EP0677713B1 - Procédé et installation pour la production de l'oxygène par distillation de l'air - Google Patents
Procédé et installation pour la production de l'oxygène par distillation de l'air Download PDFInfo
- Publication number
- EP0677713B1 EP0677713B1 EP95400752A EP95400752A EP0677713B1 EP 0677713 B1 EP0677713 B1 EP 0677713B1 EP 95400752 A EP95400752 A EP 95400752A EP 95400752 A EP95400752 A EP 95400752A EP 0677713 B1 EP0677713 B1 EP 0677713B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- column
- pressure column
- low
- argon
- air
- 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
Links
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims description 23
- 239000001301 oxygen Substances 0.000 title claims description 23
- 229910052760 oxygen Inorganic materials 0.000 title claims description 23
- 238000004821 distillation Methods 0.000 title claims description 16
- 238000000034 method Methods 0.000 title claims description 13
- 238000004519 manufacturing process Methods 0.000 title claims description 9
- 238000009434 installation Methods 0.000 title description 13
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 62
- 229910052786 argon Inorganic materials 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 30
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims 1
- 239000002609 medium Substances 0.000 description 17
- 238000010992 reflux Methods 0.000 description 7
- 239000006200 vaporizer Substances 0.000 description 6
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000007664 blowing Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000007320 rich medium Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
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
- F25J3/04006—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
- F25J3/04078—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
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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
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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
- F25J3/0429—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
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
- F25J3/04406—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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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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
- F25J2200/92—Details relating to the feed point
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/58—Argon
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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
- F25J2250/40—One fluid being 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
- 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 present invention relates to a method and an installation for oxygen and argon production by air distillation and more particularly to a process and an installation for the production of oxygen under pressure and argon.
- EP-A-0422974 describes a process for producing oxygen under pressure by cryogenic air distillation in a double column.
- Oxygen liquid is withdrawn from the tank of the low pressure column 7, as illustrated in Figure 1, and vaporizes in the auxiliary exchanger 9 by heat exchange with a fraction of the supply air.
- the remaining part of the air feed is divided into two flow rates, one of which goes directly to the column medium pressure 6, via line 14, and the other of which is relaxed in a turbine 4 before being sent to the low pressure column 7.
- EP-A-0580348 describes a process in which rich liquid is sent from a medium pressure column to a low pressure column in two fractions, one of which vaporizes at the head of an argon column before being injected into the low pressure column.
- An object of this invention is to improve the argon yields if the installation also includes an argon column supplied by the low pressure column.
- the subject of the invention is a process for the production of oxygen. gas and argon according to claim 1.
- the rich medium pressure medium liquid first, second and a third fractions and we send the first and second fractions to different levels in the low pressure column after sub-cooling prior.
- the third fraction is sent to the head condenser of the argon column. This notably makes it possible to significantly improve the extraction argon.
- the first and second fractions can be sent to the low pressure column at different temperatures, in order to improve again the reflux in the low pressure column and the argon extraction in the case where the installation also includes an argon column.
- part of the supply air is expanded before to be sent to the double column, the remaining part of the supply air being partially condensed in the auxiliary exchanger.
- the temperature difference in the auxiliary exchanger can be reduced to an average value of 0.6 ° C.
- the invention also relates to a production installation according to claim 6.
- EP-A-422,974 send some of the condensed air to the medium pressure column, a few trays above the tank so that she can participate in the less weakly, on distillation in this column.
- the installation represented in FIG. 1 essentially comprises a main air compressor 1 with variable flow, for example of the type centrifugal with movable blades, an air blower with movable blades 2, a heat exchange line 3, a turbine 4 for maintaining cold, a air distillation apparatus 5 consisting of a double column comprising itself a medium pressure column 6 surmounted by a low column pressure 7 and a minaret 7A, a vaporizer-condenser 8, a heat exchanger auxiliary heat 9 and a pump 10.
- This installation is intended for produce a variable flow of gaseous oxygen via a line 12, under a pressure higher than atmospheric pressure.
- the first overpressed fraction is cooled to the neighborhood from its dew point in passages of the exchange line then condensed in the auxiliary exchanger 9 and is divided into a first flow constant relaxed under 6 bar sent to the medium pressure column via a pipe 16, and a second constant relaxed flow towards 1 bar in a expansion valve 13 then injected into the low pressure column 7.
- the vaporizer-condenser 8 vaporizes a constant flow of oxygen liquid in the low pressure column tank by condensation of a flow at about equal to nitrogen at the head of the medium pressure column.
- Some cash rich "(oxygen-enriched air) taken from the bottom of the middle column pressure and expanded to around 1 bar in an expansion valve 18a is injected at an intermediate level of the low pressure column, and of the "lean liquid” (almost pure nitrogen) taken from the top of the medium pressure column and expanded to around 1 bar in an expansion valve 19 is injected at the top of the low pressure column.
- Liquid nitrogen is injected at the top of the 7A minaret through the expansion valve 21. Pure nitrogen is withdrawn from the top of the minaret 7A and sent to exchange line 3 to be reheated there before exiting by the line 20. The impure nitrogen leaves via line 25 from the top of the column low pressure 7 and is sent outside via line 18.
- Liquid oxygen withdrawn from the lower column tank pressure 7 is pumped to production pressure before being sprayed into the auxiliary exchanger 9 (constituted by a “film” type vaporizer) by heat exchange with partially condensed air. Oxygen vaporized comes out, after heating in the exchange line 3, by the driving 12.
- argon a fraction rich in argon is drawn off from the lower part of the low pressure column 7 and is sent to the column of argon 16 for distillation.
- This fraction includes mainly argon and oxygen.
- the tank liquid resulting from the distillation in column 16 is returned to the bottom of the low pressure column 7.
- the overhead condenser 29 of the argon column 16 is cooled by rich liquid from the medium column tank pressure 6, relieved by valve 23, vaporized and sent to the lower column pressure.
- valve 18a The remaining part of the rich liquid from the column tank medium pressure 6 is relieved by the valve 18a at a pressure slightly above atmospheric pressure and sent to the bottom column pressure 7 by valve 18, substantially at the same level as the level injection of the air expanded by the turbine 4 (the blowing air).
- the remaining part of rich liquid not vaporized in 29 is divided into two fractions: one first fraction is injected, as shown in Figure 1, after expansion by valve 18 in the low pressure column 7 at the air blast and the second fraction of rich liquid is sent to the low pressure column 7, after expansion to the pressure thereof by the valve 17, at an intermediate level between the injection level of the first fraction of rich liquid through valve 18a and the level of withdrawal of nitrogen through line 25.
- the variant of Figure 3 has only one compressor air 1, all the compressed air being sent either to turbine 4 or to exchanger 9.
- the partially condensed air in exchanger 9 passes entirely in the tank of the medium pressure column 6.
- the difference in level between the level of liquid oxygen in the BP column tank and its inlet in the fixed vaporizer 9, in this case, the vaporization pressure of oxygen; the pump 10 in Figure 2 is therefore deleted.
- the fractions of rich liquid can be sub-cooled so that the temperature of the fraction injected at the level of insufflation of air is lower than that of the fraction injected at the level intermediate.
- This arrangement of the exchanger 9 allows a gain of approximately 6% on the compression of the air and therefore on the specific energy of oxygen product.
Description
- une première fraction est envoyée dans la colonne basse pression à un premier niveau, habituellement au niveau de l'insufflation d'air dans le cas où il y a une turbine d'insufflation ;
- une deuxième fraction est envoyée dans la colonne basse pression à un niveau intermédiaire entre le premier niveau et le niveau de soutirage d'azote impur.
- la figure 1 représente schématiquement un mode de réalisation de l'installation selon l'art antérieur ; et
- les figures 2 et 3 représentent schématiquement deux modes de réalisation de l'installation conforme à l'invention.
- un premier flux est refroidi dans des passages de la ligne d'échange; une partie est sortie de cette ligne d'échange après un refroidissement partiel, détendue vers 1 bar dans la turbine 4 et insufflée dans la colonne basse pression 7 au voisinage de son point de rosée ; un second flux poursuit son refroidissement jusqu'au voisinage de son point de rosée sous 6 bar, puis est injecté au bas de la colonne moyenne pression 6 via une conduite 14.
Claims (7)
- Procédé de production d'oxygène gazeux sous pression et d'argon par distillation cryogénique d'air dans une double colonne (5) comprenant une colonne moyenne pression (6) et une colonne basse pression (7), dans lequel on divise du liquide riche provenant de la cuve de la colonne moyenne pression en une première et une deuxième fractions liquides que l'on envoie à des niveaux différents dans la colonne basse pression (7), on soutire un fluide enrichi en argon de la colonne basse pression (7), on le distille dans une colonne argon (16) et on soutire de l'argon en tête de la colonne argon, on soutire un liquide enrichi en oxygène d'une partie inférieure de la colonne basse pression, on le pressurise et on le vaporise par échange de chaleur avec de l'air destiné à la double colonne (5) pour former l'oxygène gazeux sous pression, et on envoie une troisième fraction de liquide riche au condenseur de tête de la colonne argon où il se vaporise avant d'être envoyé à un troisième niveau de la colonne basse pression (7), les niveaux différents étant au dessous d'un niveau de soutirage d'azote impur de la colonne basse pression (7).
- Procédé selon la revendication 1 dans lequel les première et deuxième fractions sont refroidies à des températures différentes avant d'être envoyées dans la colonne basse pression (7).
- Procédé selon l'une des revendications 1 ou 2, dans lequel une partie de l'air d'alimentation est insufflée à un niveau intermédiaire de la colonne basse pression (7) et les niveaux d'injection des première et deuxième fractions de liquide riche ne sont pas au-dessous de ce niveau intermédiaire.
- Procédé selon la revendication 3 dans lequel une fraction de liquide riche est envoyée à la colonne basse pression (7) sensiblement au même niveau que l'air insufflé.
- Installation de production d'oxygène gazeux sous pression et d'argon par distillation cryogénique d'air comprenant une double colonne (5), constituée par au moins une colonne moyenne pression (6) surmontée d'une colonne basse pression (7) et une colonne de distillation d'argon, des moyens (25) pour soutirer de l'azote impur de la colonne basse pression, des moyens (12) pour soutirer un liquide enrichi en oxygène de la partie inférieure de la colonne basse pression (7), pour le pressuriser (10), et le vaporiser (9) contre de l'air destiné à la double colonne afin de former l'oxygène gazeux sous pression et des moyens pour soutirer de l'argon en tête de la colonne de distillation d'argon des moyens pour soutirer du liquide riche de la cuve de la colonne moyenne pression (6) et l'envoyer à trois niveaux différents de la colonne basse pression (7), situés en dessous du niveau de soutirage de l'azote impur, et des conduites pour envoyer du liquide riche à deux niveaux différents sans passer par le condenseur de tête de la colonne de distillation d'argon et pour envoyer une troisième fraction du liquide riche au condenseur de tête de la colonne de distillation d'argon, pour le vaporiser et l'envoyer au troisième niveau de la colonne basse pression.
- Installation selon la revendication 5, comprenant des moyens pour envoyer le liquide riche dans la colonne basse pression (7) à deux températures différentes.
- Installation selon l'une des revendications 5 ou 6, comprenant des moyens (4) pour envoyer de l'air à un niveau intermédiaire de la colonne basse pression (7) et des moyens pour envoyer les deux fractions de liquide riche à des niveaux dans le voisinage de ou au-dessus du niveau intermédiaire.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9404298 | 1994-04-12 | ||
FR9404298A FR2718518B1 (fr) | 1994-04-12 | 1994-04-12 | Procédé et installation pour la production de l'oxygène par distillation de l'air. |
Publications (2)
Publication Number | Publication Date |
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EP0677713A1 EP0677713A1 (fr) | 1995-10-18 |
EP0677713B1 true EP0677713B1 (fr) | 1999-10-20 |
Family
ID=9461989
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP95400752A Expired - Lifetime EP0677713B1 (fr) | 1994-04-12 | 1995-04-04 | Procédé et installation pour la production de l'oxygène par distillation de l'air |
Country Status (7)
Country | Link |
---|---|
US (1) | US5586451A (fr) |
EP (1) | EP0677713B1 (fr) |
JP (1) | JPH0854181A (fr) |
CN (1) | CN1121172A (fr) |
CA (1) | CA2146831A1 (fr) |
DE (1) | DE69512821T2 (fr) |
FR (1) | FR2718518B1 (fr) |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB9807833D0 (en) * | 1998-04-09 | 1998-06-10 | Boc Group Plc | Separation of air |
US6178775B1 (en) * | 1998-10-30 | 2001-01-30 | The Boc Group, Inc. | Method and apparatus for separating air to produce an oxygen product |
GB9910701D0 (en) | 1999-05-07 | 1999-07-07 | Boc Group Plc | Separation of air |
GB9925097D0 (en) * | 1999-10-22 | 1999-12-22 | Boc Group Plc | Air separation |
US6253576B1 (en) * | 1999-11-09 | 2001-07-03 | Air Products And Chemicals, Inc. | Process for the production of intermediate pressure oxygen |
EP1338856A3 (fr) * | 2002-01-31 | 2003-09-10 | L'AIR LIQUIDE, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des | Procédé et installation pour la séparation d'air par distillation cryogénique |
FR2854232A1 (fr) * | 2003-04-23 | 2004-10-29 | Air Liquide | Procede de distillation d'air pour produire de l'argon |
FR2864214B1 (fr) * | 2003-12-22 | 2017-04-21 | Air Liquide | Appareil de separation d'air, appareil integre de separation d'air et de production d'un metal et procede de demarrage d'un tel appareil de separation d'air |
US20070095100A1 (en) * | 2005-11-03 | 2007-05-03 | Rankin Peter J | Cryogenic air separation process with excess turbine refrigeration |
US9279613B2 (en) | 2010-03-19 | 2016-03-08 | Praxair Technology, Inc. | Air separation method and apparatus |
CN105115244B (zh) * | 2015-08-10 | 2017-06-27 | 开封空分集团有限公司 | 一种低纯度氧空气分离的装置及方法 |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1253717A (fr) * | 1960-04-08 | 1961-02-10 | Union Carbide Corp | Séparation à basse température de l'air en oxygène, azote et argon |
DE1112997B (de) * | 1960-08-13 | 1961-08-24 | Linde Eismasch Ag | Verfahren und Einrichtung zur Gaszerlegung durch Rektifikation bei tiefer Temperatur |
US4737177A (en) * | 1986-08-01 | 1988-04-12 | Erickson Donald C | Air distillation improvements for high purity oxygen |
GB8820582D0 (en) * | 1988-08-31 | 1988-09-28 | Boc Group Plc | Air separation |
FR2655137B1 (fr) * | 1989-11-28 | 1992-10-16 | Air Liquide | Procede et installation de distillation d'air avec production d'argon. |
US4994098A (en) * | 1990-02-02 | 1991-02-19 | Air Products And Chemicals, Inc. | Production of oxygen-lean argon from air |
US5076823A (en) * | 1990-03-20 | 1991-12-31 | Air Products And Chemicals, Inc. | Process for cryogenic air separation |
GB9008752D0 (en) * | 1990-04-18 | 1990-06-13 | Boc Group Plc | Air separation |
US5228296A (en) * | 1992-02-27 | 1993-07-20 | Praxair Technology, Inc. | Cryogenic rectification system with argon heat pump |
US5275003A (en) * | 1992-07-20 | 1994-01-04 | Air Products And Chemicals, Inc. | Hybrid air and nitrogen recycle liquefier |
-
1994
- 1994-04-12 FR FR9404298A patent/FR2718518B1/fr not_active Expired - Fee Related
-
1995
- 1995-04-04 EP EP95400752A patent/EP0677713B1/fr not_active Expired - Lifetime
- 1995-04-04 DE DE69512821T patent/DE69512821T2/de not_active Expired - Fee Related
- 1995-04-10 US US08/419,441 patent/US5586451A/en not_active Expired - Fee Related
- 1995-04-11 CN CN95105136A patent/CN1121172A/zh active Pending
- 1995-04-11 JP JP7085539A patent/JPH0854181A/ja active Pending
- 1995-04-11 CA CA002146831A patent/CA2146831A1/fr not_active Abandoned
Also Published As
Publication number | Publication date |
---|---|
CN1121172A (zh) | 1996-04-24 |
US5586451A (en) | 1996-12-24 |
EP0677713A1 (fr) | 1995-10-18 |
JPH0854181A (ja) | 1996-02-27 |
FR2718518A1 (fr) | 1995-10-13 |
CA2146831A1 (fr) | 1995-10-13 |
DE69512821D1 (de) | 1999-11-25 |
DE69512821T2 (de) | 2000-05-25 |
FR2718518B1 (fr) | 1996-05-03 |
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