EP0878678A2 - Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft - Google Patents
Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft Download PDFInfo
- Publication number
- EP0878678A2 EP0878678A2 EP98107748A EP98107748A EP0878678A2 EP 0878678 A2 EP0878678 A2 EP 0878678A2 EP 98107748 A EP98107748 A EP 98107748A EP 98107748 A EP98107748 A EP 98107748A EP 0878678 A2 EP0878678 A2 EP 0878678A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- pressure column
- nitrogen gas
- nitrogen
- column
- heat exchanger
- 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
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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
- F25J3/04151—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
- 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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- 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
- F25J3/04309—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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- 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
- F25J2200/20—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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- 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
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
- 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
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- 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
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- 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
- F25J2250/50—One fluid being oxygen
Definitions
- the invention relates to a method and an apparatus for the extraction of Nitrogen by low-temperature decomposition of air by means of two-stage rectification in a double column, which has a high pressure column and a medium pressure column, the are in heat exchange relationship with one another, with the method being air compressed, cleaned, in a main heat exchanger against decomposition products cooled and fed to the rectification, at least one nitrogen product fraction discharged from the high pressure column and a nitrogen gas fraction the double column warmed up, relaxed and at least partly in indirect Heat exchange with an oxygen-enriched liquid from the bottom Area of the medium pressure column is brought, the nitrogen gas fraction at least partially condensed and at least the oxygen-enriched liquid is partially evaporated, and this with indirect heat exchange condensate formed is at least partially returned to the medium pressure column.
- the invention is therefore based on the object of such a method and specify appropriate device, which is characterized by particularly high Profitability, in particular through low energy consumption and / or low Mark apparatus costs.
- This object is achieved in that the nitrogen gas fraction upstream of the Relaxation is warmed to an intermediate temperature between the Temperatures at the cold and warm end of the main heat exchanger.
- the heating of the nitrogen gas fraction is regularly caused by indirect Heat exchange causes.
- it can be in the main heat exchanger be carried out, which is used to cool the feed air.
- the measure according to the invention is omitted at least in part by heating the Nitrogen gas fraction from the intermediate temperature to the warm temperature End of the main heat exchanger (usually about the same as the Ambient temperature) and the corresponding re-cooling.
- Corresponding the exchange losses in the corresponding heat exchanger are lower it means less energy is lost through irreversibility.
- the corresponding one Heat exchanger can also have fewer passages and thus can be produced more cheaply.
- the intermediate temperature to which the nitrogen gas fraction is heated is for example 140 to 190 K below the temperature of the warm end of the Main heat exchanger.
- the relaxation of the nitrogen gas fraction upstream of it Condensation through indirect heat exchange preferably leads to one Intermediate pressure between the pressures of the high pressure column and the medium pressure column or to a pressure below the medium pressure column pressure. Accordingly, the Pressure of the condensate reduced before introduction into the medium pressure column or can be increased, for example by a throttle valve or by a Pump.
- the nitrogen gas fraction between the heating to a The intermediate temperature and the relaxation did not cool down. This eliminates Irreversibility by heating and cooling the nitrogen gas fraction and the corresponding heat exchange devices completely.
- the nitrogen gas fraction from the high pressure column is removed. In this case in particular, it needs between heating up to the intermediate temperature and relaxation are not compressed, so that also the corresponding machine and the associated energy consumption omitted.
- the corresponding amount can also be considered High pressure product can be obtained from the high pressure column.
- High pressure product can be obtained from the high pressure column.
- Pump can be used to increase the Pressure in the condensate at the high pressure column level.
- any known method can be used to relax the nitrogen gas fraction this relaxation is preferably carried out while performing work, for example in a turbine. Part of or all of it can be used for the Process required cold can be obtained. In addition, it is possible to use the Energy gained at least partially to compress a To use product stream, for example by mechanical coupling of the Relaxation machine to a compressor.
- the relaxed amount of nitrogen gas fraction is so large is that it does not completely liquefy against the oxygenated liquid , it is favorable if part of the expanded nitrogen gas fraction in indirect heat exchange with an intermediate liquid from the medium pressure column is condensed.
- the this indirect heat exchange condensate is preferred applied to the medium pressure column. That through the evaporation of the Intermediate liquid gas is preferably in the medium pressure column returned.
- the additional heating of the medium pressure column caused by this improves the separation effect of this column.
- the corresponding additional Condenser evaporator can be inside or outside the medium pressure column be arranged.
- the intermediate liquid is preferably in an area below the point, at the bottom liquid from the high pressure column, and at least one, preferably 1 to 30, for example 20 theoretical plates above the Medium pressure column sump withdrawn.
- the invention also relates to a device for producing nitrogen according to claims 9 to 12.
- Compressed air 1 cleaned in a molecular sieve station flows through one Main heat exchanger 2 and is via line 3 in a double column 4, more precisely in whose high pressure column 5, fed.
- Oxygenated liquid 8 from the After hypothermia 9 high pressure column 5 is fed via line 10 into the medium pressure column 6 throttled.
- a part of the top fraction 7 of the high pressure column is through a Main capacitor 14 guided, condensed there and preferably completely again returned to the high pressure column 5.
- Another partial stream 17 of the top fraction 7 is led to the main heat exchanger 2.
- the intermediate temperature is for example 175 K lower than the temperature at the warm end of the Main heat exchanger 2 (approximately the same ambient temperature).
- the liquid in the sump of the medium pressure column 6 enters through the main condenser 14 Heat exchange with the condensing top fraction of the high pressure column.
- From the Medium pressure column 6 are an oxygen-enriched liquid 11 gaseous nitrogen stream 12 and optionally liquid nitrogen 13 removed.
- the gaseous nitrogen stream is via the lines 18a and 18b and through the Heat exchanger 9, 31 and 2 out. He can from line 19a under about Subtracted ambient temperature as a medium pressure product or - as in the drawing shown - brought to a further increased product pressure in a compressor 22 and be discharged as a further high-pressure product 19b.
- the nitrogen gas fraction is according to the invention at an intermediate temperature deducted from the main heat exchanger 2 (line 20) and then in one Relaxation machine (for example a turbine) 23 relaxed to perform work.
- one Relaxation machine for example a turbine
- the nitrogen gas fraction 24 is in the Liquefaction chamber of a condenser-evaporator 25 initiated.
- There she enters indirect heat exchange with possibly supercooled in 9 oxygen-enriched liquid 28 from the sump of the medium pressure column, which evaporated, drawn off via line 29 and preferably for regeneration the molecular sieve station is used.
- the pressure on the evaporation side of the Head capacitor 25 is preferably so by means of the throttle valve in line 28 set that the overpressure necessary for the regeneration of the molecular sieve is available.
- the oxygen-enriched liquid can be a pump, not shown, are promoted.
- the work obtained in the work relaxation 23 is in the example transmitted by direct mechanical coupling to a post-compressor 22 which a product stream, here nitrogen 19a from the medium pressure column, compressed.
- another process stream can be compressed or the mechanical energy can be applied a generator or to a brake blower.
- the pressure in the evaporation space of the top condenser 25 adjusted by means of the valve in line 28 so that after evaporation and after the passage through the heat exchanger 9 and 2 (line 29) still for the Regeneration of the molecular sieve required overpressure is present.
- the for Evaporation of the oxygen-enriched liquid requires the amount of nitrogen (Nitrogen gas fraction) is in the expansion machine 23 to a pressure brought, which is high enough to the evaporation of the oxygenated liquid against the condensing nitrogen gas fraction To ensure 24 in the top capacitor 25, and on the other hand ensures that the Refrigeration requirements for the procedure are covered.
- Table 1 shows preferred numerical ranges and a particularly preferred concrete numerical example for the operating pressures in the method according to FIG. 1.
- Number range example Head of the high pressure column 5 5.0 - 9.3 bar
- 6.2 bar Head of the medium pressure column 5 1.5 - 4.35 bar 2.9 bar
- Entry of relaxation machine 23 4.3 - 9.9 bar
- Exit relaxation machine 23 3.0 - 6.0 bar 4.37 bar
- Evaporation side of the condenser-evaporator 25 1.0 - 3.0 bar 1.30 bar
- FIG. 2 shows a modification of the method and the device according to FIG. 1. Corresponding features of the two examples have the same reference numerals. In the following, only the different features of the in FIG. 2 are described process described in detail.
- the condensate 203 is placed on the head of the medium pressure column 6.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
- Figur 1
- ein bevorzugtes Ausführungsbeispiel des Verfahrens und der Vorrichtung gemäß der Erfindung und
- Figur 2
- eine Abwandlung dieses Verfahrens mit einem weiteren Kondensator-Verdampfer.
Zahlenbereich | Beispiel | |
Kopf der Hochdrucksäule 5 | 5,0 - 9,3 bar | 6,2 bar |
Kopf der Mitteldrucksäule 5 | 1,5 - 4,35 bar | 2,9 bar |
Eintritt Entspannungsmaschine 23 | 4,3 - 9,9 bar | 6,1 bar |
Austritt Entspannungsmaschine 23 | 3,0 - 6,0 bar | 4,37 bar |
Verflüssigungsseite des Kondensator-Verdampfers 25 | 3,0 - 6,0 bar | 4,32 bar |
Verdampfungsseite des Kondensator-Verdampfers 25 | 1,0 - 3,0 bar | 1,30 bar |
Claims (12)
- Verfahren zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft mittels zweistufiger Rektifikation in einer Doppelsäule (4), die eine Hochdrucksäule (5) und eine Mitteldrucksäule (6) aufweist, die untereinander in Wärmeaustauschbeziehung (14) stehen, wobei bei dem Verfahren Luft verdichtet, gereinigt, in einem Hauptwärmetauscher (2) gegen Zerlegungsprodukte (17, 18, 29) abgekühlt und der Rektifikation (4) zugeführt wird, mindestens eine Stickstoff-Produktfraktion (21) aus der Hochdrucksäule (5) abgeführt und eine Stickstoffgasfraktion (20) aus der Doppelsäule (4) angewärmt (2), entspannt (23) und mindestens zum Teil in indirekten Wärmeaustausch (25) mit einer sauerstoffangereicherten Flüssigkeit (11, 28) aus dem unteren Bereich der Mitteldrucksäule (6) gebracht wird, wobei die Stickstoffgasfraktion (20) mindestens teilweise kondensiert und die sauerstoffangereicherte Flüssigkeit (11, 28) mindestens teilweise verdampft wird, und wobei das bei dem indirekten Wärmeaustausch (25) gebildete Kondensat (26) mindestens teilweise in die Mitteldrucksäule (6) eingeführt (16) wird, dadurch gekennzeichnet, daß die Stickstoffgasfraktion (20) stromaufwärts der Entspannung (23) auf eine Zwischentemperatur angewärmt wird, die zwischen den Temperaturen am kalten und warmen Ende des Hauptwärmetauschers (2) liegt.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Stickstoffgasfraktion (20) zwischen der Anwärmung (2) auf die Zwischentemperatur und der Entspannung (23) nicht abgekühlt wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß die Stickstoffgasfraktion (20) aus der Hochdrucksäule (5) entnommen (7, 17) wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die Stickstoffgasfraktion (20) zwischen der Anwärmung (2) auf die Zwischentemperatur und der Entspannung (23) nicht verdichtet wird.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß ein Teil (50) des bei dem indirekten Wärmeaustausch (25) gebildeten Kondensats (26) in die Hochdrucksäule (5) eingeführt (52) wird.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß die Entspannung (23) der Stickstoffgasfraktion (20) arbeitsleistend durchgeführt wird.
- Verfahren nach Anspruch 6, dadurch gekennzeichnet, daß bei der Entspannung (23) gewonnene Energie mindestens teilweise zur Verdichtung (22) eines Produktstroms (19a) verwendet wird.
- Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß ein Teil (201) der entspannten Stickstoffgasfraktion (24) in indirektem Wärmeaustausch (202) mit einer Zwischenflüssigkeit aus der Mitteldrucksäule (6) kondensiert wird.
- Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft mit einer Doppelsäule (4), die eine Hochdrucksäule (5), eine Mitteldrucksäule (6) aufweist, mit einem Hauptwärmetauscher (2) mit Passagen für verdichtete und gereinigte Luft (1) und Zerlegungsprodukte (17, 18, 29), mit einer Stickstoff-Produktleitung (21), die mit der Hochdrucksäule (5) verbunden ist, mit einer Stickstoffgasleitung (7, 17, 20, 24), die von der Doppelsäule (5) über den Hauptwärmetauscher (2) und eine Entspannungsmaschine (23) in den Verflüssigungsraum eines Kondensator-Verdampfers (25) führt, und mit einer Leitung (11, 28) für sauerstoffangereicherte Flüssigkeit, die mit dem unteren Bereich der Mitteldrucksäule (6) verbunden ist und zur Verdampfungsseite des Kondensator-Verdampfers (25) führt, wobei der Verflüssigungsraum des Kondensator-Verdampfers (25) über eine Kondensatleitung (26, 16) mit der Mitteldrucksäule (6) verbunden ist, dadurch gekennzeichnet, daß die Stickstoffgasleitung (20, 24) an einer Zwischenstelle zwischen dem kalten und dem warmen Ende aus dem Hauptwärmetauscher (2) herausführt.
- Vorrichtung nach Anspruch 9, dadurch gekennzeichnet, daß die Stickstoffgasleitung (20, 24) zwischen dem Hauptwärmetauscher (2) und der Entspannungsmaschine (23) keine Mittel zur Temperaturänderung und/oder kein Mittel zur Druckänderung aufweist.
- Vorrichtung nach Anspruch 9 oder 10, dadurch gekennzeichnet, daß die Stickstoffgasleitung (7, 17, 20, 24) stromaufwärts des Hauptwärmetauschers (2) mit der Hochdrucksäule (5) verbunden ist.
- Vorrichtung nach einem der Ansprüche 9 bis 11, gekennzeichnet durch eine Zweigleitung (201), die mit der Stickstoffgasleitung (24) zwischen Entspannungsmaschine (23) und Kondensator-Verdampfer (25) verbunden ist und in den Verflüssigungsraum eines weiteren Kondensator-Verdampfers (202) führt, dessen Verdampfungsraum mit einem Zwischenbereich der Mitteldrucksäule (6) verbunden ist.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP19980107748 EP0878678B1 (de) | 1997-05-15 | 1998-04-28 | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft |
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19720453A DE19720453A1 (de) | 1997-05-15 | 1997-05-15 | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft |
DE19720453 | 1997-05-15 | ||
EP97113507A EP0878677A1 (de) | 1997-05-15 | 1997-08-05 | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft |
EP97113507 | 1997-08-05 | ||
EP19980107748 EP0878678B1 (de) | 1997-05-15 | 1998-04-28 | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0878678A2 true EP0878678A2 (de) | 1998-11-18 |
EP0878678A3 EP0878678A3 (de) | 1999-04-07 |
EP0878678B1 EP0878678B1 (de) | 2002-12-04 |
Family
ID=26036581
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19980107748 Expired - Lifetime EP0878678B1 (de) | 1997-05-15 | 1998-04-28 | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0878678B1 (de) |
DE (1) | DE59806495D1 (de) |
DK (1) | DK0878678T3 (de) |
ES (1) | ES2189032T3 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102155841A (zh) * | 2010-02-11 | 2011-08-17 | 普莱克斯技术有限公司 | 低温分离方法及设备 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2548222B1 (de) * | 1975-10-28 | 1977-01-27 | Linde Ag | Verfahren und Vorrichtung zur Luftzerlegung |
US4617036A (en) * | 1985-10-29 | 1986-10-14 | Air Products And Chemicals, Inc. | Tonnage nitrogen air separation with side reboiler condenser |
DE3528374A1 (de) * | 1985-08-07 | 1987-02-12 | Linde Ag | Verfahren und vorrichtung zur erzeugung von stickstoff mit ueberatmosphaerischem druck |
DE4441920C1 (de) * | 1994-11-24 | 1996-04-04 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung |
-
1998
- 1998-04-28 ES ES98107748T patent/ES2189032T3/es not_active Expired - Lifetime
- 1998-04-28 DE DE59806495T patent/DE59806495D1/de not_active Expired - Fee Related
- 1998-04-28 EP EP19980107748 patent/EP0878678B1/de not_active Expired - Lifetime
- 1998-04-28 DK DK98107748T patent/DK0878678T3/da active
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2548222B1 (de) * | 1975-10-28 | 1977-01-27 | Linde Ag | Verfahren und Vorrichtung zur Luftzerlegung |
DE3528374A1 (de) * | 1985-08-07 | 1987-02-12 | Linde Ag | Verfahren und vorrichtung zur erzeugung von stickstoff mit ueberatmosphaerischem druck |
US4617036A (en) * | 1985-10-29 | 1986-10-14 | Air Products And Chemicals, Inc. | Tonnage nitrogen air separation with side reboiler condenser |
DE4441920C1 (de) * | 1994-11-24 | 1996-04-04 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102155841A (zh) * | 2010-02-11 | 2011-08-17 | 普莱克斯技术有限公司 | 低温分离方法及设备 |
Also Published As
Publication number | Publication date |
---|---|
DK0878678T3 (da) | 2003-03-10 |
ES2189032T3 (es) | 2003-07-01 |
EP0878678B1 (de) | 2002-12-04 |
DE59806495D1 (de) | 2003-01-16 |
EP0878678A3 (de) | 1999-04-07 |
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