EP0562893B1 - Verfahren zur Herstellung von Hochdruck-Stickstoff und Sauerstoff - Google Patents
Verfahren zur Herstellung von Hochdruck-Stickstoff und Sauerstoff Download PDFInfo
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- EP0562893B1 EP0562893B1 EP93400522A EP93400522A EP0562893B1 EP 0562893 B1 EP0562893 B1 EP 0562893B1 EP 93400522 A EP93400522 A EP 93400522A EP 93400522 A EP93400522 A EP 93400522A EP 0562893 B1 EP0562893 B1 EP 0562893B1
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- pressure
- nitrogen
- oxygen
- column
- compressor
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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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
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
- F25J3/04121—Steam turbine as the prime mechanical driver
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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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
- F25J3/04309—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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- 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
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
- F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
- F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/12—Particular process parameters like pressure, temperature, ratios
Definitions
- the present invention relates to a process for the simultaneous production on the one hand of pure nitrogen under a high pressure of nitrogen and on the other hand of oxygen, by air distillation in a double distillation column comprising a medium column pressure and a low pressure column of the "minaret" type producing pure nitrogen at the head.
- a particular application of the invention is the simultaneous production of a portion of high purity nitrogen, containing less than 10 ppm of oxygen, in large quantity (that is to say representing at least 20% and typically more 30% of the treated air flow), under 50 to 60 bar, for a unit for manufacturing ammonia, and on the other hand oxygen of medium to high purity, ie 95 to 99.5% in moles, at a pressure of the order of 65 bar with a high extraction yield, for the production of hydrogen by reaction of oxygen with heavy hydrocarbons, the hydrogen being intended to supply the same ammonia manufacturing unit .
- low pressure column of the minaret type means a low pressure column forming part of a double air distillation column, the upper end part of which is supplied at the head with “upper lean liquid” (nitrogen practically pure) withdrawn at the head of the medium pressure column and relaxed, and produces pure nitrogen at the head at low pressure.
- US-A-2,982,108 which discloses a process as defined in the preamble of claim 1, describes a process for the simultaneous production of pressurized nitrogen and oxygen in which a compressor is used to pressurize the nitrogen produced up to '' at a pressure which cannot exceed 40 bar, if it is assumed that the compressor has at most six wheels.
- a process for the simultaneous production, on the one hand of pure nitrogen under a high nitrogen pressure, on the other hand of oxygen, by distillation of air in a double distillation column comprising a medium pressure column and a low pressure column of the "minaret" type producing pure nitrogen at the top, in which after heating the nitrogen from the low pressure column, it is compressed at high pressure by means of a single nitrogen compressor of the centrifugal type having at most six compression wheels, characterized in that the low pressure column is operated under a pressure of the order of P N / ⁇ N , where P N denotes the high nitrogen pressure and ⁇ N the rate of compression of said nitrogen compressor.
- the nitrogen compressor and the air compressor can in particular be connected to a common power source.
- the installation shown in the drawings is intended to produce on the one hand, under 55 bar, high purity nitrogen gas (typically containing less than 10 ppm of oxygen), in a flow rate at least equal to 20% of the flow rate treated air, and on the other hand, under 65 bar, oxygen having a purity of 95 to 99.5%, with a high extraction yield.
- high purity nitrogen gas typically containing less than 10 ppm of oxygen
- 65 bar oxygen having a purity of 95 to 99.5%
- the installation essentially comprises an air compressor 1, an apparatus 2 for purifying the air by adsorption, a heat exchange line 3 of the counter-current type, a double distillation column 4, an expansion turbine. 5, a liquid oxygen pump 6, a nitrogen compressor 7, an oxygen compressor 8 and an energy source 9 constituted for example by a steam turbine.
- the double column 4 comprises a medium pressure column 10 surmounted by a low pressure column 11 whose upper end part forms a minaret 11A for producing pure nitrogen under low pressure.
- a condenser-vaporizer 12 puts the overhead vapor (practically pure nitrogen) from column 10 into heat exchange relationship with the tank liquid (oxygen from determined purity) of column 11.
- a pipe fitted with an expansion valve 13 makes it possible to raise the "rich liquid” (oxygen-enriched air) from the tank of the column 10 to an intermediate point of the column 11;
- a pipe fitted with an expansion valve 14 makes it possible to raise "lower lean liquid” (impure nitrogen) from an intermediate point of the column 10 at the base of the minaret 11A;
- a pipe fitted with an expansion valve 15 makes it possible to raise the "upper lean liquid” (practically pure nitrogen) from the head of the column 10 to the top of the minaret.
- the nitrogen compressor 7 consists of a single three-stage compressor.
- the first two stages each include two compression wheels and have average compression ratios per wheel of 2 and 1.73 respectively, while the third stage comprises a single compression wheel having a compression ratio of 1.83.
- the overall compression ratio of the compressor is therefore 22.
- Each wheel has a coolant at its outlet.
- the oxygen compressor 8 also consists of a single compressor. This compressor has six wheels with an average compression ratio per wheel of 1.37. The overall compression ratio is therefore 6.5.
- the shaft 16 of the compressor 7 is coupled to the shaft 17 of the compressor 1 by a coupling 18, and the assembly is driven by the common energy source 9.
- the shaft 16 can drive the different stages of the compressor 7 by means of speed multipliers suitable for each stage.
- the compressor 8 is driven by a separate energy source 19.
- the low pressure is chosen so that, multiplied by the compression ratio of the compressor 7, it provides the desired high production pressure for nitrogen.
- the incoming air is compressed to 11 bars in the compressor 1, purified in 2, cooled from the hot end to the cold end of the exchange line 3, and introduced in the vicinity of its dew point in the tank of the column 10
- the low pressure pure nitrogen leaving the gaseous top of the minaret 11A and warmed to room temperature from the cold end to the hot end of the exchange line is introduced at the suction of the first stage of the compressor 7, with the possible exception of a flow of nitrogen produced at low pressure via a pipe 20.
- the high pressure nitrogen is produced at the discharge of the third stage of the compressor and discharged via a pipe 21.
- Compressor 7 is also used as a nitrogen cycle compressor. Indeed, medium pressure nitrogen is drawn off at the top of the column 10, via a line 22, warmed to ambient temperature in the exchange line and introduced via a line 23 at the suction of the second stage of the compressor 7 Nitrogen at high cycle pressure is discharged from this second stage via a line 24, cooled, liquefied and sub-cooled in the exchange line, expanded to medium pressure in an expansion valve 25 and introduced at the top of column 10.
- the flow of nitrogen flowing in line 24 is greater by a predetermined amount than the flow of nitrogen flowing in line 23.
- the difference constitutes an additional flow of liquid nitrogen, said rectification support, introduced at reflux at the top of column 10. This flow rate is taken from the low pressure nitrogen stream drawn in by the first stage of the compressor 7.
- Impure nitrogen constituting the residual gas of the installation, is drawn off at the base of the minaret 11A via a pipe 25, heated to an intermediate temperature in the exchange line, taken out of the latter, expanded to atmospheric pressure in a turbine 5 which keeps the installation cold, then reintroduced into the exchange line, warmed up to room temperature, and finally used to regenerate the adsorption bottles of the device 2 and evacuated from installation via a pipe 26.
- Oxygen at 65 bar is produced as follows.
- the desired liquid oxygen flow rate is withdrawn from the bottom of the column 11, brought by the pump 6 to an intermediate pressure of oxygen, vaporized and warmed to room temperature in the exchange line 3, then compressed to the pressure of compressor production 8.
- the vaporization of the liquid oxygen under the intermediate oxygen pressure is carried out by condensation of the nitrogen under the high cycle pressure, with a subcritical value for this high pressure, for example 30 bars. This value corresponds to a vaporization of liquid oxygen at about 11 bars, which is therefore the pressure supplied by the pump 6.
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Claims (6)
- Verfahren zur gleichzeitigen Herstellung von einerseits reinem Stickstoff unter einem hohen Stickstoffdruck und andererseits Sauerstoff durch Destillation von Luft in einer Doppel-Destillationskolonne (4), umfassend eine Mitteldruckkolonne (10) und eine Niederdruckkolonne (11) nach Art eines "Minaretts", die an ihrem Kopf den reines Scickstoff liefert, wobei der aus der Niederdruckkolonne (11) austretende Stickstoff nach Erwärmen mittels eines einzigen Stickstoffverdichters (7) des Zentrifugentyps mit höchstens sechs Kompressionsrädern auf den hohen Druck verdichtet wird, dadurch gekennzeichnet, daß die Niederdruckkolonne (11) unter einem Druck in der Crößenordnung von PN/ρN betrieben wird, wobei PN der hohe Stickstoffdruck und ρN das Verdichtungsverhältnis des genannten Stickstoffverdichters ist;
dieser Anspruch bezieht sich nicht auf Verfahren, bei denen der hohe Druck des Stickstoffs nicht mehr als 40 bar absolut beträgt. - Verfahren nach Anspruch 1, bei dem der sauerstoff unter einem hohen Sauerstoffdruck, der mehr als etwa 10 bar absolut beträgt, erzeugt wird, dadurch gekennzeichnet, daß am Sumpf der Niederdruckkolonne (11) entnommener flüssiger Sauerstoff mit einer Pumpe (6) auf einen Sauerstoffzwischendruck gebracht wird und der Sauerstoff nach Verdampfen und Erwärmen mittels eines einzigen Sauerstoffverdichters (8) des Zentrifugentyps mit höchstens sechs Kompressionsrädern auf den hohen Sauerstoffdruck verdichtet wird, wobei der Sauerstoffzwischendruck in der Größenordnung von Po/ρo liegt, wobei Po der hohe Sauerstoffdruck und ρo das Verdichtungsverhältnis des genannten Sauerstoffverdichters ist.
- Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß ein drei stufiger Stickstoffverdichter (7) mit höchstens zwei Rädern pro Stufe verwendet wird und außerdem die zweite Stufe verwendet wird, um eine Menge Stickstoff aus dem Kreislauf, der aus der Kolonne mittleren Drucks (10) entnommen und erwärmt wurde, auf einen Zwischendruck zwischen dem mittleren Druck und dem hohen Druck zu verdichten, und der verdichtete Stickstoff aus dem Kreislauf abgekühlt, verflüssigt, auf den mittleren Druck entspannt und am Kopf der Kolonne mittleren Drucks (10) eingeleitet wird.
- Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß der Stickstoff aus dem Kreislauf auf einen unterkritischen Druck verdichtet wird, bei dem die Kondensationstemperatur des Stickstoffs ein wenig geringer ist als die Verdampfungstemperatur des Sauerstoffs unter dem genannten Sauerstoffzwischendruck.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß ein dreistufiger Stickstoffverdichter (7) mit höchstens zwei Fädern pro Stufe verwendet wird und außerdem die beiden ersten Stufen verwendet werden, um zur Rektifikationsunterstützung einen Stickstoffstrom, der am Kopf der Niederdruckkolonne (11) entnommen und erwärmt wurde, von dem niedrigen Druck auf einen Zwischendruck zwischen dem mittleren Druck und dem hohen Druck zu verdichten, und dieser verdichtete Stickstoff abgekühlt, verflüssigt, auf den mittleren Druck entspannt und am Kopf der Kolonne mittleren Drucks (10) eingeleitet wird.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß zur Kühlung der Vorrichtung zur Destillation von Luft aus der Niederdrruckkolonne (11) entnomnener Rohstickstoff in einer Turbine (5) entspannt wird, wobei dieser Rohstickstoff nach Entspannung und Erwärmung vorzugweise verwendet wird, um Adsorptionsflaschen (2), die der Reinigung der behandelten Luft dienen, zu regenerieren.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9203501A FR2689224B1 (fr) | 1992-03-24 | 1992-03-24 | Procede et installation de production d'azote sous haute pression et d'oxygene. |
FR9203501 | 1992-03-24 |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0562893A1 EP0562893A1 (de) | 1993-09-29 |
EP0562893B1 true EP0562893B1 (de) | 1997-05-07 |
EP0562893B2 EP0562893B2 (de) | 2000-12-20 |
Family
ID=9427994
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP93400522A Expired - Lifetime EP0562893B2 (de) | 1992-03-24 | 1993-03-02 | Verfahren zur Herstellung von Hochdruck-Stickstoff und Sauerstoff |
Country Status (7)
Country | Link |
---|---|
US (1) | US5341647A (de) |
EP (1) | EP0562893B2 (de) |
CA (1) | CA2092140C (de) |
DE (1) | DE69310429T3 (de) |
ES (1) | ES2101256T5 (de) |
FR (1) | FR2689224B1 (de) |
ZA (1) | ZA932796B (de) |
Families Citing this family (27)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2703140B1 (fr) * | 1993-03-23 | 1995-05-19 | Air Liquide | Procédé et installation de production d'oxygène gazeux et/ou d'azote gazeux sous pression par distillation de l'air. |
US5471843A (en) * | 1993-06-18 | 1995-12-05 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate |
FR2706595B1 (fr) * | 1993-06-18 | 1995-08-18 | Air Liquide | Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable. |
US5460003A (en) * | 1994-06-14 | 1995-10-24 | Praxair Technology, Inc. | Expansion turbine for cryogenic rectification system |
US5689975A (en) * | 1995-10-11 | 1997-11-25 | The Boc Group Plc | Air separation |
US5600970A (en) * | 1995-12-19 | 1997-02-11 | Praxair Technology, Inc. | Cryogenic rectification system with nitrogen turboexpander heat pump |
GB9618576D0 (en) * | 1996-09-05 | 1996-10-16 | Boc Group Plc | Air separation |
GB9618577D0 (en) * | 1996-09-05 | 1996-10-16 | Boc Group Plc | Air separation |
GB9619717D0 (en) * | 1996-09-20 | 1996-11-06 | Boc Group Plc | Air separation |
GB9619718D0 (en) * | 1996-09-20 | 1996-11-06 | Boc Group Plc | Air separation |
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 |
GB9810587D0 (en) * | 1998-05-15 | 1998-07-15 | Cryostar France Sa | Pump |
FR2782787B1 (fr) * | 1998-08-28 | 2000-09-29 | Air Liquide | Procede et installation de production d'oxygene impur par distillation d'air |
GB9903908D0 (en) * | 1999-02-19 | 1999-04-14 | Boc Group Plc | Air separation |
US6192707B1 (en) * | 1999-11-12 | 2001-02-27 | Praxair Technology, Inc. | Cryogenic system for producing enriched air |
GB0002084D0 (en) * | 2000-01-28 | 2000-03-22 | Boc Group Plc | Air separation method |
DE10013075A1 (de) * | 2000-03-17 | 2001-09-20 | Linde Ag | Verfahren zur Gewinnung von gasförmigem und flüssigem Stickstoff mit variablem Anteil des Flüssigprodukts |
DE60024634T2 (de) | 2000-10-30 | 2006-08-03 | L'Air Liquide, S.A. a Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Verfahren und Einrichtung für kryogenische Luftzerlegung integriert mit assoziiertem Verfahren |
WO2003016676A1 (en) | 2001-08-15 | 2003-02-27 | Shell Internationale Research Maatschappij B.V. | Tertiary oil recovery combined with gas conversion process |
EP1678275A1 (de) * | 2003-10-29 | 2006-07-12 | Shell Internationale Researchmaatschappij B.V. | Verfahren zur förderung methanols oder eines kohlenwasserstoffs |
FR2863348B1 (fr) * | 2003-12-05 | 2006-12-22 | Air Liquide | Compresseur de gaz, appareil de separation d'un melange gazeux incorporant un tel compresseur et procede de separation d'un melange gazeux incorporant un tel compresseur |
US7225637B2 (en) * | 2004-12-27 | 2007-06-05 | L'Air Liquide Société Anonyme á´ Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Integrated air compression, cooling, and purification unit and process |
US7712331B2 (en) * | 2006-06-30 | 2010-05-11 | Air Products And Chemicals, Inc. | System to increase capacity of LNG-based liquefier in air separation process |
DE102010056570A1 (de) | 2010-12-30 | 2012-07-05 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Tieftemperaturzerlegung von Luft |
EP2963367A1 (de) * | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch |
EP3059536A1 (de) * | 2015-02-19 | 2016-08-24 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines Druckstickstoffprodukts |
WO2021204424A2 (de) * | 2020-04-09 | 2021-10-14 | Linde Gmbh | Verfahren zur tieftemperaturzerlegung von luft, luftzerlegungsanlage und verbund aus wenigstens zwei luftzerlegungsanlagen |
Family Cites Families (8)
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---|---|---|---|---|
FR1138601A (fr) * | 1955-12-15 | 1957-06-17 | Air Liquide | Perfectionnements à la purification et à la séparation de l'air en ses éléments |
DE1112997B (de) * | 1960-08-13 | 1961-08-24 | Linde Eismasch Ag | Verfahren und Einrichtung zur Gaszerlegung durch Rektifikation bei tiefer Temperatur |
US3123457A (en) * | 1960-12-22 | 1964-03-03 | E smith | |
DE1263037B (de) * | 1965-05-19 | 1968-03-14 | Linde Ag | Verfahren zur Zerlegung von Luft in einer Rektifikationssaeule und damit gekoppelterZerlegung eines Wasserstoff enthaltenden Gasgemisches |
SU739316A1 (ru) † | 1977-08-22 | 1980-06-05 | Предприятие П/Я А-3605 | Способ разделени воздуха |
GB2079428A (en) * | 1980-06-17 | 1982-01-20 | Air Prod & Chem | A method for producing gaseous oxygen |
US4869741A (en) * | 1988-05-13 | 1989-09-26 | Air Products And Chemicals, Inc. | Ultra pure liquid oxygen cycle |
EP0383994A3 (de) † | 1989-02-23 | 1990-11-07 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Luftzerlegung durch Rektifikation |
-
1992
- 1992-03-24 FR FR9203501A patent/FR2689224B1/fr not_active Expired - Fee Related
-
1993
- 1993-03-02 DE DE69310429T patent/DE69310429T3/de not_active Expired - Fee Related
- 1993-03-02 ES ES93400522T patent/ES2101256T5/es not_active Expired - Lifetime
- 1993-03-02 EP EP93400522A patent/EP0562893B2/de not_active Expired - Lifetime
- 1993-03-08 US US08/027,788 patent/US5341647A/en not_active Expired - Lifetime
- 1993-03-12 ZA ZA932796A patent/ZA932796B/xx unknown
- 1993-03-22 CA CA002092140A patent/CA2092140C/fr not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
ES2101256T3 (es) | 1997-07-01 |
FR2689224B1 (fr) | 1994-05-06 |
EP0562893B2 (de) | 2000-12-20 |
DE69310429T3 (de) | 2001-08-23 |
DE69310429D1 (de) | 1997-06-12 |
US5341647A (en) | 1994-08-30 |
CA2092140C (fr) | 1998-08-18 |
DE69310429T2 (de) | 1997-12-11 |
FR2689224A1 (fr) | 1993-10-01 |
CA2092140A1 (fr) | 1993-09-25 |
ES2101256T5 (es) | 2001-03-16 |
EP0562893A1 (de) | 1993-09-29 |
ZA932796B (en) | 1993-09-30 |
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