EP1132700B1 - Verfahren und Vorrichtung zur kryogenischen Luftzerlegung - Google Patents

Verfahren und Vorrichtung zur kryogenischen Luftzerlegung Download PDF

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Publication number
EP1132700B1
EP1132700B1 EP01400413A EP01400413A EP1132700B1 EP 1132700 B1 EP1132700 B1 EP 1132700B1 EP 01400413 A EP01400413 A EP 01400413A EP 01400413 A EP01400413 A EP 01400413A EP 1132700 B1 EP1132700 B1 EP 1132700B1
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EP
European Patent Office
Prior art keywords
column
air
oxygen
process according
fraction
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.)
Expired - Lifetime
Application number
EP01400413A
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English (en)
French (fr)
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EP1132700A1 (de
Inventor
Jean-Pierre Tranier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP1132700A1 publication Critical patent/EP1132700A1/de
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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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • 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
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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    • 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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    • F25J3/0429—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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    • 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
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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
    • F25J3/04333—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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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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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    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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    • F25J3/0446—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 the heat generated by mixing two different phases
    • F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
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    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Definitions

  • the present invention relates to a method and an installation of air separation by cryogenic distillation according to the preamble of claim 1 and claim 15, respectively.
  • Such a process and a such an installation are known from DE-A-1 199 293.
  • US-A-4947649 discloses a solution where air is compressed for introduce it at least partially in a single column. Such a solution is not applicable only if it is desired to produce nitrogen at a significantly higher pressure atmospheric pressure, particularly in the case of integration with a gas turbine. Conversely, if the air pressure supplied by the turbine compressor gas is very high, it is not advisable to use this process because the distillation under high pressure (pressure greater than 15 bar) is very difficult and poses significant technological problems when we get closer to the pressure supercritical nitrogen (33 bar).
  • the other disadvantage of the cycle described in this patent is that gaseous oxygen is produced at the same pressure as the air sent to the simple column.
  • EP-A-0584420 relates to a simple column which produces oxygen and nitrogen with head condenser and two reboilers operating at between 5 and 20 bar. A reboilers is heated with compressed nitrogen at room temperature and then cooled.
  • EP-B-0606 027 also describes a single column process for produce oxygen and / or nitrogen under pressure and at least one product liquid. Such a process is not interesting if one does not wish to produce products liquid. Indeed, the air pressure is eminently dependent on the amount of liquid produced. At zero or low liquid production, the air pressure is less than 3 bar abs, which poses problems in the design of the treatment in the head, which requires a huge amount of absorbent, making this process uneconomical.
  • the US-A-5794458 also discloses a single-column air distillation process. The main complaint that can be made about such a scheme is that it includes a compressor cold compressing a fluid very rich in oxygen. Moreover, in a classical way, the air compression is performed in one or more compressors operating at the ambient temperature.
  • DE-A-1199293 discloses a method of air distillation according to the preamble of the claim 1 wherein an air flow is separated in a single column and a flow of liquid oxygen is withdrawn in the vat from the column and vaporized by exchange of heat with a compressed cycle nitrogen flow rate in a cold compressor.
  • a part compressed nitrogen in the cold compressor at between 30 and 40 atma serves to reboil the simple column. In this case it is necessary to warm the nitrogen to compress it before cooling it and liquefying it against the oxygen that vaporizes. This is expensive in energy and complicates the construction of the exchangers.
  • US-A-5475980 discloses a double-column process for distillation of air which in an original way proposes to compress some of the air necessary for the distillation in a cold compressor.
  • the disadvantage of such a solution is the complexity of the exchange line from which the cold fluid is extracted to compress before reintroduce.
  • a cold compressor compresses a fluid whose oxygen content does not not exceed 30 mol%.
  • Another advantage of such a scheme is that it is better in energy than the scheme described in US Patent 5794458 because the turbine of the invention being on a fluid entering the cold box and not a fluid coming out of the cold box, the amount of heat exchanged in the main heat exchanger is significantly lower from where less irreversibilities.
  • Another aspect of the invention is to produce oxygen at a pressure greater than the pressure of the single column by compressing a liquid rich in oxygen (either by pump or by hydrostatic head) at a pressure greater than that of the single column and vaporizing it either by heat exchange indirect in a main heat exchanger or an external vaporizer, either by direct contact in a mixing column.
  • the ambient temperature is defined by the temperature at the suction of the Main air compressor supplying the separation unit.
  • FIGS. are schematic representations of facilities according to the invention.
  • the air 1 is compressed in the compressor 3, cleaned in 5 and divided in two.
  • Fraction 7 is partially cooled in exchanger 13 and sent to a turbine 15 in which it relaxes before being sent to the first column 17.
  • the rest of the air 9 (about 35%) is overpressed in the booster 11 and then crosses the exchanger 13 where it condenses before being sent to the column after a subcooling step in the exchanger 35, a few trays above the injection point of the air of the turbine 15.
  • the column operates at a pressure of between 1.2 and 1.3 bar abs, process which can be used up to pressures of 20 bar abs, preferably less than 10 bar abs.
  • Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
  • Nitrogen 25 from the top of the column warms up in the subcooler 35 before being divided in two. Part 31 is sent to the exchanger 13 where it heats up. The rest 29 is sent to the compressor 21 with an inlet temperature of - 182 ° C where it is compressed to 4.9 bar before to be sent to the reboiler of tank 19 of the first column 17. There it is condense and is returned to the top of the column to act as reflux. turbine 15 is coupled to the cold compressor 21.
  • Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
  • a cold booster 21 with several stages in series, each feeding an intermediate vaporizer or tank.
  • the cold booster 21 may have several stages in series driven each by a turbine or combined for example via a single-turbine multiplier.
  • Nitrogen 25 from the top of the column warms up in the subcooler 21 before being divided in two. Part 31 is sent to the exchanger 13 where it heats up. The rest 29 is sent to the compressor 21 with an inlet temperature of -182 ° C where it is compressed to 4.9 bar before to be sent to the reboiler of tank 19 of the first column 17. There it is condense and is returned to the top of the column to serve as reflux.
  • the turbine 15 is coupled to the cold compressor 21.
  • Figure 3 shows the case where the pressurized tank oxygen of the colone vaporizes by direct heat exchange in a mixing column.
  • the air 1 is compressed in the compressor 3, purified at 5 and divided into two. Fraction 7 is partially cooled in exchanger 13 and sent to a turbine 15 in which it relaxes before being sent to the first column 17. The rest of the air 9 (about 25%) is overpressed in the booster 11 and then passes through the exchanger 13.
  • the first column 17 operates at a pressure of between 3 and 20 bar.
  • the air flow 9 does not liquefy in the exchanger but is sent in form gas in the vat of the mixing column. So the mixing column operates at a higher pressure than the first column 17. It is possible to envisage both columns at the same pressure or to operate the mixing column at the lowest pressure.
  • the mixing column is fed at the top with oxygen pumped from the tank of the first column 17 but can be fed at the top by another flow less rich in oxygen than the flow pumped or in tank by air from a source other than the compressor 1.
  • Nitrogen 25 from the top of the column warms up in the subcooler 21 before being divided in two. Part 31 is sent to the interchange 13 where it is warms. The remainder 29 is sent to the compressor 21 with an inlet temperature of -182 ° C where it is compressed to 4.9 bar before being sent to the tank reboiler 19 of column 17. There it condenses and is returned to the top of the column to serve as the reflux.
  • the turbine 15 is coupled to the cold compressor 21.
  • an exchanger 49 warms the pumped oxygen sent to the top of the column 47.
  • the intermediate liquid flow of the mixing column is sent to the column 17 and the impure oxygen 48 withdrawn at the top of this one is sent to the exchanger 13.
  • FIG. 4 illustrates the case where a flow enriched with argon from the column 17 feeds a mixture column 57 having a cooled head condenser 51 by an intermediate liquid of the first column 17. A fluid enriched in argon is withdrawn at the top of the 57 mixture column.
  • Nitrogen 25 from the top of the column warms up in the subcooler 21 before being divided in two. Part 31 is sent to the interchange 13 where it is warms. The remainder 29 is sent to the compressor 21 with an inlet temperature of -182 ° C where it is compressed to 4.9 bar before being sent to the tank reboiler 19 of the first column 17. There he condenses and is sent back to the top of the column to serve of reflux.
  • the turbine 15 is coupled to the cold compressor 21.
  • Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
  • FIG. 5 shows a Etienne column 67 fed in the tank with a flow rate liquid drawn off some trays below the air injection point 9 and at the same level that the air blown 7. This liquid is pressurized by the pump 63 before being sent to the Etienne column. The liquid formed at the top of the column Etienne 67 is sent in head of the first column 17.
  • the Etienne column operating at 2.5 bar has a condenser head 61 cooled by part of the tank liquid 65 of the same column, the remainder of the liquid being sent to the column 17 below the injection point of the blown air 7.
  • the relaxed liquid vaporizes in the condenser 61 before being sent some trays above condenser 19 of column 17.
  • the turbine 15 is coupled to the compressor cold 21.
  • Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.

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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)

Claims (20)

  1. Verfahren zur Luftzerlegung durch kryogene Destillation in einem Gerät, das mindestens eine Kolonne (17, 47, 57) enthält, das die folgenden Schritte umfasst:
    Verdichten der Luft, Reinigen der Luft und Leiten mindestens eines Teils (7, 9) der Luft zu einer ersten (der) Kolonne (17);
    Abscheiden der Luft in der Kolonne bei kryogener Temperatur;
    Verdichten mindestens eines Teils einer Fraktion (25), die maximal 30 Molprozent Sauerstoff enthält, die aus dem Kolonnenkopf extrahiert wird, in einem Verdichter (21);
    mindestens teilweises Abkühlen der verdichteten Fraktion, ihr Kondensieren in einem Behälterverdampfer (19) der ersten Kolonne und Zurückleiten der kondensierten Fraktion zum Kolonnenkopf und
    Extrahieren einer flüssigen Fraktion (33), die reich an Sauerstoff ist, aus der ersten Kolonne, Druckbeaufschlagen der Fraktion auf einen Druck, der größer ist als der der Kolonne (17) und Verdampfen der Fraktion, um ein gasförmiges Produkt unter Druck zu erzeugen, das reich an Sauerstoff ist,
       dadurch gekennzeichnet, dass die Ansaugtemperatur des Verdichters kleiner ist als die Umgebungstemperatur und dass der flüssige Sauerstoff durch direkten oder indirekten Wärmeaustausch mit einem Teil der Versorgungsluft (7, 9) verdampft wird.
  2. Verfahren nach Anspruch 1, bei dem die verdichtete Fraktion (25) mindestens 19 Molprozent Sauerstoff und mindestens 81 % Molprozent Stickstoff enthält.
  3. Verfahren nach einem der Ansprüche 1 und 2, bei dem mindestens ein Teil (7) der Luft in einer Turbine (15) entspannt wird, bevor er zu der (ersten) Kolonne geleitet wird.
  4. Verfahren nach Anspruch 3, bei dem das Produkt der Arbeit durch das Entspannen mindestens eines Teils der Luft mindestens teilweise zum Verdichten in einer oder mehreren Verdichtungsstufen der Fraktion dient, die maximal 30 % Sauerstoff enthält.
  5. Verfahren nach Anspruch 1, 2, 3 oder 4, bei dem mindestens ein Teil der Luft (9) auf einen hohen Druck verdichtet, kondensiert und zu der (ersten) Kolonne geleitet wird.
  6. Verfahren nach Anspruch 5, bei dem ein nicht entspannter Teil der Luft durch Verdampfen eines Fluids, das intern ist oder aus der ersten Kolonne extrahiert wird, kondensiert wird (Fig. 1, 2).
  7. Verfahren nach einem der Ansprüche 1 bis 6, bei dem das Verdampfen der flüssigen Fraktion, die reich an Sauerstoff ist, durch direkten Kontakt in einer so genannten Mischhilfskolonne (47) erfolgt (Fig. 3).
  8. Verfahren nach einem der Ansprüche 1 bis 7, bei dem eine Hilfskolonne (57), die zur Argonherstellung bestimmt ist, ausgehend von der ersten Kolonne versorgt wird (Fig. 4).
  9. Verfahren nach einem der Ansprüche 1 bis 8, bei dem man in einer Hilfskolonne eine Flüssigkeit destilliert, die mit Sauerstoff angereichert ist, der aus der einzelnen Kolonne extrahiert wird, um eine Fraktion zu erzeugen, die reicher ist an Sauerstoff, und eine Fraktion, die an Sauerstoff abgereichert ist, und die wieder in die erste Kolonne eingeführt werden (Fig. 5).
  10. Verfahren nach einem der Ansprüche 1 bis 9, bei dem mindestens ein Teil der Luft, die für eine Kolonne des Geräts bestimmt ist, von dem Verdichter einer Gasturbine kommt und/oder ein mit Stickstoff angereichertes Gas ist, das von der (ersten) Kolonne stammt, zum System der Gasturbine zurückgeleitet wird.
  11. Verfahren nach Anspruch 10, bei dem der Eingangsdruck der Gasturbine größer ist als 15 bar absolut.
  12. Verfahren nach einem der Ansprüche 1 bis 11, bei dem die Ansaugtemperatur des kalten Verdichters (21) kleiner ist als -100 °C.
  13. Verfahren nach Anspruch 12, bei dem die Ansaugtemperatur des kalten Verdichters (21) kleiner ist als -150 °C.
  14. Verfahren nach einem der Ansprüche 1 bis 13, bei dem man als Endprodukt Flüssigkeit (78) erzeugt oder nicht.
  15. Anlage zur Luftzerlegung durch Destillation in mindestens einer ersten Kolonne (17), die einen Behälterverdampfer (19) hat, der Mittel (7) umfasst, um verdichtete und gereinigte Luft zu der (ersten) Kolonne zu leiten, einen Verdichter (21), um ein Gas (25), das maximal 30 Molprozent Sauerstoff enthält, das von dem Kopf der Kolonne kommt, zu verdichten, Mittel, um das verdichtete Gas zu dem Behälterverdampfer zu leiten, Mittel (33), um das verdichtete Gas, das in dem Behälterverdampfer (19) zumindest teilweise kondensiert ist, zu dem Kolonnenkopf zurückzuleiten, eventuell Mittel, um das verdichtete Gas, dem Behälterverdampfer vorgeschaltet, mit Stickstoff anzureichern, Mittel (27), um eine Flüssigkeit abzuzapfen, die in dem Behälter der Kolonne mit Sauerstoff angereichert wird, Mittel (23) um sie mit Druck zu beaufschlagen und Mittel (13, 47), um die mit Druck beaufschlagte Flüssigkeit durch direkten oder indirekten Wärmeaustausch zu verdampfen, dadurch gekennzeichnet, dass sie Mittel umfasst, um die mit Druck beaufschlagte Flüssigkeit durch direkten oder indirekten Wärmeaustausch mit Luft (9), die für die erste Kolonne bestimmt ist, zu verdampfen, und dadurch, dass der Verdichter eine Eingangstemperatur hat, die maximal 5 °C wärmer ist als eine Temperatur der (ersten) Kolonne, und dadurch, dass der Verdichter eine Eingangstemperatur hat, die niedriger ist als die Umgebungstemperatur.
  16. Anlage nach Anspruch 15, umfassend eine Luftentspannungsturbine (15), bei der der Ausgang der Turbine mit der (ersten) Kolonne verbunden ist.
  17. Anlage nach einem der Ansprüche 15 und 16, bei der die mit Druck beaufschlagte Flüssigkeit in einer Mischkolonne (47) verdampft.
  18. Anlage nach einem der Ansprüche 15 bis 17, die eine Kolonne zur Argonproduktion (57) umfasst, die ausgehend von der Kolonne (17) versorgt wird, die einen Behälterverdampfer (19) hat.
  19. Anlage nach einem der Ansprüche 15 bis 18, bei der die Kolonne (17), die einen Behälterverdampfer (19) hat, mindestens einen Zwischenkondenser (39) hat.
  20. Anlage nach einem der Ansprüche 15 bis 19, bei der die Kolonne (17), die einen Behälterverdampfer (19) hat, keinen Kopfverdichter hat.
EP01400413A 2000-03-07 2001-02-16 Verfahren und Vorrichtung zur kryogenischen Luftzerlegung Expired - Lifetime EP1132700B1 (de)

Applications Claiming Priority (2)

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FR0002924A FR2806152B1 (fr) 2000-03-07 2000-03-07 Procede et installation de separation d'air par distillation cryogenique
FR0002924 2000-03-07

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AR (1) AR027970A1 (de)
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CA (1) CA2339392A1 (de)
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FR2830928B1 (fr) * 2001-10-17 2004-03-05 Air Liquide Procede de separation d'air par distillation cryogenique et une installation pour la mise en oeuvre de ce procede
US7296437B2 (en) * 2002-10-08 2007-11-20 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for separating air by cryogenic distillation and installation for implementing this process
JP2007512846A (ja) * 2003-12-04 2007-05-24 ゼンコー・インコーポレイテッド 増加した宿主ストリング含有量を有する変異体タンパク質の生成方法およびその組成物
EP1767884A1 (de) * 2005-09-23 2007-03-28 L'Air Liquide Société Anon. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
US8397535B2 (en) * 2009-06-16 2013-03-19 Praxair Technology, Inc. Method and apparatus for pressurized product production
WO2012155318A1 (en) * 2011-05-13 2012-11-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of oxygen at high pressure by cryogenic distillation

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DE1199293B (de) * 1963-03-29 1965-08-26 Linde Eismasch Ag Verfahren und Vorrichtung zur Luftzerlegung in einem Einsaeulenrektifikator
US3392536A (en) * 1966-09-06 1968-07-16 Air Reduction Recompression of mingled high air separation using dephlegmator pressure and compressed low pressure effluent streams
US5351492A (en) * 1992-09-23 1994-10-04 Air Products And Chemicals, Inc. Distillation strategies for the production of carbon monoxide-free nitrogen
US5379599A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Pumped liquid oxygen method and apparatus
FR2721383B1 (fr) * 1994-06-20 1996-07-19 Maurice Grenier Procédé et installation de production d'oxygène gazeux sous pression.
US5832748A (en) * 1996-03-19 1998-11-10 Praxair Technology, Inc. Single column cryogenic rectification system for lower purity oxygen production
JP2875206B2 (ja) * 1996-05-29 1999-03-31 日本エア・リキード株式会社 高純度窒素製造装置及び方法
US6082135A (en) * 1999-01-29 2000-07-04 The Boc Group, Inc. Air separation method and apparatus to produce an oxygen product

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AR027970A1 (es) 2003-04-16
US20020134105A1 (en) 2002-09-26
BR0102482A (pt) 2001-10-16
US6484534B2 (en) 2002-11-26
FR2806152A1 (fr) 2001-09-14
ES2252164T3 (es) 2006-05-16
DE60114269D1 (de) 2005-12-01
EP1132700A1 (de) 2001-09-12
CA2339392A1 (en) 2001-09-07
FR2806152B1 (fr) 2002-08-30
DE60114269T2 (de) 2006-07-20

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