions must be made to achieve the developer's specific goals, such as compliance with system-related and business-related constraints, which will vary from one implementation to another. Moreover, it will be appreciated that such a development effort might be complex and time-consuming, but would nevertheless be a routine undertaking for those of ordinary skill in the art having the benefit of this disclosure.
  • Turning to Figures 5 through 8, a system in accordance with the present invention is presented. A main air compressor (not shown) compresses air to provide feed air stream 101 which is split into main feed air stream 102 and secondary feed air stream 103, and tertiary feed air stream 301. Main feed air stream 102 is introduced into main heat exchanger 104 wherein it is cooled, thereby producing cold feed air stream 105. Secondary feed air stream 103 is introduced into first booster air compressor 106 thereby producing boosted air feed stream 107. Secondary feed air stream 103 has a first inlet pressure, and boosted air feed stream 107 has a first outlet pressure. Tertiary feed air stream 301 is introduced into second booster air compressor 302, thereby producing compressed tertiary feed air stream 304. Tertiary feed air stream 301 has a second inlet pressure and compressed tertiary feed air stream 304 has a second outlet pressure. The first inlet pressure and the second inlet pressure are the same, which is defined herein as being within 1 bar of each other, or within 0,5 bar of each other, or within 0,25 bar of each other. The first outlet pressure and the second outlet pressure are the same, which is defined herein as being within 1 bar of each other or within 0,5 bar of each other, or within 0,25 bar of each other.
  • Boosted air feed stream 107 is combined with compressed tertiary feed air stream 304, thereby producing combined boosted feed air stream 305. Thus, first booster air compressor 106 and second booster air compressor 302 are in parallel, having the same, or approximately the same, inlet pressures and outlet pressures. The term "the same, or approximately the same' means as close to the same as is reasonable given the conditions.
  • First booster air compressor 106, may control this common discharge pressure, in order to fully vaporize the oxygen stream. The load on turboexpander 119 will determine the relative flowrates between first booster air compressor 106 and second booster air compressor 302. Combined boosted feed air stream 305 is introduced into aftercooler 108, thereby producing cooled compressed air feed stream 109. Cooled compressed air feed stream 109 is then introduced into main heat exchanger 104 wherein it is cooled, thereby producing cool boosted feed air stream 110.
  • Cold feed air stream 105 is introduced into HP column 201. Cool boosted feed air stream 110 is introduced into first heat exchanger 203, wherein it exchanges heat with liquid oxygen stream 214, thereby producing at least partially condensed cold boosted feed air stream 204 and vaporised gaseous oxygen 115. The vaporised gaseous oxygen, at substantially the pressure of the LP column 202, is further warmed in heat exchanger 104. Cold boosted feed air stream 204 is split into two portions, primary cold boosted feed air stream 205 and secondary cold boosted fed air stream 206. Primary cold boosted feed air stream 205 is introduced into HP column 201 in liquid form. Secondary cold boosted fed air stream 206 is expanded (not shown) and introduced into LP column 202.
  • In one embodiment, as illustrated in Figure 5 and Figure 6, HP column 201 produces at least four output streams, rich liquid stream 208, first nitrogen reflux stream 210, second nitrogen reflux stream 212, and HP gaseous nitrogen stream 117. Rich liquid stream 208 passes through second heat exchanger 207, thereby producing cold rich liquid stream 209, which is introduced into LP column 202. First nitrogen reflux stream 210 passes through second heat exchanger 207, thereby producing cold first reflux stream 211, which is introduced into LP column 202. Second nitrogen reflux stream 212 passes through second heat exchanger 207, thereby producing cold second reflux stream 213, which is introduced into LP column 202.
  • LP column 202 produces at least three output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, and cold gaseous nitrogen stream 216. Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115. Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara. Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113. Cold gaseous nitrogen stream 216 passes through second heat exchanger 207, thereby producing gaseous nitrogen product stream 111.
  • Gaseous nitrogen product stream 111 is introduced into main heat exchanger 104, thereby producing warmed gaseous nitrogen product 112. Waste nitrogen product stream 113 is introduced into main heat exchanger 104, thereby producing warmed waste nitrogen product 114. Gaseous oxygen product stream 115 is introduced into main heat exchanger 104, thereby producing warmed gaseous oxygen product 116.
  • HP gaseous nitrogen stream 117 is introduced into main heat exchanger 104, thereby producing warmed HP gaseous nitrogen stream 118. Warmed HP gaseous nitrogen stream 118 is then introduced into turboexpander 119, thereby producing LP gaseous nitrogen stream 120. LP gaseous nitrogen stream 120 is then introduced into main heat exchanger 104 thereby producing warmed LP gaseous nitrogen stream 121. Second booster air compressor 302 and turboexpander 119 may be connected with a common drive 303.
  • In another embodiment, as illustrated in Figure 7 and Figure 8, HP column 201 produces at least 3 output streams rich liquid stream 208, nitrogen reflux stream 212, and HP gaseous nitrogen stream 117. Rich liquid stream 208 passes through second heat exchanger 207, thereby producing cold rich liquid stream 209, which is introduced into LP column 202. Nitrogen reflux stream 212 passes through second heat exchanger 207, thereby producing cold reflux stream 213, which is introduced into LP column 202.
  • LP column 202 produces at least two output streams, liquid oxygen stream 214, cold waste nitrogen stream 215, Liquid oxygen stream 214 passes through first heat exchanger 203, thereby producing gaseous oxygen product stream 115. Gaseous oxygen product stream 115 may have a pressure between 1.1 and 3 bara, preferably between 1.2 and 2 bara. Cold waste nitrogen stream 215 passes through second heat exchanger 207, thereby producing waste nitrogen stream 113. Waste nitrogen product stream 113 is introduced into main heat exchanger 104, thereby producing warmed waste nitrogen product 114. Gaseous oxygen product stream 115 is introduced into main heat exchanger 104, thereby producing warmed gaseous oxygen product 116.
  • HP gaseous nitrogen stream 117 is introduced into main heat exchanger 104, thereby producing warmed HP gaseous nitrogen stream 118. Warmed HP gaseous nitrogen stream 118 is then introduced into turboexpander 119, thereby producing LP gaseous nitrogen stream 120. Turboexpander 119 may have an inlet pressure of between 4 and 10 bara, and an outlet pressure of between atmospheric pressure and 2 bara. Turboexpander 119 may have a loading or braking device to act as a sink for the expander's energy. As a brake, turboexpander 119 may utilize a booster, a generator or oil (not shown). Typically, a booster brake is preferred to put as much energy back into the system as possible, with less overall losses and equipment cost. LP gaseous nitrogen stream 120 is then introduced into main heat exchanger 104 thereby producing warmed LP gaseous nitrogen stream 121. Second booster air compressor 302 and turboexpander 119 may be connected with a common drive 303.
  • Figure 9 shows detail of a compressor and booster setup of a process according to the invention. Air 3 to be condensed in heat exchanger E01HP is compressed In a first booster C05-1 , cooled in a cooler E1 and then compressed in two boosters in parallel C05-2, C05-3 from the second pressure to the third pressure. A single booster is replaced by two boosters in parallel, the booster C05-3 being driven by expander T03.
  • The cooler E2 is common to the two boosters C05-2 and C05-3.
  • Line 23 is an anti-surge system for both boosters.
  • In Figure 10, the separation takes place in a double column, comprising a first column K01 and a second column K02, the second column operating at a lower pressure than the first column and the bottom of the second column being heated using nitrogen from the first column.
  • The second column feeds argon enriched vapor ORG to an argon column (not shown).
  • The total air flow 1 sent to the column system K01,K02 is compressed to a first pressure, slightly higher than the first column pressure, in compressor C01. The air stream is divided in two to form two streams 3, 5. The first stream 3 is compressed in the first stage of a booster compressor C05-1 to a second pressure, higher than the first pressure and then divided in two. One part of the air is compressed in the second stage of the booster compressor C05-02 to a third pressure, which may be a supercritical pressure. This part of first stream 3 is then sent at the third pressure to a high pressure section E01HP of the main heat exchanger in which some of the streams are at pressures of above at least 10 bars. The first air stream 3 is cooled to a cryogenic temperature, thereby condensing or pseudo condensing. Condensed or pseudo condensed air 7 is expanded in a valve or a turbine T05 to form a liquid stream, part 9 of which is sent to the first column K01 and the rest 11 of which is sent to the second column K02.
  • Optionally condensed or pseudo condensed air can be divided in two. A part (not shown) is expanded in a valve 14 (or in a turbine) to the fourth pressure, preferably slightly above the second pressure to account for pressure drop. It forms a liquid stream and is vaporised in exchanger E01HP to form a gaseous stream which is mixed with the first stream downstream of booster compressor C05-1 and then compressed once again in compressor stage C05-2.
  • Another part of air stream 3 is compressed in booster T03C having the same inlet pressure and outlet pressure as booster C05-2. The boosted air streams are combined upstream of heat exchanger E01HP forming a stream 7.
  • The turbine T05 may be coupled to a generator or to booster T03C.
  • A liquid oxygen stream 21 is removed from the bottom of the second column K02, pressurized in a pump P03 and vaporised in the exchanger E01HP to form a product of the process which is pressurized gaseous oxygen. The exchanger also warms part of the waste nitrogen WN2 from the second column.
  • A second portion 5 of the air is cooled in the heat exchanger E01LP where all the streams are at at most 10 bars. The cooled air is introduced in gaseous form into the first column K01. The exchanger E01LP also warms part of the waste nitrogen WN1 from the second column.
  • Gaseous nitrogen 13 is removed from the top of the first column, warmed in heat exchanger E01LP to an intermediate temperature thereof and then expanded in a turbine T03 to the pressure of the second column K02. It is then mixed with the nitrogen from the minaret K03 of the second column and removed as waste or as a low pressure product.
  • The nitrogen turbine T03 may be coupled to a booster in order to generate more refrigeration. In the example, it is coupled to a generator. The nitrogen stream 13 used for the expansion constitutes between 5 and 10% mol of the total air stream 1. None of the nitrogen produced by the process is at the pressure of the first column K01. The quantity of nitrogen expanded is chosen to increase the energy recovered by the nitrogen expansion, whilst avoiding undue loss of oxygen recovery and permitting an argon recovery of around 65-75 %.
  • The nitrogen turbine T03 generates at least 90% of the refrigeration of the system, the rest being provided by Joule-Thomson expansion in valves. It will be appreciated that the process does not involve any air turbine sending gaseous air to the first or second columns.
  • If small amounts of nitrogen are required at higher pressure, part of the nitrogen 13 may be compressed in a booster to a pressure above that of the first column, the booster being driven by the turbine T03 expanding another part of the nitrogen 13.
  • Nitrogen enriched liquid from top of the first column is sent directly to the second column K02.
  • Oxygen enriched liquid from the first column is subcooled in subcooler SC and sent in part directly to the second column K02 and in part RL to the top condenser of the argon column. The liquid VRL vaporised in the top condenser is then sent back to the second column. The argon column is fed with argon enriched gas ORG from the second column K02 and the bottom liquid ORL of the argon column is sent back to the second column K02. The argon column produces an argon rich fluid at the top of the column which may or may not be a product of the process.
  • The heat exchangers E01HP and LP may be combined in a single heat exchanger. The first column may be thermally linked to the second column via a double stage vaporiser or a film type vaporiser.
  • The production of final product or products in liquid form is not greater than 5% mol of the feed air, preferably no more than 2% mol of the feed air.

Claims (13)

  1. A process for the separation of air by cryogenic distillation comprising:
    i) Cooling compressed air in a heat exchanger (104, E01LP, E01HP)
    ii) Sending cooled and compressed air from the heat exchanger to a distillation column system comprising a first column (201, K01) operating at a first pressure and a second column (202, K02) operating at a second pressure lower than the first pressure, including sending at least part of the air to first column
    iii) Removing a liquid oxygen stream (214, 21) from the second column, vaporizing it against feed air (110, 7) to produce a gaseous stream
    iv) Removing a gaseous nitrogen stream from the first column, warming it in the heat exchanger and expanding it in a turbine (119, T03)
    v) Dividing a portion of the compressed air into first and second parts
    vi) Compressing the first part of the compressed air portion at a first inlet pressure in a first booster air compressor (106, C05-2) to form a first outlet stream at a first outlet pressure,
    vii) Compressing the second part of the compressed air at the first inlet pressure in a second booster air compressor (302, C05-3, T03C) to form a second outlet stream at the first outlet pressure, wherein the second booster air compressor is driven by the turbine and the first outlet stream and the second outlet stream are combined to form a combined stream (109, 110, 7) and sent to the heat exchanger to be cooled before being sent to the distillation column system .
  2. The process of Claim 1, wherein the combined stream (109, 110, 7) is introduced into a common after-cooler (108, E2) upstream of the heat exchanger.
  3. The process of Claim 1 or 2, wherein the turbine (119, T03) has an inlet pressure in the range of 4 to 10 bara and outlet pressure in the range of atmospheric pressure to 2 bara.
  4. The process of any preceding claim wherein the combined stream (109, 110, 7) is at least partially condensed by heat exchange with the liquid oxygen stream.
  5. The process of Claim 4 wherein the low-pressure gaseous oxygen pressure of the vaporised stream (115) formed by vaporizing the liquid oxygen stream is in the range of 1.1 bara to 3 bara, preferably in the range of 1.2 bara and 2 bara.
  6. The process of Claim 5 wherein a stream of air (102) at the inlet pressure of the first and second booster compressors is cooled in the heat exchanger at that pressure and sent to the first column.
  7. The process of any preceding claim wherein the liquid oxygen (21) is pressurized by a pump before being vaporised.
  8. The process of any preceding claim wherein the inlet and outlet temperatures of the first and second booster compressors (106, 302, C05-2, C05-3) are higher than the inlet temperature of the heat exchanger (104, E01HP).
  9. The process of any preceding claim wherein the first booster compressor (106, C05-2) is not coupled to the turbine (T).
  10. The process of Claim 9 wherein the first booster compressor (106, C05-2) is driven by a motor.
  11. Apparatus for the separation of air by cryogenic distillation comprising: a heat exchanger, a distillation column system comprising a first column (201, K01) operating at a first pressure and a second column (202, K02) operating at a second pressure lower than the first pressure, means for cooling compressed air in the heat exchanger, means for sending cooled and compressed air from the heat exchanger to the distillation column system, including sending at least part of the air to first column, means for removing a liquid oxygen stream (214, 21) from the second column, means for vaporizing the liquid oxygen stream against feed air to produce a gaseous stream, a turbine (119, T03), means for removing a gaseous nitrogen stream (117, 13) from the first column, warming it in the heat exchanger and expanding it in the turbine, means for dividing a portion of the compressed air into first and second parts, first and second booster air compressors (106, 302, C05-2, C05-3), means for sending the first part (103) of the compressed air portion at a first inlet pressure to be compressed in the first booster air compressor to form a first outlet stream (107) at a first outlet pressure, means for sending the second part (301) of the compressed air at the first inlet pressure to be compressed in the second booster air compressor to form a second outlet stream (304) at the first outlet pressure, wherein the second booster air compressor is driven by the turbine and means for combining the first outlet stream and the second outlet stream to form a combined stream (305, 7) and means for sending the combined stream to the heat exchanger to be cooled before being sent to the distillation column system.
  12. Apparatus according to Claim 11 wherein the means for vaporizing the liquid oxygen Is a dedicated heat exchanger (203).
  13. Apparatus according to Claim 11 wherein the means for vaporizing the liquid oxygen is the heat exchanger (104, E01HP).
EP22199455.1A 2021-10-06 2022-10-04 Apparatus and process for the separation of air by cryogenic distillation Withdrawn EP4163576A1 (en)

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US17/495,456 US20230103843A1 (en) 2021-10-06 2021-10-06 Low-pressure nitrogen turbine with air booster parallel to the booster air compressor
EP22192944.1A EP4215856A1 (en) 2022-08-30 2022-08-30 Process and apparatus for air separation by cryogenic distillation

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4133662A (en) * 1975-12-19 1979-01-09 Linde Aktiengesellschaft Production of high pressure oxygen
US4817394A (en) * 1988-02-02 1989-04-04 Erickson Donald C Optimized intermediate height reflux for multipressure air distillation
US20160231053A1 (en) * 2013-09-17 2016-08-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for producing gaseous oxygen by cryogenic distillation of air
US20200355429A1 (en) * 2017-11-29 2020-11-12 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic distillation method and apparatus for producing pressurized air by means of expander booster in linkage with nitrogen expander for braking
CN112414003A (en) * 2020-11-24 2021-02-26 乔治洛德方法研究和开发液化空气有限公司 Method and equipment for producing air product based on cryogenic rectification

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4133662A (en) * 1975-12-19 1979-01-09 Linde Aktiengesellschaft Production of high pressure oxygen
US4817394A (en) * 1988-02-02 1989-04-04 Erickson Donald C Optimized intermediate height reflux for multipressure air distillation
US20160231053A1 (en) * 2013-09-17 2016-08-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for producing gaseous oxygen by cryogenic distillation of air
US20200355429A1 (en) * 2017-11-29 2020-11-12 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic distillation method and apparatus for producing pressurized air by means of expander booster in linkage with nitrogen expander for braking
CN112414003A (en) * 2020-11-24 2021-02-26 乔治洛德方法研究和开发液化空气有限公司 Method and equipment for producing air product based on cryogenic rectification

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