EP4215856A1 - Procédé et dispositif de séparation d'air par distillation cryogénique - Google Patents

Procédé et dispositif de séparation d'air par distillation cryogénique Download PDF

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Publication number
EP4215856A1
EP4215856A1 EP22192944.1A EP22192944A EP4215856A1 EP 4215856 A1 EP4215856 A1 EP 4215856A1 EP 22192944 A EP22192944 A EP 22192944A EP 4215856 A1 EP4215856 A1 EP 4215856A1
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EP
European Patent Office
Prior art keywords
pressure
air
compressor
gaseous
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.)
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Application number
EP22192944.1A
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German (de)
English (en)
Inventor
Baptiste FARA
Jean-Pierre Tranier
Alain Briglia
Feng-jie XUE
Alain Guillard
Eric Day
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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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP22192944.1A priority Critical patent/EP4215856A1/fr
Priority to EP22199455.1A priority patent/EP4163576A1/fr
Priority to CN202211229835.5A priority patent/CN115930551A/zh
Publication of EP4215856A1 publication Critical patent/EP4215856A1/fr
Withdrawn legal-status Critical Current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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, 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.
    • F25J3/04387—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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
    • 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
    • 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
    • F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the present invention relates to a process and apparatus for air separation by cryogenic distillation.
  • it relates to processes and apparatus for producing oxygen under high pressure.
  • Oxygen gas produced by air separation units often has a high pressure of about 20 to 50 bar.
  • the production process is usually a dual column process involving a first column operating at a first column pressure and a second column operating at a second column pressure, lower than the pressure of the first column.
  • the top of the first column is thermally linked to the bottom of the second column.
  • Oxygen is produced at the bottom of the second column, operating under a pressure of 1 to 4 bar.
  • Oxygen is compressed to a higher pressure, using an oxygen compressor or by pumping liquid oxygen. Due to safety problems associated with the oxygen compressors, oxygen production units generally use the process involving pumping and then vaporizing liquid.
  • an additional booster compressor is used to raise a portion of feed air or nitrogen to higher pressure, in the range of 40 to 80 bar.
  • the booster replaces the oxygen compressor.
  • the present invention therefore aims to address the shortcomings of these process, in particular by introducing all feed air flows into the columns at a temperature close to the temperature of the column at the point where the flow is introduced, in order to reduce thermodynamic irreversibilities of the system without using additional stage of compression.
  • the overall cost of the products of a production unit of oxygen can therefore be reduced.
  • the main improvement results from the use of a booster air compressor air to recirculate the air once it has been used to recover the heat produced by the vaporization of a high pressure liquid in the primary heat exchanger.
  • an air separation process by distillation in a cryogenic column system comprising a first column operating at a pressure and a second column operating at a lower pressure than the first column, comprising the steps of:
  • an air separation apparatus using distillation in a cryogenic column system comprising a first column operating at a pressure and a second column operating at a lower pressure than the first column, a first air compressor, a second compressor, a third compressor and a heat exchanger, means for sending all the feed air to be compressed in the first air compressor to a first outlet pressure which not more than one bar higher than and preferably substantially equal to the pressure at which the first column operates, means for sending a gas which is a first gaseous portion of the air at the first pressure or a stream of nitrogen to the second compressor, means for sending gas compressed in the second compressor to third compressor, means for sending gas compressed in the third compressor be cooled and condensed or pseudo condensed at the third pressure in the heat exchanger, means for sending at least part of the air, preferably a second gaseous air portion under the first outlet pressure to the system of columns, without further compression, and separation of the at least part of the air, preferably the second gaseous air portion, in the system of
  • the third compressor comprises first and second booster compressors connected in parallel, one of the booster compressors being coupled to the turbine.
  • the turbine is coupled to a booster compressor which compresses part of the expanded fraction.
  • the compressor may be connected to the heat exchanger to receive part of the expanded fraction after warming in the heat exchanger.
  • the turbine may be coupled to a booster compressor which compresses part of the feed air to the third pressure, the outlet of the booster compressor being connected to the heat exchanger.
  • the inlet of the booster compressor is in this case connected to the second compressor.
  • 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 compressed in the second stage of the booster compressor C05-02 to a third pressure, which may be a supercritical pressure.
  • the 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 and is then divided in two.
  • a first part 8 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 3 downstream of booster compressor C05-1 and then compressed once again in compressor stage C05-2.
  • the other part 7 of the condensed or pseudo condensed air 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.
  • the turbine T05 may be coupled to a generator.
  • 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.
  • 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.
  • Figure 2 shows a variant of Figures 1 and 3 in which the gas to be condensed in heat exchanger E01HP (air or nitrogen) 3 is compressed In a first booster C05-1, cooled in a cooler E1 and then compressed in two booster in parallel C05-2, C05-3 from the second pressure to the third pressure.
  • booster C05-2 of Figure 1 is replaced by two booster in parallel, the booster C05-3 being driven by expander T03.
  • the cooler E2 is common to the two booster C05-2 and C05-3 and the expanded gas 8 is recycled to the inlets of both boosters C05-2 and C05-3.
  • Line 23 is an anti-surge system for both boosters.
  • Figure 3 shows the case where the gas to be condensed and revaporised in the high pressure exchanger E01HP is nitrogen.
  • the gas to be condensed and revaporised in the high pressure exchanger E01HP is nitrogen.
  • the nitrogen from the top of column K01 is expanded in turbine T03 coupled to generator G.
  • the rest of the nitrogen is compressed first in compressor C05-1 to the second pressure and then in compressor C05-2 to the third pressure.
  • the nitrogen 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 nitrogen 3 is cooled to a cryogenic temperature, thereby condensing or pseudo condensing and is then divided in two.
  • a first part 8 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 3 downstream of booster compressor C05-1 and then compressed once again in compressor stage C05-2.
  • the other part 7 of the condensed or pseudo condensed nitrogen is expanded in a valve or a turbine T05 to form a liquid stream, part 9 of which is sent to the top of the first column K01 and the rest 11 of which is sent to the top of the second column K02.
  • Figure 4 shows the incorporation of the system of Figure 2 in a process such as that of Figure 1 .
  • the streams 3 and 5 result from the splitting in two of a stream 1 as in Figures 1 and 3 .
  • Air stream 8 is warmed in heat exchanger E01HP and is divided in two, one part being sent to the inlet of booster C05-2 and another part, here the rest, being sent to a booster T03C having the same inlet and outlet pressures as booster C05-2.
  • the booster T03C is coupled to the nitrogen turbine T03, replacing the generator.
  • the air at the second pressure coming from second compressor C05-1 may be divided in two, upstream of the point of return of stream 8 and both parts may be then compressed to the third pressure in separate booster C05-2, T03-C.
  • the booster T03C is, as before, coupled to the nitrogen turbine T03, replacing the generator.
  • the process does not require any expansion of gaseous air, thus the normal Claude turbine and/or insufflation turbine are not present.
  • the nitrogen expander coupled with the air cycle generates enough cold for the ASU in normal operation.
  • the nitrogen turbine is possibly coupled for instance to a generator: when no or only small quantities of nitrogen under pressure are required by customer, the nitrogen expander T03 will recover the energy contained in the MP nitrogen extracted from the MP column, by expanding it to atmospheric pressure.
  • the quantity of nitrogen extracted will be a trade-off between the energy recovered with by the nitrogen expansion and the loss of oxygen and argon recovery. Typically an optimum can be found in the range of a 5 to 10% expanded nitrogen / air flow ratio, with no loss of oxygen recovery and an argon recovery in the range of 70% in the case where argon is produced.

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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)
EP22192944.1A 2021-10-06 2022-08-30 Procédé et dispositif de séparation d'air par distillation cryogénique Withdrawn EP4215856A1 (fr)

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EP22192944.1A EP4215856A1 (fr) 2022-08-30 2022-08-30 Procédé et dispositif de séparation d'air par distillation cryogénique
EP22199455.1A EP4163576A1 (fr) 2021-10-06 2022-10-04 Appareil et procédé de séparation d'air par distillation cryogénique
CN202211229835.5A CN115930551A (zh) 2021-10-06 2022-10-08 用于通过低温蒸馏分离空气的设备和方法

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4345925A (en) * 1980-11-26 1982-08-24 Union Carbide Corporation Process for the production of high pressure oxygen gas
US4617037A (en) * 1984-11-02 1986-10-14 Nippon Sanso Kabushiki Kaisha Nitrogen production method
US20200132367A1 (en) * 2017-05-24 2020-04-30 L'air Liquide, Societe Anonyme Pour L'etude Et L?Exploitation Des Procedes Georges Claude Method and apparatus for air separation by cryogenic distillation
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

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4345925A (en) * 1980-11-26 1982-08-24 Union Carbide Corporation Process for the production of high pressure oxygen gas
US4617037A (en) * 1984-11-02 1986-10-14 Nippon Sanso Kabushiki Kaisha Nitrogen production method
US20200132367A1 (en) * 2017-05-24 2020-04-30 L'air Liquide, Societe Anonyme Pour L'etude Et L?Exploitation Des Procedes Georges Claude Method and apparatus for air separation by cryogenic distillation
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

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