EP1994344A1 - Method and apparatus for fractionating air at low temperatures - Google Patents
Method and apparatus for fractionating air at low temperaturesInfo
- Publication number
- EP1994344A1 EP1994344A1 EP07723062A EP07723062A EP1994344A1 EP 1994344 A1 EP1994344 A1 EP 1994344A1 EP 07723062 A EP07723062 A EP 07723062A EP 07723062 A EP07723062 A EP 07723062A EP 1994344 A1 EP1994344 A1 EP 1994344A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- air
- air flow
- nitrogen
- air stream
- distillation column
- 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- Withdrawn
Links
- 238000000034 method Methods 0.000 title claims abstract description 20
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000004821 distillation Methods 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 239000000047 product Substances 0.000 claims abstract description 7
- 239000012263 liquid product Substances 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims description 25
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 241000883306 Huso huso Species 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 238000004887 air purification Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- PDEXVOWZLSWEJB-UHFFFAOYSA-N krypton xenon Chemical compound [Kr].[Xe] PDEXVOWZLSWEJB-UHFFFAOYSA-N 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
- F25J3/04454—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
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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
- F25J3/04006—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
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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
- F25J3/04006—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
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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
- F25J3/04151—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
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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
- F25J3/04151—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
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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
- F25J3/04248—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
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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
- F25J3/04248—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
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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
- F25J3/04248—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
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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
- F25J3/04406—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
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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
- 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
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)
Abstract
Disclosed are a method and an apparatus for fractionating air at low temperatures by means of a nitrogen-oxygen separating distillation column system which comprises at least one fractionating column 21, 22). A main air flow (1, 5) is condensed in an air condenser (2) and is purified in a purifying device (4). A first and a second air flow (7, 8) are diverted from the main air flow (5). The first air flow (7) is re-condensed in two serially connected re-condensers (10, 13). The re-condensed first air flow (15) is cooled and liquefied or pseudo-liquefied at least in part by indirectly exchanging heat (16) and is then introduced into the nitrogen-oxygen separating distillation column system (20). The second air flow (8) is cooled by indirectly exchanging heat (16), is divided into two partial flows (24, 27), and is then expanded in a power-generating manner in two expanders (25, 28) which are provided with substantially the same inlet pressure. At least some of the partial flows (26, 29) of the second air flow, which have been expanded in a power-generating manner, is introduced into the nitrogen-oxygen separating distillation column system (20) (30, 129). At least some of the mechanical power generated during the power-generating expansion (25, 28) of the second air flow is used for driving the two serially connected re-condensers (10, 13). A liquid product flow (31) is removed from the nitrogen-oxygen separating distillation column system (20), is pressurized (32) in the liquid state, is evaporated or pseudo-evaporated in said pressurized state by indirectly exchanging heat (16) with the first air flow (15), and is finally withdrawn as a gaseous product flow (34). Both re-condensers (10, 13) are operated at an input temperature exceeding 250 K, especially exceeding 270 K.
Description
Beschreibung description
Verfahren und Vorrichtung zur Tieftemperaturzerlequnq von LuftMethod and apparatus for cryogenic decomposition of air
Die Erfindung betrifft ein Verfahren zur Tieftemperaturzerlegung von Luft gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to a method for the cryogenic separation of air according to the preamble of patent claim 1.
Verfahren und Vorrichtungen zur Tieftemperaturzerlegung von Luft sind zum Beispiel aus Hausen/Linde, Tieftemperaturtechnik, 2. Auflage 1985, Kapitel 4 (Seiten 281 bis 337) bekannt. Das Destilliersäulen-System der Erfindung kann als Einsäulensystem zur Stickstoff- Sauerstoff-Trennung ausgebildet sein, als Zweisäulensystem (zum Beispiel als klassisches Linde-Doppelsäulensystem), oder auch als Drei- oder Mehrsäulensystem. Zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung können weitere Vorrichtungen zur Gewinnung anderer Luftkomponenten, insbesondere von Edelgasen vorgesehen sein, beispielsweise eine Argon- oder eine Krypton-Xenon-Gewinnung.Methods and devices for the cryogenic decomposition of air are known, for example, from Hausen / Linde, Tiefftemperaturtechnik, 2nd edition 1985, Chapter 4 (pages 281 to 337). The distillation column system of the invention can be designed as a single-column system for nitrogen-oxygen separation, as a two-column system (for example as a classic Linde double column system), or as a three-column or multi-column system. In addition to the nitrogen-oxygen separation columns, other devices may be provided to recover other air components, particularly noble gases, such as argon or krypton-xenon recovery.
Die Erfindung betrifft insbesondere ein Verfahren, in dem mindestens ein gasförmiges Druckprodukt gewonnen wird, indem ein flüssiger Produktstrom aus dem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung entnommen, in flüssigem Zustand auf einen erhöhten Druck gebracht und unter diesem erhöhten Druck durch indirektem Wärmeaustausch verdampft oder (bei überkritischem Druck) pseudo- verdampft wird. Derartige Innenverdichtungsverfahren sind zum Beispiel bekannt aus DE 830805, DE 901542 (= US 2712738/US 2784572), DE 952908, DE 1103363 (= US 3083544), DE 1112997 (= US 3214925), DE 1124529, DE 1117616 (= US 3280574), DE 1226616 (= US 3216206), DE 1229561 (= US 3222878), DE 1199293, DE 1 187248 (= US 3371496), DE 1235347, DE 1258882More particularly, the invention relates to a process in which at least one gaseous product is obtained by withdrawing a liquid product stream from the nitrogen-oxygen separation distillation column system, bringing it to an elevated pressure in the liquid state, and evaporating it under this increased pressure by indirect heat exchange or (at supercritical pressure) is pseudo-evaporated. Such internal compression methods are known, for example, from DE 830805, DE 901542 (= US Pat. No. 2,712,738 / US Pat. No. 2,784,572), DE 952908, DE 1103363 (= US Pat. No. 3,883,544), DE 1112997 (= US Pat. No. 3,214,925), DE 1124529, DE 1117616 (= US Pat. No. 3,280,574) DE 1226616 (= US 3216206), DE 1229561 (= US 3222878), DE 1199293, DE 1 187248 (= US 3371496), DE 1235347, DE 1258882
(= US 3426543), DE 1263037 (= US 3401531), DE 1501722 (= US 3416323), DE 1501723 (= US 3500651 ), DE 2535132 (= US 4279631 ), DE 2646690, EP 93448 B1 (= US 4555256), EP 384483 B1 (= US 5036672), EP 505812 B1 (= US 5263328), EP 716280 B1 (= US 5644934), EP 842385 B1 (= US 5953937), EP 758733 B1 (= US 5845517), EP 895045 B1 (= US 6038885), DE 19803437 A1 , EP 949471 B1 (= US 6185960 B1), EP 955509 A1 (= US 6196022 B1 ), EP 1031804 A1 (= US 6314755), DE 19909744 A1 , EP 1067345 A1 (= US 6336345), EP 1074805 A1 (= US 6332337), DE 19954593 A1 , EP 1134525 A1 (= US 6477860), DE 10013073 A1 ,
EP 1139046 A1 , EP 1146301 A1 , EP 1150082 A1 , EP 1213552 A1 , DE 10115258 A1 , EP 1284404 A1 (= US 2003051504 A1), EP 1308680 A1 (= US 6612129 B2), DE 10213212 A1 , DE 10213211 A1 , EP 1357342 A1 oder DE 10238282 A1. Ein Verfahren der eingangs genannten Art ist aus WO 2004/099690 bekannt.(US Pat. No. 3,422,543), DE 1263037 (= US Pat. No. 3,315,331), DE 1501722 (= US Pat. No. 3,416,323), DE 1501723 (= US Pat. No. 3,500,651), DE 2535132 (= US Pat. No. 4,279,631), DE 2,646,690, EP 93448 B1 (= US Pat. No. 4,555,256), EP 384483 B1 (= US Pat. No. 5,036,672), EP 505812 B1 (= US Pat. No. 5,263,328), EP 716280 B1 (= US Pat. No. 5,644,934), EP 842385 B1 (= US Pat. No. 5,954,937), EP 758733 B1 (= US Pat. No. 5,845,517), EP 895045 B1 (= US Pat. No. 6,038,885), DE 19803437 A1, EP 949471 B1 (= US Pat. No. 6,185,960 B1), EP 955509 A1 (= US Pat. No. 6,196,022 B1), EP 1031804 A1 (= US Pat. No. 6,314,755), DE 19909744 A1, EP 1067345 A1 (= US Pat. No. 6,336,345), US Pat. EP 1074805 A1 (= US Pat. No. 6,332,337), DE 19954593 A1, EP 1134525 A1 (= US Pat. No. 6,477,860), DE 10013073 A1, EP 1139046 A1, EP 1146301 A1, EP 1150082 A1, EP 1213552 A1, DE 10115258 A1, EP 1284404 A1 (= US 2003051504 A1), EP 1308680 A1 (= US Pat. No. 6,612,129 B2), DE 10213212 A1, DE 10213211 A1, EP 1357342 A1 or DE 10238282 A1. A method of the aforementioned type is known from WO 2004/099690.
Der Erfindung liegt die Aufgabe zugrunde, ein derartiges Verfahren und eine entsprechende Vorrichtung wirtschaftlich besonders günstig zu gestalten.The invention has for its object to make such a method and a corresponding device economically particularly favorable.
Diese Aufgabe wird dadurch gelöst, dass beide Nachverdichter mit einer Eintrittstemperatur betrieben werden, die höher als 250 K, insbesondere höher als 270 K ist.This object is achieved in that both booster are operated with an inlet temperature which is higher than 250 K, in particular higher than 270 K.
Beide Nachverdichter werden also im Warmen betrieben. Hierdurch kann man wohl erprobte Technik einsetzen, zum Beispiel zwei identische Turbinen-Booster- Kombinationen. Außerdem wird das Wärmetauscher-Volumen relativ gering und damit werden Investitionskosten gespart.Both booster compressors are therefore operated in warm conditions. This can be used well proven technology, for example, two identical turbine booster combinations. In addition, the heat exchanger volume is relatively low and thus investment costs are saved.
Die Entspannungsmaschinen sind vorzugsweise als Turbinen ausgebildet. Sie weisen "im Wesentlichen denselben Einstrittsdruck" auf, das heißt ihre Eintrittsdrücke unterscheiden sich allenfalls durch verschiedene Druckverluste in Leitungen, Wärmetauscherpassagen oder Ähnlichem. Die Eintrittstemperaturen der beiden Entspannungsmaschinen sind gleich oder verschieden und liegen auf einem oder zwei Zwischenniveaus zwischen dem warmen und dem kalten Ende des Hauptwärmetauschers.The expansion machines are preferably designed as turbines. They have "substantially the same inlet pressure", that is to say their inlet pressures differ at most by different pressure losses in lines, heat exchanger passages or the like. The inlet temperatures of the two expansion machines are the same or different and are at one or two intermediate levels between the hot and cold ends of the main heat exchanger.
Die Erfindung ist auf Verfahren mit genau zwei Luftströmen und der Unterteilung des zweiten Luftstroms in genau zwei Teilströme anwendbar. Alternativ können bei der Erfindung auch ein oder mehrere zusätzliche Luftströme und/oder ein oder mehrere zusätzliche Teilströme eingesetzt werden. Beispielsweise ist es möglich, drei oder mehr Entspannungsmaschinen einzusetzen. Diese können, müssen aber nicht, eintrittsseitig parallel geschaltet sein.The invention is applicable to methods with exactly two air streams and the subdivision of the second air stream into exactly two sub-streams. Alternatively, in the invention, one or more additional air streams and / or one or more additional partial streams can be used. For example, it is possible to use three or more expansion machines. These can, but need not, be connected in parallel on the inlet side.
Die zwei oder mehr Entspannungsmaschinen der Erfindung können auch austrittsseitig parallel geschaltet sein, das heißt im Wesentlichen den gleichen Austrittsdruck und im Wesentlichen die gleiche Austrittstemperatur aufweisen. Alternativ dazu weisen
mindestens zwei der eintrittsseitig parallel geschalteten Entspannungsmaschinen unterschiedliche Drücke auf.The two or more expansion machines of the invention may also be connected in parallel on the outlet side, that is to say have substantially the same outlet pressure and substantially the same outlet temperature. Alternatively, point at least two of the inlet side parallel relaxation machines different pressures.
Die Übertragung der mechanische Energie aus der arbeitsleistenden Entspannung wird vorzugsweise durch eine direkte mechanische Kopplung einer ersten der beiden parallel geschalteten Entspannungsmaschinen mit dem ersten der beiden seriell verbundenen Nachverdichter und durch eine direkte mechanische Kopplung der zweiten der beiden Entspannungsmaschinen mit dem zweiten der beiden Nachverdichter bewirkt.The transmission of the mechanical energy from the working expansion is preferably effected by a direct mechanical coupling of a first of the two parallel relaxation machines with the first of the two serially connected booster and by a direct mechanical coupling of the second of the two expansion machines with the second of the two booster.
Besonders günstig ist die Anwendung der Erfindung auf ein Zwei- oder Mehr-Säulen- System, das mindestens eine Hochdrucksäule und eine Niederdrucksäule aufweist, wobei der Betriebsdruck der Niederdrucksäule niedriger als der Betriebsdruck der Hochdrucksäule ist.Particularly advantageous is the application of the invention to a two- or multi-column system having at least one high pressure column and a low pressure column, wherein the operating pressure of the low pressure column is lower than the operating pressure of the high pressure column.
Vorzugsweise wird ein erster der beiden Teilströme stromabwärts seiner arbeitsleistenden Entspannung in die Hochdrucksäule eingeleitet. Der Austrittsdruck der entsprechenden Entspannungsturbine liegt dabei etwa auf dem Niveau des Betriebsdrucks der Hochdrucksäule.Preferably, a first of the two partial streams is introduced downstream of its work-performing expansion in the high-pressure column. The outlet pressure of the corresponding expansion turbine is approximately at the level of the operating pressure of the high pressure column.
Der zweite der beiden Teilströme kann dann ebenfalls auf etwa Hochdrucksäulendruck entspannt und beispielsweise gemeinsam mit den ersten in die Hochdrucksäule eingeleitet werden.The second of the two partial streams can then also be expanded to about high-pressure column pressure and, for example, introduced into the high-pressure column together with the first.
Alternativ dazu wird der zweite der beiden Teilströme des zweiten Luftstroms mindestens zum Teil in die Niederdrucksäule eingeleitet. Damit ist es möglich, den Austrittsdruck der entsprechenden Entspannungsturbine niedriger zu wählen und durch das erhöhte Druckverhältnis mehr Arbeit bei der Entspannung zu leisten und damit mehr Kälte zu erzeugen.Alternatively, the second of the two partial streams of the second air stream is at least partially introduced into the low-pressure column. This makes it possible to choose the outlet pressure of the corresponding expansion turbine lower and to perform more work in the relaxation and thus more cold by the increased pressure ratio.
Bei einem Drei- oder Mehr-Säulen-System, wenn also das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eine Hochdrucksäule, eine Mitteldrucksäule und eine Niederdrucksäule aufweist, die unter verschiedenen Drücken betrieben werden, kann der erste Teilstrom mindestens zum Teil in die Hochdrucksäule und der zweite
Teilstrom mindestens zum Teil in die Mitteldrucksäule und/oder die Niederdrucksäule eingeleitet werden.In a three or more column system, that is, if the distillation column system for nitrogen-oxygen separation has a high-pressure column, a medium-pressure column and a low-pressure column, which are operated under different pressures, the first partial flow can at least partially in the high-pressure column and the second Partial flow at least partially into the medium-pressure column and / or the low-pressure column are introduced.
In vielen Fällen ist es günstig, wenn der erste Luftstrom stromaufwärts des ersten Nachverdichters und der erste Luftstrom stromabwärts des zweiten Nachverdichters in indirekten Wärmeaustausch gebracht werden. Hierbei wird der erste Luftstrom vor dem ersten Nachverdichter angewärmt und nach dem zweiten Nachverdichter wieder abgekühlt. Damit tritt der erste Luftstrom mit einer Temperatur in den Hauptwärmetauscher ein, die niedriger als die Temperatur nach dem zweiten Nachverdichter beziehungsweise nach dessen Nachkühler ist. Typischerweise beträgt diese Temperaturdifferenz 1 bis 10 K, vorzugsweise 2 bis 5 K. Damit können die Produktströme unter niedrigerer Temperatur aus dem Hauptwärmetauscher abgeführt werden, was günstige Auswirkungen für die Vorkühlung der Luft und für das Kühlen des Molekularsiebs für die Luftreinigung hat.In many cases, it is favorable if the first air stream upstream of the first post-compressor and the first air stream downstream of the second post-compressor are brought into indirect heat exchange. In this case, the first air stream is heated before the first booster and cooled again after the second booster. Thus, the first air flow occurs at a temperature in the main heat exchanger, which is lower than the temperature after the second booster or after the aftercooler. Typically, this temperature difference is 1 to 10 K, preferably 2 to 5 K. Thus, the product streams can be removed at lower temperature from the main heat exchanger, which has favorable effects for the pre-cooling of the air and for cooling the molecular sieve for air purification.
Alternativ oder zusätzlich werden klassische Zwischen- beziehungsweise Nachkühler eingesetzt, welche die in den Nachverdichtern anfallende Kompression durch indirekten Wärmeaustausch mit einem externen Kühlmittel, beispielsweise mit Kühlwasser, entfernen. Hierbei können ein oder zwei Nachkühler eingesetzt werden, indem nur der erste Nachverdichter, nur der zweite Nachverdichter oder beideAlternatively or additionally, classic intermediate or aftercoolers are used which remove the compression occurring in the after-compressors by indirect heat exchange with an external coolant, for example with cooling water. Here, one or two aftercoolers can be used by only the first booster, only the second booster or both
Nachverdichter je einen Nachkühler aufweisen. Grundsätzlich ist es auch möglich, auf Nachkühler und den oben beschriebenen indirekten Wärmeaustausch vollständig zu verzichten. In der Regel weist jedoch mindestens der erste Nachverdichter einen Nachkühler (Zwischenkühler) auf.After-compressor each have an aftercooler. In principle, it is also possible to completely dispense with aftercooler and the indirect heat exchange described above. As a rule, however, at least the first after-compressor has an aftercooler (intercooler).
Die Erfindung betrifft außerdem eine Vorrichtung zur Tieftemperaturzerlegung von Luft gemäß Patentanspruch 9.The invention also relates to a device for the cryogenic separation of air according to claim 9.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand von in den Zeichnungen schematisch dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:The invention and further details of the invention are explained below with reference to embodiments schematically illustrated in the drawings. Hereby show:
Figur 1 ein erstes Ausführungsbeispiel der Erfindung und Figur 2 ein zweites Ausführungsbeispiel mit Kaltverdichter.
In dem Ausführungsbeispiel von Figur 1 wird atmosphärische Luft als Hauptluftstrom über Leitung 1 von einem Luftverdichter 2 angesaugt, dort auf einen ersten Druck von 10 bis 30 bar, vorzugsweise etwa 19 bar gebracht, in einer Vorkühlung 3 auf etwa Umgebungstemperatur abgekühlt und einer adsorptiven Luftreinigung 4 zugeführt. Der gereinigte Hauptluftstrom 5 wird bei 6 in einen ersten Luftstrom 7 und einen zweiten Luftstrom 8 verzweigt.1 shows a first embodiment of the invention and Figure 2 shows a second embodiment with cold compressor. In the embodiment of Figure 1 atmospheric air is sucked as the main air flow via line 1 from an air compressor 2, there brought to a first pressure of 10 to 30 bar, preferably about 19 bar, cooled in a pre-cooling 3 to about ambient temperature and an adsorptive air cleaning. 4 fed. The purified main air stream 5 is branched at 6 into a first air stream 7 and a second air stream 8.
Der erste Luftstrom wird in einem Booster-Wärmetauscher 9 auf etwa Kühlwassertemperatur angewärmt und in einem ersten Nachverdichter 10 weiter auf einen Zwischendruck von 15 bis 60 bar, vorzugsweise etwa 25 bar verdichtet. Anschließend wird die Verdichtungswärme mindestens teilweise in einem ersten Nachkühler 11 entfernt. Der erste Luftstrom 12 wird dann in einem zweiten Nachverdichter 13 noch weiter auf einen Enddruck von 22 bis 90 bar, vorzugsweise etwa 40 bar komprimiert und anschließend in einem zweiten Nachkühler 14 und dem Booster-Wärmetauscher 9 auf etwas über Kühlwassertemperatur angewärmt. Unter diesem Enddruck tritt der erste Luftstrom 15 in einen Hauptwärmetauscher 16 ein und wird dort abgekühlt und verflüssigt, beziehungsweise (bei überkritischem Druck) pseudo-verflüssigt. Der kalte erste Luftstrom 17 wird auf einen Druck von 4 bis 10 bar, vorzugsweise etwa 6 bar entspannt (in dem Beispiel in einem Drosselventil 18) und unter diesem Druck in mindestens teilweise flüssigem Zustand über Leitung 19 in die Hochdrucksäule 21 eines Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung 20 eingeleitet, das außerdem eine Niederdrucksäule 22, einen nicht dargestellten Kondensator-Verdampfer und einen Unterkühlungs-Gegenströmer 23 aufweist.The first air stream is heated in a booster heat exchanger 9 to about the cooling water temperature and further compressed in a first booster 10 to an intermediate pressure of 15 to 60 bar, preferably about 25 bar. Subsequently, the heat of compression is at least partially removed in a first aftercooler 11. The first air stream 12 is then further compressed in a second booster 13 to a final pressure of 22 to 90 bar, preferably about 40 bar and then heated in a second aftercooler 14 and the booster heat exchanger 9 to slightly above the cooling water temperature. Under this final pressure, the first air stream 15 enters a main heat exchanger 16 and is cooled and liquefied there, or (at supercritical pressure) pseudo-liquefied. The cold first air stream 17 is expanded to a pressure of 4 to 10 bar, preferably about 6 bar (in the example in a throttle valve 18) and under this pressure in at least partially liquid state via line 19 into the high-pressure column 21 of a distillation column system Nitrogen-oxygen separation 20 introduced, which also has a low-pressure column 22, a not shown condenser-evaporator and a supercooling countercurrent 23.
Nicht nachverdichtet wird der zweite Luftstrom 8. Er wird unter dem ersten Druck in den Hauptwärmetauscher 16 eingeleitet und dort auf eine Zwischentemperatur von 125 bis 200 K, vorzugsweise etwa 140 K abgekühlt. Der zweite Luftstrom wird bei dieser Zwischentemperatur in zwei teilströme 24, 27 verzweigt und der arbeitsleistenden Entspannung in zwei parallel geschalteten Turbinen 25, 28 unterworfen, die beide auf etwa den Betriebsdruck der Hochdrucksäule 21 entspannen. Die beiden entspannten Teilströme 26, 29 werden wieder vereinigt und über Leitung 30 im Wesentlichen im Gaszustand in die Hochdrucksäule 21 eingeleitet.It is not recompressed, the second air stream 8. It is introduced under the first pressure in the main heat exchanger 16 and there cooled to an intermediate temperature of 125 to 200 K, preferably about 140 K. The second air stream is branched at this intermediate temperature into two partial streams 24, 27 and subjected to the work-performing expansion in two parallel-connected turbines 25, 28, which both relax to approximately the operating pressure of the high-pressure column 21. The two relaxed partial streams 26, 29 are reunited and introduced into the high-pressure column 21 via line 30 essentially in the gas state.
Aus der Niederdrucksäule 22 des Destilliersäulen-Systems zur Stickstoff-Sauerstoff- Trennung 20 wird direkt oder über einen Flüssigtank Sauerstoff 31 als "flüssiger
Produktstrom" abgezogen, durch eine Pumpe 32 in flüssigem Zustand auf einen erhöhten Druck von 4 bis 70 bar, vorzugsweise etwa 40 bar gebracht. Unter diesem erhöhten Druck wird der flüssige beziehungsweise überkritische Sauerstoff 33 in dem Hauptwärmetauscher 16 durch indirektem Wärmeaustausch mit dem ersten Luftstrom verdampft beziehungsweise pseudo-verdampft und auf etwa Umgebungstemperatur angewärmt. Der Sauerstoff wird schließlich als gasförmiger Produktstrom 34 abgegeben. Aus dem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung 20 können ein oder mehrere weitere Produkt- oder Restströme 35 über den Hauptwärmetauscher abgezogen werden. Zusätzlich oder alternativ zu der in den Zeichnungen dargestellten Innenverdichtung von Sauerstoff kann auch Stickstoff, beispielsweise aus dem Hauptkondensator oder aus der Hochdrucksäule des Destilliersäulen-Systems zur Stickstoff-Sauerstoff-Trennung 20 auf analoge Weise innenverdichtet werden.From the low pressure column 22 of the distillation column system for nitrogen-oxygen separation 20 is directly or via a liquid tank oxygen 31 as "liquid Product flow ", brought by a pump 32 in the liquid state to an elevated pressure of 4 to 70 bar, preferably about 40. Under this increased pressure, the liquid or supercritical oxygen 33 is vaporized in the main heat exchanger 16 by indirect heat exchange with the first air stream The oxygen is finally released as gaseous product stream 34. From the distillation column system for nitrogen-oxygen separation 20, one or more further product or residual streams 35 can be withdrawn via the main heat exchanger As an alternative to the internal compression of oxygen shown in the drawings, nitrogen, for example from the main condenser or from the high-pressure column of the distillation column system for nitrogen-oxygen separation 20, can also be internally compressed in an analogous manner.
In dem Ausführungsbeispiel der Figur 1 sind die erste Turbine 25 und der ersteIn the embodiment of Figure 1, the first turbine 25 and the first
Nachverdichter 10 sowie die zweite Turbine 28 und der zweite Nachverdichter 13 über jeweils eine gemeinsame Welle paarweise mechanisch gekoppelt.Post-compressor 10 and the second turbine 28 and the second booster 13 mechanically coupled in pairs via a common shaft.
Der Booster-Wärmetauscher 9 und der Nachkühler 14 sind optional. Sie können einzeln oder insgesamt weggelassen werden.The booster heat exchanger 9 and the aftercooler 14 are optional. They can be omitted individually or altogether.
Figur 2 zeigt ein Ausführungsbeispiel, das zwei Abwandlungen gegenüber dem Verfahren von Figur 1 enthält, die beide unabhängig voneinander anwendbar sind. Gleiche oder vergleichbare Verfahrensschritte tragen dieselben Bezugszeichen wie in Figur 1.Figure 2 shows an embodiment containing two modifications to the method of Figure 1, both of which are independently applicable. The same or comparable method steps bear the same reference numerals as in FIG. 1.
Die erste Abwandlung betrifft den Austrittsdruck der zweiten Turbine 28. Diese entspannt hier auf 1 ,2 bis 4 bar, vorzugsweise etwa 1 ,4 bar, also etwa den Betriebsdruck der Niederdrucksäule 22. Der entspannte Unterteilstrom 129 wird anschließend in die Niederdrucksäule eingeblasen. Die Eintrittsdrücke der beidenThe first modification relates to the outlet pressure of the second turbine 28. This relaxes here to 1, 2 to 4 bar, preferably about 1, 4 bar, that is about the operating pressure of the low pressure column 22. The relaxed lower part stream 129 is then blown into the low pressure column. The entry pressures of the two
Turbinen 25, 28 sind aber nach wie vor gleich, die Eintrittstemperaturen können gleich oder verschieden sein.Turbines 25, 28 are still the same, the inlet temperatures may be the same or different.
In einer zweiten Abwandlung ist der zweite Nachverdichter 113 als Kaltverdichter ausgebildet. Der erste Luftstrom 12a, 12b, 12c wird daher bereits unter dem
Zwischendruck in den Hauptwärmetauscher 16 eingeführt und bei einer zweiten Zwischentemperatur von 120 bis 180 K, vorzugsweise etwa 48 K wieder aus dem Hauptwärmetauscher 16 entnommen. Diese zweite Zwischentemperatur kann kleiner oder gleich der Eintrittstemperatur der Turbinen 25, 28 sein, vorzugsweise ist sie - entgegen der Darstellung in der Zeichnung - höher. Stromabwärts der Kaltverdichtung 113 wird der zweite Luftstrom 115 bei einer dritten Zwischentemperatur, die höher als die Turbinen-Eintrittstemperatur ist und 140 bis 220 K, vorzugsweise etwa 180 K beträgt wieder in den Hauptwärmetauscher 16 eingeführt.In a second modification, the second after-compressor 113 is designed as a cold compressor. The first air flow 12a, 12b, 12c is therefore already below the Intermediate pressure introduced into the main heat exchanger 16 and removed at a second intermediate temperature of 120 to 180 K, preferably about 48 K again from the main heat exchanger 16. This second intermediate temperature may be less than or equal to the inlet temperature of the turbines 25, 28, preferably it is - contrary to the representation in the drawing - higher. Downstream of the cold compression 113, the second air stream 115 is reintroduced into the main heat exchanger 16 at a third intermediate temperature which is higher than the turbine inlet temperature and 140 to 220 K, preferably about 180 K.
Abweichend von dem Ausführungsbeispiel in Figur 2 kann der zweite Luftstrom stromaufwärts des kalten Nachverdichters 1 13 auch bis zum kalten Ende des Hauptwärmetauschers 16 geführt und dabei mindestens teilweise verflüssigt werden: Er wird dann anschließend leicht abgedrosselt, wieder in das kalte Ende des Hauptwärmetauschers eingeführt, wieder verdampft und schließlich bis zur Eintrittstemperatur des Verdichters 113 angewärmt, wie es beispielsweise in EP 1067345 B1 im Einzelnen erläutert ist.
Notwithstanding the embodiment in Figure 2, the second air flow upstream of the cold booster 1 13 can also be led to the cold end of the main heat exchanger 16 and thereby at least partially liquefied. He is then then slightly throttled, reintroduced into the cold end of the main heat exchanger, again vaporized and finally heated to the inlet temperature of the compressor 113, as explained in detail for example in EP 1067345 B1.
Claims
1. Verfahren zur Tieftemperaturzerlegung von Luft mit einem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (20), das mindestens eine Trennsäule (21 , 22) aufweist, bei dem - ein Hauptluftstrom (1 , 5) in einem Luftverdichter (2) verdichtet und in einerA process for the cryogenic separation of air with a distillation column system for nitrogen-oxygen separation (20) having at least one separation column (21, 22) in which - a main air stream (1, 5) in an air compressor (2) compacted and in one
Reinigungsvorrichtung (4) gereinigt wird,Cleaning device (4) is cleaned,
- ein erster und ein zweiter Luftstrom (7, 8) aus dem Hauptluftstrom (5) abgezweigt werden,- a first and a second air stream (7, 8) are diverted from the main air stream (5),
- der erste Luftstrom (7) in zwei seriell verbundenen Nachverdichtern (10, 13) nachverdichtet wird,- the first air stream (7) in two serially connected after-compressors (10, 13) is recompressed,
- der nachverdichtete erste Luftstrom (15) durch indirekten Wärmeaustausch (16) abgekühlt und mindestens teilweise verflüssigt oder pseudo-verflüssigt und anschließend in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (20) eingeleitet wird, - der zweite Luftstrom (8) durch indirekten Wärmeaustausch (16) abgekühlt und anschließend, in zwei Teilströme (24, 27) aufgeteilt, in zwei Entspannungsmaschinen (25, 28) arbeitsleistend entspannt wird, wobei die beiden Entspannungsmaschinen im Wesentlichen den gleichen Eintrittsdruck aufweisen, - die arbeitsleistend entspannten Teilströme (26, 29) des zweiten Luftstroms mindestens zum Teil in das Destilliersäulen-System zur Stickstoff-Sauerstoff- Trennung (20) eingeleitet (30, 129) werden,- The recompressed first air stream (15) by indirect heat exchange (16) is cooled and at least partially liquefied or pseudo-liquefied and then introduced into the distillation column system for nitrogen-oxygen separation (20), - the second air stream (8) cooled indirect heat exchange (16) and then divided into two partial streams (24, 27), in two expansion machines (25, 28) is performed work-performing, the two expansion machines have substantially the same inlet pressure, - the work performing relaxed partial flows (26, 29) of the second air stream are introduced (30, 129) at least in part into the distillation column system for nitrogen-oxygen separation (20),
- die bei der arbeitsleistenden Entspannung (25, 28) des zweiten Luftstroms erzeugte mechanische Energie mindestens teilweise zum Antrieb der beiden seriell verbundenen Nachverdichter (10. 13) genutzt wird,- The mechanical energy generated in the work-performing expansion (25, 28) of the second air flow is at least partially used to drive the two series-connected booster (10. 13),
- ein flüssiger Produktstrom (31 ) aus dem Destilliersäulen-System zur Stickstoff- Sauerstoff-Trennung (20) entnommen, in flüssigem Zustand auf einen erhöhten Druck gebracht (32) und unter diesem erhöhten Druck durch indirekten Wärmeaustausch (16) mit dem ersten Luftstrom (15) verdampft oder pseudo- verdampft und schließlich als gasförmiger Produktstrom (34) abgezogen wird, dadurch gekennzeichnet, dass beide Nachverdichter (10, 13) mit einer- A liquid product stream (31) from the distillation column system for nitrogen-oxygen separation (20) removed, brought in the liquid state to an elevated pressure (32) and under this increased pressure by indirect heat exchange (16) with the first air flow ( 15) evaporated or pseudo-vaporized and finally withdrawn as a gaseous product stream (34), characterized in that both after-compressors (10, 13) with a
Eintrittstemperatur betrieben werden, die höher als 250 K, insbesondere höher als 270 K ist. Inlet temperature can be operated, which is higher than 250 K, in particular higher than 270 K.
2. Verfahren nach Anspruch 1 , dadurch gekennzeichnet, dass das Destilliersäulen- System zur Stickstoff-Sauerstoff-Trennung (20) eine Hochdrucksäule (21) und eine Niederdrucksäule (22) aufweist.2. The method according to claim 1, characterized in that the distillation column system for nitrogen-oxygen separation (20) has a high pressure column (21) and a low pressure column (22).
3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass ein erster (26) der beiden Teilströme des zweiten Luftstroms mindestens zum Teil in die Hochdrucksäule (21 ) eingeleitet (30) wird.3. The method according to claim 2, characterized in that a first (26) of the two partial streams of the second air stream is at least partially introduced into the high-pressure column (21) (30).
4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, dass der zweite (29) der beiden Teilströme des zweiten Luftstroms mindestens zum Teil in die4. The method according to claim 3, characterized in that the second (29) of the two partial flows of the second air flow at least partially into the
Hochdrucksäule (21 ) eingeleitet (30) wird.High-pressure column (21) introduced (30) is.
5. Verfahren nach einem der Ansprüche 2 bis 4, dadurch gekennzeichnet, dass der zweite der beiden Teilströme des zweiten Luftstroms mindestens zum Teil in die Niederdrucksäule (22) eingeleitet (129) wird.5. The method according to any one of claims 2 to 4, characterized in that the second of the two partial streams of the second air flow at least partially introduced into the low pressure column (22) (129).
6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eine Hochdrucksäule, eine Mitteldrucksäule und eine Niederdrucksäule aufweist, wobei der erste Teilstrom mindestens zum Teil in die Hochdrucksäule und der zweite Teilstrom mindestens zum Teil in die Mitteldrucksäule und/oder die Niederdrucksäule eingeleitet wird.6. The method according to any one of claims 1 to 5, characterized in that the distillation column system for nitrogen-oxygen separation comprises a high pressure column, a medium pressure column and a low pressure column, wherein the first partial flow at least partially into the high pressure column and the second partial flow at least partly introduced into the medium-pressure column and / or the low-pressure column.
7. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass der erste Luftstrom stromaufwärts des ersten Nachverdichters und der erste Luftstrom stromabwärts des zweiten Nachverdichters in indirekten Wärmeaustausch (9) miteinander gebracht werden.7. The method according to any one of claims 1 to 7, characterized in that the first air flow upstream of the first after-compressor and the first air flow downstream of the second after-compressor in indirect heat exchange (9) are brought together.
8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass nur der erste Nachverdichter, nur der zweite Nachverdichter oder beide8. The method according to any one of claims 1 to 7, characterized in that only the first booster, only the second booster or both
Nachverdichter je einen Nachkühler (11 , 14) aufweisen.After-compressor each have an aftercooler (11, 14).
9. Vorrichtung zur Tieftemperaturzerlegung von Luft zur Tieftemperaturzerlegung von Luft mit einem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (20), das mindestens eine Trennsäule (21 , 22) aufweist, mit - einem Luftverdichter (2) zur Verdichtung eines Hauptluftstroms (1)9. An apparatus for cryogenic separation of air for cryogenic separation of air with a distillation column system for nitrogen-oxygen separation (20) having at least one separation column (21, 22), with - An air compressor (2) for the compression of a main air flow (1)
- Reinigungsvorrichtung (4) zur Reinigung des verdichteten Hauptluftstroms- Cleaning device (4) for cleaning the compressed main air flow
- Mitteln zum Abzweigen eines ersten und eines zweiten Luftstroms (7, 8) aus dem Hauptluftstrom (5), - zwei seriell verbundenen Nachverdichtern (10, 13) zum Nachverdichten des ersten Luftstroms (7),- means for branching off a first and a second air stream (7, 8) from the main air stream (5), - two serially connected after-compressors (10, 13) for recompressing the first air stream (7),
- Mitteln (16, 20) zum Abkühlen und Verflüssigen oder beziehungsweise Pseudo- Verflüssigen des nachverdichteten ersten Luftstroms (15) durch indirekten Wärmeaustausch und zu dessen Einleiten in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (20),- means (16, 20) for cooling and liquefying or pseudo-liquefying the post-compressed first air stream (15) by indirect heat exchange and for introducing it into the distillation column system for nitrogen-oxygen separation (20),
- Mitteln (16) zum Abkühlen des zweiten Luftstrom (8) durch indirekten Wärmeaustausch (16) auf eine Zwischentemperatur- means (16) for cooling the second air stream (8) by indirect heat exchange (16) to an intermediate temperature
- zwei eintrittsseitig parallel geschalteten Entspannungsmaschinen (25, 28) zur arbeitsleistenden Entspannung des abgekühlten zweiten Luftstroms in zwei Teilströmen (24, 27),two relaxation machines (25, 28) connected in parallel on the inlet side for work-performing expansion of the cooled second air stream into two partial streams (24, 27),
- Mitteln (26, 29, 30, 129) zum Einleiten der arbeitsleistend entspannten Teilströme (26, 29) des zweiten Luftstroms in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (20),- Means (26, 29, 30, 129) for introducing the work-performing relaxed partial streams (26, 29) of the second air stream in the distillation column system for nitrogen-oxygen separation (20),
- Mitteln zur Übertragung der bei der arbeitsleistenden Entspannung (25, 28) des zweiten Luftstroms erzeugten mechanische Energie auf die beiden seriell verbundenen Nachverdichter (10. 13),Means for transmitting the mechanical energy generated in the work-performing expansion (25, 28) of the second air flow to the two serially connected after-compressors (10. 13),
- Mittel (31 , 32, 33, 16, 34) zum Entnehmen eines flüssigen Produktstroms (31 ) aus dem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung (20), zur Druckerhöhung des flüssigen Produktstroms im flüssigen Zustand auf einen erhöhten Druck gebracht (32), zum Verdampfen oder Pseudo-Verdampfen unter diesem erhöhten Druck durch indirektem Wärmeaustausch mit dem ersten Luftstrom (15) und zum Abziehen als gasförmiger Produktstrom (34), dadurch gekennzeichnet, dass beide Nachverdichter (10, 13) mit Mitteln zur Zufuhr des ersten Luftstroms unter einer Eintrittstemperatur, die höher als 250 K, insbesondere höher als 270 K ist, verbunden sind. - Means (31, 32, 33, 16, 34) for removing a liquid product stream (31) from the distillation column system for nitrogen-oxygen separation (20), brought to increase the pressure of the liquid product stream in the liquid state to an elevated pressure ( 32), for vaporizing or pseudo-vaporizing under this increased pressure by indirect heat exchange with the first air stream (15) and for withdrawal as gaseous product stream (34), characterized in that both re-compressors (10, 13) are provided with means for feeding the first Air flow at an inlet temperature which is higher than 250 K, in particular higher than 270 K.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DE102006012241A DE102006012241A1 (en) | 2006-03-15 | 2006-03-15 | Method and apparatus for the cryogenic separation of air |
PCT/EP2007/001917 WO2007104449A1 (en) | 2006-03-15 | 2007-03-06 | Method and apparatus for fractionating air at low temperatures |
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EP1994344A1 true EP1994344A1 (en) | 2008-11-26 |
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EP07723062A Withdrawn EP1994344A1 (en) | 2006-03-15 | 2007-03-06 | Method and apparatus for fractionating air at low temperatures |
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US (1) | US20090188280A1 (en) |
EP (1) | EP1994344A1 (en) |
JP (1) | JP2009529648A (en) |
CN (1) | CN101421575B (en) |
DE (1) | DE102006012241A1 (en) |
WO (1) | WO2007104449A1 (en) |
Families Citing this family (29)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BRPI0918769B1 (en) * | 2008-09-09 | 2021-01-05 | Conocophillips Company | system to improve gas turbine performance in a natural gas plant |
WO2011018207A2 (en) * | 2009-08-11 | 2011-02-17 | Linde Aktiengesellschaft | Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air |
DE102009048456A1 (en) * | 2009-09-21 | 2011-03-31 | Linde Aktiengesellschaft | Method and apparatus for the cryogenic separation of air |
DE102010052544A1 (en) | 2010-11-25 | 2012-05-31 | Linde Ag | Process for obtaining a gaseous product by cryogenic separation of air |
DE102010052545A1 (en) | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
DE102010055448A1 (en) * | 2010-12-21 | 2012-06-21 | Linde Ag | Method and apparatus for the cryogenic separation of air |
FR2973487B1 (en) * | 2011-03-31 | 2018-01-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | PROCESS AND APPARATUS FOR PRODUCING PRESSURIZED AIR GAS BY CRYOGENIC DISTILLATION |
EP2520886A1 (en) | 2011-05-05 | 2012-11-07 | Linde AG | Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air |
DE102011112909A1 (en) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Process and apparatus for recovering steel |
EP2758734B1 (en) * | 2011-09-20 | 2018-07-18 | Linde Aktiengesellschaft | Method and device for cryogenic decomposition of air |
EP2600090B1 (en) * | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Method and device for generating pressurised oxygen by cryogenic decomposition of air |
DE102011121314A1 (en) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
US20130255313A1 (en) * | 2012-03-29 | 2013-10-03 | Bao Ha | Process for the separation of air by cryogenic distillation |
DE102012017488A1 (en) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements |
EP2784420A1 (en) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
WO2014154339A2 (en) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
EP2801777A1 (en) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Air separation plant with main compressor drive |
DE102013017590A1 (en) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer |
FR3014545B1 (en) * | 2013-12-05 | 2018-12-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
EP2963367A1 (en) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Method and device for cryogenic air separation with variable power consumption |
PL2963369T3 (en) | 2014-07-05 | 2018-10-31 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
EP2963370B1 (en) * | 2014-07-05 | 2018-06-13 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
TR201808162T4 (en) * | 2014-07-05 | 2018-07-23 | Linde Ag | Method and apparatus for recovering a pressurized gas product by decomposing air at low temperature. |
US20160025408A1 (en) * | 2014-07-28 | 2016-01-28 | Zhengrong Xu | Air separation method and apparatus |
EP2980514A1 (en) * | 2014-07-31 | 2016-02-03 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
EP3179185A1 (en) * | 2015-12-07 | 2017-06-14 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
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 (en) * | 2016-07-12 | 2018-06-13 | Linde Aktiengesellschaft | Method and device for extracting pressurised nitrogen and pressurised nitrogen by cryogenic decomposition of air |
CN109442867B (en) * | 2018-12-19 | 2023-11-07 | 杭州特盈能源技术发展有限公司 | Device and method for preparing pure nitrogen by external pressurization and internal liquefaction |
Family Cites Families (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2535132C3 (en) * | 1975-08-06 | 1981-08-20 | Linde Ag, 6200 Wiesbaden | Process and device for the production of pressurized oxygen by two-stage low-temperature rectification of air |
FR2461906A1 (en) * | 1979-07-20 | 1981-02-06 | Air Liquide | CRYOGENIC AIR SEPARATION METHOD AND INSTALLATION WITH OXYGEN PRODUCTION AT HIGH PRESSURE |
DE3216510A1 (en) * | 1982-05-03 | 1983-11-03 | Linde Ag, 6200 Wiesbaden | Process for recovery of gaseous oxygen under elevated pressure |
JP2909678B2 (en) * | 1991-03-11 | 1999-06-23 | レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Method and apparatus for producing gaseous oxygen under pressure |
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 |
FR2711778B1 (en) * | 1993-10-26 | 1995-12-08 | Air Liquide | Process and installation for the production of oxygen and / or nitrogen under pressure. |
GB9404991D0 (en) * | 1994-03-15 | 1994-04-27 | Boc Group Plc | Cryogenic air separation |
US5737940A (en) * | 1996-06-07 | 1998-04-14 | Yao; Jame | Aromatics and/or heavies removal from a methane-based feed by condensation and stripping |
GB9609099D0 (en) * | 1996-05-01 | 1996-07-03 | Boc Group Plc | Oxygen steelmaking |
JP3703943B2 (en) * | 1997-01-28 | 2005-10-05 | 大陽日酸株式会社 | Method and apparatus for producing low purity oxygen |
US5802873A (en) * | 1997-05-08 | 1998-09-08 | Praxair Technology, Inc. | Cryogenic rectification system with dual feed air turboexpansion |
JP3737611B2 (en) * | 1997-08-08 | 2006-01-18 | 大陽日酸株式会社 | Method and apparatus for producing low purity oxygen |
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 |
US5901579A (en) * | 1998-04-03 | 1999-05-11 | Praxair Technology, Inc. | Cryogenic air separation system with integrated machine compression |
FR2787560B1 (en) * | 1998-12-22 | 2001-02-09 | Air Liquide | PROCESS FOR CRYOGENIC SEPARATION OF AIR GASES |
DE19908451A1 (en) * | 1999-02-26 | 2000-08-31 | Linde Tech Gase Gmbh | A low temperature air fractionating system uses a rectification unit comprising pressure and low pressure columns and a nitrogen fraction recycle to the system air feed inlet, to provide bulk nitrogen |
GB9910701D0 (en) * | 1999-05-07 | 1999-07-07 | Boc Group Plc | Separation of air |
DE19933558C5 (en) * | 1999-07-16 | 2010-04-15 | Linde Ag | Three-column process and apparatus for the cryogenic separation of air |
DE10103968A1 (en) * | 2001-01-30 | 2002-08-01 | Linde Ag | Three-pillar system for the low-temperature separation of air |
DE10139097A1 (en) * | 2001-08-09 | 2003-02-20 | Linde Ag | Method and device for producing oxygen by low-temperature separation of air |
FR2844344B1 (en) * | 2002-09-11 | 2005-04-08 | Air Liquide | PLANT FOR PRODUCTION OF LARGE QUANTITIES OF OXYGEN AND / OR NITROGEN |
FR2854682B1 (en) * | 2003-05-05 | 2005-06-17 | Air Liquide | METHOD AND INSTALLATION OF AIR SEPARATION BY CRYOGENIC DISTILLATION |
US6694776B1 (en) * | 2003-05-14 | 2004-02-24 | Praxair Technology, Inc. | Cryogenic air separation system for producing oxygen |
-
2006
- 2006-03-15 DE DE102006012241A patent/DE102006012241A1/en not_active Withdrawn
-
2007
- 2007-03-06 WO PCT/EP2007/001917 patent/WO2007104449A1/en active Application Filing
- 2007-03-06 EP EP07723062A patent/EP1994344A1/en not_active Withdrawn
- 2007-03-06 CN CN2007800135967A patent/CN101421575B/en not_active Expired - Fee Related
- 2007-03-06 JP JP2008558680A patent/JP2009529648A/en not_active Ceased
- 2007-03-06 US US12/282,606 patent/US20090188280A1/en not_active Abandoned
Non-Patent Citations (1)
Title |
---|
See references of WO2007104449A1 * |
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CN101421575A (en) | 2009-04-29 |
US20090188280A1 (en) | 2009-07-30 |
DE102006012241A1 (en) | 2007-09-20 |
JP2009529648A (en) | 2009-08-20 |
CN101421575B (en) | 2012-11-07 |
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