DE2307004A1 - Liquefied nitrogen - with liquefied natural gas as refrigerant - Google Patents

Liquefied nitrogen - with liquefied natural gas as refrigerant

Info

Publication number
DE2307004A1
DE2307004A1 DE19732307004 DE2307004A DE2307004A1 DE 2307004 A1 DE2307004 A1 DE 2307004A1 DE 19732307004 DE19732307004 DE 19732307004 DE 2307004 A DE2307004 A DE 2307004A DE 2307004 A1 DE2307004 A1 DE 2307004A1
Authority
DE
Germany
Prior art keywords
nitrogen
natural gas
liquid
air separation
plant
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
DE19732307004
Other languages
German (de)
Inventor
Guenther Dipl Ing Rueckborn
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 DE19732307004 priority Critical patent/DE2307004A1/en
Publication of DE2307004A1 publication Critical patent/DE2307004A1/en
Pending legal-status Critical Current

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Classifications

    • 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
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—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
    • F25J1/0221—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 using the cold stored in an external cryogenic component in an open refrigeration loop
    • F25J1/0224—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 using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
    • 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
    • F25J3/0406—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 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—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
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/044—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 single pressure main column system only
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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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
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    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
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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
    • 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
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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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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
    • 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
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead 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
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • 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
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Liquid N2 is obtained by low-temp. rectification of air, using liquefied natural gas as the evaporating refrigerant for the liquefaction of the gaseous N2 obtained in >=2 cooperating air fractionators connected to a nautral gas evaporation plant. The cold from the natural gas is transmitted before liquefaction of the N2, solely to one air fractionation plant.

Description

Verfahren un Vorrichtung zur Gewinnung von flüssigem Stickstoff Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur Gewinnung von flüssigem Stickstoff durch Tieftemperaturrektifikation von Luft unter Verwendung von flüssigem Erdgas als verdampfendem Kältemittel für die Verflüssigung des bei der Tieftemperaturrektifikation gasförmig erzeugten Stickstoffs. Method and device for the production of liquid nitrogen The invention relates to a method and a device for extracting liquid Nitrogen by cryogenic rectification of air using liquid Natural gas as an evaporating refrigerant for the liquefaction of the cryogenic rectification nitrogen generated in gaseous form.

aus der US-PS 7 183 677 ist bereits ein Vcrraliren zur Erzeugung von flüssigem Stickstoff durch Kombination einer Luftzerlegungsanlage und einer Erdgasverdampfungsanlage bekannt. from US-PS 7,183,677 is already a Vcrraliren for generation of liquid nitrogen by combining an air separation unit and a Natural gas evaporation plant known.

Hierbei wird am Kopf eines Einsäulenrektifikators, in den durch Zerlegungsprodukte und f@üssiges Erdgas abgekühlte Luft eingespeist wlrd, gasförmiger Stickstoff abgezogen, komprimiert und genen verdampfendes Erdgas abgekühlt. Ein Teil wird im Sumpf der Säule verflüssigt und dieser als Rücklauf aufgeOeben, während ein zweiter Teil höher komprimiert und gegen verdampfendes Erdgas kondensiert wird.This is done at the top of a single-column rectifier, in which the decomposition products and liquid natural gas, cooled air is fed in wlrd, more gaseous Nitrogen is drawn off, compressed and cooled down by evaporating natural gas. A Part is liquefied in the bottom of the column and this is given up as reflux while a second part is compressed higher and condensed against evaporating natural gas.

Sollen auf diese Weise, also unter Ausnutzung der im flüssigen Erdgas gebundenen Kälte, sehr große Mengen Stickstoff verflüssigt werden, dann steigt der apparative Aufwand, insbesondere die Größe der einzelnen Bauteile erheblich an, so daß es sinnvoll ist, neben gasförmigem Stickstoff auch noch gasförmigen Sauerstoff, wie aus dem bekannten Verfahren auch hervorgeht, zu erzeugen und an naheliegende Sauerstoffverbraucher zu verkaufen. Should in this way, that is, taking advantage of the liquid natural gas Bound cold, very large amounts of nitrogen are liquefied, then the increases equipment expenditure, in particular the size of the individual components, increases considerably, so that it makes sense to use gaseous oxygen as well as gaseous nitrogen, as can also be seen from the known method, to generate and to the obvious Sell oxygen consumers.

Die Größe der hierzu benötigten Luftzerlegungsanlagen aber bereitet vor allem bei der Lieferung oft unüberwindliche Schwierigkeiten, da die zulässigen Transportmaße, z.B. bei Rektiflzierkolonnen häufig überschritten werden.However, the size of the air separation plants required for this is sufficient especially with the delivery often insurmountable difficulties, since the permissible Transport dimensions, e.g. for rectifying columns, are often exceeded.

Der Erfindung liegt daher die Aufgabe zugrunde, ein Verftren der beschriebenen Art zu entwickeln, das selbst bei der Erzeugung großer Mengen flüssigen Stickstoffs nur Apparate durchschnittlicher Größe erfordert. The invention is therefore based on the object of a Verftren to develop the type described, even when producing large quantities of liquid Nitrogen only requires apparatus of average size.

Diese Aufgabe wird erfindungsgemäß dadurch gelöst, daß die Erzeugung des gasförmigen StiOkstOffs auf mindestens zwei im Verbund arbeitenae Luftzerlegungsanlagen, die mit einer Erdgasverdampfungsanlage in Verbindung stehen, aufgeteilt wird und daß die Übertragung der Kälte des flüssigen Erdgases vor der Verflüssigung des Stickstoffs lediglich auf eine ijuftzerlegungsanlaoe erfolgt. This object is achieved according to the invention in that the generation the gaseous nitrogen on at least two air separation plants working in a network, which are connected to a natural gas evaporation plant, is divided and that the transfer of the cold of the liquid natural gas before the liquefaction of the nitrogen only takes place on an air decomposition facility.

Dadurch ergibt sich eine wesentliche Verbilligung des gesamten Verfahrens, da eine Aufteilung der Gesamtstickstoffproduktion und somit der Gesamtluftmenge auf mehrere kleinere Einheiten sich kostensenkend, vor allem hinsichtlich des Transports auswirkt. Darüber hinaus wird ein günstiges Umwandlungsverhältnis, das sind die pro Gewichtsteil flüssiges Erdgas erzeugten Gewichtsteile Flüss-gstickstoff, erreicht. This results in a significant reduction in the cost of the entire procedure, there is a division of the total nitrogen production and thus the total amount of air on several smaller units, reducing costs, especially with regard to transport affects. In addition, a favorable conversion ratio, these are the parts by weight of liquid nitrogen produced per part by weight of liquid natural gas.

Besondere Vorteile ergeben sich bei einer Weiterbildung des Erfindungsgedankens, die darin besteht, daß in einer ersten Luftzerlegungsanlage in einer ersten Rektifiziersäule eine flüssige Stickstofffraktion erzeugt und einer zweiten, unter höherem Druck als die erste Rektifiziersäule arbeitenden Rektifiziersäule als Waschflüssigkeit aufgegeben wird. Diese Maßnahme hat einerseits eine Aufteilung der Zerlegungsluft auf zwei Rektifiziersäulen zur Folge, was s-ch bei Großanlagen günstig auf deren Abmessungen auswirkt, und führt andererseits zu einer Ern--edrigung der Gesamtluftmenge, da die Erzeugung der Rücklaufflüssigkeit bei geringem Druck, also bei günstigen Rektifikationsbedingungen erfolgt. Particular advantages result from a further development of the concept of the invention, which consists in that in a first air separation plant in a first rectification column a liquid nitrogen fraction is generated and a second, under higher pressure as the first rectifying column working as the washing liquid is abandoned. This measure has, on the one hand, a division of the separation air on two rectifying columns, which is beneficial for large systems Dimensions, and on the other hand leads to a reduction in the total air volume, because the generation of the return liquid at low pressure, so at favorable Rectification conditions takes place.

Da es weiterhin wünschenswert ist, neben Stickstoff auch Sauerstoff zu gewinnen, muß die gesamte eintretende Zerlegungsluft von ihren Verunreinigungen, wie Wasser und Kohlendioxid, befreit werden, wozu, soll eine möglichst große Sauerstoffmenge gewonnen werden, eine kostspielige Adsorption notwendig ist. Aufgrund dessen ist der Anmeldungsgegenstand zweckmäßigerweise derart weitergebildet, daß ein in einer ersten Luftzerlegungsanlage neben gasförmigem Stickstoff anfallendes Restgas einer zweiten Luftzerlegungsanlage zur weiteren Zerlegung zugefahrt wird. Dies hat den VorteS1, daß nur ein Teil der insgesamt in das Verfahren eingebrachten Gasmenge, nämlich das Restgas, das stark mit Sauerstoff angereichert ist und die in den selbstreinigenden Wärmetauschern der ersten Luftzerlegungsanlage abgelagerten Verunreinigungen enthalt, adsorptiv gereinigt werden muß. Die Hauptmenge des gasförmigen Stickstoffs wird daher in der ersten Luftzerlegungsanlage, die ausschließlich mit selbstreinigenden Wärmetauschern ausgestattet ist, hergestellt. Since it is still desirable to have oxygen as well as nitrogen to win must all the air entering of theirs Impurities such as water and carbon dioxide are to be freed, for which purpose, one should if possible large amount of oxygen can be obtained, an expensive adsorption is necessary. Because of this, the subject of the application is expediently developed in such a way that that an accumulating in a first air separation plant in addition to gaseous nitrogen Residual gas is fed to a second air separation plant for further separation. This has the advantage that only a part of the total brought into the process Amount of gas, namely the residual gas that is heavily enriched with oxygen and the deposited in the self-cleaning heat exchangers of the first air separation plant Contains impurities, must be cleaned by adsorption. The bulk of the gaseous Nitrogen is therefore used exclusively in the first air separation plant self-cleaning heat exchangers.

Eine besonders günstige Ausführungsform des Anmeldungsgegenstandes besteht weiterhin darin, daß die wärmemäßige Verknüpfung zwischen den Luftzerlegungsanlagen einerseits und der Stickstoffverflüssigung andererseits über im Kreislauf geführten gasförmigen Stickstoff aus der Hochdrucksäule einer zweiten iuftzerlegungsanlage erfolgt. Dadurch wird in der Drucksäule ein erhöhter Nengenumsatz erzielt, der es ermöglicht, sowohl am Kopf der Drucksäule große Mengen an Produktstlckstoff abzuziehen, als auch aus der Mitte eine nennenswerte Waschflüssigkeitsmenge für die Niederdrucksäule zu entnehmen. Mit dieser Waschflüssigkeit gelingt es, die im Sumpf der Drucksäule anfallende sauerstoffreiche Flüssigkeit in der Niederdrucksäule in drei Fraktionen zu zerlegen, nämlich in reinen Sauerstoff, 90 %igen Sauerstoff und in eine Restgasfraktion, die zum Regenerieren der Adsorber ausreicht. A particularly favorable embodiment of the subject of the application is also that the thermal link between the air separation units on the one hand and nitrogen liquefaction on the other hand via circulating gaseous nitrogen from the high pressure column of a second air separation plant he follows. As a result, an increased volume turnover is achieved in the pressure column, which it enables large amounts of product solids to be withdrawn from the top of the pressure column, as well as a significant amount of washing liquid from the middle for to take the low pressure column. With this washing liquid it succeeds in the Bottom of the pressure column, oxygen-rich liquid accumulating in the low-pressure column to be broken down into three fractions, namely into pure oxygen, 90% oxygen and into a residual gas fraction that is sufficient to regenerate the adsorber.

Die sich durch die Kreislaufführung des Stickstoffs ergebenden Vorteile lassen sich noch dadurch ergänzen, daß als wärmeübertragende Medien zwischen dem Kreislaufstickstoff und dem flüssigen Erdgas ausschließlich Stickstofffraktionen verwendet werden. Dadurch wird verhindert, daß im Falle eines Rohrbruches Erdgas mit Sauerstoff aus den Luftzerlegungsanlagen in Berührung kommt, was zu einer Explosion führen könnte. The advantages resulting from the circulation of nitrogen can be supplemented by the fact that as heat transfer media between the Cycle nitrogen and the liquid natural gas only nitrogen fractions be used. This prevents natural gas from being released in the event of a pipe burst comes into contact with oxygen from the air separation units, causing an explosion could lead.

Eine weitere kostensenkende Variante des erfindungsgemäßen Verfahrens besteht darin,daß das zur Verf lüssigung des gesförmig erzeugten Stickstoffs verwendete flüssige Erdgas im flüssigen Zustand auf seinen Abgabedruck verdichtet wird. Damit entfallen die Erdgaskompressoren, allerdings sind andere Investitionen, be-spielsweise eine Entspannungsturbine, DUr einen zu sätzlichen Stickstoffkreislauf notwendig. Doch hat diese zusätzliche Einrichtung den großen Vorteii, daß auch ohne flüssiges Erdgas ein Flüssigstickstoffvorrat gebildet werden kann. Another cost-reducing variant of the method according to the invention consists in the fact that the nitrogen used to liquefy the gaseous produced liquid natural gas is compressed in the liquid state to its delivery pressure. In order to the natural gas compressors are no longer necessary, but other investments are required, for example an expansion turbine, which requires an additional nitrogen cycle. But this additional device has the great advantage that even without liquid Natural gas a liquid nitrogen supply can be formed.

Eine Vorrichtung zur Durchführung des Verfahrens weist zwei über eine Rohrleitung in Verbindung stehende uftzerlegungsanlagen und eine an diese angeschlossene Erdgasverdampfungsanlage auf. Vorteilhafterweise ist diese Vorrichtung derart weitergebildet, daß die Erdgasverdampfungsanlage über einen Wärmetauscher mit einer Luftzerlegungsanlage in Verbindung steht. An apparatus for performing the method has two a pipeline connected air separation plants and a natural gas evaporation system connected to this. Is advantageous this device developed in such a way that the natural gas evaporation system via a Heat exchanger is connected to an air separation plant.

Dadurch ist es möglich, die Kälteenergie optimal auf die Erzeugung des gasfdrmigen-Stickstoffs einerseits und auf die Verflüssigung des gasfdrmigen Stickstoffs andererseits aufzuteilen.This makes it possible to optimally generate the cooling energy the gaseous nitrogen on the one hand and the liquefaction of the gaseous nitrogen On the other hand to divide nitrogen.

äußerst zweckmäßig ist es weiterhin, die Vorrichtung zur Durchführung des Verfahrens in der Weise auszubilden, daß die Erdgasverdampfungsanlage eine Flüssigpumpe aufweist, da dadurch die aufwendigen Erdgaskompressoren entfallen. It is also extremely useful to implement the device of the method in such a way that the natural gas evaporation system is a liquid pump since this eliminates the need for complex natural gas compressors.

Weitere Einzelheiten der Erfindung werden anhand des in der Figur schematisch dargestellten Ausführungsbeispieles näher erläutert. Further details of the invention are based on the in the figure schematically illustrated embodiment explained in more detail.

Die Figur zeigt ein Verfahren zur Erzeugung von flUssigem Stickstoff unter Verwendung zweier Luftzerlegungsanlagen und einer Erdgasverdampfungsanlage. Über eine Leitung 1 und einen Verdichter 2, wo sie auf ca. 5 ata komprimiert wird, gelang gen 100 000 Nm3/h Zerlegungsluft in umschaltbare Wärmetauscher 3 und 4, werden hier gegen Zerlegungsprodukte abgekühlt und in drei Ströme aufgeteilt. Der erste Strom wird in einem Strömungsquerschnitt 5 des Wärmetauschers 4 wieder etwas angewärmt, mit dem zweiten Strom in Leitung 6 vereinigt, mit diesem zusammen in einer Entspannungsturbine 7 auf ca. 3D6 ata entspannt und am Fuß einer Rektifiziersäule Q eingespeist Infolge des relativ hohen Druckes der Zerlegungsluft vor der Entspannungsturbine 7 kann einerseits mit einem kleineren Durchsatz, d.h. mit einer kleineren Entspannungsturbine gearbeitet werden und andererseits, da innerhalb der Rektifiziersäule 8 ein extrem niedriger, genauer der für die Stickstofferzeugung geringst mögliche Druck von ca. 3,2 ata herrscht, die Rektifikation unter günstigsten Bedingungen durchgefillift werden. The figure shows a process for generating liquid nitrogen using two air separation plants and a natural gas evaporation plant. Via a line 1 and a compressor 2, where it is compressed to approx. 5 ata, succeeded in reaching 100,000 Nm3 / h of separation air in switchable heat exchangers 3 and 4 cooled here against decomposition products and divided into three streams. The first Current is warmed up again somewhat in a flow cross section 5 of the heat exchanger 4, combined with the second stream in line 6, with this together in an expansion turbine 7 relaxed to approx. 3D6 ata and fed in at the foot of a rectifying column Q. As a result the relatively high pressure of the decomposition air in front of the expansion turbine 7 can on the one hand with a smaller throughput, i.e. with a smaller expansion turbine be worked and on the other hand, since within the rectifying column 8 an extremely lower, more precisely the lowest possible pressure for nitrogen generation of approx. 3.2 ata prevails, rectification is carried out under the most favorable conditions will.

Aus der Rektifiziersäule 8 wird flüssiger Stickstoff über eine Leitung 9 entnommen und mit Hilfe einer Pumpe 10 in eine zweite, unter einem höherem Druck von ca. 4,8 ata arbeitende Rektifiziersäule 11, an deren Fuß die dritte Teilluftmenge über eine Leitung 12 eingeleitet wird, als Rücklaufflüssigkeit aufgegeben. Am Kopf der zweiten Rektifiziersäule 11 werden 50 000 Nm3/h gasförmiger Stickstoff mit einem Druck von ca. From the rectification column 8 is liquid nitrogen via a line 9 removed and with the help of a pump 10 in a second, under a higher pressure of approx. 4.8 ata working rectifying column 11, at the foot of which the third partial air volume is introduced via a line 12, abandoned as reflux liquid. On the head the second rectification column 11 are 50,000 Nm3 / h of gaseous nitrogen with a Pressure of approx.

4,8 ata über eine Leitung 13 abgezogen, in den Wärmetauschern 4 und 3 gegen eintretende Zeriegungsluft angewärmt und der Erdgasverdampfungsanlage zugeführt. Am Kopf der ersten Rektifiziersäule 8 werden 50 000 N2 je der in einem Kondensator 14 verdampften Restgasfraktion Uber eine Leitung 15 abgezogen, ebenfalls in den Wärmetauschern 4 und 3 gegen eintretende Zerlegungsluft angewärmt, wobei sie die in der vorhergehenden Periode abgelagerten Verunreinigungen, wie Wasser und C02, aufnimmt und mit einem Sauerstoffgehalt von ca. 41 % der zweiten Luftzerlegungsanlage zugeführt.4.8 ata withdrawn via a line 13, in the heat exchangers 4 and 3 warmed against incoming decomposition air and fed to the natural gas evaporation system. At the top of the first rectification column 8, 50,000 N2 are each in a condenser 14 evaporated residual gas fraction withdrawn via a line 15, also in the Heat exchangers 4 and 3 against incoming decomposition air, where they the impurities deposited in the previous period, such as water and C02, absorbs and with an oxygen content of approx. 41% of the second air separation plant fed.

Das Restgas wird in einem Verdichter 15 auf ca. The residual gas is reduced to approx.

7,4 ata komprimiert, in Molsiebadsorbern 17 von Wasser und Kohlendioxid befreit, in Wärmetauschern 18 und 19 gegen Zerlegungsprodukte auf Luftverflüssigungstemperatur abgekühlt und etwa in der Mitte einer Drucksäule 20 einer Doppelrektifiziersäule 21 eingespeist.7.4 ata compressed, in molecular sieve adsorbers 17 of water and carbon dioxide freed, in heat exchangers 18 and 19 against decomposition products at air liquefaction temperature cooled and approximately in the middle of a pressure column 20 of a double rectification column 21 fed in.

Am Kopf der Drucksäule 20 wird über eine Leitung 22 gasrörmiger Stickstoff abgezogen, in einem Verdichter 23 auf ca. 20 ata komprimiert, in einem Wärmetauscher 24 gegen Stickstoff aus der Erdgasverdampfungsanlage abgekühlt und nach Kondensation im Sumpf der Drucksäule 20 in diese als zusätzliche Rücklaufflüssigkeit entspannt. Sowohl Surnpffltlssigkeit aus der Drucksäule 20 als auch eine flüssige Fraktion aus deren Mitte werden über die Leitungen 25 bzw. 26 in eine Niederdrucksäule 27 entspannt und bilden dort die nötige Waschflüssigkeit. At the top of the pressure column 20, gaseous nitrogen is supplied via a line 22 withdrawn, compressed in a compressor 23 to approx. 20 ata, in a heat exchanger 24 cooled against nitrogen from the natural gas evaporation system and after condensation relaxed in the bottom of the pressure column 20 in this as an additional reflux liquid. Both liquid from the pressure column 20 and a liquid fraction from the center thereof, via the lines 25 and 26, respectively, into a low-pressure column 27 relaxes and form the necessary washing liquid there.

Infolge des relativ hohen Druckes in der Drucksäule 20 besitzt einerseits der Kreislaufstickstoff in Leitung 22 ein höheres Druckniveau, wodurch die Kompressionswärme bei einem höheren Temperaturniveau anfällt und somit günstiger abgegeben werden kann, während andererseits dadurch der Druck in der Niederdrucksäule 27 angehoben werden kann und somit die daraus über die Leitungen 28 und 29 abgezogenen Sauerstoffprodukte ebenfalls einen beachtlichen Uberdruck aufweisen. Uber die Leitung 28 werden 5000 Nm3/h gasförmiges Sauerstoffprodukt mit ca. As a result of the relatively high pressure in the pressure column 20 has on the one hand the circulating nitrogen in line 22 has a higher pressure level, whereby the compression heat occurs at a higher temperature level and can therefore be given off more cheaply can, while on the other hand thereby the pressure in the low-pressure column 27 is increased and thus the oxygen products withdrawn therefrom via lines 28 and 29 also have a considerable overpressure. Over the line 28 are 5000 Nm3 / h gaseous oxygen product with approx.

99,5 ß Sauerstoff, über Leitung 29 15 000 Nm3/h einer Fraktion mit ca. 90 ß 3auerstoef entnommen, in den Wärmetauschern 19 und 18 jeweils angewärmt und den Verbrauchern zugeführt. Am Kopf der Niederdrucksäule 27 werden über eine Leitung 30 5000 Nm3/h Restgas abgezogen, das zur Reinigung der Adsorber 17 dient.99.5 ß oxygen, via line 29 with 15,000 Nm3 / h of a fraction Approx. 90 ß 3auerstoef removed, warmed in each of the heat exchangers 19 and 18 and fed to consumers. At the top of the low pressure column 27 are about a Line 30 5,000 Nm3 / h of residual gas, which is used to clean the adsorber 17, is withdrawn.

Neben dem Kreislaufstickstoff werden am Kopf der Drucksäule 20 über eine Leitung 31 25 000 Nm3/h gasförmiger Produktstickstoff entnommen, teilweise im Wärmetauscher 19 angewärmt, in einer Entsp&nnungsturbine 32 auf ca. 4,8 ata entspannt, in den Wärmetauschern 19 und 18 angewärmt und über die Leitung 33 mit dem Produktstickstoff aus der ersten Luftzerlegungsanlage vereinigt, In der ersten Luftzerlegungsanlage werden somit 2/3, in der zweiten Luftzerlegungsanlage 1/3 des gesamten Froduktstickstof£s erzeugt. In addition to the circulatory nitrogen are at the top of the pressure column 20 over a line 31 25 000 Nm3 / h of gaseous product nitrogen removed, partially warmed in the heat exchanger 19, in an expansion turbine 32 to approx. 4.8 ata relaxed, warmed in the heat exchangers 19 and 18 and via line 33 with combined with the product nitrogen from the first air separation plant, in the first The air separation plant is 2/3, in the second air separation plant 1/3 of the total product nitrogen produced.

Dieser Produkt stickstoff wird zusammen mit Kreislaufstickstoff aus der Erdgasverdampfungsanlage, in Kompressoren 34 und 35 auf 11 bzw. 30 ata verdichtet, teilweise in einem Wärmetauscher 36 gegen verdampfendes Erdgas und teilweise gegen Kreislaufstickstoff im Wärmetauscher 37 abgekühlt, in einem weiteren Wärmetauscher J8 gegen verdampfendes Erdgas noch weiter abgekühlt und dann in zwei Ströme 39 mit 94 000 Nm3/h und 40 mit 182 000 Nm3/h aufgetrennt. Der Teilstrom-39 wird in einem Verdichter 41 auf ca. 71 ata verdichtet, in einem Wärmetauscher 42 gegen Kreislaufstickstoff Abgekühlt und in weitere drei Ströme 43, 44 und 45 aufgeteilt. Der Strom in Leitung 43 wird in einem Wärmetauscher 46 gegen entspannten, gasförmigen Stickstoff aus einem Abscheider 47 abgekühlt, mit dem in einem Wärmetauscher 48 gegen Kreislaufstickstoff abgekühlten Strom 44 und schließlich mit dem dritten, in einem Wärmetauseher 49 gegen flüssiges Erdgas gekühlten Strom 45 in Leitung 50 vereint. This product nitrogen is made up along with circulatory nitrogen the natural gas evaporation plant, compressed in compressors 34 and 35 to 11 or 30 ata, partly in a heat exchanger 36 against evaporating natural gas and partly against Circulation nitrogen is cooled in the heat exchanger 37, in a further heat exchanger J8 cooled even further against vaporizing natural gas and then in two streams 39 with 94,000 Nm3 / h and 40 with 182,000 Nm3 / h separated. The partial flow 39 is in one Compressor 41 compressed to approx. 71 ata, in a heat exchanger 42 against circulating nitrogen Chilled and put in another three Streams 43, 44 and 45 split. The flow in line 43 is in a heat exchanger 46 against expanded, gaseous Nitrogen cooled from a separator 47, with which in a heat exchanger 48 Stream 44 cooled against circulating nitrogen and finally with the third, Stream 45 in line 50, cooled against liquid natural gas in a heat exchanger 49 united.

Das flüssige Erdgas tritt über eine leitung 51 in die Anlage ein, wird mit Hilfe einer Pumpe 52 auf den Abgabedruck von ca. 77 ata verdichtet und durchläuft nacheinander die Wärmetauscher 49, 60, 38 und 36, wobei es verdampft. The liquid natural gas enters the plant via a line 51, is compressed with the help of a pump 52 to the delivery pressure of approx. 77 ata and passes through the heat exchangers 49, 60, 38 and 36 one after the other, whereupon it evaporates.

Der Stickstoff aus Leitung 50 wird gegen entspannten Kreislaufstickstoff in einem Wärmetauscher 53 noch weiter abgekühlt und in einem Drosseiventil 54 auf einen Zwischendruck von ca. 4 ata entspannt, wobei sich ein Teil verflüssigt, Der flüssige, in einem Abscheider 55 gesammelte Anteil wird in einem Drosseiventil 56 auf ca. 1 ata entspannt, wobei ein Teil des Stickstoffs wieder verdampft,und in einen Abscheider 47 geleitet. Aus dem Abscheider 47 werden über I.ei tung 57 75 000 Nm3/h flüssiger produktstickstoff entnommen. Über eine Leitung 58 werden 12 000 Nm3/h verdampfter Stickstoff am Kopf des Abscheiders 47 abgezogen, im Wärmetauscher 46 gegen gasförmigen Stickstoff angewärmt, in einem Verdichter 59 auf den Anfangsdruck von ca. 4,5 ata komprimiert und dem gasförmigen Produktstickstoff aus den Luftzerlegungsanlagen in Leitung 33 zugemischt. The nitrogen from line 50 is against relaxed circulatory nitrogen In a heat exchanger 53 cooled even further and in a throttle valve 54 on an intermediate pressure of approx. 4 ata relaxes, whereby a part liquefies, The liquid, collected in a separator 55 is in a throttle valve 56 relaxed to about 1 ata, with part of the nitrogen evaporating again, and in a separator 47 passed. From the separator 47 are 57 75 via I.ei device 000 Nm3 / h of liquid product nitrogen removed. Via a line 58, 12 000 Nm3 / h evaporated nitrogen drawn off at the top of the separator 47, in the heat exchanger 46 warmed against gaseous nitrogen, in a compressor 59 to the initial pressure 4.5 ATA compressed and the gaseous product nitrogen from the air separation plants admixed in line 33.

Der Teilstrom 40 des hinter dem Wärmetauschers 38 aufgeteilten Stickstoffs wird in einem Wärmetauscher 60 gegen verdampfendes Fraga abgekühlt, in einer Entspannungsturbine 61 auf ca. 45 ata arbeitsleistend entspannt, mit dem nach der ersten Drosselentspannung gasförmig gebliebenen Stickstoff aus dem abscheider 55 vereint, im Wärme tau scher 53 gegen zu entspannenden stickstoff aus Leitung 50 angewärmt und in zwei Teilströme 62 und 63 aufgeteilt. Der Teilstrom 62 nimmt im Wärmetauscher 24 die Kompressionswärme des Kreislaufstickstoffs aus Leitung 22 der zweiten Luftzerlegungsanlage auf, wird mit dem Teilstrom 63, der im Wärmetauscher 48 gegen zu entspannenden Stickstoff angewärmt wird, vereinigt und wiederum in zwei Teilströme 64 mit 138 V00 Nn/h und 65 mit 57 000 N2 /h auf aufgetrennt. The partial flow 40 of the nitrogen divided behind the heat exchanger 38 is cooled in a heat exchanger 60 against evaporating fragments, in an expansion turbine 61 relaxed to approx. 45 ATa while performing work, with the one after the first throttle relaxation Nitrogen remaining in gaseous form from the separator 55 is combined in the heat exchanger 53 warmed against nitrogen to be released from line 50 and divided into two partial flows 62 and 63 split. The partial flow 62 takes the heat of compression in the heat exchanger 24 of the circulating nitrogen from line 22 of the second air separation plant with the substream 63, which in the heat exchanger 48 against nitrogen to be expanded is heated, combined and again in two substreams 64 with 138 V00 Nn / h and 65 with 57,000 N2 / h.

Der Teilstrom 64 wird nach Erwärmung im Wärmetauscher 42 im Verdichter 66 auf 11 ata verdichtet und dem gasförmigen Produktstickstoff aus den 1 'uftzerlegungsanlagen zwischen den Verdichtern 34 und 35 zugemischt. Der andere Teilstrom 65 wird im Wärmetauscher 37 gegen den auf 30 ata verdichteten Fintrittstickstoff angewärmt und zusammen mit Stickstoff aus Leitung 58 dem gasförmigen Produktstickstoff der Luftzerlegungsanlagen vor dem Verdichter 34 zugeführt.The partial flow 64 is after being heated in the heat exchanger 42 in the compressor 66 compressed to 11 ATA and the gaseous product nitrogen from the 1 'air separation plants admixed between the compressors 34 and 35. The other substream 65 is in the heat exchanger 37 warmed up against the final nitrogen compressed to 30 ATA and together with Nitrogen from line 58 the gaseous product nitrogen of the air separation plants fed in front of the compressor 34.

9 Patentansprüche 1 Blatt Zeichnungen9 claims 1 sheet of drawings

Claims (1)

Patentansprüche 1. Verfahren zur Gewinnung von flüssigem Stickstoff durch Tieftemperaturrektifikation von Luft unter Verwendung von flüssigem Erdgas als verdampfendem Kältemittel für die Verflüssigung des bei der Tieftemperaturrektifikation gasförmig erzeugten Stickstoffs, dadurch gekennzeichnet, daß die Erzeugung des gasförmigen Stickstoffs auf mindestens zwei im Verbund arbeitende Luftzerlegungsanlagen, die mit einer Erdgasverdampfungsanlage in Verbindung stehen, aufgeteilt wird, und daß die Übertragung der Kälte des flüssigen Erdgases vor der Verflüssigung des Stickstoffs lediglich auf eine Luftzerlegungsanlage erfolgt, 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß in einer ersten Luftzerlegungsanlage in einer ersten Rektifiziersäule eine flüssige Stickstorffraktion erzeugt und einer zweiten, unter höherem Druck als die erste Rektifiziersäule arbeitenden Rektifiziersäule als Waschflüssigkeit aufgegeben wird. Claims 1. Process for the production of liquid nitrogen by cryogenic rectification of air using liquefied natural gas as an evaporating refrigerant for the liquefaction of the cryogenic rectification gaseous nitrogen, characterized in that the production of the gaseous Nitrogen to at least two air separation plants working in a network that are connected to a natural gas evaporation plant, is divided, and that the transfer of the coldness of the liquid natural gas before the liquefaction of the nitrogen takes place only on an air separation plant, 2. The method according to claim 1, characterized characterized in that in a first air separation plant in a first rectification column one liquid nitrogen fraction is generated and a second one under higher pressure as the first rectifying column working as the washing liquid is abandoned. 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß ein in einer ersten Luftzerlegungsanlage neben gasförmigem Stickstoff anfallendes Restgas einer zweiten Luftzerlegungsanlage zur weiteren Zerlegung zugeführt wird. 3. The method according to claim 1 or 2, characterized in that one in a first air separation plant in addition to gaseous nitrogen Residual gas is fed to a second air separation plant for further separation. 4. Verfahren nach einem der Ansprüche 1 his 3, dadurch gekennzeichnet, daß die wärmemäßige Verknüpfung zwischen den Luftzerlegungsanlagen eineseits und der Stickstoffverflüssig'ung andererseits über im Kreislauf geführten gasförmigen Stickstoff aus der Hochdrucksäule einer zweiten Luftzerlegungsanlage erfolgt.4. The method according to any one of claims 1 to 3, characterized in that that the thermal link between the air separation plants on one side and the nitrogen liquefaction on the other hand via circulating gaseous Nitrogen from the high pressure column of a second air separation plant takes place. 5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß als wärmeübertragende Medien zwischen dem Kreislaufstickstoff und den flüssigen Erdgas ausschließlich Stickstofffraktionen verwendet werden.5. The method according to claim 4, characterized in that the heat transferring Media between the cycle nitrogen and the liquid natural gas exclusively Nitrogen fractions are used. 6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß das zur Verflüssigung des gasförmig erzeugten Stickstoffs verwendete flüssige Erdgas in flüssigem Zustand auf seinen Abgabedruck verdichtet wird.6. The method according to any one of claims 1 to 5, characterized in that that the liquid used to liquefy the nitrogen generated in gaseous form Natural gas is compressed in liquid state to its delivery pressure. 7. Vorrichtung zur Duch@ührung des Verfahren n?ch einem der Ansprüche 1 bis 6, gekennzeichnet durch zwei über eine Rohrleitung (1@) in Verbindung stehende Luftzerlegungsanlagen und ein an diese angeschlossene Erdgasverdampfungsanlage.7. Device for carrying out the method according to one of the claims 1 to 6, characterized by two connected via a pipe (1 @) Air separation plants and a natural gas evaporation plant connected to them. 8. Vorrichtung nach Anspruch 7, dadurch gekennzeichnet, daß die Erdgasverdampfungsanlage über einen Wärmetauscher (24) mit einer Luftzerlegungsanlage in Verbindung steht.8. Apparatus according to claim 7, characterized in that the natural gas evaporation system is in communication with an air separation plant via a heat exchanger (24). 9. Vorrichtung nach Anspruch 7 oder 8, dadurch gekennzeichnet, daß die Erdgasverdampfungsanlage eine Flüssigpumpe (52) .9. Apparatus according to claim 7 or 8, characterized in that the natural gas evaporation system has a liquid pump (52). aufweist. having.
DE19732307004 1973-02-13 1973-02-13 Liquefied nitrogen - with liquefied natural gas as refrigerant Pending DE2307004A1 (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5139547A (en) * 1991-04-26 1992-08-18 Air Products And Chemicals, Inc. Production of liquid nitrogen using liquefied natural gas as sole refrigerant
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
WO2007148984A2 (en) * 2006-06-20 2007-12-27 Aker Engineering & Technology As Method and plant for re-gasification of lng

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5139547A (en) * 1991-04-26 1992-08-18 Air Products And Chemicals, Inc. Production of liquid nitrogen using liquefied natural gas as sole refrigerant
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
WO2007148984A2 (en) * 2006-06-20 2007-12-27 Aker Engineering & Technology As Method and plant for re-gasification of lng
WO2007148984A3 (en) * 2006-06-20 2008-02-07 Aker Kvaerner Engineering & Te Method and plant for re-gasification of lng

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