EP0384483B1 - Procédé et dispositif de rectification d'air - Google Patents
Procédé et dispositif de rectification d'air Download PDFInfo
- Publication number
- EP0384483B1 EP0384483B1 EP90103572A EP90103572A EP0384483B1 EP 0384483 B1 EP0384483 B1 EP 0384483B1 EP 90103572 A EP90103572 A EP 90103572A EP 90103572 A EP90103572 A EP 90103572A EP 0384483 B1 EP0384483 B1 EP 0384483B1
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- Prior art keywords
- nitrogen
- pressure
- pressure stage
- compressed
- stage
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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- 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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- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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- F25J3/04642—Recovering noble gases from air
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- F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
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- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/923—Inert gas
- Y10S62/924—Argon
Definitions
- the invention relates to a method for air separation by rectification, in which air is compressed, pre-cleaned, cooled and pre-separated in the pressure stage of a two-stage rectification into a nitrogen-rich fraction and an oxygen-rich liquid, and the two fractions are at least partially fed to the medium-pressure stage of the rectification and in oxygen and nitrogen are broken down, with at least one gaseous nitrogen fraction being led out of the medium pressure stage, heated and at least partially compressed.
- the invention also relates to a device for carrying out the method with the flagpoles of the first part of claim 6.
- the object of the invention is to improve the economy of the method and the device of the type mentioned at the outset and, in particular, to provide process cooling in a particularly advantageous manner without the reuse of the gaseous nitrogen fraction, in particular for applications which require an increased pressure level, restrict.
- This object is achieved in that the nitrogen is relieved of work prior to compression and reheated, the cold obtained during the expansion being given off to one or more other process streams and at least part of the work obtained during expansion being used to compress the nitrogen.
- the work-relieving expansion with recompression is particularly favorable to use in air separation plants which are operated under increased pressure, since the pressure at the inlet of the expansion turbine is also relatively high here and a favorable efficiency can thus be achieved.
- the expanded nitrogen content can be brought back to its original pressure (before the expansion) or to a higher pressure if it is to be used further with the appropriate parameters.
- the recompressed nitrogen can be fed into the combustion chamber, which is generally under increased pressure.
- the nitrogen which has been relieved of work is compressed to a pressure which is substantially equal to the pressure prior to the relaxation of work, and the relaxed and re-compressed nitrogen is again the non-expanded part of the gaseous nitrogen fraction is fed from the medium pressure stage.
- the entire gaseous nitrogen fraction is also available under the (generally increased) pressure of the medium pressure stage in the type of cold generation according to the invention and can be used, for example, in the combustion chamber of a coal gasification power plant.
- the product purities achieved are often unsatisfactory, particularly in those applications in which the entire air separation and in particular the medium pressure stage must be carried out at relatively high pressures. This applies to the nitrogen produced, but particularly to the oxygen product.
- a further nitrogen fraction is removed from the head of the medium pressure stage, heated, compressed, then cooled again and introduced into the pressure stage.
- the (pure) nitrogen fraction is therefore at least partially carried out in a so-called amplification circuit.
- the amount of nitrogen passed through the boost circuit into the pressure stage is condensed in indirect heat exchange with sump liquid of the medium pressure stage, drawn off in liquid form and added to the medium pressure stage as an additional return flow.
- the invention also relates to a device for carrying out the method according to claims 6 and 7.
- Compressed and pre-cleaned air is introduced via line 1, cooled in a main heat exchanger 17 in indirect heat exchange with product streams and fed into pressure stage 3 of a two-stage rectification column 2.
- the pressure level 3 (operating pressure: 6 to 20 bar, preferably 8 to 17 bar) is with the medium pressure level 4 (operating pressure: 1.5 to 10 bar, preferably 2.0 to 8.0 bar) via a common condenser / evaporator 13 in heat exchanging connection.
- the introduced air is pre-divided in pressure stage 3 into nitrogen and into an oxygen-enriched fraction.
- the oxygen-enriched fraction is discharged in the liquid state via line 6, subcooled in heat exchanger 18 and throttled into the medium pressure stage 4.
- Nitrogen from the head of pressure stage 3 is also drawn off in liquid form via line 5, subcooled in heat exchanger 18 and partly discharged as a liquid product via line 8.
- the other part of the nitrogen from the pressure stage 3 is fed via line 9 as a return to the medium pressure stage 4.
- Another liquid fraction is discharged via line 7 from pressure stage 3 and fed to low pressure stage 4.
- liquid oxygen (line 14), gaseous pure nitrogen (line 15) and impure nitrogen (line 16) are removed and the nitrogen streams are additionally heated in the main heat exchanger 17, in the heat exchanger 18.
- part (line 21) of the air in line 1 can be condensed in heat exchange 20 with oxygen 14 from the bottom of medium pressure stage 4.
- the liquid 14 from the sump of the medium pressure stage 4 is brought to high pressure by means of a pump 19 and at which Heat exchange in the condenser 20 partially evaporates.
- the partially condensed air 22 is introduced into the pressure stage 3 above the first feed point (line 1).
- the vaporized portion of the oxygen is removed via line 23 and warmed (17). Another part of the oxygen is withdrawn via line 42 as a liquid product stream.
- part of the impure nitrogen in line 16 is drawn off from the main heat exchanger 17 via line 30 at an average temperature of approximately 110 to 210 K, preferably 135 to 185 K, and in a pressure-reducing turbine 31 to perform a pressure of 2.6 to 1 , 4 bar, preferably about 2.0 bar relaxed.
- the expanded nitrogen is again conducted via line 32 to the cold end of the main heat exchanger 17 and warmed to approximately ambient temperature. He releases the cold obtained during relaxation to air to be separated in line 1.
- the pure nitrogen is required under a pressure higher than medium pressure level 4, it can be compressed after it has been heated. This is generally done in several compressor stages 40, 41. As a rule, each is behind Stage 40, 41 the heat of compression removed (not shown in the drawing) water cooler.
- the additional nitrogen condenses at the top and thereby evaporates liquid in the bottom of the medium pressure stage 4. In liquid form, it is additionally removed via line 5 and fed as a return to the medium pressure column. A correspondingly increased amount of nitrogen is then drawn off via line 15, warmed (18, 17) and compressed in the compressor stage 40, so that the amplification circuit closes and the balances of the heat exchangers 18 and 17 are balanced.
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)
Claims (7)
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE3905521 | 1989-02-23 | ||
DE19893905521 DE3905521A1 (de) | 1989-02-23 | 1989-02-23 | Verfahren und vorrichtung zur luftzerlegung durch rektifikation |
EP89113815 | 1989-07-26 | ||
EP19890113815 EP0383994A3 (fr) | 1989-02-23 | 1989-07-26 | Procédé et dispositif de rectification d'air |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0384483A2 EP0384483A2 (fr) | 1990-08-29 |
EP0384483A3 EP0384483A3 (en) | 1990-11-07 |
EP0384483B1 true EP0384483B1 (fr) | 1992-07-22 |
Family
ID=25878076
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19890113815 Withdrawn EP0383994A3 (fr) | 1989-02-23 | 1989-07-26 | Procédé et dispositif de rectification d'air |
EP90103572A Expired - Lifetime EP0384483B1 (fr) | 1989-02-23 | 1990-02-23 | Procédé et dispositif de rectification d'air |
Family Applications Before (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19890113815 Withdrawn EP0383994A3 (fr) | 1989-02-23 | 1989-07-26 | Procédé et dispositif de rectification d'air |
Country Status (6)
Country | Link |
---|---|
US (1) | US5036672A (fr) |
EP (2) | EP0383994A3 (fr) |
JP (1) | JPH02245201A (fr) |
CN (1) | CN1025068C (fr) |
AU (1) | AU618659B2 (fr) |
DE (1) | DE59000211D1 (fr) |
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DE3913880A1 (de) * | 1989-04-27 | 1990-10-31 | Linde Ag | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
FR2670278B1 (fr) * | 1990-12-06 | 1993-01-22 | Air Liquide | Procede et installation de distillation d'air en regime variable de production d'oxygene gazeux. |
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FR2681416B1 (fr) * | 1991-09-13 | 1993-11-19 | Air Liquide | Procede de refroidissement d'un gaz dans une installation d'exploitation de gaz de l'air, et installation. |
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FR2739439B1 (fr) * | 1995-09-29 | 1997-11-14 | Air Liquide | Procede et installation de production d'un gaz sous pression par distillation cryogenique |
US5799508A (en) * | 1996-03-21 | 1998-09-01 | Praxair Technology, Inc. | Cryogenic air separation system with split kettle liquid |
US5682762A (en) * | 1996-10-01 | 1997-11-04 | Air Products And Chemicals, Inc. | Process to produce high pressure nitrogen using a high pressure column and one or more lower pressure columns |
JP3527609B2 (ja) * | 1997-03-13 | 2004-05-17 | 株式会社神戸製鋼所 | 空気分離方法および装置 |
WO1998053258A1 (fr) * | 1997-05-21 | 1998-11-26 | Caifeng Ouyang | Conditionneur d'air pour enrichir l'air en oxygene |
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 |
US5878597A (en) * | 1998-04-14 | 1999-03-09 | Praxair Technology, Inc. | Cryogenic rectification system with serial liquid air feed |
US5901578A (en) * | 1998-05-18 | 1999-05-11 | Praxair Technology, Inc. | Cryogenic rectification system with integral product boiler |
JP2002541421A (ja) * | 1999-04-05 | 2002-12-03 | レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・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 | 可変生産能力の流体混合物分離装置及びプロセス |
WO2003006890A1 (fr) * | 2001-07-13 | 2003-01-23 | Ebara Corporation | Appareil de climatisation deshumidifiant |
CN100436989C (zh) * | 2004-01-29 | 2008-11-26 | 宝山钢铁股份有限公司 | 一种用全低压空分装置制取高纯氧的方法 |
JP4460975B2 (ja) * | 2004-08-20 | 2010-05-12 | 三菱重工業株式会社 | 海水処理方法および海水処理装置 |
US7421856B2 (en) * | 2005-06-17 | 2008-09-09 | Praxair Technology, Inc. | Cryogenic air separation with once-through main condenser |
EP2087301B1 (fr) * | 2006-11-07 | 2018-11-14 | Tiax LLC | système et méthode de déshumidification |
CN101886871B (zh) * | 2010-08-04 | 2012-08-08 | 四川空分设备(集团)有限责任公司 | 一种空气分离制取压力氧气的方法及装置 |
US20130139547A1 (en) * | 2011-12-05 | 2013-06-06 | Henry Edward Howard | Air separation method and apparatus |
CN104833174B (zh) * | 2015-05-26 | 2017-08-11 | 杭州杭氧股份有限公司 | 一种带压辅助氧塔低能耗生产带压低纯氧和高纯氧产品的装置及方法 |
CN105066587A (zh) * | 2015-09-16 | 2015-11-18 | 开封空分集团有限公司 | 深冷分离及生产低纯度氧、高纯度氧和氮的装置及方法 |
EP3179186A1 (fr) * | 2015-12-07 | 2017-06-14 | Linde Aktiengesellschaft | Procede de production d'un produit comprime riche en oxygene, gazeux et liquide dans une installation de decomposition de l'air et installation de decomposition de l'air |
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GB2192407B (en) * | 1986-07-07 | 1990-12-19 | Metal Box Plc | Electro-coating apparatus and method |
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US4842625A (en) * | 1988-04-29 | 1989-06-27 | Air Products And Chemicals, Inc. | Control method to maximize argon recovery from cryogenic air separation units |
-
1989
- 1989-07-26 EP EP19890113815 patent/EP0383994A3/fr not_active Withdrawn
-
1990
- 1990-01-23 CN CN90100335A patent/CN1025068C/zh not_active Expired - Fee Related
- 1990-02-21 AU AU49960/90A patent/AU618659B2/en not_active Ceased
- 1990-02-22 US US07/483,143 patent/US5036672A/en not_active Expired - Fee Related
- 1990-02-22 JP JP2042309A patent/JPH02245201A/ja active Pending
- 1990-02-23 EP EP90103572A patent/EP0384483B1/fr not_active Expired - Lifetime
- 1990-02-23 DE DE9090103572T patent/DE59000211D1/de not_active Expired - Fee Related
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DE102007031765A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren zur Tieftemperaturzerlegung von Luft |
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EP2015012A2 (fr) | 2007-07-07 | 2009-01-14 | Linde Aktiengesellschaft | Procédé pour la séparation cryogénique d'air |
EP2015013A2 (fr) | 2007-07-07 | 2009-01-14 | Linde Aktiengesellschaft | Procédé et dispositif de production d'un gaz sous pression par séparation cryogénique d'air |
DE102009034979A1 (de) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff |
EP2312248A1 (fr) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Procédé et dispositif de production d'oxygène sous pression et de crypton/xénon |
EP2458311A1 (fr) | 2010-11-25 | 2012-05-30 | Linde Aktiengesellschaft | Procédé et dispositif de production d'un produit d'impression gazeux par décomposition à basse température d'air |
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 |
EP2466236A1 (fr) | 2010-11-25 | 2012-06-20 | Linde Aktiengesellschaft | Procédé de production d'un produit d'impression gazeux par décomposition à basse température de l'air |
EP2520886A1 (fr) | 2011-05-05 | 2012-11-07 | Linde AG | Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air |
EP2551619A1 (fr) | 2011-07-26 | 2013-01-30 | Linde Aktiengesellschaft | Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air |
EP2568242A1 (fr) | 2011-09-08 | 2013-03-13 | Linde Aktiengesellschaft | Procédé et dispositif destinés à la production d'acier |
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WO2014154339A2 (fr) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Procédé de séparation d'air et installation de séparation d'air |
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EP2963369A1 (fr) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Procede et dispositif cryogeniques de separation d'air |
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Also Published As
Publication number | Publication date |
---|---|
CN1025068C (zh) | 1994-06-15 |
EP0384483A3 (en) | 1990-11-07 |
JPH02245201A (ja) | 1990-10-01 |
AU4996090A (en) | 1990-08-30 |
EP0383994A2 (fr) | 1990-08-29 |
CN1045173A (zh) | 1990-09-05 |
AU618659B2 (en) | 1992-01-02 |
EP0384483A2 (fr) | 1990-08-29 |
DE59000211D1 (de) | 1992-08-27 |
EP0383994A3 (fr) | 1990-11-07 |
US5036672A (en) | 1991-08-06 |
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