EP0955509B1 - Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff - Google Patents
Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff Download PDFInfo
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- EP0955509B1 EP0955509B1 EP98116041A EP98116041A EP0955509B1 EP 0955509 B1 EP0955509 B1 EP 0955509B1 EP 98116041 A EP98116041 A EP 98116041A EP 98116041 A EP98116041 A EP 98116041A EP 0955509 B1 EP0955509 B1 EP 0955509B1
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- Prior art keywords
- pressure column
- low
- liquid
- fraction
- nitrogen
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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
- 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
- F25J3/04084—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 nitrogen
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—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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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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- F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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- 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
- F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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- 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
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- 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
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- F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
- F25J2215/44—Ultra high purity nitrogen, i.e. generally less than 1 ppb impurities
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
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- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/42—One fluid being nitrogen
Definitions
- the invention relates to a method and a device for obtaining high-purity oxygen according to L the preamble of claim 1 respectively 9.
- the invention has for its object in a method of the beginning mentioned type to obtain a high-purity oxygen product, in particular in addition to a pressure nitrogen product.
- This object is achieved in that the oxygen-containing liquid fraction, which in the low pressure column is fed, at least one theoretical or practical soil above the sump of the pressure column is taken from that Bottom liquid of the pressure column in the evaporation space of the top condenser the low pressure column is passed and that from the lower area of the Low pressure column a high purity oxygen product is removed.
- the solution according to the invention manages without additional rectification columns and uses the lower part of the pressure column or an additional one Mass transfer section in the lower section of the pressure column for the separation of the less volatile impurities.
- the oxygen-containing liquid Fraction that is fed into the low pressure column not from the bottom of the Pressure column deducted, but from one above the sump, in particular intermediate point located above the feed of the feed air.
- the information in practical soil numbers apply; if pack, Packings or combinations of different types of mass transfer elements are used, the information in theoretical plate numbers are to be used.
- the high-purity oxygen can be liquid and / or gaseous be drawn off directly at the bottom of the low pressure column.
- the operating pressures of the columns can be in the inventive method for example 6 to 20, preferably 7 to 16 bar in the pressure column and for example 3 to 8, preferably 3 to 6 bar in the low pressure column.
- the top condenser of the low pressure column is at least partially Bottom liquid of the pressure column operated as a refrigerant.
- Return for the pressure column is usually generated by a condenser-evaporator, over which the head the pressure column and the sump of the low pressure column in heat exchanging Connect.
- a residual fraction of one Intermediate point of the low pressure column are deducted.
- the remaining fraction will preferably formed by an impure nitrogen fraction and above the point of Feeding of the oxygen-containing liquid fraction from the pressure column taken.
- the turbine exhaust gas preferably fed to the pressure column or removed from the process, for example by mixing with another residual stream.
- the relaxed air in any case, must not be fed into the low pressure column, as this is a new one Contamination by less volatile components would cause.
- the high-purity oxygen product can be compressed at one pressure by means of internal compression brought, which is higher than the low pressure column pressure by at least one Part of the oxygen product is led out of the low pressure column in liquid form and below a pressure that is higher than the operating pressure of the low pressure column evaporates becomes.
- a heating medium during evaporation for example, can be correspondingly high compressed air can be used.
- a nitrogen fraction is liquid the low pressure column or its top condenser is removed and the pressure the nitrogen fraction in the liquid state is increased to a value higher than is the operating pressure of the low pressure column.
- more gaseous Nitrogen can be obtained under a pressure that is higher than the operating pressure of the Is low pressure column.
- the liquid pressurized nitrogen can be in the Pressure column returned or bypassing the pressure column in indirect Heat exchange can be evaporated.
- the nitrogen fraction is removed from at least one theoretical or practical base below the top of the low pressure column and at least part of the liquid nitrogen fraction is evaporated by indirect heat exchange under a pressure which is higher than the operating pressure of the low pressure column dissipated as a high-purity pressure nitrogen product.
- a gas from the upper area of the pressure column and / or a gas from the lower area of the low-pressure column can be used, for example, as the heating means in the indirect heat exchange. Details of this heat exchange step can be found in the older patent applications DE 19735154 and WO 98/19122.
- High-purity pressure nitrogen is understood to mean, for example, nitrogen with a total contamination of 1 ppm or less, in particular between 1 ppm and 10 -3 ppb and under a superatmospheric pressure, in particular above 3 bar.
- the section of the section above the removal of the nitrogen fraction Low pressure column is used to separate volatile impurities.
- This section can be formed from packs or packing, the Mass transfer effect corresponds to or from at least one theoretical floor one or more conventional rectification trays, for example sieve trays. He can be from up to 10, preferably from 2 to 5 theoretical or practical floors exist.
- the more volatile impurities are called gaseous residual fraction from the liquefaction space of the top condenser Low pressure column deducted.
- the invention also relates to a device for extracting high-purity Oxygen according to claims 9 and 10, respectively.
- compressed and cleaned air 1 is combined in one Main heat exchanger 2 cooled and a pressure column 4 under a pressure of 14 bar supplied (3).
- the rectification system also has a low pressure column 5 on, which is operated at a pressure of 5 bar and with the pressure column via a common condenser-evaporator (main condenser) 6 in heat-exchanging Connection is established.
- Part 8 of the nitrogen 7 removed at the top of the pressure column is liquefied in the main condenser 6 and via lines 9 and 10 as a return placed on the pressure column.
- the main capacitor 6 can be connected via line 57 Residual steam, which is particularly volatile impurities such as helium, neon and / or contains hydrogen.
- An oxygen-containing liquid Fraction 411 from the pressure column is after subcooling 15 in the low pressure column 5 throttled (412).
- the low pressure column 5 has a top condenser 17, in the Liquefaction space of gaseous nitrogen 18 from the top of the low pressure column 5 condensed; the condensate 19 is at least partially in the low pressure column returned.
- the top condenser 17 of the low pressure column 5 is not or not operated exclusively with sump liquid of the low pressure column (see booth the technology according to DE 3528374 A1), but with sump liquid 457 of the pressure column 4.
- the oxygen-containing liquid fraction 411, which is in the low pressure column 5 throttled (412) comes from an intermediate point above one additional mass transfer section 458 in the lower region of the pressure column.
- the additional mass transfer section 458 has five theoretical in the example Floors on.
- In the bottom of the low pressure column 5 is a high purity oxygen product produced with a purity of 99.99 vol% and liquid (459) and / or gaseous (460, 461) under the pressure of the low pressure column.
- About a residual fraction (Impure nitrogen fraction) 462, argon is discharged from the low-pressure column 5.
- the impure nitrogen is preferably with the remaining streams 31, 57, 51 and 53 united.
- the embodiment also serves to obtain high-purity Pressure nitrogen.
- a mass transfer section 54 which in the Example has three theoretical plates, some of which in the pressure column 4th flowing down liquid taken as a liquid raw nitrogen fraction 55 and in throttled the head of the low pressure column 5 (56).
- part of the gaseous nitrogen 7 can be removed from the head the pressure column in the main heat exchanger 2 warmed and as a further print product lower purity can be obtained (not shown). In this case it is possible on the transfer of liquid nitrogen 55 from the pressure column 4 in the Low pressure column 5 to do without.
- part of the liquid nitrogen fraction 20 can be removed from the low pressure column can be obtained as a liquid product 30.
- cold is caused by relaxation 33 of the residual gas 432 is generated.
- the one obtained in the relaxation machine 33 Mechanical energy can be used, for example, to recompress the Product evaporator 23 vaporized pressure nitrogen product 24 or Pressure increase in the residual gas upstream of the expansion machine 33 is used are, preferably by direct mechanical coupling of Relaxation machine 33 and a corresponding compressor. Its cheap, when the residual vapors 57, 51 and 53 are also introduced into the residual gas line 432 become.
- the main heat exchanger 2 serves as Product evaporator for the high-purity oxygen, alternatively, a separate one Product evaporator may be provided. After (further) warming up in the Main heat exchanger 2, the pressurized oxygen product is withdrawn at 564.
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- 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)
Description
- Restgas aus dem Verdampfungsraum des Kopfkondensators der Niederdrucksäule
- Dampf aus dem mittleren Bereich der Niederdrucksäule (beispielsweise obige Restfraktion)
- Teilstrom der Einsatzluft
- Stickstoff aus der Drucksäule oder aus der Niederdrucksäule
- Figur 1
- ein erstes Ausführungsbeispiel der Erfindung mit gasförmiger und/oder flüssiger Entnahme des hochreinen Sauerstoffprodukts aus der Niederdrucksäule und
- Figur 2
- eine zweites Ausführungsbeispiel mit Innenverdichtung des Sauerstoffprodukts.
Claims (10)
- Verfahren zur Gewinnung von hochreinem Sauerstoff durch Tieftemperaturzerlegung von Luft in einem Rektifiziersystem, das eine Drucksäule (4) und eine Niederdrucksäule (5) aufweist, wobei bei dem VerfahrenEinsatzluft (1, 3) in die Drucksäule (4) eingeleitet wird,eine sauerstoffhaltige flüssige Fraktion (411) aus der Drucksäule (4) entnommen und in die Niederdrucksäule (5) eingespeist wird undgasförmiger Stickstoff (18) aus der Niederdrucksäule (5) in einem Kopfkondensator (17) durch indirekten Wärmeaustausch mit einer verdampfenden Flüssigkeit (457) mindestens teilweise kondensiert wird,die sauerstoffhaltige flüssige Fraktion (411), die in die Niederdrucksäule (5) eingespeist wird, mindestens einen theoretischen oder praktischen Boden oberhalb des Sumpfs der Drucksäule (4) entnommen wird, daßmindestens ein Teil der Sumpfflüssigkeit (457) der Drucksäule (4) in den Verdampfungsraum des Kopfkondensators (17) der Niederdrucksäule (5) geleitet wird und daßaus dem unteren Bereich der Niederdrucksäule (5) ein hochreines Säuerstoffprodukt (459, 460, 461, 563, 564) entnommen wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß eine Restfraktion (462) von einer Zwischenstelle der Niederdrucksäule abgezogen wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß eine gasförmige Fraktion (31) aus dem Verdampfungsraum des Kopfkondensators (17) der Niederdrucksäule und/oder eine gasförmige Fraktion (462) aus der Niederdrucksäule arbeitsleistend entspannt (33) werden.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß Luft arbeitsleistend entspannt wird.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß mindestens ein Teil (563) des hochreinen Sauerstoffprodukts flüssig aus der Niederdrucksäule (5) herausgeführt und unter einem Druck, der höher als der Betriebsdruck der Niederdrucksäule (5) ist, verdampft (2) wird.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß eine Stickstofffraktion (20) flüssig aus der Niederdrucksäule (5) oder deren Kopfkondensator (17) entnommen wird und der Druck der Stickstofffraktion (20) in flüssigem Zustand auf einen Wert erhöht (21) wird, der höher als der Betriebsdruck der Niederdrucksäule (5) ist.
- Verfahren nach Anspruch 6, dadurch gekennzeichnet, daß die flüssige Stickstofffraktion (20) mindestens einen theoretischen oder praktischen Boden unterhalb des Kopfs der Niederdrucksäule entnommen und mindestens ein Teil der flüssigen Stickstofffraktion (22) unter einem Druck, der höher als der Betriebsdruck der Niederdrucksäule (5) ist, durch indirekten Wärmeaustausch (23) verdampft und als hochreines Druckstickstoffprodukt (24, 25) abgeführt wird.
- Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß der Drucksäule (4) mindestens einen theoretischen oder praktischen Boden unterhalb des Kopfs eine flüssige Rohstickstofffraktion (55) entnommen und an einer Stelle auf die Niederdrucksäule (5) aufgegeben wird, die mindestens einen theoretischen oder praktischen Boden oberhalb der Stelle der Entnahme der flüssigen Stickstofffraktion (20) liegt.
- Vorrichtung zur Gewinnung von hochreinem Sauerstoff durch Tieftemperaturzerlegung von Luft mit einem Rektifiziersystem, das eine Drucksäule (4) und eine Niederdrucksäule (5) aufweist, und miteiner Einsatzluftleitung (1, 3), die in die Drucksäule (4) führt,einer Rohsauerstoffleitung (411) zur Einleitung einer sauerstoffhaltigen flüssigen Fraktion aus der Drucksäule (4) in die Niederdrucksäule (5) und miteinem Kopfkondensator (17) zur mindestens teilweisen Kondensation von gasförmigem Stickstoff (18) aus der Niederdrucksäule (5) durch indirekten Wärmeaustausch mit einer verdampfenden Flüssigkeit (457),einen Stoffaustauschabschnitt (458), der in der Drucksäule (4) unterhalb der Rohsauerstoffleitung (411) und insbesondere oberhalb der Einsatzluftleitung (3) angeordnet ist und mindestens einen theoretischen oder praktischen Boden aufweist,durch eine Sumpfflüssigkeitsleitung (457) zur Einleitung der Sumpfflüssigkeit der Drucksäule (4) in den Verdampfurtgsraum des Kopfkondensators (17) der Niederdrucksäule (5) und durcheine Produktleitung zur Entnahme von hochreinem Sauerstoffprodukt (459, 460, 461, 563, 564) aus dem unteren Bereich der Niederdrucksäule (5).
- Vorrichtung nach Anspruch 9, gekennzeichnet durch eine Restfraktionsleitung (462, 432), die mit einer Zwischenstelle der Niederdrucksäule (5) verbunden ist.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19819338 | 1998-04-30 | ||
DE19819338A DE19819338A1 (de) | 1997-10-30 | 1998-04-30 | Verfahren und Vorrichtung zur Gewinnung von hochreinem Druckstickstoff |
Publications (2)
Publication Number | Publication Date |
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EP0955509A1 EP0955509A1 (de) | 1999-11-10 |
EP0955509B1 true EP0955509B1 (de) | 2004-12-22 |
Family
ID=7866294
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP98116041A Expired - Lifetime EP0955509B1 (de) | 1998-04-30 | 1998-08-25 | Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff |
Country Status (3)
Country | Link |
---|---|
US (1) | US6196022B1 (de) |
EP (1) | EP0955509B1 (de) |
JP (1) | JP4450886B2 (de) |
Families Citing this family (28)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6330812B2 (en) * | 2000-03-02 | 2001-12-18 | Robert Anthony Mostello | Method and apparatus for producing nitrogen from air by cryogenic distillation |
DE10058332A1 (de) * | 2000-11-24 | 2002-05-29 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff |
EP1300640A1 (de) * | 2001-10-04 | 2003-04-09 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von hoch reinem Stickstoff durch Tieftemperaturzerlegung von Luft |
US6568208B1 (en) * | 2002-05-03 | 2003-05-27 | Air Products And Chemicals, Inc. | System and method for introducing low pressure reflux to a high pressure column without a pump |
DE10245379A1 (de) * | 2002-09-28 | 2004-04-08 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von hoch reinem Stickstoff |
FR2853405A1 (fr) * | 2003-04-01 | 2004-10-08 | Air Liquide | Procede et installation de separation d'air par distillation cryogenique |
DE102007031759A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft |
DE102007031765A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren zur Tieftemperaturzerlegung von Luft |
DE102009034979A1 (de) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff |
EP2312248A1 (de) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Verfahren und Vorrichtung Gewinnung von Drucksauerstoff und Krypton/Xenon |
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 |
US8991209B2 (en) * | 2010-12-13 | 2015-03-31 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for producing high-pressure nitrogen |
EP2520886A1 (de) | 2011-05-05 | 2012-11-07 | Linde AG | Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102011112909A1 (de) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Stahl |
EP2600090B1 (de) | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft |
DE102011121314A1 (de) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
EP2662654A1 (de) * | 2012-05-07 | 2013-11-13 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Verfahren und Vorrichtung zur Abscheidung von Luft durch kryogene Destillation |
DE102012017488A1 (de) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren |
WO2014154339A2 (de) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Verfahren zur luftzerlegung und luftzerlegungsanlage |
EP2784420A1 (de) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Verfahren zur Luftzerlegung und Luftzerlegungsanlage |
EP2801777A1 (de) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Luftzerlegungsanlage mit Hauptverdichterantrieb |
DE102013017590A1 (de) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage |
EP2963371B1 (de) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft |
EP2963369B1 (de) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
EP2963367A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch |
PL2963370T3 (pl) | 2014-07-05 | 2018-11-30 | Linde Aktiengesellschaft | Sposób i urządzenie do kriogenicznego rozdziału powietrza |
EP3559576A2 (de) | 2016-12-23 | 2019-10-30 | Linde Aktiengesellschaft | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2461906A1 (fr) * | 1979-07-20 | 1981-02-06 | Air Liquide | Procede et installation cryogeniques de separation d'air avec production d'oxygene sous haute pression |
DE3528374A1 (de) * | 1985-08-07 | 1987-02-12 | Linde Ag | Verfahren und vorrichtung zur erzeugung von stickstoff mit ueberatmosphaerischem druck |
FR2655137B1 (fr) * | 1989-11-28 | 1992-10-16 | Air Liquide | Procede et installation de distillation d'air avec production d'argon. |
US5123947A (en) * | 1991-01-03 | 1992-06-23 | Air Products And Chemicals, Inc. | Cryogenic process for the separation of air to produce ultra high purity nitrogen |
US5471842A (en) * | 1994-08-17 | 1995-12-05 | The Boc Group, Inc. | Cryogenic rectification method and apparatus |
US5582032A (en) * | 1995-08-11 | 1996-12-10 | Liquid Air Engineering Corporation | Ultra-high purity oxygen production |
US5963666A (en) * | 1995-08-18 | 1999-10-05 | International Business Machines Corporation | Confusion matrix mediated word prediction |
DE19735154A1 (de) * | 1996-10-30 | 1998-05-07 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff |
-
1998
- 1998-08-25 EP EP98116041A patent/EP0955509B1/de not_active Expired - Lifetime
-
1999
- 1999-04-30 US US09/302,443 patent/US6196022B1/en not_active Expired - Lifetime
- 1999-04-30 JP JP12389399A patent/JP4450886B2/ja not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
JP4450886B2 (ja) | 2010-04-14 |
EP0955509A1 (de) | 1999-11-10 |
JPH11351738A (ja) | 1999-12-24 |
US6196022B1 (en) | 2001-03-06 |
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