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EP0383994A2 - Air rectification process and apparatus - Google Patents

Air rectification process and apparatus Download PDF

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Publication number
EP0383994A2
EP0383994A2 EP89113815A EP89113815A EP0383994A2 EP 0383994 A2 EP0383994 A2 EP 0383994A2 EP 89113815 A EP89113815 A EP 89113815A EP 89113815 A EP89113815 A EP 89113815A EP 0383994 A2 EP0383994 A2 EP 0383994A2
Authority
EP
European Patent Office
Prior art keywords
nitrogen
pressure
heat exchanger
fraction
relaxed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP89113815A
Other languages
German (de)
French (fr)
Other versions
EP0383994A3 (en
Inventor
Dietrich Dipl.-Ing. Rottmann
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
Priority claimed from DE19893905521 external-priority patent/DE3905521A1/en
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP19890113815 priority Critical patent/EP0383994A3/en
Priority to CN90100335A priority patent/CN1025068C/en
Priority to AU49960/90A priority patent/AU618659B2/en
Priority to US07/483,143 priority patent/US5036672A/en
Priority to JP2042309A priority patent/JPH02245201A/en
Priority to DE9090103572T priority patent/DE59000211D1/en
Priority to EP90103572A priority patent/EP0384483B1/en
Publication of EP0383994A2 publication Critical patent/EP0383994A2/en
Publication of EP0383994A3 publication Critical patent/EP0383994A3/en
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/04151—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
    • F25J3/0423—Subcooling of liquid process streams
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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04327—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 argon or argon enriched 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual 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
    • F25J2200/20—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude oxygen"
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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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
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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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

Definitions

  • the invention relates to a method for air separation by rectification, in which air is compressed, pre-cleaned, cooled and pre-separated in the pressure stage of a two-stage rectification into a nitrogen-rich fraction and an oxygen-rich liquid, and the two fractions are at least partially fed to the medium-pressure stage of the rectification and in oxygen and nitrogen are broken down, at least one gaseous nitrogen fraction being led out, heated and at least partially relaxed in a work-performing manner.
  • the invention also relates to a device for carrying out the method.
  • the object of the invention is to improve the economy of the method and the device of the type mentioned at the outset and, in particular, to provide process cooling in a particularly advantageous manner without restricting the further use of the gaseous nitrogen fraction.
  • This object is achieved in that at least part of the nitrogen which has been expanded to perform the work is heated and compressed again, at least part of the work obtained during the relaxation being used for the compression.
  • the relaxed portion of the gaseous nitrogen fraction is compressed to a pressure which is substantially equal to the pressure when the gaseous nitrogen fraction is divided, and then subsequently fed back to the non-relaxed part of the gaseous nitrogen fraction becomes.
  • the entire gaseous nitrogen fraction is also available under the (generally increased) pressure of the medium pressure stage in the type of cold generation according to the invention and can be used, for example, in the Combustion chamber of a coal gasification power plant can continue to be used.
  • the invention also relates to a device for carrying out the method according to claims 5 and 6.
  • Compressed and pre-cleaned air is introduced via line 1, cooled in a main heat exchanger 17 in indirect heat exchange with product streams and fed into pressure stage 3 of a two-stage rectification column 2.
  • the pressure level 3 (operating pressure: 6 to 20 bar, preferably 8 to 17 bar) is with the medium pressure level 4 (operating pressure: 1.5 to 10 bar, preferably 2.0 to 8.0 bar) via a common condenser / evaporator 13 in heat exchanging connection.
  • the introduced air is pre-divided in pressure stage 3 into nitrogen and into an oxygen-enriched fraction.
  • the oxygen-enriched fraction is discharged in the liquid state via line 6, subcooled in heat exchanger 32 and throttled into the medium pressure stage 4.
  • Nitrogen from the top of pressure stage 3 is also drawn off in liquid form via line 5, supercooled in heat exchanger 32 and partly discharged as a liquid product via line 8.
  • the other part of the nitrogen from the pressure stage 3 is fed via line 9 as a return to the medium pressure stage 4.
  • liquid oxygen (line 14), gaseous pure nitrogen (line 15) and impure nitrogen (line 16) are removed and the nitrogen streams in the main heat exchanger 17 are additionally heated in the heat exchanger 32.
  • part (line 21) of the air in line 1 can be condensed in heat exchange 20 with oxygen 14 from the bottom of medium pressure stage 4.
  • the liquid 14 from the sump of the medium pressure stage 4 is brought to high pressure by means of a pump 19 and partially evaporated during the heat exchange in the condenser 20.
  • the partially condensed air 22 is introduced into the pressure stage 3 above the first feed point (line 1).
  • the vaporized portion of the oxygen is removed via line 23 and warmed (17). Another part of the oxygen is withdrawn via line 42 as a liquid product stream.
  • part of the impure nitrogen in line 16 is drawn off from the main heat exchanger 17 via line 30 at an average temperature of approximately 110 to 210 K, preferably 135 to 185 K, and in a pressure-reducing turbine 31 to perform a pressure of 2.6 to 1 , 4 bar, preferably about 2.0 bar relaxed.
  • the expanded nitrogen is again conducted via line 32 to the cold end of the main heat exchanger 17 and warmed to approximately ambient temperature. He releases the cold obtained during relaxation to air to be separated in line 1.

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Abstract

Es werden ein Verfahren und eine Vorrichtung zur Luftzerlegung durch Rektifikation beschrieben. Aus dem Verfahren abgezogener Stickstoff (16) wird auf eine mittlere Temperatur angewärmt, teilweise aus dem Hauptwärmetauscher (17) herausgeleitet (30) und arbeitsleistend entspannt (31). Das entspannte Gas (32) gibt seine Kälte im Hauptwärmetauscher (17) an Zerlegungsluft (1) ab und wird erneut verdichtet (33, 36).A method and a device for air separation by rectification are described. Nitrogen (16) drawn off from the process is warmed to a medium temperature, partly led out (30) from the main heat exchanger (17) and expanded to perform work (31). The expanded gas (32) releases its cold in the main heat exchanger (17) to decomposition air (1) and is compressed again (33, 36).

Description

Die Erfindung betrifft ein Verfahren zur Luftzerlegung durch Rektifikation, bei dem Luft verdichtet, vorgereinigt, abgekühlt und in der Druckstufe einer zweistufigen Rektifikation in eine stickstoffreiche Fraktion und in eine sauerstoffreiche Flüssig­keit vorzerlegt wird und die beiden Fraktionen mindestens teil­weise der Mitteldruckstufe der Rektifikation zugeführt und in Sauerstoff und Stickstoff zerlegt werden, wobei mindestens eine gasförmige Stickstofffraktion herausgeführt, angewärmt und mindestens teilweise arbeitsleistend entspannt wird. Gegenstand der Erfindung ist außerdem eine Vorrichtung zur Durchführung des Verfahrens.The invention relates to a method for air separation by rectification, in which air is compressed, pre-cleaned, cooled and pre-separated in the pressure stage of a two-stage rectification into a nitrogen-rich fraction and an oxygen-rich liquid, and the two fractions are at least partially fed to the medium-pressure stage of the rectification and in oxygen and nitrogen are broken down, at least one gaseous nitrogen fraction being led out, heated and at least partially relaxed in a work-performing manner. The invention also relates to a device for carrying out the method.

Ein derartiges Verfahren ist aus der US-PS 2 666 303 bekannt. Hier wird Stickstoff aus der Mitteldruckstufe zur Herstellung von Verfahrenskälte entspannt. Dies ist wirtschaftlicher als ein mit Druckstufenstickstoff betriebener Kältekreislauf, wenn die Mitteldruckstufe unter höherem als Atmosphärendruck betrieben wird. Das vorbekannte Verfahren weist jedoch den Nachteil auf, daß der entspannte Anteil der gasförmigen Stickstofffraktion aus der Mitteldruckstufe nicht mehr für Zwecke weiterverwendet werden kann, für die er unter erhöhtem Druck benötigt wird.Such a method is known from US Pat. No. 2,666,303. Here, nitrogen from the medium pressure stage is released to produce process cold. This is more economical than a refrigeration cycle operated with pressure stage nitrogen if the medium pressure stage is operated at higher than atmospheric pressure. However, the known method has the disadvantage that the relaxed portion of the gaseous nitrogen fraction from the medium pressure stage can no longer be used for purposes for which it is required under increased pressure.

Der Erfindung liegt die Aufgabe zugrunde, die Wirtschaftlichkeit des Verfahrens und der Vorrichtung der eingangs genannten Art zu verbessern und insbesondere auf besonders günstige Weise Verfah­renskälte zur Verfügung zu stellen, ohne dabei die Weiterverwen­dung der gasförmigen Stickstofffraktion einzuschränken.The object of the invention is to improve the economy of the method and the device of the type mentioned at the outset and, in particular, to provide process cooling in a particularly advantageous manner without restricting the further use of the gaseous nitrogen fraction.

Diese Aufgabe wird dadurch gelöst, daß mindestens ein Teil des arbeitleistend entspannten Stickstoffs angewärmt und erneut verdichtet wird, wobei mindestens ein Teil der beim Entspannen gewonnenen Arbeit zum Verdichten verwendet wird.This object is achieved in that at least part of the nitrogen which has been expanded to perform the work is heated and compressed again, at least part of the work obtained during the relaxation being used for the compression.

Es erweist sich als vorteilhaft, wenn ein Teil der Leistung beim Verdichten durch von außerhalb des Verfahrens importierte Ener­gie aufgebracht wird. Dadurch kann der entspannte Stickstoffan­teil wieder auf seinen ursprünglichen Druck (vor dem Entspannen) oder auf einen höheren Druck gebracht werden, falls er mit den entsprechenden Parametern weiterverwendet werden soll. Dies ist insbesondere bei Luftzerlegungsanlagen der Fall, welche im Zu­sammenhang Kraftwerken stehen, die zusammen mit einer Kohle- oder Schwerölvergasung betrieben werden. Bei solchen Anlagen wird der Stickstoff in die unter erhöhtem Druck stehende Brenn­kammer geführt.It proves to be advantageous if part of the power during compression is applied by energy imported from outside the process. This allows the expanded nitrogen content to be brought back to its original pressure (before decompression) or to a higher pressure if it is to be used further with the appropriate parameters. This is particularly the case with air separation plants that are connected to power plants that are operated together with coal or heavy oil gasification. In such systems, the nitrogen is fed into the combustion chamber, which is under increased pressure.

Dabei ist es insbesondere vorteilhaft, wenn gemäß weiteren Merk­malen der Erfindung der entspannte Anteil der gasförmigen Stick­stofffraktion auf einen Druck verdichtet wird, der im wesentli­chen gleich dem Druck bei der Aufteilung der gasförmigen Stick­stofffraktion ist, und außerdem anschließend wieder dem nicht entspannten Teil der gasförmigen Stickstofffraktion zugeführt wird.It is particularly advantageous if, according to further features of the invention, the relaxed portion of the gaseous nitrogen fraction is compressed to a pressure which is substantially equal to the pressure when the gaseous nitrogen fraction is divided, and then subsequently fed back to the non-relaxed part of the gaseous nitrogen fraction becomes.

Mit Hilfe dieser Verfahrensweise steht auch bei der erfindungs­gemäßen Art der Kältegewinnung die gesamte gasförmige Stick­stofffraktion unter dem (im allgemeinen erhöhten) Druck der Mitteldruckstufe zur Verfügung und kann beispielsweise in der Brennkammer eines Kohlevergasungskraftwerkes weiterverwendet werden.With the aid of this procedure, the entire gaseous nitrogen fraction is also available under the (generally increased) pressure of the medium pressure stage in the type of cold generation according to the invention and can be used, for example, in the Combustion chamber of a coal gasification power plant can continue to be used.

Die Erfindung betrifft auch eine Vorrichtung zur Durchführung des Verfahrens gemäß den Patentansprüchen 5 und 6 .The invention also relates to a device for carrying out the method according to claims 5 and 6.

Anhand der Zeichnung, in welcher eine Auführungsform des erfin­dungsgemäßen Verfahrens schematisch dargestellt ist, werden die Erfindung und weitere Einzelheiten der Erfindung näher erläutert.The invention and further details of the invention are explained in more detail with reference to the drawing, in which an embodiment of the method according to the invention is shown schematically.

Über Leitung 1 wird verdichtete und vorgereinigte Luft herange­führt, in einem Hauptwärmetauscher 17 in indirektem Wärmeaus­tausch mit Produktströmen abgekühlt und in die Druckstufe 3 einer zweistufigen Rektifiziersäule 2 eingespeist. Die Druck­stufe 3 (Betriebsdruck: 6 bis 20 bar, vorzugsweise 8 bis 17 bar) steht mit der Mitteldruckstufe 4 (Betriebsdruck: 1,5 bis 10 bar, vorzugsweise 2,0 bis 8,0 bar) über einen gemeinsamen Kon­densator/Verdampfer 13 in wärmetauschender Verbindung. Die eingeführte Luft wird in der Druckstufe 3 in Stickstoff und in eine sauerstoffangereicherte Fraktion vorzerlegt. Die sauer­stoffangereicherte Fraktion wird über Leitung 6 in flüssigem Zustand abgeführt, in Wärmetauscher 32 unterkühlt und in die Mitteldruckstufe 4 eingedrosselt. Stickstoff vom Kopf der Druck­stufe 3 wird über Leitung 5 ebenfalls flüssig abgezogen, in Wärmetauscher 32 unterkühlt und zum einen Teil über Leitung 8 als flüssiges Produkt abgeführt. Der andere Teil des Stickstoffs aus der Druckstufe 3 wird über Leitung 9 als Rücklauf auf die Mitteldruckstufe 4 aufgegeben.Compressed and pre-cleaned air is introduced via line 1, cooled in a main heat exchanger 17 in indirect heat exchange with product streams and fed into pressure stage 3 of a two-stage rectification column 2. The pressure level 3 (operating pressure: 6 to 20 bar, preferably 8 to 17 bar) is with the medium pressure level 4 (operating pressure: 1.5 to 10 bar, preferably 2.0 to 8.0 bar) via a common condenser / evaporator 13 in heat exchanging connection. The introduced air is pre-divided in pressure stage 3 into nitrogen and into an oxygen-enriched fraction. The oxygen-enriched fraction is discharged in the liquid state via line 6, subcooled in heat exchanger 32 and throttled into the medium pressure stage 4. Nitrogen from the top of pressure stage 3 is also drawn off in liquid form via line 5, supercooled in heat exchanger 32 and partly discharged as a liquid product via line 8. The other part of the nitrogen from the pressure stage 3 is fed via line 9 as a return to the medium pressure stage 4.

Als Produkte der Mitteldruckstufe 4 werden flüssiger Sauerstoff (Leitung 14), gasförmiger Reinstickstoff (Leitung 15) und unrei­ner Stickstoff (Leitung 16) entnommen und im Hauptwärmetauscher 17, die Stickstoffströme zusätzlich im Wärmetauscher 32, ange­wärmt.As products of medium pressure stage 4, liquid oxygen (line 14), gaseous pure nitrogen (line 15) and impure nitrogen (line 16) are removed and the nitrogen streams in the main heat exchanger 17 are additionally heated in the heat exchanger 32.

Vor der Einspeisung in die Druckstufe 3 kann ein Teil (Leitung 21) der Luft in Leitung 1 in Wärmetausch 20 mit Sauerstoff 14 aus dem Sumpf der Mitteldruckstufe 4 kondensiert werden. Die Flüssigkeit 14 aus dem Sumpf der Mitteldruckstufe 4 wird dazu mittels einer Pumpe 19 auf hohen Druck gebracht und bei dem Wärmeaustausch im Kondensator 20 teilweise verdampft. Die teil­weise kondensierte Luft 22 wird oberhalb der ersten Einspeise­stelle (Leitung 1) in die Druckstufe 3 eingeführt. Der verdampf­te Anteil des Sauerstoffs wird über Leitung 23 abgeführt und angewärmt (17). Ein anderer Teil des Sauerstoffs wird über Leitung 42 als flüssiger Produktstrom abgezogen.Before being fed into pressure stage 3, part (line 21) of the air in line 1 can be condensed in heat exchange 20 with oxygen 14 from the bottom of medium pressure stage 4. For this purpose, the liquid 14 from the sump of the medium pressure stage 4 is brought to high pressure by means of a pump 19 and partially evaporated during the heat exchange in the condenser 20. The partially condensed air 22 is introduced into the pressure stage 3 above the first feed point (line 1). The vaporized portion of the oxygen is removed via line 23 and warmed (17). Another part of the oxygen is withdrawn via line 42 as a liquid product stream.

Erfindungsgemäß wird ein Teil des unreinen Stickstoffs in Lei­tung 16 auf einer mittleren Temperatur von etwa 110 bis 210 K, vorzugsweise 135 bis 185 K, über Leitung 30 aus dem Hauptwärme­tauscher 17 abgezogen und in einer Entspannungsturbine 31 ar­beitsleistend auf einen Druck von 2,6 bis 1,4 bar, vorzugsweise etwa 2,0 bar entspannt. Der entspannte Stickstoff wird über Leitung 32 erneut zum kalten Ende des Hauptwärmetauschers 17 geführt und auf etwa Umgebungstemperatur angewärmt. Er gibt dabei die beim Entspannen gewonnene Kälte an zu zerlegende Luft in Leitung 1 ab.According to the invention, part of the impure nitrogen in line 16 is drawn off from the main heat exchanger 17 via line 30 at an average temperature of approximately 110 to 210 K, preferably 135 to 185 K, and in a pressure-reducing turbine 31 to perform a pressure of 2.6 to 1 , 4 bar, preferably about 2.0 bar relaxed. The expanded nitrogen is again conducted via line 32 to the cold end of the main heat exchanger 17 and warmed to approximately ambient temperature. He releases the cold obtained during relaxation to air to be separated in line 1.

Um den entspannten Teil des Stickstoffs gemeinsam mit dem nicht entspannten Anteil (Leitung 39) abziehen zu können, wird dieser in zwei Stufen 33, 36 wieder verdichtet, wobei jeweils die Kompressionswärme anschließend entfernt wird (Kühler 35, 37). Die zweite Verdichtungsstufe 36 ist mit der Entspannungsturbine 31 gekoppelt, so daß die bei der Entspannung gewonnene Arbeit für das Verfahren zurückgewonnen wird. Um das Gas wieder auf seinen Anfangsdruck (in Leitung 30 bzw. 39) zu bringen ist jedoch eine weitere Verdichtungsstufe 33 erforderlich, die mit von außen eingebrachter Energie betrieben wird. Diese zusätzlich aufgewandte Energie wird jedoch durch die erfindungsgemäße Verfahrensweise außerordentlich effektiv in Verfahrenskälte umgesetzt.In order to be able to draw off the relaxed part of the nitrogen together with the non-relaxed portion (line 39), this is compressed again in two stages 33, 36, the compression heat then being removed in each case (cooler 35, 37). The second compression stage 36 is coupled to the expansion turbine 31, so that the work gained in the expansion is recovered for the process. In order to bring the gas back to its initial pressure (in line 30 or 39), however, a further compression stage 33 is required, which is operated with energy introduced from outside. However, this additional energy is converted extremely effectively into process cold by the procedure according to the invention.

Claims (6)

1. Verfahren zur Luftzerlegung durch Rektifikation, bei dem Luft (1) verdichtet, vorgereinigt, abgekühlt (17) und in der Druckstufe (3) einer zweistufigen Rektifikation (2) in eine stickstoffreiche Fraktion (5) und in eine sauerstoffreiche Flüssigkeit (6) vorzerlegt wird und die beiden Fraktionen (5, 6) mindestens teilweise der Mitteldruckstufe (4) der Rektifikation (2) zugeführt und in Sauerstoff und Stickstoff zerlegt werden, wobei mindestens eine gasförmige Stickstofffraktion herausgeführt (16), angewärmt (17) und mindestens teilweise (30) arbeitsleistend entspannt (31) wird, dadurch gekennzeichnet, daß mindestens ein Teil des arbeitleistend entspannten (31) Stickstoffs (32) angewärmt (17) und erneut verdichtet (33, 36) wird, wobei mindestens ein Teil der beim Entspannen (31) gewonnenen Arbeit zum Verdichten (36) verwendet wird.1. Process for air separation by rectification, in which air (1) is compressed, pre-cleaned, cooled (17) and in the pressure stage (3) a two-stage rectification (2) into a nitrogen-rich fraction (5) and into an oxygen-rich liquid (6) is pre-separated and the two fractions (5, 6) are at least partially fed to the medium pressure stage (4) of the rectification (2) and broken down into oxygen and nitrogen, at least one gaseous nitrogen fraction being led out (16), heated (17) and at least partially ( 30) is relaxed during work (31), characterized in that at least part of the nitrogen (32) which has been relaxed during work (31) is warmed (17) and compressed again (33, 36), at least part of the pressure being released (31) won work for compression (36) is used. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß ein Teil der Leistung beim Verdichten (33) durch von außerhalb des Verfahrens importierte Energie aufgebracht wird.2. The method according to claim 1, characterized in that part of the power during compression (33) is applied by energy imported from outside the process. 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß der entspannte Anteil (32) der gasförmigen Stickstoff­fraktion auf einen Druck verdichtet (33, 36) wird, der im wesentlichen gleich dem Druck bei der Aufteilung (30, 39) der gasförmigen Stickstofffraktion (16) ist.3. The method according to claim 1 or 2, characterized in that the relaxed portion (32) of the gaseous nitrogen fraction is compressed to a pressure (33, 36) which is substantially equal to the pressure in the division (30, 39) of the gaseous nitrogen fraction (16) is. 4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß der entspannte und wieder verdichtete Anteil (38) der gasförmi­gen Stickstofffraktion wieder dem nicht entspannten Teil (39) der gasförmigen Stickstofffraktion (16) zugeführt wird.4. The method according to claim 3, characterized in that the relaxed and re-compressed portion (38) of the gaseous nitrogen fraction is again supplied to the non-relaxed part (39) of the gaseous nitrogen fraction (16). 5. Vorrichtung zur Durchführung des Verfahrens nach einem der Ansprüche 1 bis 4 mit einem Hauptwärmetauscher (17), der Passagen für Luft (1) und für Stickstoff (16, 39) enthält, und mit einer Doppelrektifiziersäule (2) bestehend aus Drucksäule (3) und Mitteldrucksäule (4), gekennzeichnet durch eine Leitung (30), die aus dem mittleren Bereich des Hauptwärmetauschers (17) herausführt und mit der Stickstoff­passage (16) und mit dem Eingang einer Entspannungsturbine (31) verbunden ist, und durch eine weitere Leitung (32), die den Ausgang der Entspannungsturbine (31) mit dem Eingang eines Verdichters (33, 36) verbindet und als Passage durch den Hauptwärmetauscher (17) geführt wird.5. Apparatus for carrying out the method according to one of claims 1 to 4 with a main heat exchanger (17) which contains passages for air (1) and for nitrogen (16, 39), and with a double rectification column (2) consisting of a pressure column (3 ) and medium pressure column (4), characterized by a line (30) which leads out of the central region of the main heat exchanger (17) and is connected to the nitrogen passage (16) and to the inlet of an expansion turbine (31), and by a further line (32), which connects the outlet of the expansion turbine (31) to the inlet of a compressor (33, 36) and is guided as a passage through the main heat exchanger (17). 6. Vorrichtung nach Anspruch 5, dadurch gekennzeichnet, daß der Ausgang des Verdichters (33, 36) mit dem Ausgang der Stick­stoffpassage (39) des Hauptwärmetauschers (17) verbunden ist.6. The device according to claim 5, characterized in that the output of the compressor (33, 36) with the output of the nitrogen passage (39) of the main heat exchanger (17) is connected.
EP19890113815 1989-02-23 1989-07-26 Air rectification process and apparatus Withdrawn EP0383994A3 (en)

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EP19890113815 EP0383994A3 (en) 1989-02-23 1989-07-26 Air rectification process and apparatus
CN90100335A CN1025068C (en) 1989-02-23 1990-01-23 Method and device for separating air by rectification
AU49960/90A AU618659B2 (en) 1989-02-23 1990-02-21 Process and apparatus for air fractionation by rectification
US07/483,143 US5036672A (en) 1989-02-23 1990-02-22 Process and apparatus for air fractionation by rectification
JP2042309A JPH02245201A (en) 1989-02-23 1990-02-22 Air decomposition by rectification and its apparatus
DE9090103572T DE59000211D1 (en) 1989-02-23 1990-02-23 METHOD AND DEVICE FOR AIR DISASSEMBLY BY RECTIFICATION.
EP90103572A EP0384483B1 (en) 1989-02-23 1990-02-23 Air rectification process and apparatus

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DE19893905521 DE3905521A1 (en) 1989-02-23 1989-02-23 METHOD AND DEVICE FOR AIR DISASSEMBLY BY RECTIFICATION
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EP0384483A2 (en) 1990-08-29
AU4996090A (en) 1990-08-30
AU618659B2 (en) 1992-01-02
US5036672A (en) 1991-08-06
EP0383994A3 (en) 1990-11-07
EP0384483B1 (en) 1992-07-22
JPH02245201A (en) 1990-10-01
CN1045173A (en) 1990-09-05
DE59000211D1 (en) 1992-08-27
CN1025068C (en) 1994-06-15
EP0384483A3 (en) 1990-11-07

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