EP1209431A1 - Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff - Google Patents
Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff Download PDFInfo
- Publication number
- EP1209431A1 EP1209431A1 EP01127958A EP01127958A EP1209431A1 EP 1209431 A1 EP1209431 A1 EP 1209431A1 EP 01127958 A EP01127958 A EP 01127958A EP 01127958 A EP01127958 A EP 01127958A EP 1209431 A1 EP1209431 A1 EP 1209431A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- pressure column
- low pressure
- nitrogen
- oxygen
- liquid
- 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.)
- Granted
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Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04357—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 and comprising a gas work expansion loop
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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
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
Definitions
- the invention relates to a process for the production of oxygen and nitrogen Cryogenic air separation in a rectification system that includes a pressure column and has a low pressure column, with the process feed air into the pressure column initiated, an oxygen-containing liquid fraction removed from the pressure column and is fed into the low pressure column, gaseous nitrogen from the Low pressure column in a top condenser by indirect heat exchange with an evaporating cooling fluid is at least partially condensed Low pressure column and / or a nitrogen product stream removed from the pressure column and an oxygen product stream is discharged from the low pressure column.
- EP 1022530 A1 Methods with head cooling of the low pressure column are known from EP 1022530 A1, WO 9819122 or EP 811816 A2 known.
- a process of the type mentioned at the outset is shown in EP 955509 A1.
- the invention has for its object a method of the type mentioned and specify a corresponding device that is particularly economical work.
- cooling fluid for the top condenser Low pressure column is formed by an intermediate liquid, which is from a Intermediate point of the low pressure column is withdrawn.
- this cooling liquid is caused by the bottom liquid Pressure column formed.
- the invention has two advantages.
- the composition of the cooling fluid can be chosen so that the Product yield, in particular the oxygen yield is increased.
- the cooling fluid has a lower pressure so that it is before it is introduced into the Head capacitor only has to be throttled relatively slightly; corresponding the flash gas losses are lower.
- the intermediate liquid, which is used as cooling fluid in the top condenser, from an intermediate point is subtracted, which is above the point at which the oxygen-containing liquid Fraction from the pressure column is fed into the low pressure column. Between there are, for example, 10 to 20 theoretical floors.
- the process can use liquid nitrogen from or from the low pressure column Top condenser removed and discharged as a liquid nitrogen product.
- the process preferably has a nitrogen cycle on.
- cycle nitrogen becomes gaseous from the upper area of the pressure column withdrawn and compressed in a circuit compressor, a first partial flow of compressed cycle nitrogen is relieved of work and a second Partial stream of the compressed cycle nitrogen liquefied and into the rectification system fed back and / or taken as a further liquid nitrogen product.
- Such a cycle can also be carried out without oxygen production, for example with Use of the bottom liquid from low pressure column or pressure column as cooling fluid in the top condenser of the low pressure column.
- the liquefied circulating nitrogen can be one of the Columns of the rectification system are fed, preferably the pressure column. The the corresponding amount can then be a liquid nitrogen and / or oxygen product be withdrawn from the rectification system.
- Top nitrogen from the pressure column is liquefied in a main condenser. That included generated condensate is at least partially, preferably largely, as Return to the pressure column abandoned. Another part of the condensate can be on top introduced into the low pressure column and / or immediately as a liquid nitrogen product subtracted from.
- the circuit can be designed as a two or more turbine system by one third partial stream of compressed cycle nitrogen independent of the first Partial stream is relaxed while working.
- the invention also relates to a device according to claim 8 or 9.
- An oxygen-containing liquid fraction (8) from the bottom of the pressure column is in one Cooled subcooler 9 and via line 10 at an intermediate point in the Low pressure column 5 initiated.
- gaseous top nitrogen is converted into a first part 11 in Main condenser 6 at least partially, preferably completely liquefied.
- the the condensate 12 produced thereby becomes a first part 13 as a return flow onto the head the pressure column 4 abandoned.
- a second part 14 of the main capacitor 6 condensed nitrogen 11 is introduced into the low pressure column.
- liquid nitrogen 19 is drawn off and on Separation of flash gas in a separator 20 via line 21 as a liquid Withdrawn nitrogen product and introduced a tank 22.
- the flash gas 23 is the Residual gas 16 admixed.
- the residual mixture 24 is in the subcoolers 25, 9 and Main heat exchanger 2 warmed up and finally via line 27 into the atmosphere blown off and / or as a regeneration gas for the device, not shown Purification of the feed air used.
- a second partial stream of the compressed cycle nitrogen is passed through line 42 two series-connected post-compressors 43, 45, each of which has an after-cooler 44, 46 follows.
- the second partial flow continues to the first circuit heat exchanger 37 (Line 47), is further cooled in the second circuit heat exchanger 40 and finally liquefied or - in the third circuit heat exchanger 48 supercritical pressure - pseudo-liquefied.
- a third partial flow of the compressed cycle nitrogen is combined with the second partial flow through the post-compressors 43, 45 and the first and second Circuit heat exchanger 37, 40 out.
- the third substream 56 becomes one cold turbine 57 led.
- the work-relieved, relaxed third partial flow overflows Line 58 through the three circuit heat exchangers 48, 40, 37 to the entry of Circuit compressor back.
- the cold parts of the system are in an insulating housing (cold box) 64 arranged.
- the bottom liquid 8, 10 from the pressure column 4th also be introduced into the low pressure column 5 directly above the sump, the simultaneously represents the evaporation space of the main condenser 6.
- the cooling fluid 15 for the top condenser 7 either from the bottom of the Low pressure column withdrawn or directly from the pressure column sump liquid 10 are branched off.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Catalysts (AREA)
Abstract
Description
WO 9819122 oder EP 811816 A2 bekannt. Ein Prozess der eingangs genannten Art ist in EP 955509 A1 gezeigt.
Claims (9)
- Verfahren zur Erzeugung von Sauerstoff und Stickstoff durch Tieftemperaturzerlegung von Luft in einem Rektifiziersystem, das eine Drucksäule (4) und eine Niederdrucksäule (5) aufweist, wobei bei dem Verfahren Einsatzluft (1, 3) in die Drucksäule (4) eingeleitet, eine sauerstoffhaltige flüssige Fraktion (8, 10) aus der Drucksäule (4) entnommen und in die Niederdrucksäule (5) eingespeist wird, gasförmiger Stickstoff (17) aus der Niederdrucksäule (5) in einem Kopfkondensator (7) durch indirekten Wärmeaustausch mit einem verdampfenden Kühlfluid (15) mindestens teilweise kondensiert wird, der Niederdrucksäule (5) und/oder der Drucksäule (4) ein Stickstoff-Produktstrom (19) entnommen und aus der Niederdrucksäule (5) ein Sauerstoff-Produktstrom (61, 62, 63) flüssig und/oder gasförmig abgeführt wird, dadurch gekennzeichnet, dass das Kühlfluid für den Kopfkondensator (7) der Niederdrucksäule (5) durch eine Zwischenflüssigkeit (15) gebildet wird, die von einer Zwischenstelle der Niederdrucksäule (5) abgezogen wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Zwischenflüssigkeit (15) von einer Zwischenstelle abgezogen wird, die oberhalb der Stelle liegt, an der die sauerstoffhaltige flüssige Fraktion (8, 10) aus der Drucksäule (4) in die Niederdrucksäule (5) eingespeist wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass flüssiger Stickstoff (19) aus der Niederdrucksäule (5) oder aus deren Kopfkondensator (7) abgezogen und als flüssiges Stickstoffprodukt (22) abgeführt wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass Kreislauf-Stickstoff (28, 29, 30, 31, 32) gasförmig aus dem oberen Bereich der Drucksäule (4) abgezogen und in einem Kreislauf-Verdichter (33) verdichtet wird, wobei ein erster Teilstrom (36) des verdichteten Kreislauf-Stickstoffs (35) arbeitsleistend (38) entspannt wird und ein zweiter Teilstrom (42, 47, 50) des verdichteten Kreislauf-Stickstoffs (35) verflüssigt und in das Rektifiziersystem zurückgespeist (52) und/oder als weiteres flüssiges Stickstoffprodukt entnommen wird.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass Kopfstickstoff (11) aus der Drucksäule (4) in einem Hauptkondensator (6) verflüssigt wird.
- Verfahren nach Anspruch 5, dadurch gekennzeichnet, dass das im Hauptkondensator gebildete Kondensat (12) mindestens zum Teil (14) in die Niederdrucksäule eingeleitet wird.
- Verfahren nach Anspruch 5 oder 6, dadurch gekennzeichnet, dass das im Hauptkondensator gebildete Kondensat (12) mindestens zum Teil als flüssiges Stickstoffprodukt (22) abgezogen wird.
- Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff durch Tieftemperaturzerlegung von Luft mit einem Rektifiziersystem, das eine Drucksäule (4) und eine Niederdrucksäule (5) aufweist, mit einer Einsatzleitung (1, 3) zum Einleiten von Einsatzluft in die Drucksäule (4), mit einer Flüssigkeitsleitung (8, 10) zum Überleiten einer sauerstoffhaltigen flüssigen Fraktion aus der Drucksäule (4) in die Niederdrucksäule (5), einem Kopfkondensator (7), dessen Verflüssigungsraum mit dem oberen Bereich der Niederdrucksäule (5) verbunden (17, 18) ist und dessen Verdampfungsraum mit einer Kühlmittelleitung (15) zum Einleiten eines Kühlfluids verbunden ist, mit einer Stickstoff-Produktleitung (19), die mit der Niederdrucksäule (5) und/oder mit der Drucksäule (4) verbunden ist und mit einer Sauerstoff-Produktleitung (61, 62, 63), die mit der Niederdrucksäule (5) verbunden ist, dadurch gekennzeichnet, dass die Kühlmittelleitung (15) mit einer Zwischenstelle der Niederdrucksäule (5) verbunden ist.
- Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, dass die Zwischenstelle, an der die Kühlmittelleitung (15) mit der Niederdrucksäule (5) verbunden ist, oberhalb der Stelle liegt, an der die Flüssigkeitsleitung (8, 10) zum Überleiten einer sauerstoffhaltigen flüssigen Fraktion aus der Drucksäule (4) in die Niederdrucksäule (5) einmündet.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10058332A DE10058332A1 (de) | 2000-11-24 | 2000-11-24 | Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff |
DE10058332 | 2000-11-24 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1209431A1 true EP1209431A1 (de) | 2002-05-29 |
EP1209431B1 EP1209431B1 (de) | 2004-06-09 |
Family
ID=7664493
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP01127958A Expired - Lifetime EP1209431B1 (de) | 2000-11-24 | 2001-11-23 | Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff |
Country Status (4)
Country | Link |
---|---|
US (1) | US6490884B2 (de) |
EP (1) | EP1209431B1 (de) |
AT (1) | ATE268893T1 (de) |
DE (2) | DE10058332A1 (de) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20150168058A1 (en) * | 2013-12-17 | 2015-06-18 | L'air Liquide, Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Apparatus for producing liquid nitrogen |
US20150168057A1 (en) * | 2013-12-17 | 2015-06-18 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for producing liquid nitrogen |
CN109676367A (zh) * | 2018-12-28 | 2019-04-26 | 乔治洛德方法研究和开发液化空气有限公司 | 一种热交换器组件及装配所述热交换器组件的方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4832719A (en) * | 1987-06-02 | 1989-05-23 | Erickson Donald C | Enhanced argon recovery from intermediate linboil |
US5137559A (en) * | 1990-08-06 | 1992-08-11 | Air Products And Chemicals, Inc. | Production of nitrogen free of light impurities |
WO1998019122A1 (de) * | 1996-10-30 | 1998-05-07 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung von druckstickstoff |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4439220A (en) * | 1982-12-02 | 1984-03-27 | Union Carbide Corporation | Dual column high pressure nitrogen process |
US5006139A (en) * | 1990-03-09 | 1991-04-09 | Air Products And Chemicals, Inc. | Cryogenic air separation process for the production of nitrogen |
US5697229A (en) * | 1996-08-07 | 1997-12-16 | Air Products And Chemicals, Inc. | Process to produce nitrogen using a double column plus an auxiliary low pressure separation zone |
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 |
EP0955509B1 (de) * | 1998-04-30 | 2004-12-22 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff |
DE19902255A1 (de) | 1999-01-21 | 2000-07-27 | Linde Tech Gase Gmbh | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff |
-
2000
- 2000-11-24 DE DE10058332A patent/DE10058332A1/de not_active Withdrawn
-
2001
- 2001-11-23 AT AT01127958T patent/ATE268893T1/de not_active IP Right Cessation
- 2001-11-23 DE DE50102525T patent/DE50102525D1/de not_active Expired - Fee Related
- 2001-11-23 EP EP01127958A patent/EP1209431B1/de not_active Expired - Lifetime
- 2001-11-23 US US09/990,365 patent/US6490884B2/en not_active Expired - Fee Related
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4832719A (en) * | 1987-06-02 | 1989-05-23 | Erickson Donald C | Enhanced argon recovery from intermediate linboil |
US5137559A (en) * | 1990-08-06 | 1992-08-11 | Air Products And Chemicals, Inc. | Production of nitrogen free of light impurities |
WO1998019122A1 (de) * | 1996-10-30 | 1998-05-07 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung von druckstickstoff |
Also Published As
Publication number | Publication date |
---|---|
US20020062658A1 (en) | 2002-05-30 |
DE10058332A1 (de) | 2002-05-29 |
EP1209431B1 (de) | 2004-06-09 |
DE50102525D1 (de) | 2004-07-15 |
US6490884B2 (en) | 2002-12-10 |
ATE268893T1 (de) | 2004-06-15 |
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