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EP2489968A1 - Procédé et dispositif destinés à la décomposition à basse température d'air - Google Patents

Procédé et dispositif destinés à la décomposition à basse température d'air Download PDF

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Publication number
EP2489968A1
EP2489968A1 EP12000697A EP12000697A EP2489968A1 EP 2489968 A1 EP2489968 A1 EP 2489968A1 EP 12000697 A EP12000697 A EP 12000697A EP 12000697 A EP12000697 A EP 12000697A EP 2489968 A1 EP2489968 A1 EP 2489968A1
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EP
European Patent Office
Prior art keywords
pressure column
low
pressure
column
oxygen
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Withdrawn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
EP12000697A
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German (de)
English (en)
Inventor
Alexander Dr. Alekseev
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 EP12000697A priority Critical patent/EP2489968A1/fr
Publication of EP2489968A1 publication Critical patent/EP2489968A1/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Withdrawn legal-status Critical Current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
    • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
    • F25J3/04454—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • 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
    • F25J3/04018—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 main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—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
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    • 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
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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
    • 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
    • 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
    • F25J3/04303—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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • 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
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    • 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
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
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    • 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"
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    • 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
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/10—Processes or apparatus using separation by rectification in a quadruple, or more, column or pressure system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • 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]
    • 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
    • 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
    • F25J2205/34—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]
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/62—Purifying more than one feed stream in multiple adsorption vessels, e.g. for two feed streams at different pressures
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film

Definitions

  • the invention relates to a method according to the preamble of patent claim 1.
  • the distillation column systems of the invention may be designed as two-column systems (for example, as a classic Linde double column system), or as three or more column systems.
  • they may comprise further apparatuses for obtaining highly pure products and / or other air components, in particular noble gases, for example argon recovery and / or krypton-xenon recovery.
  • distillation column in particular under “high-pressure column” and under “low-pressure column”, is understood here to mean an apparatus which has mass transfer elements for the direct countercurrent mass transfer between an ascending gas and a liquid flowing down.
  • the mass transfer elements are formed by exchange trays or packing or by a combination of both.
  • the two high-pressure column head condensers are used to generate liquid reflux from the top gas of the respective high-pressure column and are cooled with bottom liquid of the corresponding low-pressure column or another suitable cooling fluid.
  • Both high-pressure column head capacitors are designed as a condenser-evaporator.
  • Each "condenser-evaporator” has a liquefaction space and an evaporation space, which consist of liquefaction passages or evaporation passages. In the liquefaction space, the condensation of a first fluid flow is performed, in the evaporation space, the evaporation of a second fluid flow.
  • the two fluid streams are in indirect heat exchange. Evaporation and Liquefaction space is formed by groups of passages that are in heat exchange relationship with each other.
  • the "main heat exchanger” is used for cooling feed air against return flows and may be formed from one or more parallel and / or serially connected heat exchanger sections, for example from one or more plate heat exchanger blocks.
  • the "first oxygen-enriched fraction” is usually taken from the bottom of the first high-pressure column; Alternatively, it can also be taken from some practical or theoretical soils higher.
  • the "second oxygen-enriched fraction” is usually taken from the bottom of the second high-pressure column; Alternatively, it can also be taken from some practical or theoretical soils higher.
  • the "third oxygen-enriched fraction” is usually taken from the bottom of the second low-pressure column; Alternatively, it can also be taken from some practical or theoretical soils higher.
  • the invention has for its object to provide a method of the type mentioned above and a corresponding device, which have a particularly low energy consumption.
  • the gaseous oxygen product is preferably delivered with a purity of less than 98%. (These and all other percentages are to be understood molar.) It can be supplied, for example, to the combustion chamber of a power plant in which a carbonaceous fuel is burned (oxyfuel).
  • the discharge pressure is less than 2.0 bar when no pressure increase is made in an oxygen fan or compressor.
  • the third oxygen-enriched fraction which is transferred from the second to the first low-pressure column, has a lower oxygen concentration than the gaseous oxygen product; it is in the range of 40 to 90%.
  • the main heat exchanger is preferably formed by plate heat exchanger blocks. Additionally or alternatively, regenerators for cooling the second feed air stream can be used in the main heat exchanger.
  • a fourth oxygen-enriched fraction is taken off liquid from the lower region of the first high-pressure column and fed to the second low-pressure column.
  • first oxygen-enriched Fraction fed directly into the first low-pressure column
  • second part is introduced as" fourth oxygen-enriched fraction "in the second low-pressure column.
  • the further features of claim 3 allow a further reduction of the operating pressure of the second distillation column system.
  • the regeneration gas for both cleaning devices (which are usually formed by molecular sieve adsorber) is namely taken from the first low-pressure column. Only this must therefore be operated under a pressure sufficient to deliver the regeneration gas after flowing through the purifier to the atmosphere.
  • the top gas of the second low-pressure column can have a lower pressure and, after heating in the main heat exchanger, can be discharged directly to the atmosphere or into an evaporative cooler.
  • the second distillation column system may be formed as a two-capacitor system or multi-capacitor system by the second main capacitor is cooled by means of an intermediate liquid of the second low-pressure column and the second low-pressure column also comprises a sump evaporator, which is designed as a condenser-evaporator and is heated by means of a partial flow of the second feed air stream.
  • a sump evaporator which is designed as a condenser-evaporator and is heated by means of a partial flow of the second feed air stream.
  • another intermediate evaporator can be used between the two condenser evaporators (three-capacitor system).
  • the formulations which refer to "about" the first or second pressure, mean here that the corresponding pressure must be so high that the first or second feed air stream after deduction of the natural pressure losses, which he flows through lines, heat exchangers and the like Apparatus experiences, the first and second high-pressure column reached under the first and second pressure.
  • the invention also relates to a device for the cryogenic separation of air according to claims 5 to 8.
  • atmospheric air (AIR) 1 is compressed in two strands in an air compressor system. It is first brought via a pair of filters 3 from a pair of first air compressor stages 4 to a "second pressure" of 2 to 4 bar (plus pressure losses) and cooled in a pair of first aftercooler 5. Subsequently, the feed air is split into a first partial flow 100 and a second partial flow 200.
  • the first partial flow 100 includes the "first feed air stream” of the claims, but in this embodiment additionally contains a turbine air flow, which will be described in more detail below.
  • the second partial stream 200 forms the "second feed air stream" in the sense of the claims (smaller air fractions, which are used for other purposes, so-called instrument air, are neglected here).
  • first pressure 4.0 to 5.8 bar (plus pressure losses)
  • second aftercooler 7 a direct contact cooler or a combination of aftercooler and direct contact cooler can also be used.
  • a chiller for cooling the cooling water can be used.
  • the air compressor stages which are shown on the right or left in the drawing, are each formed by a single machine (each with a housing and a drive). Overall, the system has two air compressor strands. Alternatively it could be different from FIG. 1 be formed single-stranded. .
  • the first partial flow 101 is pre-cooled under the high pressure in a first direct contact cooler 102 in direct heat exchange with cooling water 103.
  • the pre-cooled first partial flow 104 is purified in a first cleaning device 105, which consists of a pair of switchable molecular sieve adsorber, and then fed via line 106 to the warm end of a main heat exchanger 8. Before it is branched into the first feed air stream 107 and a turbine air stream 9.
  • a first cleaning device 105 which consists of a pair of switchable molecular sieve adsorber
  • the first feed air stream is cooled to about dew point temperature, removed at the cold end of the main heat exchanger 8 via line 108 and fed to the first high pressure column 110 of a first distillation column system 109 which also has a first low pressure column 111 and a "first high pressure column top condenser" 113 is designed as a classic main capacitor of a conventional double column.
  • a first part of the overhead gas of the first high-pressure column 110 is condensed.
  • a second portion 128 of this head gas is warmed in the main heat exchanger and partially withdrawn via lines 129 and 130 as a gaseous medium pressure nitrogen product (MPGAN).
  • MPGAN gaseous medium pressure nitrogen product
  • the liquid nitrogen 114 obtained in the first main condenser 113 is fed to a first part 115 as reflux to the first high-pressure column 110.
  • the remainder 116 is subcooled in a first subcooling countercurrent 117 and fed via line 118 as reflux to the top of the first low pressure column 111.
  • a part 119 can be obtained from liquid nitrogen product (LIN) if needed.
  • the bottoms liquid 120 of the first high pressure column 110 is also subcooled in the subcooling countercurrent 117.
  • a first part 122 of the supercooled bottoms liquid 121 forms a "first oxygen-enriched fraction" and is introduced at a first intermediate point into the first low-pressure column 111.
  • a portion of the vaporized in the evaporation space of the main condenser oxygen is removed as "gaseous oxygen product" 123, heated in the main heat exchanger 8 to about ambient temperature and finally withdrawn via line 124 as the final product (GOX).
  • liquid oxygen is withdrawn from the sump of the first low-pressure column 111 and discharged to at least a portion 136 - optionally after subcooling in the first supercooling countercurrent 117 - as a liquid oxygen product (LOX).
  • LOX liquid oxygen product
  • a small portion 137 of the liquid sump oxygen is removed as purge stream, brought in a pump 138 to supercritical pressure, heated in the main heat exchanger 8 to about ambient temperature and finally combined with the gaseous oxygen product in line 124.
  • the top nitrogen of the first low-pressure column 111 is removed under a pressure of more than 1.3 bar, for example 1.4 to 2.0 bar, as the "first gaseous top product" 125 and after heating in the first supercooling countercurrent 117 and in the main heat exchanger 8 withdrawn warm via line 126 and finally at least temporarily blown off via line 127 into the atmosphere (ATM).
  • ATM atmosphere
  • parts 52, 53 of the warm first gaseous overhead product are used as regeneration gas in both cleaning devices 105, 205, optionally after heating in a common regeneration gas heater 54.
  • the second partial flow 201 of the feed air is pre-cooled below about the second pressure in a second direct contact cooler 202 in direct heat exchange with cooling water 203.
  • the pre-cooled second substream 204 is purified in a second purification device 205, which consists of a pair of reversible molecular sieve adsorber, at about the second pressure and then fed via line 206 to the hot end of a main heat exchanger 8.
  • the second feed air stream is cooled to about dew point temperature, taken at the cold end of the main heat exchanger 8 via line 208 and the second high-pressure column 210 of a second distillation column system 209 fed, which also has a second low-pressure column 211 and a "second high-pressure column head capacitor" 213.
  • the second high-pressure column top condenser 213 is likewise designed here as a classic main condenser of a conventional double column.
  • a first part of the overhead gas of the second high-pressure column 210 is condensed.
  • a second portion 228 of the overhead gas of the second high pressure column 110 is warmed in the main heat exchanger and partially withdrawn via line 230 as gaseous pressure nitrogen product (PGAN).
  • GPN gaseous pressure nitrogen product
  • the liquid nitrogen 214 obtained in the second main condenser 213 is fed to a first part 215 as reflux to the second high-pressure column 210.
  • the remainder 216 is subcooled in a second subcooling countercurrent 217 and fed via line 218 as reflux to the top of the second low pressure column 211.
  • the bottom liquid 220 of the second high-pressure column 210 forms a "second oxygen-enriched fraction" and is subcooled in the subcooling countercurrent 217.
  • the supercooled bottoms liquid 221 is introduced into the second low pressure column 211 at an intermediate location via an optional LOX filter 219 formed by a liquid adsorber.
  • LOX filter 219 formed by a liquid adsorber.
  • a part 229 of the supercooled bottoms liquid 121 from the first high-pressure column 110 is fed in at this intermediate point.
  • the top nitrogen of the second low-pressure column 211 is removed under a pressure of less than 1.3 bar as "second gaseous top product" 225 and after warming in the second supercooling countercurrent 217 and in the main heat exchanger 8 via line 226 warm withdrawn and finally via line 127 without pressure Evaporative cooler 50 fed as a dry gas.
  • the evaporative cooler generates cold cooling water 51, 103, 203 for both direct contact coolers 102, 202.
  • the turbine air flow 9, 10 is supplied from below an intermediate temperature of the main heat exchanger 8 of an air turbine 11, which is coupled to a generator 12, and there relaxed about to the operating pressure of the first low-pressure column 111.
  • the relaxed turbine air stream 13 is fed to the first low-pressure column 11.
  • a portion 131 of the second portion 129 of the overhead gas of the first high-pressure column 110 in a nitrogen turbine 132 which is coupled to a generator 133, working expanded to slightly above atmospheric pressure, fed via line 134 to the main heat exchanger 8 and there mixed with the first gaseous top product 125, 126 from the first low-pressure column 11.
  • both main capacitors 113, 213 are designed as liquid bath evaporators, that is to say they are formed by heat exchanger blocks which are immersed in a bath of bottom liquid of the corresponding low pressure column 111, 211, this liquid being thrown over the evaporation passages by the thermosiphon effect.
  • the warm turbine may be formed by the air turbine 11 and the cold turbine by the nitrogen turbine 132.
  • the exit stream 134 of the nitrogen turbine 132 can be warmed in separate passages of the main heat exchanger 8 and blown off into the atmosphere or mixed with the stream 225/226.
  • the embodiment of FIG. 2 differs therefrom in that the second main condenser (the "second high pressure column head condenser") 213 is formed as a falling film evaporator and that in the second distillation column system, the high pressure column 210 and the low pressure column 211 are arranged side by side instead of one above the other. From the bottom of the second low pressure column 211, the entire bottoms liquid via line 423 and a pump 435 is removed liquid. A first part thereof is led to the first low-pressure column 111 as a "third oxygen-enriched fraction" 436. The remaining bottom liquid 437 is conducted into the evaporation space of the second main condenser 213 and partially evaporated there.
  • the second main condenser the "second high pressure column head condenser”
  • the partially vaporized fraction 438 is returned to the bottom of the second low-pressure column 211.
  • the pump 435 thus fulfills two functions, namely the lifting of the third oxygen-enriched fraction 436 to the second intermediate point of the first low-pressure column 111 and ensuring the circulation in the falling-film evaporator 213.
  • second high-pressure column 210 and second low-pressure column 211 are generally particularly favorable.
  • the two columns can be analogous to FIG. 1 be arranged one above the other as a conventional double column with falling-film evaporator 213 therebetween.
  • FIG. 3 similar FIG. 2 However, here the entire bottom liquid 423, 537 of the second low pressure column 211 is introduced by means of the pump 435 in the evaporation space of the falling film evaporator 213.
  • the partially vaporized fraction flowing out of the falling film evaporator is subjected to phase separation in a separator 539.
  • the gas portion 538 is returned to the second low-pressure column, the liquid portion 540 is guided by means of another pump 541 as a "third oxygen-enriched fraction" 436 to the first low-pressure column 111.
  • the average temperature difference in the second high-pressure column top condenser 213 and thus the operating pressure in the second high-pressure column 210 and the energy consumption during compression of the second feed air stream 208 are reduced.
  • FIG. 4 corresponds largely FIG. 3 , Here, however, the columns and the main condenser of the second distillation column system are stacked in an unusual manner.
  • the second high-pressure column 210 is not arranged as in a conventional double column below, but above the second low-pressure column 211; the turn designed as a falling film evaporator second high-pressure column head capacitor sits at the top.
  • the procedural advantage of the procedure of FIG. 3 can be achieved without a second pump 541; the third oxygen-enriched fraction 436, by virtue of its hydrostatic potential, flows by itself to the second intermediate point of the first low-pressure column 111.
  • the procedure of FIG. 5 has a divided low-pressure column 611, 612 in the second distillation column system. This contains a total of three condenser-evaporator 213, 614, 615th
  • the section 611 of the second low-pressure column corresponds to the upper section (slightly below the feeds of the oxygen-enriched liquids) of the second low-pressure column 211 in FIG FIG. 4 , He is in FIG. 5 analogous to FIG. 4 arranged below the second high-pressure column 210.
  • the remaining part 612 of the second low-pressure column is located above the second high-pressure column 210 and contains the three condenser-evaporators 213, 614, 615, all of which are designed as falling-film evaporators.
  • the top one represents the high pressure column top condenser but here not with bottoms liquid, but with an intermediate liquid 616 of the second low-pressure column 611, 612 operated, which is raised by a pump 617.
  • the second intermediate evaporator 614 is used for partial evaporation of a second, oxygen-rich intermediate liquid of the second low-pressure column; the condenser-evaporator 615 represents the sump evaporator of the second low-pressure column 611, 612. Both are heated by means of a heating air flow 609, which is introduced together with the second feed air stream 208 via line 608.
  • the heating air stream 620, 622 flows through first the bottom evaporator 615 and then the intermediate evaporator 614. Liquid recovered in the condenser-evaporators 615, 614 or the fraction remaining in vapor form are passed via the lines 621 and 623 to the second high-pressure column 210 and there at suitable intermediate points fed.
  • the second distillation column system of the FIG. 4 with only one liquid pump.
  • the third oxygen-enriched fraction 236 alone can flow from the second low-pressure column 612 into the first low-pressure column 111 due to the hydrostatic potential.
  • FIG. 6 shows a second distillation column system 210, 611, 612, the procedurally with that of FIG. 5 is identical.
  • the section 611 of the second low-pressure column is arranged next to the two other column sections 210, 612.
  • the pump 617 must thereby overcome a smaller height difference; however, another pump 235 for the third oxygen-enriched fraction 223, 236 is needed regularly.
  • FIGS. 7 and 8th differ solely by the Figures 5 or 6, that an intermediate portion 812 is not disposed below, but above the second high-pressure column 210.
  • the second intermediate evaporator 614 is omitted.
  • a small portion of the liquid nitrogen (118 in FIG. 1 ) from the first main capacitor (113 in FIG. 1 ) on the Head of the second low-pressure column 211 and the portion 611 of the second low-pressure column are abandoned.
  • FIG. 9 shows one opposite FIG. 1 modified air compressor system that can be used in the invention.
  • This consists of two air compressor strands 3a / 4a / 5a and 3b / 4b / 5b with different final pressure.
  • the illustrated on the left strand 3a / 4a / 5a is formed by a machine with a housing and a drive, the right represented by another machine with a housing and a drive.
  • the compressor symbols 4, 4a, 4b, 6 can each stand for one or more compressor stages, optionally with appropriate intermediate cooling.
  • the two distillation column systems are not shown in detail (box 800).
  • the portion 131 of the head gas of the first high-pressure column is work-expanded in two parallel nitrogen turbines 732a, 732b, of which the first 732a as in FIG. 1 is coupled to a generator 133.
  • the second nitrogen turbine 732b drives a cold compressor 733 in which a part 706, 707 of the feed air 206 compressed to the second pressure is recompressed to the first pressure.
  • the cold-compressed air portion 708 is then combined with the remaining high-pressure air 106. As a result, energy is saved on the inlet side air compressor system.
  • FIG. 10 shown air compressor system (analog FIG. 1 ) can also the air compressor system of FIG. 9 be used.
  • FIG. 11 similar FIG. 10 However, here another air stream 906, 907, 908 is passed through the cold compressor 733. This represents a part of the high-pressure air flow 106 from the air compressor system and is further compressed in the cold compressor 733 well beyond the first pressure to then serve as a turbine stream 9. As a result, the cooling capacity of the air turbine 11 increases.
  • FIG. 12 will be like in FIG. 10 a portion 706, 707, 708 of the second partial flow of the feed air, which is below the lower second pressure, post-compressed in the cold compressor 733.
  • the main heat exchanger is constructed of two physically separate and parallel sections 8a and 8b, each consisting of one or more heat exchanger blocks.
  • second gaseous top product 226 from the second low-pressure column (not shown here) into two partial streams 726, 727 branches, which are passed through the main heat exchanger sections 8a and 8b.
  • the warm stream 728 is blown off into the atmosphere (ATM). Power 727/728 serves as equalizing current.
  • the turbine stream 9 are recompressed in the cold compressor.
  • FIG. 13 As a compensating flow for the two main heat exchanger sections 8a, 8b is in FIG. 13 a portion 506 of the partial air flow 106 is used, which is below the higher first pressure. Alternatively, could also be in FIG. 13 analogous to FIG. 11 the turbine stream 9 are recompressed in the cold compressor.
  • FIG. 14 becomes different from FIG. 13 the purge stream 137, which is pressurized by the pump 138, is vaporized (or pseudo-vaporized if the pressure is supercritical) in a separate third main heat exchanger section 8c in indirect heat exchange with at least a portion 508, 509 of the cold recompressed air stream 708 and warmed up.
  • the turbine stream 9 are recompressed in the cold compressor.
  • FIG. 15 has a fourth separate main heat exchanger section 8d, in which the air 707 to be cold-compressed is cooled upstream of the cold compressor 733 against the exhaust gas 734b of the nitrogen turbine 732b.
  • the heated turbine exhaust gas 735b is then no longer introduced into the main heat exchanger section 8b, in contrast to the exhaust gas 734a of the generator-braked nitrogen turbine 732a.
  • FIG. 15 could also be in FIG. 15 analogous to FIG. 11 the turbine stream 9 are recompressed in the cold compressor.
  • the main heat exchanger section 8a may also be formed by a pair of regenerators instead of the otherwise conventional plate heat exchanger blocks.
  • the Figures 16 and 17 show two concrete examples of this, their heat exchanger and turbine circuits otherwise on FIG. 12 based.
  • One regenerator of the regenerator pair 88 heats a partial flow 726 of the "second gaseous overhead" 226 from the second low pressure column while the other cools the airflow 206 which is below the lower second pressure.
  • FIG. 17 differs from FIG. 16 in that the regenerator 88 is also used for cleaning the second air part 204, 206 by freezing water and carbon dioxide. This is sufficient for a single-stranded cleaning device 105, which is operated at about the first pressure.
  • the LOX filter 219 above becomes FIG. 1 has been described as optional, mandatory.

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2767787A1 (fr) 2013-02-19 2014-08-20 Linde Aktiengesellschaft Procédé de production d'oxygène gazeux par décomposition à basse température de l'air
WO2015003785A1 (fr) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de gaz comprimé et procédé et dispositif de séparation d'air à basse température
FR3013105A1 (fr) * 2013-11-14 2015-05-15 Air Liquide Procede et appareil de separation d’air par distillation cryogenique
DE102016006714A1 (de) 2016-06-01 2017-12-07 Linde Aktiengesellschaft Mehrsäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung
US10794630B2 (en) 2017-08-03 2020-10-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
WO2023051946A1 (fr) * 2021-09-29 2023-04-06 Linde Gmbh Procédé de séparation cryogénique de l'air et installation de séparation d'air

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US4254629A (en) 1979-05-17 1981-03-10 Union Carbide Corporation Cryogenic system for producing low-purity oxygen
DE3709588A1 (de) * 1986-04-02 1987-10-08 Voest Alpine Ag Vorrichtung zur zerlegung von gasen mittels koaxial ineinander angeordneter rektifikationskolonnen
EP0342436A2 (fr) * 1988-05-20 1989-11-23 Linde Aktiengesellschaft Procédé de séparation de l'air à basse température
US5571309A (en) * 1995-07-28 1996-11-05 The Boc Group, Inc. Adsorption process
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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2767787A1 (fr) 2013-02-19 2014-08-20 Linde Aktiengesellschaft Procédé de production d'oxygène gazeux par décomposition à basse température de l'air
DE102013002835A1 (de) 2013-02-19 2014-08-21 Linde Aktiengesellschaft Verfahren zur Erzeugung von gasförmigem Sauerstoff durch Tieftemperaturzerlegung von Luft
WO2015003785A1 (fr) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de gaz comprimé et procédé et dispositif de séparation d'air à basse température
FR3013105A1 (fr) * 2013-11-14 2015-05-15 Air Liquide Procede et appareil de separation d’air par distillation cryogenique
WO2015071578A2 (fr) 2013-11-14 2015-05-21 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
WO2015071578A3 (fr) * 2013-11-14 2015-12-03 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
US10605523B2 (en) 2013-11-14 2020-03-31 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for separating air by cryogenic distillation
DE102016006714A1 (de) 2016-06-01 2017-12-07 Linde Aktiengesellschaft Mehrsäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung
US10794630B2 (en) 2017-08-03 2020-10-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
US10866024B2 (en) 2017-08-03 2020-12-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation
WO2023051946A1 (fr) * 2021-09-29 2023-04-06 Linde Gmbh Procédé de séparation cryogénique de l'air et installation de séparation d'air

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