US20090188280A1 - Process and device for low-temperature separation of air - Google Patents

Process and device for low-temperature separation of air Download PDF

Info

Publication number
US20090188280A1
US20090188280A1 US12/282,606 US28260607A US2009188280A1 US 20090188280 A1 US20090188280 A1 US 20090188280A1 US 28260607 A US28260607 A US 28260607A US 2009188280 A1 US2009188280 A1 US 2009188280A1
Authority
US
United States
Prior art keywords
air stream
column
pressure
distilling
nitrogen
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.)
Abandoned
Application number
US12/282,606
Other languages
English (en)
Inventor
Alexander Alekseev
Dietrich Rottmann
Florian Schliebitz
Dirk Schwenk
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
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SCHLIEBITZ, FLORIAN, ROTTMANN, DIETRICH, ALEKSEEV, ALEXANDER, SCHWENK, DIRK
Publication of US20090188280A1 publication Critical patent/US20090188280A1/en
Abandoned legal-status Critical Current

Links

Images

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
    • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
    • F25J3/04454—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04151—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • the invention relates to a process for low-temperature separation of air according to the introductory clause of Claim 1 .
  • the distilling-column system of the invention can be designed as a one-column system for nitrogen-oxygen separation, as a two-column system (for example as a standard Linde double-column system), or else as a three-column or multiple-column system.
  • additional devices can be provided for recovering other air components, in particular noble gases, for example an argon- or a krypton-xenon recovery.
  • the invention relates in particular to a process in which at least one gaseous compressed product is recovered by a liquid product stream being removed from the distilling-column system for nitrogen-oxygen separation, brought to an elevated pressure in the liquid state, and evaporated under this elevated pressure by indirect heat exchange or pseudo-evaporated (at supercritical pressure).
  • the object of the invention is to structure such a process and a corresponding device in an especially advantageous manner economically.
  • both secondary compressors are operated at an inlet temperature that is higher than 250 K, in particular higher than 270 K.
  • the expanders are preferably designed as turbines. They have “essentially the same inlet pressure,” i.e., their inlet pressures are distinguished, if necessary, by various pressure losses in lines, heat exchanger passages or the like.
  • the inlet temperatures of the two expanders are the same or different and rest on one or two intermediate levels between the hot and the cold ends of the main heat exchanger.
  • the invention can be applied to processes with exactly two air streams and the division of the second air stream into exactly two partial streams.
  • one or more additional air streams and/or one or more additional partial streams can be used.
  • the two or more expanders of the invention can also be connected in parallel on the outlet side, i.e., they can have essentially the same outlet pressure and essentially the same outlet temperature.
  • at least two of the expanders that are connected in parallel on the inlet side have different pressures.
  • the transfer of the mechanical energy from the active depressurization is preferably produced by a direct mechanical coupling of a first of two expanders that are connected in parallel to the first of two secondary compressors that are connected in series and by a direct mechanical coupling of the second of two expanders to the second of two secondary compressors.
  • the application of the invention to a two-column or multiple-column system, which has at least one high-pressure column and one low-pressure column, is especially advantageous, whereby the operating pressure of the low-pressure column is less than the operating pressure of the high-pressure column.
  • a first of the two partial streams is introduced into the high-pressure column downstream from its active depressurization.
  • the outlet pressure of the corresponding expansion turbine is in this case approximately at the level of the operating pressure of the high-pressure column.
  • the second of the two partial streams can then also be reduced in pressure to approximately high-pressure column pressure and can be introduced, for example, together with the first into the high-pressure column.
  • the second of the two partial streams of the second air stream is introduced at least partially into the low-pressure column. It is thus possible to set the outlet pressure of the corresponding expansion turbine at a lower value and under decompression to do more work owing to the elevated pressure ratio and thus to produce more cold.
  • the distilling-column system for nitrogen-oxygen separation has a high-pressure column, a medium-pressure column and a low-pressure column, which are operated under various pressures
  • the first partial stream can be introduced at least in part into the high-pressure column and the second partial stream can be introduced at least in part into the medium-pressure column and/or the low-pressure column.
  • the first air stream upstream from the first secondary compressor and the first air stream downstream from the second secondary compressor are brought into indirect heat exchange.
  • the first air stream is heated before the first secondary compressor and cooled again behind the second secondary compressor.
  • the first air stream enters the main heat exchanger at a temperature that is lower than that behind the second secondary compressor or behind its secondary condenser.
  • this temperature difference is 1 to 10 K, preferably 2 to 5 K.
  • the product streams can be drawn off from the main heat exchanger under lower temperatures, which has advantageous effects for the pre-cooling of air and for the cooling of the molecular sieve for the air purification.
  • standard intermediate condensers or secondary condensers can be used that remove the compression that accumulates in the secondary compressors by indirect heat exchange with an external coolant, for example with cooling water.
  • one or two secondary condensers can be used by having only the first secondary compressor, only the second secondary compressor or both secondary compressors per secondary condenser.
  • at least the first secondary compressor has a secondary condenser (intermediate condenser).
  • the invention relates to a device for low-temperature separation of air according to claim 9 .
  • FIG. 1 shows a first embodiment of the invention
  • FIG. 2 shows a second embodiment with a cold compressor.
  • atmospheric air is suctioned off as a main air stream via line 1 from an air compressor 2 , brought there to a first pressure of 10 to 30 bar, preferably approximately 19 bar, cooled in a pre-cooling stage 3 to approximately ambient temperature and fed to an adsorptive air purification stage 4 .
  • the purified main air stream 5 is divided at 6 into a first air stream 7 and a second air stream 8 .
  • the first air stream is heated in a booster-heat exchanger 9 to approximately cooling-water temperature and further compressed in a first secondary compressor 10 to an intermediate pressure of 15 to 60 bar, preferably approximately 25 bar. Then, the compression heat is removed at least partially in a first secondary condenser 1 .
  • the first air stream 12 is then still further compressed in a second secondary compressor 13 to a final pressure of 22 to 90 bar, preferably approximately 40 bar, and then heated in a second secondary condenser 14 and the booster-heat exchanger 9 to slightly above cooling-water temperature. Under this final pressure, the first air stream 15 enters into a main heat exchanger 16 and is cooled there and liquefied, or (at supercritical pressure) pseudo-liquefied.
  • the first air stream 17 which is cold, is reduced to a pressure of 4 to 10 bar, preferably approximately 6 bar (in the example in a butterfly valve 18 ), and introduced under this pressure in at least partially liquid state via line 19 into the high-pressure column 21 of a distilling-column system for nitrogen-oxygen separation 20 , which in addition has a low-pressure column 22 , a condenser-evaporator, not shown, and a subcooling countercurrent device 23 .
  • the second air stream 8 is not further compressed. It is introduced under the first pressure into the main heat exchanger 16 and is cooled there to an intermediate temperature of 125 to 200 K, preferably approximately 140 K.
  • the second air stream is divided at this intermediate temperature into two partial streams 24 , 27 , and is subjected to the active depressurization in two turbines 25 , 28 that are connected in parallel, which both reduce the pressure to approximately the operating pressure of the high-pressure column 21 .
  • the two depressurized partial streams 26 , 29 are purified again and introduced essentially in the gas state into the high-pressure column 21 via line 30 .
  • Oxygen 31 is drawn off directly or via a liquid tank as a “liquid product stream” from the low-pressure column 22 of the distilling-column system for nitrogen-oxygen separation 20 and is brought by a pump 32 in the liquid state to an elevated pressure of 4 to 70 bar, preferably approximately 40 bar. Under this elevated pressure, the liquid or supercritical oxygen 33 is evaporated or pseudo-evaporated in the main heat exchanger 16 by indirect heat exchange with the first air stream and heated to approximately ambient temperature. The oxygen is ultimately released as a gaseous product stream 34 .
  • One or more additional product or residual streams 35 can be drawn off via the main heat exchanger from the distilling-column system for nitrogen-oxygen separation 20 .
  • nitrogen for example from the main condenser or from the high-pressure column of the distilling-column system for nitrogen-oxygen separation 20 —can also be compressed internally in an analogous way.
  • first turbine 25 and the first secondary compressor 10 as well as the second turbine 28 and the second secondary compressor 13 are coupled mechanically in pairs in each case via a common shaft.
  • booster-heat exchanger 9 and the secondary condenser 14 are optional. They can be omitted individually or in their entirety.
  • FIG. 2 shows an embodiment that contains two variants relative to the process of FIG. 1 , which can both be applied independently of one another.
  • the same or comparable process steps carry the same reference numbers as in FIG. 1 .
  • the first variant relates to the outlet pressure of the second turbine 28 .
  • the latter reduces the pressure here to 1.2 to 4 bar, preferably approximately 1.4 bar, i.e., approximately the operating pressure of the low-pressure column 22 .
  • the depressurized lower partial stream 129 is then blown into the low-pressure column.
  • the inlet pressures of the two turbines 25 , 28 are, however, still the same; the inlet temperatures can be the same or different.
  • the second secondary compressor 113 is designed as a cold compressor.
  • the first air stream 12 a, 12 b, 12 c is therefore already introduced under intermediate pressure into the main heat exchanger 16 and is removed again from the main heat exchanger 16 at a second intermediate temperature of 120 to 180 K, preferably approximately 48 K.
  • This second intermediate temperature can be less than or equal to the inlet temperature of the turbines 25 , 28 , preferably it is—contrary to the depiction in the drawing—higher.
  • the second air stream 115 Downstream from the cold compression stage 113 , the second air stream 115 is introduced at a third intermediate temperature, which is higher than the turbine inlet temperature, and 140 to 220 K, preferably approximately 180 K, is again introduced into the main heat exchanger 16 .
  • the second air stream can be conveyed upstream from the cold secondary compressor 113 up to the cold end of the main heat exchanger 16 , and in this case, it is at least partially liquefied. It is then slightly throttled, again introduced into the cold end of the main heat exchanger, again evaporated, and finally heated to the inlet temperature of the compressor 113 , as it is explained in detail in, for example, EP 1067345 B1.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US12/282,606 2006-03-15 2007-03-06 Process and device for low-temperature separation of air Abandoned US20090188280A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102006012241.0 2006-03-15
DE102006012241A DE102006012241A1 (de) 2006-03-15 2006-03-15 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
PCT/EP2007/001917 WO2007104449A1 (de) 2006-03-15 2007-03-06 Vefahren und vorrichtung zur tieftemperaturzerlegung von luft

Publications (1)

Publication Number Publication Date
US20090188280A1 true US20090188280A1 (en) 2009-07-30

Family

ID=38267644

Family Applications (1)

Application Number Title Priority Date Filing Date
US12/282,606 Abandoned US20090188280A1 (en) 2006-03-15 2007-03-06 Process and device for low-temperature separation of air

Country Status (6)

Country Link
US (1) US20090188280A1 (enExample)
EP (1) EP1994344A1 (enExample)
JP (1) JP2009529648A (enExample)
CN (1) CN101421575B (enExample)
DE (1) DE102006012241A1 (enExample)
WO (1) WO2007104449A1 (enExample)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100058801A1 (en) * 2008-09-09 2010-03-11 Conocophillips Company System for enhanced gas turbine performance in a liquefied natural gas facility
US20130139548A1 (en) * 2011-12-01 2013-06-06 Linde Aktiengesellschaft Method and apparatus for producing pressurized oxygen by low-temperature separation of air
US20130255313A1 (en) * 2012-03-29 2013-10-03 Bao Ha Process for the separation of air by cryogenic distillation
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
WO2011018207A3 (de) * 2009-08-11 2014-03-13 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung eines gasförmigen sauerstoff-druckprodukts durch tieftemperaturzerlegung von luft
US20170234614A1 (en) * 2014-07-31 2017-08-17 Linde Aktiengesellschaft Method for the cryogenic separation of air and air separation plant

Families Citing this family (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009048456A1 (de) * 2009-09-21 2011-03-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052544A1 (de) * 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010055448A1 (de) * 2010-12-21 2012-06-21 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
FR2973487B1 (fr) * 2011-03-31 2018-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de production d'un gaz de l'air sous pression par distillation cryogenique
EP2520886A1 (de) 2011-05-05 2012-11-07 Linde AG Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
CN103998883B (zh) * 2011-09-20 2016-12-14 林德股份公司 低温分离空气的方法和设备
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
WO2014154339A2 (de) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Verfahren zur luftzerlegung und luftzerlegungsanlage
EP2784420A1 (de) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Verfahren zur Luftzerlegung und Luftzerlegungsanlage
EP2801777A1 (de) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Luftzerlegungsanlage mit Hauptverdichterantrieb
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
FR3014545B1 (fr) * 2013-12-05 2018-12-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d’air par distillation cryogenique
EP2963367A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch
TR201808162T4 (tr) * 2014-07-05 2018-07-23 Linde Ag Havanın düşük sıcaklıkta ayrıştırılması vasıtasıyla bir basınçlı gaz ürününün kazanılmasına yönelik yöntem ve cihaz.
EP2963369B1 (de) 2014-07-05 2018-05-02 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
PL2963370T3 (pl) 2014-07-05 2018-11-30 Linde Aktiengesellschaft Sposób i urządzenie do kriogenicznego rozdziału powietrza
US20160025408A1 (en) * 2014-07-28 2016-01-28 Zhengrong Xu Air separation method and apparatus
EP3179185A1 (de) * 2015-12-07 2017-06-14 Linde Aktiengesellschaft Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungs anlage
US10281207B2 (en) * 2016-06-30 2019-05-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with variable liquid production and power usage
EP3290843A3 (de) * 2016-07-12 2018-06-13 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung von druckstickstoff und flüssigstickstoff durch tieftemperaturzerlegung von luft
CN109442867B (zh) * 2018-12-19 2023-11-07 杭州特盈能源技术发展有限公司 一种外增压内液化纯氮制取装置及方法

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4279631A (en) * 1975-08-06 1981-07-21 Linde Aktiengesellschaft Process and apparatus for the production of oxygen by two-stage low-temperature rectification of air
US4303428A (en) * 1979-07-20 1981-12-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic processes for separating air
US5329776A (en) * 1991-03-11 1994-07-19 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of gaseous oxygen under pressure
US5515687A (en) * 1993-10-26 1996-05-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion
US5901579A (en) * 1998-04-03 1999-05-11 Praxair Technology, Inc. Cryogenic air separation system with integrated machine compression
US5980607A (en) * 1996-05-01 1999-11-09 The Boc Group Plc Steelmaking method with oxygen from rectification of air
US6112549A (en) * 1996-06-07 2000-09-05 Phillips Petroleum Company Aromatics and/or heavies removal from a methane-rich feed gas by condensation and stripping
US6257020B1 (en) * 1998-12-22 2001-07-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the cryogenic separation of gases from air
US6305191B1 (en) * 1999-05-07 2001-10-23 The Boc Group Plc Separation of air
US6314755B1 (en) * 1999-02-26 2001-11-13 Linde Aktiengesellschaft Double column system for the low-temperature fractionation of air
US6694776B1 (en) * 2003-05-14 2004-02-24 Praxair Technology, Inc. Cryogenic air separation system for producing oxygen
US6945076B1 (en) * 2002-09-11 2005-09-20 L'air Liquide, Societe Anonyme Pour L'etude Et, L'exploitation Des Procedes Georges Claude Production unit for large quantities of oxygen and/or nitrogen

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3216510A1 (de) * 1982-05-03 1983-11-03 Linde Ag, 6200 Wiesbaden Verfahren zur gewinnung von gasfoermigem sauerstoff unter erhoehtem druck
US5379599A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Pumped liquid oxygen method and apparatus
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
GB9404991D0 (en) * 1994-03-15 1994-04-27 Boc Group Plc Cryogenic air separation
JP3703943B2 (ja) * 1997-01-28 2005-10-05 大陽日酸株式会社 低純度酸素の製造方法及び装置
JP3737611B2 (ja) * 1997-08-08 2006-01-18 大陽日酸株式会社 低純度酸素の製造方法及び装置
US6009723A (en) * 1998-01-22 2000-01-04 Air Products And Chemicals, Inc. Elevated pressure air separation process with use of waste expansion for compression of a process stream
DE19933558C5 (de) * 1999-07-16 2010-04-15 Linde Ag Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
DE10103968A1 (de) * 2001-01-30 2002-08-01 Linde Ag Drei-Säulen-System zur Tieftemperaturzerlegung von Luft
DE10139097A1 (de) * 2001-08-09 2003-02-20 Linde Ag Verfahren und Vorrichtung zur Erzeugung von Sauerstoff durch Tieftemperatur-Zerlegung von Luft
FR2854682B1 (fr) * 2003-05-05 2005-06-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4279631A (en) * 1975-08-06 1981-07-21 Linde Aktiengesellschaft Process and apparatus for the production of oxygen by two-stage low-temperature rectification of air
US4303428A (en) * 1979-07-20 1981-12-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic processes for separating air
US5329776A (en) * 1991-03-11 1994-07-19 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of gaseous oxygen under pressure
US5515687A (en) * 1993-10-26 1996-05-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure
US5980607A (en) * 1996-05-01 1999-11-09 The Boc Group Plc Steelmaking method with oxygen from rectification of air
US6112549A (en) * 1996-06-07 2000-09-05 Phillips Petroleum Company Aromatics and/or heavies removal from a methane-rich feed gas by condensation and stripping
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion
US5901579A (en) * 1998-04-03 1999-05-11 Praxair Technology, Inc. Cryogenic air separation system with integrated machine compression
US6257020B1 (en) * 1998-12-22 2001-07-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the cryogenic separation of gases from air
US6314755B1 (en) * 1999-02-26 2001-11-13 Linde Aktiengesellschaft Double column system for the low-temperature fractionation of air
US6305191B1 (en) * 1999-05-07 2001-10-23 The Boc Group Plc Separation of air
US6945076B1 (en) * 2002-09-11 2005-09-20 L'air Liquide, Societe Anonyme Pour L'etude Et, L'exploitation Des Procedes Georges Claude Production unit for large quantities of oxygen and/or nitrogen
US6694776B1 (en) * 2003-05-14 2004-02-24 Praxair Technology, Inc. Cryogenic air separation system for producing oxygen

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100058801A1 (en) * 2008-09-09 2010-03-11 Conocophillips Company System for enhanced gas turbine performance in a liquefied natural gas facility
AU2009292077B2 (en) * 2008-09-09 2015-05-07 Conocophillips Company System for enhanced gas turbine performance in a liquefied natural gas facility
US9841230B2 (en) * 2008-09-09 2017-12-12 Conocophillips Company System for enhanced gas turbine performance in a liquefied natural gas facility
WO2011018207A3 (de) * 2009-08-11 2014-03-13 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung eines gasförmigen sauerstoff-druckprodukts durch tieftemperaturzerlegung von luft
US20130139548A1 (en) * 2011-12-01 2013-06-06 Linde Aktiengesellschaft Method and apparatus for producing pressurized oxygen by low-temperature separation of air
US20130255313A1 (en) * 2012-03-29 2013-10-03 Bao Ha Process for the separation of air by cryogenic distillation
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
US20170234614A1 (en) * 2014-07-31 2017-08-17 Linde Aktiengesellschaft Method for the cryogenic separation of air and air separation plant
US10480853B2 (en) * 2014-07-31 2019-11-19 Linde Aktiengesellschaft Method for the cryogenic separation of air and air separation plant

Also Published As

Publication number Publication date
DE102006012241A1 (de) 2007-09-20
WO2007104449A1 (de) 2007-09-20
CN101421575B (zh) 2012-11-07
CN101421575A (zh) 2009-04-29
EP1994344A1 (de) 2008-11-26
JP2009529648A (ja) 2009-08-20

Similar Documents

Publication Publication Date Title
US20090188280A1 (en) Process and device for low-temperature separation of air
US20090064714A1 (en) Process for low-temperature separation of air
US6662595B2 (en) Process and device for obtaining a compressed product by low temperature separation of air
US20090013869A1 (en) Process and device for producing a pressurized gaseous product by low-temperature separation of air
JP2909678B2 (ja) 圧力下のガス状酸素の製造方法及び製造装置
US20010052244A1 (en) Process and apparatus for producing a pressurized product by low-temperature fractionation of air
US6564581B2 (en) Three-column system for the low-temperature fractionation of air
US20120131952A1 (en) Method for recovering a gaseous pressure product by low-temperature separation of air
US20170153058A1 (en) Method and device for the low-temperature separation of air at variable energy consumption
TWI737770B (zh) 藉由低溫分離空氣製造加壓氮及液態氮之方法及裝置
US20110214453A1 (en) Process and device for cryogenic air fractionation
JP4728219B2 (ja) 空気の低温蒸留により加圧空気ガスを製造するための方法及びシステム
US20110067444A1 (en) Processes and Device for Low Temperature Separation of Air
US11193710B2 (en) Method and apparatus for the cryogenic separation of air
US20180023890A1 (en) Method And Apparatus For Obtaining A Compressed Nitrogen Product
US9733014B2 (en) Method and device for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air
US6257020B1 (en) Process for the cryogenic separation of gases from air
US20120285197A1 (en) Process and unit for the separation of air by cryogenic distillation
US8191386B2 (en) Distillation method and apparatus
US20130047666A1 (en) Method and device for obtaining pressurized nitrogen and pressurized oxygen by low-temperature separation of air
US20030140654A1 (en) Systems and methods for production of high pressure oxygen
US20130139548A1 (en) Method and apparatus for producing pressurized oxygen by low-temperature separation of air
CN113924452A (zh) 用于低温分离空气的方法和设备
TWI691356B (zh) 藉由低溫分離空氣獲得壓縮氣體產物之方法及裝置
US5901577A (en) Process and plant for air separation by cryogenic distillation

Legal Events

Date Code Title Description
AS Assignment

Owner name: LINDE AKTIENGESELLSCHAFT, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ALEKSEEV, ALEXANDER;ROTTMANN, DIETRICH;SCHLIEBITZ, FLORIAN;AND OTHERS;REEL/FRAME:022152/0681;SIGNING DATES FROM 20080119 TO 20090122

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION