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EP3343158A1 - Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air - Google Patents

Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air Download PDF

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Publication number
EP3343158A1
EP3343158A1 EP16020517.5A EP16020517A EP3343158A1 EP 3343158 A1 EP3343158 A1 EP 3343158A1 EP 16020517 A EP16020517 A EP 16020517A EP 3343158 A1 EP3343158 A1 EP 3343158A1
Authority
EP
European Patent Office
Prior art keywords
air
pressure column
column
feed air
pressure
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Withdrawn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
EP16020517.5A
Other languages
German (de)
English (en)
Inventor
Dimitri GOLUBEV
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.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP16020517.5A priority Critical patent/EP3343158A1/fr
Priority to AU2017276222A priority patent/AU2017276222A1/en
Priority to US15/847,990 priority patent/US20180180357A1/en
Priority to CN201711441963.5A priority patent/CN108253732A/zh
Publication of EP3343158A1 publication Critical patent/EP3343158A1/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Withdrawn legal-status Critical Current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
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04763—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
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—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
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04133—Electrical motor as the prime mechanical driver
    • 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
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—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
    • F25J3/04284—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
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
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    • 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
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    • 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
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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    • 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
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    • 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
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    • 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
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    • 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
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    • F25J3/04927—Liquid or gas distribution devices
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
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    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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    • 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
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    • 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
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    • 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
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
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    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being oxygen
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

Definitions

  • the invention relates to a method for the cryogenic separation of air and an air separation plant according to the preambles of the independent claims.
  • Air separation plants have distillation column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • distillation columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • the distillation columns of said distillation column systems are operated at different pressure levels.
  • Known double column systems have a so-called high-pressure column (also referred to as a pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as the upper column).
  • the pressure level of the high-pressure column is for example 4 to 6 bar, in particular about 5.3 bar.
  • the low-pressure column is operated at a pressure level of, for example, 1.3 to 1.7 bar, in particular about 1.4 bar.
  • pressures of 3 to 4 bar can also be used in the low pressure column.
  • the pressures given here and below are absolute pressures at the top of said columns.
  • the object of the present invention is to make the low-temperature decomposition of air more energy-efficient and cost-effective.
  • the present invention proposes a method for the cryogenic separation of air and an air separation plant with the features of the respective independent claims.
  • Embodiments are each the subject of the dependent claims and the following description.
  • Fluids and gases may be rich or poor in one or more components as used herein, with “rich” being for a content of at least 50%, 75%, 90%, 95%, 99%, 99.5%, 99, 9% or 99.99% and “poor” for a content of at most 50%, 25%, 10%, 5%, 1%, 0.1% or 0.01% on a molar, weight or volume basis ,
  • the term "predominantly” can correspond to the definition of "rich”.
  • Liquids and gases may also be enriched or depleted in one or more components, which terms refer to a content in a source liquid or gas from which the liquid or gas was recovered.
  • the liquid or gas is "enriched” if it or this is at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times 100 times or 1000 times, and depleted ", if this or this contains at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting liquid or the starting gas. If, for example, “oxygen” or “nitrogen” is mentioned here, one of them is one below Liquid or a gas that is rich in oxygen or nitrogen, but need not necessarily consist exclusively of it.
  • pressure level and "temperature level” to characterize pressures and temperatures, thereby indicating that corresponding pressures and temperatures in a given plant need not be used in the form of exact pressure or temperature values to realize the innovative concept.
  • pressures and temperatures typically range in certain ranges that are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about an average.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another. In particular, for example, pressure levels include unavoidable or expected pressure drops. The same applies to temperature levels.
  • the pressure levels indicated here in bar are absolute pressures.
  • turboexpanders can be used for cooling and liquefaction at different locations, as is generally known to those skilled in the art.
  • the function and purpose of such turboexpander is on specialist literature, for example FG Kerry, Industrial Gas Handbook: Gas Separation and Purification, CRC Press, 2006 , especially the Sections 2.4, “Contemporary Liquefaction Cycles", 2.6 , “Theoretical Analysis of the Claude Cycle” and 3.8.1, “The Lachman Principle ", directed.
  • impure nitrogen from the high-pressure column can also be fed to a pressurized nitrogen turbine, as is the case within the scope of the present invention.
  • a corresponding pressure nitrogen turbine is also referred to as "impure-pressure nitrogen turbine”.
  • An impure-pressure nitrogen turbine is characterized in that it is fed to a nitrogen-rich fluid from the high-pressure column whose nitrogen content is below the nitrogen of the top product of the high-pressure column, ie below the maximum nitrogen content that can be generated in the high-pressure column.
  • a turboexpander can be coupled via a common shaft with other expansion machines or energy converters such as oil brakes, generators or compressor stages. If one or more turbo expanders are coupled with one or more compressor stages (see below) and if necessary additionally mechanically braked, so that the compressor stage (s) are operated without external energy, for example by means of an electric motor, the term is also generally used for this arrangement "Boosterturbine” used.
  • the compressor stage (s) of a corresponding booster turbine is or are generally referred to as a "booster".
  • Such a booster turbine compresses at least one current by the relaxation of at least one other current, but without external, for example by means of an electric motor, supplied energy.
  • a compressor is understood here to mean an externally, typically electrically, driven device which is set up for compressing at least one gaseous stream from at least one inlet pressure at which it is fed to the compressor to at least one final pressure at which it is taken from the compressor is.
  • the compressor forms a structural unit, which, however, several single compressor units or “compressor stages” in the form of known piston, screw and / or Schaufelrad- or turbine assemblies (ie radial or axial compressor stages) may have.
  • these compressor stages are driven by means of a common drive, for example via a common shaft or a common electric motor.
  • Several compressor stages can thus together form one or more compressors.
  • Rotating units for example expansion machines or expansion turbines, compressors or compressor stages, booster turbines or booster, rotors of electric motors and the like, can be mechanically coupled to one another, wherein a "mechanical coupling" in the parlance of this application is understood that via mechanical elements such Gears, belts, gears and the like, a fixed or mechanically adjustable speed relationship between such rotating units can be produced.
  • a mechanical coupling can generally be made by two or more elements, each engaging, such as in form-engagement or frictional engagement, such as gears or traction sheaves with belts, or a non-rotatable connection.
  • a mechanical coupling can in particular be effected via a common shaft, on which the rotating units are each secured in a rotationally fixed manner. The rotational speed of the rotating units is the same in this case.
  • the present invention is used in particular in connection with so-called MAC-BAC (Main Air Compressor / Booster Air Compressor) methods.
  • a MAC-BAC process is characterized in that only a portion of the total amount of feed air supplied to the distillation column system is compressed to a pressure level which is substantially, i. is at least 3, 4 or 5 bar above the pressure level of the high pressure column. Another part of the distillation column system total supplied amount of feed air is only compressed to the pressure level of the high pressure column or a typically not more than 1 to 2 bar deviating from this pressure level and fed to this in the high pressure column.
  • the compressed to the higher pressure level of the distillation column system total supplied compressed air can be relaxed in a MAC-BAC process after cooling partly in a Claude turbine, as illustrated in the accompanying drawings.
  • HAP process which are also used in the air separation, however, the total, the distillation column system total supplied amount of feed air is compressed to a pressure level that is substantially, ie at least 3 bar, above the pressure level of the high pressure column.
  • the pressure difference is at least 3 bar, but can also be significantly higher, for example at 4, 5, 6, 7, 8, 9 or 10 bar and up to 14, 16, 18 or 20 bar.
  • HAP methods are for example from EP 2 980 514 A1 and the EP 2 963 367 A1 known.
  • Such nitrogen is nitrogen taken from the air separation plant in the form of a liquid or gaseous nitrogen product, and the nitrogen which, as explained, is expanded and otherwise utilized in the pressurized nitrogen turbine.
  • This also includes internally compressed nitrogen, ie liquid nitrogen, which is taken from the high-pressure column, pressurized in a pump and evaporated in the main heat exchanger.
  • the internal compression is also included, for example Haring, Section 2.2.5.2, "Internal Compression "explains.
  • argon discharge is here generally understood as a measure in which a fluid is withdrawn from the low-pressure column which is enriched in argon with respect to an oxygen-rich liquid fed from the low-pressure column, in particular the low-pressure column bottoms product, i. For example, has at least twice, five times or ten times the argon content.
  • Argon ejection further includes not returning at least a portion of the argon contained in a corresponding withdrawn fluid to the low pressure column.
  • the fluid is in particular subjected to an argon removal and only then returned to the low-pressure column.
  • Classical types of argon discharge are a transfer of a corresponding fluid into a crude argon column or argon discharge column, from which only an argon-poor, oxygen-rich fluid is returned to the low-pressure column.
  • the advantageous effect of the argon discharge is due to the fact that the oxygen-argon separation for the discharged argon in the low-pressure column is no longer required.
  • the separation of the argon from the oxygen in the low pressure column itself is basically expensive and requires a corresponding "heating" performance of the main capacitor.
  • Argon is discharged and thus omits the oxygen-argon separation or is this
  • the corresponding amount of argon no longer has to be separated in the oxygen section of the low pressure column and the heating power of the main capacitor can be reduced. Therefore, with the same yield of oxygen, either more air can be blown into the low-pressure column or more pressure nitrogen can be removed from the high-pressure column, which in turn offers energetic advantages.
  • an "argon discharge column” can be understood to mean a separation column for the argon-oxygen separation, which does not serve to obtain a pure argon product but to remove argon from the air to be separated in the high-pressure column and low-pressure column.
  • Their circuit differs only slightly from that of a conventional crude argon column, but it contains significantly less theoretical plates, namely less than 40, especially between 15 and 30.
  • an argon discharge column Like a crude argon column, the bottom region of an argon discharge column is connected to an intermediate point of the low pressure column and the argon discharge column is passed through cooled a top condenser, on its evaporation side typically relaxed bottoms liquid from the high pressure column is introduced.
  • An argon discharge column typically does not have a bottom evaporator.
  • a significant advantage of the present invention is that, as also explained below, a known double column system with high and low pressure column used more efficiently, i. better "exhausted” than with the use of conventional methods.
  • the rectification system can be operated with an optimal so-called Einblaseäquivalent, which energy can be saved.
  • the EinblaseEquivalent is usually defined as the sum of the amount of nitrogen taken from the high pressure column and returned neither as a return in this nor used as a liquid reflux to the low pressure column, and the amount of relaxed in the low pressure column compressed air in proportion to the total in the Distillation column system fed compressed air.
  • the oxygen content in the turbine stream supplied to the impure nitrogen turbine advantageously corresponds approximately to the oxygen content of a so-called impure nitrogen stream (also referred to as waste gas) from the low-pressure column.
  • impure nitrogen stream also referred to as waste gas
  • the stated material flows are in equilibrium with each other and no additional separation work (for cleaning the turbine stream to the purity of "pure" compressed nitrogen with an oxygen content in the ppm range) can be used.
  • the Nachboostern of the throttle current leads in the context of the present invention also to a cost reduction, since in this case the booster can be reduced by one or two stages and therefore can be created and operated cost-effective.
  • the present invention proposes a method for producing one or more air products by cryogenic separation of air in an air separation plant having a distillation column system comprising a high pressure column and a low pressure column, wherein an amount of feed air in a main air compressor is compressed to a first pressure level, of which a first fraction and a second portion be post-compacted in a reboiler. This corresponds to performing a MAC-BAC process as previously explained.
  • the post-compressed first portion of the amount of feed air is further compressed in the context of the inventive method successively using a first booster and a second booster and then cooled, relaxed to the first pressure level and fed into the high-pressure column.
  • This proportion is the already mentioned Joule-Thomson flow, with the previously described Joule-Thomson turbine or a combination of turbine and throttle valves being used for the expansion of the after-compressed and twice-boosted first portion of the feed air quantity ,
  • the post-compressed second portion of the feed air quantity is cooled in the context of the present invention and then using a first Turboexpanders, which is mechanically coupled to the second booster, relaxed to the first pressure level and fed into the high-pressure column.
  • the first turboexpander is a so-called medium-pressure turbine, which was also mentioned earlier.
  • the first portion and the second portion of the amount of feed air in the secondary compressor are recompressed from the first pressure level to a second pressure level and removed together from the after-compressor at the second pressure level.
  • the Joule-Thomson stream and the medium pressure turbine supplied compressed air stream are taken together from the booster, there is no intermediate removal of at least these shares from the booster.
  • high-pressure column is further removed from impure nitrogen at the first pressure level and expanded using a second turboexpander, which is mechanically coupled to the first booster, that is to say the already mentioned impure-pressure nitrogen turbine.
  • a second turboexpander which is mechanically coupled to the first booster, that is to say the already mentioned impure-pressure nitrogen turbine.
  • the impure nitrogen removed from the high-pressure column has an oxygen content of from 0.1 to 5 mol%, in particular from 0.5 to 2 mol%.
  • the cooling of the first portion of the amount of feed air after its compression using the first booster and the second booster is carried out in the context of present invention, in particular in the main heat exchanger of the air separation plant, wherein the first portion of the amount of feed air in the main heat exchanger to a temperature level of 95 to 110 K, in particular from 97 to 105 K, is cooled.
  • the cooling of the second portion of the amount of feed air before its relaxation using the first turboexpander can also be carried out in the main heat exchanger of the air separation plant, wherein the second portion of the feed air amount to the main heat exchanger at a temperature level of 130 ... to 200 K, in particular from 150 to 180 K. , is taken.
  • the impure nitrogen can be heated to a temperature level of 110 to 160 K, in particular from 120 to 150 K, in the context of the present invention before its expansion in the second turboexpander in the main heat exchanger of the air separation plant.
  • the impure nitrogen may be heated to a corresponding temperature level prior to its expansion in the second turboexpander in a secondary heat exchanger provided in addition to the main heat exchanger of the air separation plant.
  • the depletion of the argon-enriched fluid to argon is accomplished by means of a distillation column having less than 40 theoretical plates, in particular an argon discharge column having the characteristics given above.
  • a distillation column having less than 40 theoretical plates in particular an argon discharge column having the characteristics given above.
  • a third portion of the amount of feed air is advantageously cooled at the first pressure level and also fed to the high-pressure column. This is the regular feed air into the high pressure column.
  • the first portion of the feed air quantity of 15 to 40 percent, in particular from 20 to 30 percent of Feed air amount
  • the second portion of the feed air amount of 5 to 30 percent in particular from 10 to 20 percent of the feed air and / or the third portion of the feed air amount of 40 to 70 percent, in particular from 45 to 60 percent of the amount of feed air.
  • the low-pressure column can also be taken from impure nitrogen and, in particular, heated together with the impure nitrogen removed from the high-pressure column and expanded using the second turboexpander.
  • the impure nitrogen removed from the low pressure column and taken from the high pressure column and expanded using the second turboexpander advantageously have an identical or comparable oxygen content.
  • the invention also extends to an air separation plant having a distillation column system comprising a high pressure column and a low pressure column as set forth in the corresponding independent claim.
  • FIG. 1 shows an air separation plant, which is adapted for operation according to an embodiment of the present invention.
  • the air separation plant is designated 100 in total.
  • feed air in the form of a stream a is sucked in by means of a main air compressor 101 in an amount of feed air via a filter 102 and compressed to a first pressure level.
  • the feed air compressed to the first pressure level is branched off in part in the form of a stream b (Air1) and, moreover, in the form of a stream c subjected to a further processing known per se in a post-cooling unit 103 and an adsorber station 104.
  • the feed air of the material flow c compressed to the first pressure level and subjected to the treatment becomes a part in the form of a stream d of a recompression in a secondary compressor 105 and to a further part in the form of a stream e directly a cooling in a secondary heat exchanger 106 and a main heat exchanger 107 supplied.
  • the secondary compressor 105 comprises two compressor sections not designated separately and corresponding aftercoolers.
  • a partial stream of the material stream d is taken in the illustrated example the post-compressor 105 in the form of a stream f at an intermediate pressure level (Air2), the rest is compressed in the secondary compressor 105 to a second pressure level and leaves the after-compressor in the form of a mass flow g.
  • Air2 intermediate pressure level
  • the stream g is divided into a stream h and a stream i, the stream h at the second pressure level supplied to the main heat exchanger 107 and the flow i subjected to a further pressure increase to a third pressure level in a first booster 108 and a second booster 109 and on the third pressure level is supplied to the main heat exchanger 107.
  • the stream h is taken from the main heat exchanger 107 at an intermediate temperature level, in a first turboexpander 110, which is mechanically coupled to the second booster 109, relaxed again to the first pressure level and (see also linkage A) in a high pressure column 111 of a distillation column system 10, the Further, a low-pressure column 112 and an argon discharge column 113, fed.
  • the material flow i is taken from the main heat exchanger 107 cold side, using a generator turbine 114 or in a throttle valve (without designation) or both relaxed, thereby at least partially liquefied, and also fed into the high-pressure column 111.
  • the relaxation of the material flow i prior to feeding into the high-pressure column 111 also takes place at the first pressure level.
  • the high-pressure column 111 is taken from impure nitrogen in the form of a stream k with the above-mentioned exemplary specifications at the first pressure level, the main heat exchanger 107 cold side supplied (see link B), this taken at an intermediate temperature and relaxed in a second turboexpander 115, which in turn is mechanically coupled to the first booster 108.
  • the second turboexpander 115 is the repeatedly mentioned impure-pressure nitrogen turbine.
  • the air of the material stream i is also referred to as the "first fraction" of the feed air quantity (of the material stream a), the air of the material stream h also as the “second fraction” of the feed air quantity and the air of the material stream e as the "third fraction” of the Used quantity of air.
  • the amount of feed air is, as shown here, compressed in the main air compressor 101 to the first pressure level.
  • the first portion and the second portion of the amount of feed air are in the secondary compressor 105 to the second Compressed pressure level and the re-compressor 105 taken together at the second pressure level.
  • the first portion of the feed air quantity is further compressed using the first booster 108 and the second booster 109 to a third pressure level, cooled in the main heat exchanger 107, then expanded to the first pressure level and fed into the high-pressure column 111.
  • the second portion of the feed air quantity is expanded to the first pressure level in the first turboexpander 110, which is mechanically coupled to the second booster 109, and fed into the high-pressure column 111.
  • the high-pressure column is taken from impure nitrogen at the first pressure level and expanded in the second turbo-expander 115 mechanically coupled to the first booster 108.
  • the third portion of the amount of feed air ie the air of the stream e, is supplied to the secondary heat exchanger 106 in the form of two partial streams I and m, wherein the partial flow I the secondary heat exchanger 106 cold side and the partial flow m is taken from the secondary heat exchanger 106 at an intermediate temperature.
  • the partial flow m is further cooled in the main heat exchanger 107 and removed from this cold side.
  • a subset of the third portion of the feed air quantity can also be cooled only in the main heat exchanger 107.
  • the third portion of the amount of feed air is ultimately fed into the high-pressure column 111 as well.
  • an oxygen-enriched liquid in the form of a stream n is withdrawn, passed through a subcooler 116 and fed after use as a cooling medium in a top condenser of the argon discharge column 113 in the low pressure column 112.
  • Gaseous nitrogen is withdrawn from the top of the high-pressure column 111 in the form of a stream o, heated in the main heat exchanger 107 and provided in the form of one or more printed products (seal gas, PGAN). Further gaseous nitrogen is withdrawn from the top of the high-pressure column 111 in the form of a stream p and in a main condenser 117, the high-pressure column 111 and the Low pressure column 112 connects heat exchanging, at least partially liquefied.
  • a partial flow q is returned to the high pressure column 111, a partial flow r is passed through the subcooler 116 and provided as a liquid nitrogen product (LIN). Impure nitrogen is drawn off liquid in addition to the mentioned stream k in the form of a stream s from the high pressure column 111, passed through the subcooler 116 and fed into the low pressure column 112.
  • oxygen in the form of a stream t is withdrawn, in a pump 118 liquid pressure increases (internal compression), heated in the main heat exchanger 107 at least partially in the form of streams u, v and transferred to the gaseous or supercritical state and as appropriate Printed products (IC GOX1, IC GOX2) delivered.
  • Further oxygen is withdrawn in the form of a stream w from the low pressure column 112, passed in part through the subcooler 116 and discharged as a liquid product (LOX).
  • the stream w can also be branched off from the stream of material at the pump outlet or from the stream v, throttled to a lower pressure, fed to the subcooler 116 and then discharged as product.
  • impurity nitrogen is passed in the form of a stream x through the subcooler 116, then heated to parts in the secondary heat exchanger 106 and the main heat exchanger 107 and finally at will and as needed in the Nachkühlmaschine 103 and / or in the adsorber 104th be used (see also link C).
  • Fluid withdrawn from the head of the argon discharge column 113 can be heated (see also linkage D) in the secondary heat exchanger 106 and released to the atmosphere (ATM). So it is not won argon product, but only discharged argon.
  • a corresponding plant can also be equipped with a classical argon system, which may in particular comprise a crude and a pure argon column.
  • FIG. 1 While in FIG. 1 an air separation plant 100 is illustrated, in which the stream k, ie the impure nitrogen from the high pressure column 111, is fed after its expansion in the turboexpander 115 to the guided through the main heat exchanger 107 portion of the stream x is in FIG. 2 a Air separation plant illustrated in which the feed to the guided through the secondary heat exchanger 106 portion illustrates.
  • the stream m is not performed by the secondary heat exchanger 106 but by the main heat exchanger 107 (corresponding to the flow z according to FIGS. 1 and 2 ).
  • the secondary heat exchanger 106 instead of the stream k (see links B and E) is heated.
  • the secondary heat exchanger 106 is not present, the material flow e is therefore completely guided by the main heat exchanger 107. Accordingly, the stream x is completely heated in the main heat exchanger 107. The stream y is heated in the main heat exchanger 107.
  • the low-pressure column 112 is extended by a section 112a for the production of low-pressure nitrogen. Therefore, a low-pressure nitrogen stream j can be withdrawn from the top of the low-pressure column 112.
  • the low pressure nitrogen stream j is passed through the subcooler 116 and heated in a separate passage of the main heat exchanger 107.
  • a partial stream of the stream r can be liquid at the top of the low pressure column 112 abandoned.
  • the secondary heat exchanger 106 may or may not be present.

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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)
EP16020517.5A 2016-12-28 2016-12-28 Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air Withdrawn EP3343158A1 (fr)

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EP16020517.5A EP3343158A1 (fr) 2016-12-28 2016-12-28 Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air
AU2017276222A AU2017276222A1 (en) 2016-12-28 2017-12-13 Process for producing one or more air products, and air separation plant
US15/847,990 US20180180357A1 (en) 2016-12-28 2017-12-20 Process for producing one or more air products, and air separation plant
CN201711441963.5A CN108253732A (zh) 2016-12-28 2017-12-27 用于制造一个或多个空气产物的方法和空气分离设备

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WO2022053172A1 (fr) 2020-09-08 2022-03-17 Linde Gmbh Procédé d'obtention d'un ou de plusieurs produits à base d'air, et installation de fractionnement d'air
WO2023030689A1 (fr) 2021-09-02 2023-03-09 Linde Gmbh Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air

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US10746461B2 (en) * 2016-08-30 2020-08-18 8 Rivers Capital, Llc Cryogenic air separation method for producing oxygen at high pressures
CN113195991B (zh) * 2018-12-19 2023-05-02 乔治洛德方法研究和开发液化空气有限公司 低温空气分离单元的启动方法和相关联的空气分离单元
JP7313608B2 (ja) * 2019-04-08 2023-07-25 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 高純度酸素および窒素製造システム
FR3102548B1 (fr) * 2019-10-24 2023-03-10 Air Liquide Procédé et appareil de séparation d’air par distillation cryogénique
US20230055205A1 (en) * 2021-08-17 2023-02-23 Neil M. Prosser Nitrogen producing cryogenic air separation unit with excess air circuit
CN113758150A (zh) * 2021-09-18 2021-12-07 乔治洛德方法研究和开发液化空气有限公司 空气的低温分离方法和空气分离装置
WO2024105022A1 (fr) * 2022-11-15 2024-05-23 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'air par distillation cryogénique

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WO2022053172A1 (fr) 2020-09-08 2022-03-17 Linde Gmbh Procédé d'obtention d'un ou de plusieurs produits à base d'air, et installation de fractionnement d'air
WO2023030689A1 (fr) 2021-09-02 2023-03-09 Linde Gmbh Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air

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