EP4018143A1 - Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant - Google Patents

Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant

Info

Publication number
EP4018143A1
EP4018143A1 EP20767968.9A EP20767968A EP4018143A1 EP 4018143 A1 EP4018143 A1 EP 4018143A1 EP 20767968 A EP20767968 A EP 20767968A EP 4018143 A1 EP4018143 A1 EP 4018143A1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
passages
heat
operating mode
evaporation
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.)
Pending
Application number
EP20767968.9A
Other languages
German (de)
English (en)
Inventor
Stefan Lochner
Ralph Spöri
Axel Lehmacher
Pascal Freko
Paul Heinz
Felix RÖßLER
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
Publication of EP4018143A1 publication Critical patent/EP4018143A1/fr
Pending legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0248—Stopping of the process, e.g. defrosting or deriming, maintenance; Back-up mode or systems
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0251—Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0261—Details of cold box insulation, housing and internal structure
    • 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
    • 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
    • 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
    • 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
    • F25J3/04242—Cold end purification of the 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
    • F25J3/04248—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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04478—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
    • 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
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • 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
    • F25J3/04945—Details of internal structure; insulation and housing of the cold box
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/58—Argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/20—Control for stopping, deriming or defrosting after an emergency shut-down of the installation or for back up 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0033—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for cryogenic applications

Definitions

  • the present invention relates to a method for operating a heat exchanger, an arrangement with a correspondingly operable heat exchanger and an installation with a corresponding arrangement according to the preambles of the respective independent claims.
  • heat exchangers are operated with cryogenic fluids, i.e. fluids with temperatures well below 0 ° C, in particular well below -50 ° C or -100 ° C.
  • cryogenic fluids i.e. fluids with temperatures well below 0 ° C, in particular well below -50 ° C or -100 ° C.
  • the present invention is mainly described with reference to the main heat exchangers of air separation plants, but it is basically also suitable for use in other areas of application, for example for plants for storing and recovering energy using liquid air or natural gas liquefaction or plants in the petrochemical industry.
  • the present invention is also particularly suitable in plants for liquefying gaseous air products, for example gaseous nitrogen.
  • Corresponding systems can, in particular, be supplied with gaseous nitrogen by air separation systems and liquefy it. The liquefaction is not followed by a rectification as in an air separation plant. Therefore, when the problems explained below are overcome, for example when there is no need for corresponding liquefaction products, these systems can be completely switched off and kept on standby until the next use.
  • heat exchangers in air separation plants and other heat exchangers through which warm and cryogenic media flow achieve temperature equalization and heat up when the associated plant is shut down and the heat exchanger is shut down, or the temperature profile that forms in a corresponding heat exchanger in stationary operation can be in such a Case not be held. If, for example, cryogenic gas is then fed into a heated heat exchanger when it is restarted, or vice versa, there are high thermal stresses as a result of different thermal expansion due to differential temperature differences, which in the long term can lead to damage to the heat exchanger or require a disproportionately high cost of materials and manufacturing to avoid such damage.
  • the temperatures at the previously warm end and at the previously cold end are equalized due to the good heat conduction (longitudinal heat conduction) in its metallic material.
  • the previously warm end of the heat exchanger becomes colder over time and the previously cold end of the heat exchanger becomes warmer until the temperatures mentioned are at or near an average temperature.
  • the temperatures which were around -175 ° C or +20 ° C at the time of shutdown, equalize over several hours and almost reach an average temperature.
  • DE 10 2014018412 A1 discloses a method for operating a liquefaction process for liquefying a hydrocarbon-rich stream, in particular natural gas.
  • a partial refrigerant stream from a refrigerant circuit which is at a suitable temperature level, is passed through at least one heat exchanger in an amount that is controlled during commissioning instead of the hydrocarbon-rich stream to be liquefied and which, when normal operation is reached, is dimensioned in such a way that it compensates for the amount of heat introduced into the refrigeration circuit by the hydrocarbon-rich stream to be liquefied during normal operation.
  • US 2015/226094 A1 and EP 2 880 267 A2 describe the generation of electrical energy in a combined system comprising a power plant and an air treatment system.
  • a storage fluid is produced and stored in the air treatment system from feed air.
  • the storage fluid is evaporated or pseudo-evaporated under superatmospheric pressure and a gaseous high-pressure fluid formed in the process is expanded in a gas expansion unit of the power plant.
  • gaseous natural gas is liquefied or pseudo-liquefied against the evaporating or pseudo-evaporating storage fluid.
  • CN 102 778 105 A describes a quick start of an oxygen generator in which, on the one hand, feed air is expanded in a turboexpander before it is liquefied and fed into the main rectification column, and in which, on the other hand, liquid argon, which is stored in a storage tank, is used in a refrigeration cycle is used to cool the feed air.
  • US 2012/1617616 A1 or EP 2 449 324 B1 discloses a method for operating a liquefaction system for gas liquefaction using a main heat exchanger.
  • a refrigerant compression circuit is provided, of which a low-pressure part conducts evaporated refrigerant from the main heat exchanger to a compressor and a high-pressure part returns the compressed and cooled refrigerant from the compressor to the main heat exchanger.
  • the pressure within the condensing system is controlled by regulating the amount of vaporized refrigerant in either or both of the low pressure and high pressure parts of the condensing system.
  • the object of the present invention is to specify measures which enable a corresponding heat exchanger, in particular in one of the aforementioned systems, to be restarted after a long period of shutdown without the aforementioned disadvantageous effects occurring.
  • the present invention proposes a method for operating a heat exchanger, an arrangement with a correspondingly operable heat exchanger and a system with a corresponding arrangement with the features of the respective independent claims.
  • a heat exchanger is an apparatus which is designed for the indirect transfer of heat between at least two fluid flows, for example, which are guided in countercurrent to one another.
  • a heat exchanger for use in the context of the present invention can be formed from a single or a plurality of heat exchanger sections connected in parallel and / or in series, for example from one or more plate heat exchanger blocks.
  • a heat exchanger has “passages” which are set up to guide fluid and which are separated from other passages by separating plates or only connected on the inlet and outlet side via the respective headers. The passages are separated from the outside by means of side bars.
  • heat exchanger passages The passages mentioned are hereinafter referred to as "heat exchanger passages" designated.
  • the two terms “heat exchanger” and “heat exchanger” are used synonymously in accordance with common usage. The same applies to the terms “heat exchange” and “heat exchange”.
  • the present invention relates in particular to the apparatus referred to in the German version of ISO 15547-2: 2005 as plate-fin heat exchangers. If a “heat exchanger” is used below, this should therefore be understood in particular as a rib-plate heat exchanger.
  • a fin-plate heat exchanger has a large number of flat chambers or elongated channels lying one above the other, which are separated from one another by corrugated or otherwise structured and interconnected, for example soldered plates, usually made of aluminum. The panels are stabilized by means of side bars and connected to one another via these.
  • the structuring of the heat exchanger plates serves in particular to enlarge the heat exchange surface, but also to increase the stability of the heat exchanger.
  • the invention particularly relates to brazed fin and plate heat exchangers made of aluminum. In principle, however, corresponding heat exchangers can also be made from other materials, for example from stainless steel, or from various different materials.
  • the present invention can be used in air separation plants of a known type, but also, for example, in plants for storing and recovering energy using liquid air.
  • the storage and recovery of energy using liquid air is also known as Liquid Air Energy Storage (LAES).
  • LAES Liquid Air Energy Storage
  • a corresponding system is disclosed, for example, in EP 3 032 203 A1.
  • Systems for liquefying nitrogen or other gaseous air products are also known from the specialist literature and are also described with reference to FIG.
  • the present invention can also be used in any further systems in which a heat exchanger can be operated accordingly.
  • It can be, for example, plants for natural gas liquefaction and separation of natural gas, the LAES plants mentioned, plants for air separation, liquefaction cycles of all kinds (especially for air and nitrogen) with and without air separation, ethylene plants (i.e. especially separation plants that process gas mixtures Steamerackern are set up), systems in which Cooling circuits, for example with ethane or ethylene at different pressure levels, and systems in which carbon monoxide and / or carbon dioxide circuits are provided act.
  • cryogenic liquids formed using air can also be stored in the first operating mode and used in the second operating mode to generate electrical energy.
  • corresponding cryogenic liquids are liquid nitrogen or liquid oxygen or component mixtures which predominantly consist of liquid nitrogen or liquid oxygen.
  • external heat and fuel can also be coupled in to increase efficiency and output power, in particular using a gas turbine whose exhaust gas is expanded together with the pressure flow formed from the air product in the second operating mode.
  • the invention is also suitable for such systems.
  • the present invention can in particular also be used in a so-called nitrogen liquefier. Also systems for liquefaction and / or Decomposition of gases other than air benefit from the measures proposed according to the invention.
  • cold gas from a tank or exhaust gas from the stationary system can flow through a heat exchanger during a shutdown of the associated system in order to avoid heating or to maintain the temperature profile developed in stationary operation (i.e. in particular the usual production operation of a corresponding system) .
  • Such an operation in which the usual, also normal operation, passages are used accordingly, can, however, only be implemented with great effort in conventional methods.
  • heat from the surroundings can also be introduced there via thermal bridges in order to avoid the cooling of the warm end of a corresponding heat exchanger. If there is no process unit downstream of the heat exchanger with a significant buffer capacity for cold (e.g. no rectification column system with the accumulation of cryogenic liquids), such as in a pure air liquefaction system, excessive thermal stresses can occur when hot process streams are suddenly supplied to the warm end of the Recommissioning can be reduced.
  • a significant buffer capacity for cold e.g. no rectification column system with the accumulation of cryogenic liquids
  • the warm process streams supplied after restarting can be at least partially relaxed in an expansion machine after exiting the cold end of the heat exchanger and as cold streams (which in this case, however, do not yet have the low temperature as they would later in normal operation present at the cold end) can be returned via the cold end to the warm end.
  • the heat exchanger can be slowly brought to its normal temperature profile by Joule-Thomson cooling.
  • the present invention relates less to this case, i.e. less to processes in which, after restarting, the cold end of the heat exchanger is not directly connected to cold process streams (on the one that is present in normal operation Final temperature), but rather the case that cryogenic fluids are available from the start of restarting, which are to be heated by the heat exchanger, and which are therefore fed to the heat exchanger at the cold end from the restart.
  • a process unit with a significant buffer capacity for cold is located downstream of the heat exchanger (e.g. a rectification column system with an accumulation of cryogenic liquids, as is the case in an air separation plant), one can use the above-described Measures to minimize the occurrence of thermal voltages at this point, however, at the simultaneously heated cold end, the sudden onset of the flow of colder fluid can lead to the occurrence of thermal voltages due to impermissibly high (temporal and local) temperature gradients. Keeping the warm end warm even promotes the formation of higher temperature differences at the cold end and thus the occurrence of increased thermal stresses. Therefore, in such cases, cooling or keeping the cold end of the heat exchanger cold is desirable or advantageous.
  • the present invention relates in particular to the case just explained.
  • the case is considered that (in addition to the always possible heating at the warm end of the heat exchanger) the cold end of the heat exchanger is cooled down or kept cold during standstill phases.
  • the area to be cooled can be equipped with additional cooling passages that can be applied to the outside of the heat exchanger (block) in particular.
  • additional cooling passages that can be applied to the outside of the heat exchanger (block) in particular.
  • the heat exchanger can in particular be part of a corresponding arrangement, which in turn can be designed as part of a larger system.
  • the present invention can be used in particular in air processing systems of the type explained in detail above and below. In principle, however, it can also be used in other areas of application in which a flow through a corresponding heat exchanger is prevented during certain times and the heat exchanger heats up during these times or a temperature profile formed in the heat exchanger is equalized.
  • the present invention can be used in an air separation plant, since in a corresponding air separation plant there is a buffer capacity for cold fluid at the cold end of the heat exchanger and it is therefore desirable to keep the cold end cold during standstill phases.
  • the present invention also relates in embodiments to those measures which avoid excessive thermal stress on the warm end of a heat exchanger.
  • Such measures can be combined within the scope of the present invention with the measures proposed according to the invention, which are aimed at reducing thermal stresses at the cold end of the heat exchanger.
  • the present invention is based in one embodiment (hereinafter referred to as "first" embodiment) on the knowledge that cooling using an in particular cryogenic liquid that is evaporated in evaporation passages on or in the heat exchanger, but not previously, offers particular advantages.
  • first embodiment By using the measures proposed according to the invention, it is possible, in particular, to dispense with expensive pumps for providing a cooling flow.
  • the operation of the heat exchanger proposed according to the invention offers advantages because it reduces both the consumption of cold fluids and the corresponding hardware and control and regulation technology does not have to be made available in a complex manner.
  • a further advantageous embodiment of the invention (hereinafter referred to as “second” embodiment) is based on the knowledge that it can also offer particular advantages if gas is used as the cooling fluid, this but not through the entire heat exchanger, but only over a section at the cold end through its heat exchanger passages.
  • the first embodiment is explained below.
  • the cooling at the cold end of a corresponding heat exchanger is carried out with liquid, for example with liquid nitrogen, which is taken from a container.
  • the container can, in particular, be fed with a corresponding liquid during regular operation.
  • the liquid is withdrawn in liquid form from the container and evaporation passages are fed into or on the heat exchanger.
  • the evaporation passages can also be formed by line sections of a line provided in a suitable arrangement on or in the heat exchanger.
  • passages which are also used in the regular operation of a corresponding heat exchanger for cooling and / or heating fluids, as corresponding evaporation passages is also possible in principle.
  • the corresponding liquid is removed from the container and fed into the evaporation passages in particular when a maximum temperature is exceeded at the cold end of the heat exchanger.
  • the liquid in the container is at or near its boiling point.
  • the container can be fed from another container or tank or from another source (e.g. the low-pressure column of an air separation plant).
  • the arrangement in the first embodiment of the present invention is such that a gas formed during the evaporation of the liquid (partially or completely) flows back into the tank (circulation principle).
  • a pressure regulator at a gas phase outlet of the container can be used to set a defined container pressure in order to set the desired evaporation temperature level of the refrigerant. This is in particular a limit temperature for the cold end of the heat exchanger to be kept cold.
  • the arrangement is overall such that, due to the evaporation of the liquid, a driving pressure gradient and thus a natural circulation are established.
  • the supply of the liquid to the container can also be regulated in that, for example, a metal temperature measurement on the heat exchanger determines the flow of refrigerant into the container.
  • heat can be introduced at the warm end of the heat exchanger, for example by means of convective heat supply, heat supply by radiation or electro-thermal resistance heating. Details are explained below.
  • the cooling provided according to the invention at the cold end can in particular be matched to a heating power input at the head end. Adequate adjustment of the amount of heat supplied and removed results in a defined temperature gradient due to the longitudinal heat conduction in the metallic heat exchanger, which is determined by the conductive cross-sectional area, effective thermal conductivity and other geometry and process parameters.
  • the almost linear temperature gradient is adjusted so that the steady-state temperature levels of the metallic heat exchanger at the warm and cold ends are maintained during the system shutdown.
  • the coordination of the heating and cooling capacities with the equipment and process boundary conditions can take place in all embodiments of the invention, for example on the basis of the measurement of current and metal temperatures of the heat exchanger.
  • the method proposed according to the invention according to the first embodiment can have the advantage that the liquid supply of the The liquid used for cooling or keeping cold is the drainable The amount of heat is greater and refrigerant can be saved.
  • particularly targeted cooling can take place at the cold end of the heat exchanger.
  • the present invention proposes performing the method in first time periods in a first operating mode and in second time periods, which alternate with the first time periods, in a second operating mode.
  • the first time periods and the second time periods do not overlap within the scope of the present invention.
  • the first periods of time or the first operating mode carried out in a first period corresponds within the scope of the present invention to the production operation of a corresponding plant, i.e. in the case of an air separation plant that is the focus of the invention, to that operating mode in which liquid and / or gaseous air products flow through Air separation can be provided.
  • the second operating mode which is carried out in the second operating time periods, represents an operating mode in which corresponding products are not formed.
  • Corresponding second periods of time or a second operating mode are used in particular to save energy, for example in systems for liquefying and re-evaporation of air products for energy generation or in the previously mentioned LAES systems.
  • the heat exchanger is preferably not flowed through in the second operating mode or is flowed through to a significantly lesser extent than in the first operating mode.
  • the present invention does not fundamentally rule out that certain quantities of gases are also passed through a corresponding heat exchanger in the second operating mode.
  • the amount of fluids passed through the heat exchanger in the second operating mode is always well below the amounts of fluids that are passed through the heat exchanger in a regular first operating mode.
  • the amount of fluids passed through the heat exchanger in the second operating mode is, in the context of the present invention, for example, no more than 20%, 10%, 5%, or 1% or 0.1%, based on that in the first operating mode through the heat exchanger amount of fluid carried.
  • the first operating mode and the second operating mode alternate in the respective time periods carried out, ie on a respective first period in which the first operating mode is carried out, there always follows a second period in which the second operating mode is carried out and the second period or the second operating mode is followed by a first period of time with the first operating mode, etc.
  • this does not rule out that further time periods with further operating modes can be provided between the respective first and second time periods, for example a third period with a third operating mode.
  • a third operating mode the following sequence results in particular: first operating mode - second operating mode - third operating mode - first operating mode, etc.
  • a first fluid flow is formed at a first temperature level, fed into the heat exchanger in a first area at the first temperature level, and partially or completely cooled in the heat exchanger.
  • a gas mixture to be broken down by a gas mixture decomposition method for example by air, which is decomposed in an air separation plant, can be used as a corresponding first fluid flow.
  • a second fluid flow is formed at a second temperature level, fed into the heat exchanger in a second region at the second temperature level and partially or completely heated in the heat exchanger.
  • the formation of the second fluid flow can in particular represent the formation of a return flow in an air separation plant in the form of an air product or a waste flow.
  • the second temperature level corresponds in particular to the temperature at which a corresponding return flow is formed in one. It is preferably at cryogenic temperatures, in particular from -50 ° C. to -200 ° C., for example from -100 ° C. to -200 ° C. or from -150 ° C. to -200 ° C.
  • the first temperature level is at the first fluid stream is formed and fed to the heat exchanger in the first region, preferably at bypass temperature, but in any case typically at a temperature level well above 0 ° C, for example from 10 ° C to 50 ° C.
  • first or second fluid flow is formed at the first or second temperature level
  • further fluid flows are formed at the first or second temperature level.
  • Corresponding further fluid flows can have the same or different composition as or than the fluid of the first or second fluid flow.
  • a total flow can initially be formed from which the second fluid flow is formed by branching off.
  • fluid flows can optionally also be formed and then combined with one another and used in this way to form the second fluid flow.
  • a fluid flow in the heat exchanger is "partially or completely" cooled or heated, this is understood to mean that either the entire fluid flow is passed through the heat exchanger, either from a warm end or an intermediate temperature level to the cold one End or an intermediate temperature level or vice versa, or that the corresponding fluid flow in the heat exchanger is divided into two or more partial flows which are taken from the heat exchanger at the same or different temperature levels.
  • a corresponding fluid flow is fed into the heat exchanger, specifically at the first or second temperature level, and this is cooled or heated in the heat exchanger (alone or together with other flows as explained above).
  • first and second fluid streams can also be cooled or heated in the heat exchanger, namely to the same or different temperature levels and / or starting from the same or different temperature levels as the first or second fluid stream .
  • Corresponding measures are customary and known in the field of air separation, so that reference can be made in this regard to the relevant specialist literature, as cited at the beginning.
  • the feeding of the first fluid flow and the second fluid flow into the heat exchanger and the respective cooling or heating in the heat exchanger are partially or completely suspended. For example, instead of the first fluid flow, which is passed through the heat exchanger in the first operating mode and is cooled in the heat exchanger, no fluid can be passed through the heat exchanger.
  • the heat exchanger passages of the heat exchanger which are used in the first operating mode to cool the first fluid flow, therefore remain impervious to flow in this case.
  • the first fluid flow which is passed through the heat exchanger and cooled in the first operating mode, to pass a different fluid flow through the heat exchanger, in particular in a significantly smaller amount.
  • the second fluid flow which can be replaced by another gas in the second operating mode, but without causing cooling at the cold end of the heat exchanger, i.e. the mentioned second area, within the scope of the present invention.
  • the second area is cooled in the second period.
  • first and second configurations for which important aspects have been explained above, are particularly advantageous here.
  • the first area is arranged at the warm end and the second area is arranged at the cold end of the heat exchanger, or the first area starts out from the warm end in the direction of the cold end of the heat exchanger and the second area starts out from the cold end End extends towards the warm end of the heat exchanger.
  • the passages are evaporation passages through which the flow in the second region of the heat exchanger (but not in the first region). It can be applied separately to the heat exchanger Passages, but also sections of passages that are used for regular heat exchange. These passages or sections can in particular run on or in a region of the heat exchanger which, starting from the second, cold end, extends a maximum of 50%, 40%, 30% or 20% in the direction of the first, warm end. As mentioned, however, these are not arranged on or in the first area, which comprises the terminal 30% of the heat exchanger at the warm end.
  • the second area is cooled by evaporating a liquid, which is used as the cooling fluid, in evaporation passages which are in thermal contact with the second area.
  • the liquid used here as mentioned in particular liquid nitrogen, is taken from a container, gas formed in the evaporation is (partially or completely) returned to the container, and the liquid is through a pressure built up by the evaporation of the gas in the container through the Pressed evaporation passages. In this way, natural circulation is established and the amount of refrigerant used is reduced.
  • the evaporation temperature and the cooling temperature can be set in particular by setting the pressure in the entire system, in particular using a pressure control and corresponding blowing off gas from the container. Because, within the scope of the first embodiment of the present invention, a liquid medium is made to evaporate for cooling, the amount of heat dissipated can be significantly increased compared to known methods in which a gas is used, with a reduced refrigerant requirement.
  • an amount in which the liquid is evaporated in the evaporation passages is advantageously set by feeding the liquid into the container, wherein the feeding of the liquid into the container can be regulated in particular by means of a temperature control. In this way, too, the temperature at which the second end of the heat exchanger is cooled can be adjusted accordingly.
  • a gaseous cooling fluid is used.
  • the passages used for cooling are each sections of heat exchanger passages which run in the heat exchanger between the first end and the second end, and which in particular in the first operating mode for normal heat exchange, in particular for the first and / or second fluid flow or further fluid flows, be used.
  • a section can in particular be formed by appropriate (intermediate) removal options, for example page headers.
  • the passages in which corresponding partial stretches are formed can in particular also comprise only a part, for example less than 50%, of the total number of passages.
  • the sections have a length of no more than 50%, 40%, 30% or 20%, for example 5 to 15%, of a total length of the heat exchanger passages, in particular between the first (warm) end and the second (cold) The End.
  • these are not arranged on or in the first area, which according to the invention comprises the terminal 30% of the heat exchanger at the warm end.
  • the second area or the cold end of the heat exchanger can be cooled in a targeted manner without causing (undesired) heat dissipation in the first area or in the warm end.
  • heat can be supplied to the first area in the second time period in that this heat is provided by means of a heat source and is transferred from outside the heat exchanger to the first area.
  • a corresponding heat source can be ambient heat, which by means of suitable measures, for example, can be introduced into a corresponding area of a coldbox or led to the first area of the heat exchanger.
  • the heat source can also be an active heating device, as will also be explained in more detail below.
  • this heat can be provided by means of the heat source and transferred to the first region via a gas space located outside the heat exchanger, or this heat can be via a heat exchanger contacting component, for example via metallic or non-metallic supports, suspensions or fastenings, are fed to the heat exchanger block.
  • electrical heating tapes with solid contact can also be used.
  • the heat transfer takes place in the configuration in which the heat is transferred via the gas space, predominantly or exclusively without solid body contact, ie predominantly or exclusively in the form of heat transfer in the gas space, ie without or predominantly without heat transfer by solid heat conduction.
  • the term "predominantly” here denotes a proportion of the amount of heat of less than 20% or less than 10%. In the case of the use of other heating devices such as electrical heating strips, these ratios naturally differ accordingly.
  • the present invention therefore provides for active heating of the warm end of a corresponding heat exchanger to be carried out in the second period of time or for passive heating to be permitted via heat conduction.
  • the term “outside of the heat exchanger” distinguishes the present invention from alternatively likewise possible heating by means of a targeted fluid flow through the heat exchanger passages. In this embodiment, the heating does not take place by transferring heat from a fluid guided through the heat exchanger passages.
  • the heat can be transferred to the heat exchanger from outside the heat exchanger passages by means of the heat source by solid-state heat conduction via a heat conducting element contacting the first region.
  • a heat conducting element contacting the first region.
  • This can be done, for example, as already mentioned, via supports or metallic or non-metallic elements as heat conducting elements which contact the heat exchanger and which in turn are heated, for example, by means of a resistive or inductive heater.
  • a corresponding arrangement can basically be designed as proposed in US Pat. No. 5,233,839 A.
  • the heat provided by the heat source can also be transferred to the first area via a gas space located outside the heat exchanger, as explained, namely at least partially convectively and / or at least partially radiatively, i.e. by thermal radiation.
  • the present invention in the embodiment in which heat is transferred from the heating device via the gas space located outside the heat exchanger to the first area, the particular advantage that, for example, in contrast to the aforementioned US Pat. No. 5,233,839 A, no suspension of a corresponding area is required, which is provided there for the transfer of heat.
  • the present invention thus allows temperature control in this embodiment even in cases in which a heat exchanger block is stored in other areas, for example at the bottom or in the middle, in order in this way to relieve the stresses on the lines that connect a corresponding heat exchanger to the environment reduce.
  • the method presented in the prior art on the other hand, can only be used if a corresponding heat exchanger block is suspended from the top.
  • Another disadvantage of the method described in the mentioned prior art compared to the mentioned embodiment of the invention is that heat is only introduced there to a limited extent at the supports and not over the entire surface of a heat exchanger in a corresponding area. This can, for example, lead to icing at the sheet metal jacket transitions of a corresponding heat exchanger.
  • the present invention in the mentioned embodiment enables an advantageous introduction of heat and in this way an effective temperature control without the disadvantages described above.
  • the heat is transmitted at least partially convectively and / or radiatively to the first region via the gas space.
  • gas turbulence can be induced for convective heat transfer so that heat build-up can be avoided.
  • pure radiant heating can act directly on the first area of the first heat exchanger via the corresponding infrared radiation.
  • the method of the present invention is particularly suitable for use in the context of a gas separation process, for example within the framework of a process for the low-temperature separation of air or natural gas, in which a correspondingly liquefied gas mixture is fed to a separation.
  • the first fluid stream is therefore advantageously at least partially fed to a rectification after the partial or complete cooling in the heat exchanger.
  • the gas separation process provides for the first fluid flow to be at least partially liquefied and, in particular, to be broken down into fractions of different material compositions. Certain changes, albeit slight changes compared to decomposition, can also result from the liquefaction itself due to the different condensation temperatures.
  • the present invention extends to an arrangement with a heat exchanger, the arrangement having means which are configured to carry out a first operating mode in first periods of time and to carry out a second operating mode in second periods of time which alternate with the first periods of time, in which first operating mode to form a first fluid flow at a first temperature level, to feed it into the heat exchanger in a first region at the first temperature level, and to cool partially or completely in the heat exchanger, in the first operating mode furthermore to form a second fluid flow at a second temperature level, in feed a second region at the second temperature level into the heat exchanger, and partially or completely heat it in the heat exchanger, and partially or completely shut off the feeding of the first fluid flow and the second fluid flow into the heat exchanger in the second operating mode etting.
  • passages are provided in or on the heat exchanger in the second area, but not in the first area, which according to the invention comprises the terminal 30% at the warm end of the heat exchanger, and means are also provided which are set up for the second To cool the region in the second time period using cooling fluid which can be guided through the passages in or on the heat exchanger in the second region, but not in the first region.
  • the passages are used as evaporation passages through which the flow in the second area of the heat exchanger (but not in the first area), and a container is provided which can accommodate a cryogenic Liquid is set up as the cooling fluid.
  • Means are provided which are designed to remove the liquid from the container and to evaporate it in the evaporation passages, these means being arranged to return gas formed during the evaporation into the container, and the liquid by means of a pressure built up by the evaporation of the gas in the container through the evaporation passages.
  • the evaporation passages are provided in particular separately from passages formed inside the heat exchanger on an outside of the heat exchanger.
  • the passages are each partial sections of heat exchanger passages that run in the heat exchanger, in particular between the first (warm) end and the second (cold) end, the partial sections having a length of no more than 50% or 40%, in particular not more than 30% or 20% and in particular more than 5% or 10%, of a total length of the heat exchanger passages, in particular between the first (warm) end and the second (cold) end, and wherein the cooling fluid can be provided in gaseous form and through the sections the heat exchanger passages can be guided.
  • the sections mentioned are not formed in the first area, which includes the terminal 30% of the heat exchanger at the warm end.
  • a heat source in particular a heating device, is also provided, which is set up to supply heat to the first area in the second period by providing the heat by means of the heat source and transferring it from outside the heat exchanger to the first area.
  • the heat exchanger is advantageously arranged in a coldbox, a gas space through which the heat can be transferred being formed by an area within the coldbox that is free of insulating material.
  • the first area of the heat exchanger can be arranged in the gas space within the coldbox in particular without suspensions contacting the first area.
  • the heat source can in particular be designed as a heating device in the form of a radiant heater, which can be heated electrically or using heating gas, for example.
  • the heating device can, however, also be designed, in particular, as a resistive or convective heating device which heats up a heat-conducting element contacting the first region of the heat exchanger.
  • the present invention also extends to a plant, which is characterized in that it has an arrangement as it has been explained above.
  • the system can in particular be designed as a gas mixture separation system. It is also distinguished in particular by the fact that it is set up to carry out a method, as was previously explained in embodiments.
  • the invention is explained in more detail below with reference to the accompanying drawings, which show an embodiment of the invention and corresponding heat exchange diagrams.
  • Figure 1 illustrates temperature profiles in a heat exchanger after shutdown without the use of measures according to an embodiment of the present invention.
  • Figure 2 illustrates an arrangement with a heat exchanger according to a particularly preferred embodiment of the invention.
  • FIG. 3 illustrates an arrangement with a heat exchanger according to a further particularly preferred embodiment of the invention.
  • FIG. 4 illustrates an air separation plant which can be equipped with an arrangement according to an embodiment of the invention.
  • FIG. 1 illustrates temperature profiles in a heat exchanger after shutdown (through which there is no flow) without the use of measures according to advantageous embodiments of the present invention in the form of a temperature diagram.
  • a temperature labeled F1 at the warm end of a corresponding heat exchanger and a temperature labeled C at the cold end are shown in ° C on the ordinate versus a time in hours on the abscissa.
  • the temperature H at the warm end of the heat exchanger at the start of shutdown which still corresponds to the temperature in regular operation of the heat exchanger, is approx. 20 ° C and the temperature C at the cold end is approx. -175 ° C . Over time, these temperatures increasingly converge.
  • the high thermal conductivity of the materials built into the heat exchanger is responsible for this. In other words, here heat flows from the warm end towards the cold end. Together with the heat input from the environment, this results in an average temperature of approx. -90 ° C.
  • the significant increase in temperature at the cold end is largely due to the internal temperature equalization in the heat exchanger and only to a lesser extent due to external heat input.
  • thermal stresses can arise in the case shown if the warm end of the heat exchanger is exposed to a warm fluid of approx. 20 ° C. in the example shown after regeneration for some time without further measures.
  • thermal stresses can also arise if a system downstream of the heat exchanger immediately supplies cryogenic fluids again, for example cryogenic liquids from a rectification column system of an air separation system.
  • the present invention relates to plants in which the latter problem occurs less or not at all.
  • FIG. 2 an arrangement with a heat exchanger according to a particularly preferred embodiment of the present invention is illustrated and denoted as a whole by 10.
  • the configuration according to FIG. 2 essentially corresponds to the previously explained first configuration.
  • the heat exchanger is provided with the reference number 1. It has a first area 11 and a second area 12, which here are not structurally differentiated from the rest of the heat exchanger 1.
  • the first area 11 and the second area 12 are characterized in particular by the feeding in and removal of fluid flows.
  • two fluid flows A and B are passed through the heat exchanger 1, with the fluid flow A previously being the first fluid flow and the fluid flow B previously referred to as the second fluid stream.
  • the first fluid flow A is cooled in the heat exchanger 1, whereas the second fluid flow B is heated.
  • the routing of the fluid flows A and B through the heat exchanger typically takes place only during normal operation, that is to say during the first time period or operating mode explained above.
  • the cooling explained below takes place in a second period or operating mode.
  • the heat exchanger is not flowed through by the corresponding fluid flows A and B, or not to the same extent as in the first operating mode.
  • the second operating mode other than the fluid flows A and B or the fluid flows A and B can be used in a smaller amount.
  • the heat exchanger 1 can be accommodated in the arrangement 10 in a cold box (not shown), which can in particular be partially filled with an insulating material, for example perlite.
  • a heating device 3 is provided in the arrangement 10, which heats the first region 11 of the heat exchanger 1 during certain periods of time in the second operating mode or during the entire second operating mode.
  • heat F1 illustrated here in the form of a plurality of arrows
  • the transfer of the heat via the gas space G is illustrated here, this can in principle also take place via a, for example, metallic heat-conducting element, if the heating device 3 is designed accordingly.
  • the second region 12 of the heat exchanger is cooled in accordance with the embodiment of the invention illustrated here, or heat is actively dissipated from it, as explained below.
  • the second region 12 of the heat exchanger 1 is converted into by an evaporation of a liquid Evaporation passages 13, which are in thermal contact with the second region 12, are cooled.
  • the liquid is withdrawn from a container 2, and the gas formed during the evaporation is partially or completely returned to the container 2.
  • the liquid is forced through the evaporation passages 13 by a pressure of the gas in the container 2 that has built up as a result of the evaporation. So there is a natural cycle.
  • an amount in which the liquid is evaporated in the evaporation passages 13 is set by feeding the liquid into the container 2 via a feed line F.
  • the feeding of the liquid into the container 2 is regulated by means of a temperature control TC on the basis of a value recorded by means of a temperature transmitter TI.
  • the pressure built up in the container 2 by the evaporation of the gas is set by blowing gas out of the container 2, for which purpose a pressure control PC with a pressure transducer is used here. This acts on a valve in an off-gas line O, which is not specifically designated.
  • the evaporation temperature and thus the cooling temperature are also set by means of a corresponding pressure setting.
  • FIG. 3 an arrangement with a heat exchanger according to a particularly preferred embodiment of the present invention is illustrated.
  • the configuration according to FIG. 3 essentially corresponds to the previously explained second configuration.
  • the heat exchanger is again provided with the reference number 1. It has a first area 11 and a second area 12. Reference is made to the explanations relating to FIG. 2 for further details.
  • two fluid flows A and B are passed through the heat exchanger 1, the fluid flow A previously being referred to as the first fluid flow and the fluid flow B being previously referred to as the second fluid flow.
  • the first fluid flow A is cooled in the heat exchanger 1, whereas the second fluid flow B is heated.
  • the routing of the fluid flows A and B through the heat exchanger typically takes place only during normal operation, that is to say during the first time period or operating mode explained above.
  • the cooling explained below takes place in a second period or operating mode.
  • heat exchanger 1 In the heat exchanger 1, only indicated heat exchanger passages 14 run between the first end 11 and the second end 12.
  • the passages each have sections 14 'which are no more than 20% of a total length of the heat exchanger passages 14 between the first end 11 and the second end 12.
  • a cooling fluid C is provided in gaseous form and passed through the sections 14 ′ of the heat exchanger passages 14.
  • FIG. 4 illustrates an air separation plant with an arrangement with a heat exchanger, which can be operated using a method according to an advantageous embodiment of the present invention.
  • Air separation plants of the type shown are, as mentioned, often described elsewhere, for example at H.-W. Häring (Ed.), Industrial Gases Processing, Wiley-VCH, 2006, in particular Section 2.2.5, "Cryogenic Rectification".
  • An air separation plant for using the present invention can be designed in the most varied of ways. The use of the present invention is not restricted to the embodiment according to FIG.
  • the air separation plant shown in FIG. 4 is denoted by 100 as a whole. It has, among other things, a main air compressor 101, a pre-cooling device 102, a cleaning system 103, a post-compressor arrangement 104, a main heat exchanger 105, which can represent the heat exchanger 1 as explained above and in particular is part of a corresponding arrangement 10, an expansion turbine 106, a throttle device 107 , a pump 108 and a distillation column system 110.
  • the distillation column system 110 comprises a classic double column arrangement comprising a high pressure column 111 and a low pressure column 112 as well as a crude argon column 113 and a pure argon column 114.
  • a feed air flow is sucked in and compressed by means of the main air compressor 101 via a filter (not designated).
  • the compressed feed air stream is fed to the pre-cooling device 102 operated with cooling water.
  • the pre-cooled feed air stream is purified in the cleaning system 103.
  • the cleaning system 103 which typically comprises a pair of adsorber containers used in alternating operation, the precooled feed air stream is largely freed of water and carbon dioxide.
  • the feed air flow Downstream of the cleaning system 103, the feed air flow is divided into two partial flows. One of the partial flows is completely cooled down to the pressure level of the feed air flow in the main heat exchanger 105. The other partial flow is recompressed in the booster arrangement 104 and also cooled in the main heat exchanger 105, but only to an intermediate temperature level. After cooling to the intermediate temperature level, this so-called turbine stream is expanded to the pressure level of the completely cooled partial stream by means of the expansion turbine 106, combined with it and fed into the high-pressure column 111.
  • An oxygen-enriched liquid bottom fraction and a nitrogen-enriched gaseous top fraction are formed in the high-pressure column 111.
  • the oxygen-enriched liquid bottom fraction is withdrawn from the high pressure column 111, partly used as a heating medium in a bottom evaporator of the pure argon column 114 and fed in defined proportions into a top condenser of the pure argon column 114, a top condenser of the crude argon column 113 and the low pressure column 112. Fluid evaporating in the evaporation chambers of the top condensers of the crude argon column 113 and the pure argon column 114 is likewise transferred to the low-pressure column 112.
  • the gaseous nitrogen-rich top product g is withdrawn from the top of the high-pressure column 111, liquefied in a main condenser, which creates a heat-exchanging connection between the high-pressure column 111 and the low-pressure column 112, and fed in portions as a return to the high-pressure column 111 and expanded into the low-pressure column 112.
  • An oxygen-rich liquid bottom fraction and a nitrogen-rich gaseous top fraction are formed in the low-pressure column 112.
  • the former is partially pressurized in liquid form in the pump 108, heated in the main heat exchanger 105, and made available as a product.
  • a liquid nitrogen-rich stream is withdrawn from a liquid retention device at the top of the low-pressure column 112 and discharged from the air separation plant 100 as a liquid nitrogen product.
  • a gaseous nitrogen-rich stream withdrawn from the top of the low-pressure column 112 is passed through the main heat exchanger 105 and provided as a nitrogen product at the pressure of the low-pressure column 112. From the low-pressure column 112, a stream is also withdrawn from an upper region and, after heating, in the
  • Main heat exchanger 105 is used as what is known as impure nitrogen in the pre-cooling device 102 or, after heating by means of an electric heater, in the cleaning system 103.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Abstract

L'invention concerne un procédé de fonctionnement d'un échangeur de chaleur (1), dans laquelle un premier mode de fonctionnement est réalisé dans des premières périodes de temps, et un second mode de fonctionnement est réalisé dans des secondes périodes de temps qui alternent avec les premières périodes de temps; dans le premier mode de fonctionnement, un premier écoulement de fluide (A) est formé à un premier niveau de température, est introduit dans l'échangeur de chaleur (1) dans une première région (2) au premier niveau de température, et est partiellement ou totalement refroidi dans l'échangeur de chaleur (1); dans le premier mode de fonctionnement, un second écoulement de fluide (B) est formé à un second niveau de température, est introduit dans l'échangeur de chaleur (1) dans une seconde région (3) au niveau du deuxième niveau de température, et est partiellement ou totalement chauffé dans l'échangeur de chaleur (1); et dans le second mode de fonctionnement, l'alimentation du premier écoulement de fluide (A) et du second écoulement de fluide (B) dans l'échangeur de chaleur (1) est partiellement ou complètement arrêtée. Dans la seconde période de temps, la seconde région (12) est refroidi à l'aide d'un fluide de refroidissement qui est conduit à travers des passages dans ou sur l'échangeur de chaleur (1) dans la deuxième région (12) mais pas dans la première région (11) qui comprend la borne 30% à l'extrémité chaude de l'échangeur de chaleur (1). Un agencement correspondant (10) et un système (100) avec un tel agencement (10) sont également couverts par la présente invention.
EP20767968.9A 2019-08-23 2020-08-18 Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant Pending EP4018143A1 (fr)

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PCT/EP2020/025378 WO2021037391A1 (fr) 2019-08-23 2020-08-18 Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant

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CN113646601B (zh) * 2019-04-05 2023-11-03 林德有限责任公司 用于操作热交换器的方法、具有热交换器的排布结构以及具有对应排布结构的系统
CN113670003B (zh) * 2021-07-29 2022-08-09 北京科技大学 高安全性的储能、发电和物质回收外压缩空分工艺流程
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US5233839A (en) 1991-03-13 1993-08-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for operating a heat exchanger
JP4688843B2 (ja) * 2007-05-07 2011-05-25 株式会社神戸製鋼所 空気分離装置
US9851141B2 (en) * 2009-07-02 2017-12-26 Bluewater Energy Services B.V. Pressure control of gas liquefaction system after shutdown
US9810103B2 (en) 2012-08-02 2017-11-07 Linde Aktiengesellschaft Method and device for generating electrical energy
CN102778105B (zh) 2012-08-06 2015-02-18 济南鲍德气体有限公司 一种制氧机快速启动装置及方法
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EP3032203A1 (fr) 2014-12-09 2016-06-15 Linde Aktiengesellschaft Procédé et installation combinée destinés à stocker et à récupérer l'énergie
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US20220316811A1 (en) 2022-10-06

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