EP1143216A1 - Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation - Google Patents
Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation Download PDFInfo
- Publication number
- EP1143216A1 EP1143216A1 EP01400749A EP01400749A EP1143216A1 EP 1143216 A1 EP1143216 A1 EP 1143216A1 EP 01400749 A EP01400749 A EP 01400749A EP 01400749 A EP01400749 A EP 01400749A EP 1143216 A1 EP1143216 A1 EP 1143216A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- argon
- enriched
- flow
- column
- oxygen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 239000001301 oxygen Substances 0.000 title claims abstract description 50
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000012530 fluid Substances 0.000 title claims abstract description 21
- 238000004821 distillation Methods 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims abstract description 203
- 229910052786 argon Inorganic materials 0.000 claims abstract description 97
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000007789 gas Substances 0.000 claims abstract description 41
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 31
- 239000003463 adsorbent Substances 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 3
- 230000002441 reversible effect Effects 0.000 claims description 11
- 238000011144 upstream manufacturing Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 239000000047 product Substances 0.000 claims description 3
- 239000012467 final product Substances 0.000 claims 2
- 239000000203 mixture Substances 0.000 abstract description 17
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract description 9
- 239000007788 liquid Substances 0.000 description 26
- 238000009834 vaporization Methods 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- VVTSZOCINPYFDP-UHFFFAOYSA-N [O].[Ar] Chemical compound [O].[Ar] VVTSZOCINPYFDP-UHFFFAOYSA-N 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
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- F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
Definitions
- the present invention relates to a production method and apparatus of a fluid enriched in oxygen by cryogenic distillation of a mixture containing nitrogen, oxygen and argon.
- it relates to a method and an apparatus for separating air by cryogenic distillation allowing the production of pure oxygen, i.e. oxygen containing at least 95% mol. oxygen, preferably at least 98% mol. oxygen or even 99.5% mol. oxygen.
- Patent application EP-A-0540900 describes a production process impure oxygen in which part of the impure argon containing at least 90% of argon from a column of mixture is mixed with the residual nitrogen from a simple column.
- the mixing column operates at the same low pressure as the low column pressure, up to 1.75 bara.
- EP-A-0384213 has a low pressure column operating at between 1.5 and 10 bara but the argon column operates at a lower pressure.
- US-A-4932212 describes the case in which the low pressure column and the argon column operate at pressures between 1 and 2 bars.
- EP-A-0518491 describes a process for the production of nitrogen gas under pressure and incidentally liquid nitrogen, liquid argon and liquid oxygen in which the low pressure column and the argon column operate at a pressure substantially identical above 2.5 bara. No argon gas flow is produced.
- EP-A-0952415 describes an apparatus comprising a double column and a argon column operating with a yield lower than the optimal yield.
- An object of the present invention is to increase the yield of pure oxygen an air separation device.
- Another object of the invention is to provide an air separation device particularly well suited to the demands of large quantities of nitrogen under pressure (typically when integrated with an IGCC gas turbine).
- the flow enriched in argon or the flow enriched in argon mixed with a gas enriched in nitrogen can be sent upstream of the expansion machine of a gas turbine.
- the flow enriched in argon can contain between 10 and 95 mol%. argon (or between 40 and 95% mol. argon), between 2 and 40.% mol of oxygen and between 2 and 40% mol. nitrogen.
- the flow enriched in argon which is released to the atmosphere and / or which is used to regenerate adsorbent beds or reversible exchangers and / or which is mixed with a gas enriched in nitrogen from the device and / or another device and / or which is sent upstream of the expansion machine of a gas turbine can constitute between 0.3 and 2% of the air, preferably between 0.5 and 1% of the air. For this reason, it is best to mix the flow enriched in argon with a gas enriched in nitrogen containing at least 90% mol.
- the mixture formed comprises less than 2% mol. argon, preferably less than 1% mol. argon.
- the low pressure column can operate between 2 and 10 bara, preferably above 2.5 bara.
- the apparatus may include an auxiliary separation column a flow containing at least argon and oxygen and two other columns, of which a high pressure column and a low pressure column thermally connected between them, the auxiliary column being supplied from the low pressure column.
- the apparatus may include an auxiliary separation column of a flow rate containing at least argon and oxygen and at least three others columns, including a high pressure column, an intermediate pressure column and a low pressure column thermally connected to each other, the auxiliary column being supplied from the low pressure column or the intermediate pressure column.
- an integrated method of separation comprising a method according to one of claims 1 to 12 in which a nitrogen-enriched gas is sent from the operating column preferably at the lowest pressure at the gas turbine, after one step possible compression and, optionally, a fluid enriched with oxygen is sent from an appliance column to a gasifier.
- the auxiliary column contains between 30 and 40 trays theoretical.
- the separation of oxygen and argon in the low pressure column tank is facilitated.
- the fluid enriched in argon withdrawn from the auxiliary column is not necessarily an end product of the device but can be used to cool flows re-entering the columns or supplying frigories by expansion.
- Figure 1 is a diagram of an oxygen production apparatus according to the invention using a double column.
- Figure 2 is a diagram of an oxygen production apparatus according to the invention using a triple column.
- an air flow 1 of 1000Nm3 / h is purified by beds adsorbent 4 is divided into two.
- the flow 2 is boosted at a higher pressure, sent to the heat exchanger 3 where it cools ensuring the vaporization of liquid oxygen and then to a hydraulic turbine 5 where it comes out at least partially liquid.
- This liquid (or two-phase mixture) 7 is sent to the column high pressure 9 operating between 14 and 15 bar and possibly partly at the column low pressure 11 operating between 4 and 6 bar (or even between 2 and 10 bar), either sending part of the capacity liquid upstream of the medium pressure column either by withdrawing a flow having a composition similar to that of the liquid air of the high pressure column 9, as shown in Figure 1.
- the device may include an insufflation turbine which serves during start-up or a low-pressure nitrogen turbine 55.
- a flow of rich liquid 15 is withdrawn from the high pressure column and sent to the sub-cooler 17, divided in two and sent in part to the lower column pressure, after expansion in the valve 21 and in part at the head condenser 23 of the auxiliary column 25 after expansion in the valve 27. At least the rich liquid partially vaporized in the overhead condenser is sent to the lower column pressure 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the low pressure column.
- a nitrogen gas flow 19 can optionally be withdrawn from the head of the high pressure column 9.
- the auxiliary column is supplied by a gas flow 29 containing between 5 and 15% mol. argon, preferably around 7 mol%. argon.
- the tank liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.
- the auxiliary column 25 can alternatively be supplied with a liquid flow containing between 5 and 15 mol%. argon, preferably around 7 mol%. argon.
- column 25 will have a tank reboiler, heated by a gas flow such as air or nitrogen from the high pressure column 9.
- a liquid air flow 33 and a lean liquid flow 35 are sent from the high pressure column 9 to low pressure column 11, after having been sub-cooled in the sub-cooler 17 and expanded in valves.
- a liquid oxygen flow 37 containing 99.5% mol. oxygen is drawn in low pressure column tank, pressurized by a pump 39 and vaporized in the exchanger 3.
- the mixture 53 heats up in the sub-cooler 17 then heats up in the exchanger 3.
- the mixture can then be discharged into the atmosphere and / or can be used to regenerate the adsorbent beds 4 or reversible exchangers and / or sent in upstream of the expansion machine 51 of a gas turbine after a step of compression.
- part of the mixture 53 can be expanded in a turbine 55 (dotted line).
- a triple column is used in place of the double column of Figure 1.
- An air flow 1 is purified by adsorbent beds 4 is divided into two.
- Flow 2 is boosted to a higher pressure, sent to the heat exchanger heat 3 where it cools by ensuring the vaporization of liquid oxygen and then at a hydraulic turbine 5 where it exits in at least partially liquid form.
- This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly at the low pressure column 11 operating between 4 and 6 bar and / or possibly at the intermediate pressure column 40 operating between 7 and 9 bar, either by sending part of the liquid of a capacity upstream of the middle column pressure either by withdrawing a flow having a composition similar to that of liquid air of the high pressure column 9, as shown in FIG. 2.
- the device may include an insufflation turbine which serves during start-up or a low-pressure nitrogen turbine 55.
- a flow of rich liquid 15 is withdrawn from the high pressure column and sent to the sub-cooler 17, divided in two and sent partly to the middle of the column operating at intermediate pressure 40, after expansion in valve 21 and partly at head condenser 23 of the auxiliary column 25 after expansion in the valve 27.
- the at least partially vaporized rich liquid in the overhead condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a flow gases are sent from the condenser to the low pressure column.
- a nitrogen gas flow 19 can optionally be withdrawn from the head of the high pressure column 9.
- the auxiliary column is supplied with part of a gas flow 29 containing between 5 and 15 mol%. argon, preferably around 7 mol%. argon.
- the liquid tank 31 of the auxiliary column is returned to the low pressure column which operates at substantially the same pressure as the auxiliary column.
- the auxiliary column 25 can alternatively be supplied with a liquid flow containing between 5 and 15 mol%. argon, preferably around 7 mol%. argon.
- column 25 will have a tank reboiler, heated by a gas flow such as air or nitrogen from the high pressure column 9.
- the rest of the gas flow 29 is used to heat the tank reboiler 41 of the column 40 and after condensation is returned to the low pressure column with the flow rate 31.
- the tank liquid 43 of the column 40 is partly sent directly to the low pressure column and partly to the condenser at the top of column 40 where it at least partially vaporizes before being sent to the low pressure column at its tower.
- the overhead liquid 47 of the column 40 is sub-cooled in the exchanger 17, expanded, mixed with expanded flow 35 and sent to the top of the lower column pressure.
- a liquid air flow 33 and a lean liquid flow 35 are sent from the high pressure column 9 to low pressure column 11, after having been sub-cooled in the sub-cooler 17 and expanded in valves.
- a liquid oxygen flow 37 containing 99.5% mol. oxygen is drawn in low pressure column tank, pressurized by a pump 39 and vaporized in the exchanger 3.
- the mixture 53 heats up in the sub-cooler 17 then heats up in the exchanger 3.
- the mixture can then be discharged into the atmosphere and / or can be used to regenerate the adsorbent beds 4 or reversible exchangers and / or sent in upstream of the expansion machine 51 of a gas turbine after a step of possible compression.
- part of the mixture 53 can be expanded in a turbine 55 (dotted line).
- the method according to the invention is of particular interest in the case in which the nitrogen in the low pressure column is valued, for example by sending it to an expansion machine 51 of a gas turbine.
- at least part of the air 1 can come from compressor 53 of the gas turbine and the oxygen produced by the device distillation can be used for the gasification necessary to produce the fuel for the gas turbine.
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- Engineering & Computer Science (AREA)
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- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
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- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
Description
La présente invention est relative à un procédé et à un appareil de production d'un fluide enrichi en oxygène par distillation cryogénique d'un mélange contenant de l'azote, de l'oxygène et de l'argon.The present invention relates to a production method and apparatus of a fluid enriched in oxygen by cryogenic distillation of a mixture containing nitrogen, oxygen and argon.
En particulier il concerne un procédé et à un appareil de séparation d'air par distillation cryogénique permettant la production d'oxygène pur, c'est à dire de l'oxygène contenant au moins 95% mol. oxygène, de préférence au moins 98% mol. d'oxygène ou même 99,5% mol. d'oxygène.In particular, it relates to a method and an apparatus for separating air by cryogenic distillation allowing the production of pure oxygen, i.e. oxygen containing at least 95% mol. oxygen, preferably at least 98% mol. oxygen or even 99.5% mol. oxygen.
Lorsqu'on veut faire de l'oxygène pur, on doit nécessairement séparer l'oxygène de l'argon. Si les colonnes de l'appareil opèrent toutes à une pression au-dessus de 2 bar, la distillation est difficile.When we want to make pure oxygen, we must necessarily separate the oxygen argon. If the columns of the device all operate at a pressure above 2 bar, distillation is difficult.
La production d'argon pur nécessite une colonne ayant plus que 100 plateaux théoriques.The production of pure argon requires a column with more than 100 trays theoretical.
La demande de brevet EP-A-0540900 décrit un procédé de production d'oxygène impur dans lequel une partie de l'argon impur contenant au moins 90% d'argon d'une colonne de mixture est mélangé avec l'azote résiduaire d'une simple colonne. La colonne de mixture opère à la même pression basse que la colonne basse pression, jusqu'à 1,75 bara.Patent application EP-A-0540900 describes a production process impure oxygen in which part of the impure argon containing at least 90% of argon from a column of mixture is mixed with the residual nitrogen from a simple column. The mixing column operates at the same low pressure as the low column pressure, up to 1.75 bara.
EP-A-0384213 a une colonne basse pression opérant à entre 1,5 et 10 bara mais la colonne argon opère à une pression plus basse.EP-A-0384213 has a low pressure column operating at between 1.5 and 10 bara but the argon column operates at a lower pressure.
US-A-4932212 décrit le cas dans lequel la colonne basse pression et la colonne argon opèrent à des pressions entre 1 et 2 bars.US-A-4932212 describes the case in which the low pressure column and the argon column operate at pressures between 1 and 2 bars.
EP-A-0518491 décrit un procédé de production d'azote gazeux sous pression et accessoirement de l'azote liquide, de l'argon liquide et de l'oxygène liquide dans lequel la colonne basse pression et la colonne argon opèrent à une pression substantiellement identique au-dessus de 2,5 bara. Aucun débit d'argon gazeux n'est produit.EP-A-0518491 describes a process for the production of nitrogen gas under pressure and incidentally liquid nitrogen, liquid argon and liquid oxygen in which the low pressure column and the argon column operate at a pressure substantially identical above 2.5 bara. No argon gas flow is produced.
EP-A-0952415 décrit un appareil comprenant une double colonne et une colonne argon opérant avec un rendement inférieur au rendement optimal.EP-A-0952415 describes an apparatus comprising a double column and a argon column operating with a yield lower than the optimal yield.
Un but de la présente invention est d'augmenter le rendement en oxygène pur d'un appareil de séparation d'air.An object of the present invention is to increase the yield of pure oxygen an air separation device.
Un autre but de l'invention est de fournir un appareil de séparation d'air particulièrement bien adapté aux demandes de grandes quantités d'azote sous pression (typiquement en cas d'intégration avec une turbine à gaz d'un IGCC). Another object of the invention is to provide an air separation device particularly well suited to the demands of large quantities of nitrogen under pressure (typically when integrated with an IGCC gas turbine).
Selon un objet de l'invention, il est prévu un procédé de production d'un débit
enrichi en oxygène dans un appareil de distillation cryogénique comprenant les étapes
de:
Par exemple le débit enrichi en argon ou le débit enrichi en argon mélangé avec un gaz enrichi en azote peut être envoyé en amont de la machine de détente d'une turbine à gaz..For example the flow enriched in argon or the flow enriched in argon mixed with a gas enriched in nitrogen can be sent upstream of the expansion machine of a gas turbine..
Le débit enrichi en argon peut contenir entre 10 et 95 % mol. d'argon (ou entre 40 et 95% mol. d'argon) ,entre 2 et 40.% mol d'oxygène et entre 2 et 40 % mol. d'azote.The flow enriched in argon can contain between 10 and 95 mol%. argon (or between 40 and 95% mol. argon), between 2 and 40.% mol of oxygen and between 2 and 40% mol. nitrogen.
Optionnellement tout le débit enrichi en argon est rejeté à l'atmosphère et/ou sert à régénérer des lits d'adsorbants ou des échangeurs réversibles et/ou est mélangé avec un gaz résiduaire de l'appareil et/ou un autre appareil et/ou envoyé en amont de la machine de détente d'une turbine à gaz.Optionally all the flow enriched in argon is released to the atmosphere and / or used to regenerate adsorbent beds or reversible exchangers and / or is mixed with a waste gas from the appliance and / or another appliance and / or sent upstream of the gas turbine expansion machine.
Dans ce cas, il peut tout de même y avoir une production d'argon, par exemple en soutirant un débit plus riche en argon de la colonne auxiliaire qui est le produit.In this case, there can still be a production of argon, for example by drawing off a richer flow of argon from the auxiliary column which is the product.
Le débit enrichi en argon qui est rejeté à l'atmosphère et/ou qui sert à régénérer des lits d'adsorbants ou des échangeurs réversibles et/ou qui est mélangé avec un gaz enrichi en azote de l'appareil et/ou un autre appareil et/ou qui est envoyé en amont de la machine de détente d'une turbine à gaz peut constituer entre 0,3 et 2% de l'air, de préférence entre 0,5 et 1% de l'air. Pour cette raison, il est préférable de mélanger le débit enrichi en argon avec un gaz enrichi en azote contenant au moins 90 %mol. d'azote provenant par exemple de la colonne basse pression d'une double colonne et d'utiliser le mélange pour régénérer des lits d'adsorbants ou des échangeurs réversibles et/ou pour envoyer le mélange à une turbine à gaz et/ou de détendre le mélange dans une turbine. Ainsi le mélange formé comprend moins de 2 % mol. d'argon, de préférence moins de 1% mol. d'argon.The flow enriched in argon which is released to the atmosphere and / or which is used to regenerate adsorbent beds or reversible exchangers and / or which is mixed with a gas enriched in nitrogen from the device and / or another device and / or which is sent upstream of the expansion machine of a gas turbine can constitute between 0.3 and 2% of the air, preferably between 0.5 and 1% of the air. For this reason, it is best to mix the flow enriched in argon with a gas enriched in nitrogen containing at least 90% mol. nitrogen coming for example from the low pressure column of a double column and use the mixture to regenerate adsorbent beds or reversible exchangers and / or to send the mixture to a gas turbine and / or to expand the mixture in a turbine. Thus the mixture formed comprises less than 2% mol. argon, preferably less than 1% mol. argon.
La colonne basse pression peut opérer entre 2 et 10 bara, de préférence au-dessus de 2,5 bara.The low pressure column can operate between 2 and 10 bara, preferably above 2.5 bara.
Par exemple, l'appareil peut comprendre une colonne auxiliaire de séparation d'un débit contenant au moins de l'argon et de l'oxygène et deux autres colonnes, dont une colonne haute pression et une colonne basse pression reliées thermiquement entre elles, la colonne auxiliaire étant alimentée à partir de la colonne basse pression.For example, the apparatus may include an auxiliary separation column a flow containing at least argon and oxygen and two other columns, of which a high pressure column and a low pressure column thermally connected between them, the auxiliary column being supplied from the low pressure column.
Alternativement l'appareil peut comprendre une colonne auxiliaire de séparation d'un débit contenant au moins de l'argon et de l'oxygène et au moins trois autres colonnes, dont une colonne haute pression, une colonne pression intermédiaire et une colonne basse pression reliées thermiquement entre elles, la colonne auxiliaire étant alimentée à partir de la colonne basse pression ou la colonne pression intermédiaire.Alternatively the apparatus may include an auxiliary separation column of a flow rate containing at least argon and oxygen and at least three others columns, including a high pressure column, an intermediate pressure column and a low pressure column thermally connected to each other, the auxiliary column being supplied from the low pressure column or the intermediate pressure column.
Selon un autre objet de l'invention, il est prévu un procédé intégré de séparation d'air et de production d'énergie comprenant un procédé selon l'une des revendications 1 à 12 dans lequel on envoie un gaz enrichi en azote de la colonne opérant préférablement à la pression la plus basse à la turbine à gaz ,après une étape éventuelle de compression et, éventuellement on envoie un fluide enrichi en oxygène d'une colonne de l'appareil à un gazéifieur.According to another object of the invention, an integrated method of separation is provided. of air and energy production comprising a method according to one of claims 1 to 12 in which a nitrogen-enriched gas is sent from the operating column preferably at the lowest pressure at the gas turbine, after one step possible compression and, optionally, a fluid enriched with oxygen is sent from an appliance column to a gasifier.
Selon un autre objet de l'invention, il est prévu un appareil de production
d'oxygène par distillation cryogénique comprenant :
De préférence il n'y a pas de moyen de détente entre la colonne alimentant la colonne auxiliaire et la colonne auxiliaire.Preferably there is no means of expansion between the column supplying the auxiliary column and the auxiliary column.
Optionnellement la colonne auxiliaire contient entre 30 et 40 plateaux théoriques.Optionally the auxiliary column contains between 30 and 40 trays theoretical.
Ainsi avec une colonne auxiliaire opérant à la même pression que la colonne basse pression, et de préférence opérant à une pression au-dessus de 2 bar, la séparation d'oxygène et argon en cuve de la colonne basse pression est facilitée. Dans ce cas le fluide enrichi en argon soutiré de la colonne auxiliaire n'est pas nécessairement un produit final de l'appareil mais peut servir à refroidir les débits rentrant dans les colonnes ou à fournir des frigories par détente.So with an auxiliary column operating at the same pressure as the column low pressure, and preferably operating at a pressure above 2 bar, the separation of oxygen and argon in the low pressure column tank is facilitated. In in this case the fluid enriched in argon withdrawn from the auxiliary column is not necessarily an end product of the device but can be used to cool flows re-entering the columns or supplying frigories by expansion.
L'invention sera décrite en plus de détail en se référant aux figures.The invention will be described in more detail with reference to the figures.
La figure 1 est un schéma d'un appareil de production d'oxygène selon l'invention utilisant une double colonne.Figure 1 is a diagram of an oxygen production apparatus according to the invention using a double column.
La figure 2 est un schéma d'un appareil de production d'oxygène selon l'invention utilisant une triple colonne.Figure 2 is a diagram of an oxygen production apparatus according to the invention using a triple column.
Dans la figure 1, un débit d'air 1 de 1000Nm3/h est épuré par des lits
d'adsorbants 4 est divisé en deux. Le débit 2 est surpressé à une pression plus élevée,
envoyé dans l'échangeur de chaleur 3 où il se refroidit en assurant la vaporisation de
l'oxygène liquide et ensuite à une turbine hydraulique 5 où il sort sous forme au moins
partiellement liquide. Ce liquide (ou mélange diphasique) 7 est envoyé à la colonne
haute pression 9 opérant entre 14 et 15 bar et éventuellement en partie à la colonne
basse pression 11 opérant entre 4 et 6 bar (ou même entre 2 et 10 bar), soit en
envoyant une partie du liquide d'une capacité en amont de la colonne moyenne pression
soit en soutirant un débit ayant une composition similaire à celle de l'air liquide de la
colonne haute pression 9, comme montré à la figure 1.In figure 1, an air flow 1 of 1000Nm3 / h is purified by beds
adsorbent 4 is divided into two. The
Le reste de l'air 13 à 14,4 bara est envoyé à la colonne haute pression 9.The rest of the
Eventuellement l'appareil peut comporter une turbine d'insufflation qui sert
pendant le démarrage ou une turbine d'azote basse pression 55. Optionally the device may include an insufflation turbine which serves
during start-up or a low-
Un débit de liquide riche 15 est soutiré de la colonne haute pression et envoyé
au sous refroidisseur 17, divisé en deux et envoyé en partie à la colonne basse
pression, après détente dans la vanne 21 et en partie au condenseur de tête 23 de la
colonne auxiliaire 25 après détente dans la vanne 27. Le liquide riche au moins
partiellement vaporisé dans le condenseur de tête est envoyé à la colonne basse
pression 11. Si la vaporisation est partielle, un débit liquide et un débit gazeux sont
envoyés du condenseur à la colonne basse pression.A flow of rich liquid 15 is withdrawn from the high pressure column and sent
to the sub-cooler 17, divided in two and sent in part to the lower column
pressure, after expansion in the
Un débit d'azote gazeux 19 peut éventuellement être soutiré de la tête de la
colonne haute pression 9.A
La colonne auxiliaire est alimentée par un débit gazeux 29 contenant entre 5 et
15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Le liquide de cuve 31 de la
colonne auxiliaire est renvoyé à la colonne basse pression qui opère substantiellement à
la même pression que la colonne auxiliaire.The auxiliary column is supplied by a
Le colonne auxiliaire 25 peut alternativement être alimentée par un débit liquide
contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Dans ce
cas la colonne 25 aura un rebouilleur de cuve, chauffe par un débit gazeux tel que l'air
ou de l'azote de la colonne haute pression 9.The
Un débit d'air liquide 33 et un débit de liquide pauvre 35 sont envoyés de la
colonne haute pression 9 à la colonne basse pression 11, après avoir été sous-refroidis
dans le sous refroidisseur 17 et détendus dans des vannes.A
Un débit d'oxygène liquide 37 contenant 99,5% mol. d'oxygène est soutiré en
cuve de la colonne basse pression, pressurisé par une pompe 39 et vaporisé dans
l'échangeur 3.A
Un gaz enrichi en argon 49 constituant entre 0,5 et 1% de l'air envoyé à
l'appareil et contenant entre 40 et 95 % mol. d'argon soutiré de la tête de la colonne
auxiliaire 25 est mélangé avec de l'azote résiduaire 47 de la tête de la colonne basse
pression. Le mélange 53 se réchauffe dans le sous refroidisseur 17 puis se réchauffe
dans l'échangeur 3. Le mélange peut ensuite être rejeté à l'atmosphère et/ou peut servir
à régénérer les lits d'adsorbants 4 ou des échangeurs réversibles et/ou envoyé en
amont de la machine de détente 51 d'une turbine à gaz après une étape de
compression.A gas enriched in
Eventuellement auparavant une partie du mélange 53 peut être détendue dans
une turbine 55 (en pointillés).Possibly beforehand, part of the
Par rapport à un système classique avec une colonne haute pression à 14,3 bara et une colonne basse pression à 4,8 bara mais sans colonne auxiliaire, le procédé de la Figure 1 permet d'augmenter le rendement en oxygène de 78% à 90%. Compared to a conventional system with a high pressure column at 14.3 bara and a low pressure column at 4.8 bara but without an auxiliary column, the process in Figure 1 increases the oxygen yield from 78% to 90%.
Dans la Figure 2, une triple colonne est utilisée à la place de la double colonne
de la Figure 1. Un débit d'air 1 est épuré par des lits d'adsorbants 4 est divisé en deux.
Le débit 2 est surpressé à une pression plus élevée, envoyé dans l'échangeur de
chaleur 3 où il se refroidit en assurant la vaporisation de l'oxygène liquide et ensuite à
une turbine hydraulique 5 où il sort sous forme au moins partiellement liquide. Ce liquide
(ou mélange diphasique) 7 est envoyé à la colonne haute pression 9 opérant entre 14 et
15 bar et éventuellement en partie à la colonne basse pression 11 opérant entre 4 et 6
bar et/ou éventuellement à la colonne pression intermédiaire 40 opérant entre 7 et 9 bar,
soit en envoyant une partie du liquide d'une capacité en amont de la colonne moyenne
pression soit en soutirant un débit ayant une composition similaire à celle de l'air liquide
de la colonne haute pression 9, comme montré à la figure 2.In Figure 2, a triple column is used in place of the double column
of Figure 1. An air flow 1 is purified by adsorbent beds 4 is divided into two.
Le reste de l'air 13 à 14,4 bara est envoyé à la colonne haute pression 9.The rest of the
Eventuellement l'appareil peut comporter une turbine d'insufflation qui sert
pendant le démarrage ou une turbine d'azote basse pression 55.Optionally the device may include an insufflation turbine which serves
during start-up or a low-
Un débit de liquide riche 15 est soutiré de la colonne haute pression et envoyé
au sous refroidisseur 17, divisé en deux et envoyé en partie au milieu de la colonne
opérant à pression intermédiaire 40, après détente dans la vanne 21 et en partie au
condenseur de tête 23 de la colonne auxiliaire 25 après détente dans la vanne 27. Le
liquide riche au moins partiellement vaporisé dans le condenseur de tête est envoyé à la
colonne basse pression 11. Si la vaporisation est partielle, un débit liquide et un débit
gazeux sont envoyés du condenseur à la colonne basse pression.A flow of rich liquid 15 is withdrawn from the high pressure column and sent
to the sub-cooler 17, divided in two and sent partly to the middle of the column
operating at
Un débit d'azote gazeux 19 peut éventuellement être soutiré de la tête de la
colonne haute pression 9.A
La colonne auxiliaire est alimentée par une partie d'un débit gazeux 29
contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Le liquide
de cuve 31 de la colonne auxiliaire est renvoyé à la colonne basse pression qui opère
substantiellement à la même pression que la colonne auxiliaire.The auxiliary column is supplied with part of a
Le colonne auxiliaire 25 peut alternativement être alimentée par un débit liquide
contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Dans ce
cas la colonne 25 aura un rebouilleur de cuve, chauffe par un débit gazeux tel que l'air
ou de l'azote de la colonne haute pression 9.The
Le reste du débit gazeux 29 sert à chauffer le rebouilleur de cuve 41 de la
colonne 40 et après condensation est renvoyé à la colonne basse pression avec le débit
31.The rest of the
Le liquide de cuve 43 de la colonne 40 est envoyé en partie directement à la
colonne basse pression et en partie au condenseur de tête de la colonne 40 où il se
vaporise au moins partiellement avant d'être envoyé à la colonne basse pression à son
tour.The
Le liquide de tête 47 de la colonne 40 est sousrefroidi dans l'échangeur 17,
détendu, mélangé avec le débit détendu 35 et envoyé en tête de la colonne basse
pression.The
Un débit d'air liquide 33 et un débit de liquide pauvre 35 sont envoyés de la
colonne haute pression 9 à la colonne basse pression 11, après avoir été sous-refroidis
dans le sous refroidisseur 17 et détendus dans des vannes.A
Un débit d'oxygène liquide 37 contenant 99,5% mol. d'oxygène est soutiré en
cuve de la colonne basse pression, pressurisé par une pompe 39 et vaporisé dans
l'échangeur 3.A
Un gaz enrichi en argon 49 constituant entre 0,5 et 1% de l'air envoyé à
l'appareil et contenant entre 40 et 95 % mol. d'argon soutiré de la tête de la colonne
auxiliaire 25 est mélangé avec de l'azote résiduaire 47 de la tête de la colonne basse
pression. Le mélange 53 se réchauffe dans le sous refroidisseur 17 puis se réchauffe
dans l'échangeur 3. Le mélange peut ensuite être rejeté à l'atmosphère et/ou peut servir
à régénérer les lits d'adsorbants 4 ou des échangeurs réversibles et/ou envoyé en
amont de la machine de détente 51 d'une turbine à gaz après une étape de
compression éventuelle.A gas enriched in
Eventuellement auparavant une partie du mélange 53 peut être détendue dans
une turbine 55 (en pointillés).Possibly beforehand, part of the
Le procédé selon l'invention présente un intérêt particulier dans le cas dans
lequel l'azote de la colonne basse pression est valorisé, par exemple en l'envoyant à
une machine de détente 51 d'une turbine à gaz. Dans ce cas au moins une partie de l'air
1 peut provenir du compresseur 53 de la turbine à gaz et l'oxygène produit par l'appareil
de distillation peut servir à la gazéification nécessaire pour produire le carburant de la
turbine à gaz.The method according to the invention is of particular interest in the case in
which the nitrogen in the low pressure column is valued, for example by sending it to
an
Claims (16)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0004284 | 2000-04-04 | ||
FR0004284A FR2807150B1 (en) | 2000-04-04 | 2000-04-04 | PROCESS AND APPARATUS FOR PRODUCING OXYGEN ENRICHED FLUID BY CRYOGENIC DISTILLATION |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1143216A1 true EP1143216A1 (en) | 2001-10-10 |
EP1143216B1 EP1143216B1 (en) | 2012-03-07 |
Family
ID=8848848
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP01400749A Expired - Lifetime EP1143216B1 (en) | 2000-04-04 | 2001-03-22 | Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation |
Country Status (6)
Country | Link |
---|---|
US (1) | US6434973B2 (en) |
EP (1) | EP1143216B1 (en) |
JP (1) | JP2001349669A (en) |
AT (1) | ATE548619T1 (en) |
ES (1) | ES2382453T3 (en) |
FR (1) | FR2807150B1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1249676B1 (en) * | 2001-04-10 | 2005-11-02 | L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Nitrogen gas supply process for a gas turbine combustor combined with an air distillation unit |
WO2016146246A1 (en) * | 2015-03-13 | 2016-09-22 | Linde Aktiengesellschaft | Plant for producing oxygen by cryogenic air separation |
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US6546748B1 (en) * | 2002-06-11 | 2003-04-15 | Praxair Technology, Inc. | Cryogenic rectification system for producing ultra high purity clean dry air |
FR2874249A1 (en) * | 2004-08-10 | 2006-02-17 | Air Liquide | Air separation by cryogenic distillation using medium and low pressure columns, for production of oxygen and/or nitrogen, with residual stream extracted from low pressure column to maintain product purity |
US20070095100A1 (en) * | 2005-11-03 | 2007-05-03 | Rankin Peter J | Cryogenic air separation process with excess turbine refrigeration |
FR2913758B3 (en) * | 2007-03-12 | 2009-11-13 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
FR2930629B1 (en) * | 2008-04-23 | 2010-05-07 | Air Liquide | APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
US20110138856A1 (en) * | 2009-12-10 | 2011-06-16 | Henry Edward Howard | Separation method and apparatus |
EP2634517B1 (en) * | 2012-02-29 | 2018-04-04 | L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
EP2713128A1 (en) * | 2012-10-01 | 2014-04-02 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for the separation of air by cryogenic distillation |
FR3074274B1 (en) * | 2017-11-29 | 2020-01-31 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
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2001
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- 2001-03-22 ES ES01400749T patent/ES2382453T3/en not_active Expired - Lifetime
- 2001-03-22 EP EP01400749A patent/EP1143216B1/en not_active Expired - Lifetime
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- 2001-04-04 US US09/825,341 patent/US6434973B2/en not_active Expired - Lifetime
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WO2016146246A1 (en) * | 2015-03-13 | 2016-09-22 | Linde Aktiengesellschaft | Plant for producing oxygen by cryogenic air separation |
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Also Published As
Publication number | Publication date |
---|---|
ES2382453T3 (en) | 2012-06-08 |
FR2807150A1 (en) | 2001-10-05 |
JP2001349669A (en) | 2001-12-21 |
US20010052243A1 (en) | 2001-12-20 |
FR2807150B1 (en) | 2002-10-18 |
ATE548619T1 (en) | 2012-03-15 |
US6434973B2 (en) | 2002-08-20 |
EP1143216B1 (en) | 2012-03-07 |
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