EP1966554B1 - Appareil de séparation d'air par distillation cryogénique - Google Patents
Appareil de séparation d'air par distillation cryogénique Download PDFInfo
- Publication number
- EP1966554B1 EP1966554B1 EP06842175.9A EP06842175A EP1966554B1 EP 1966554 B1 EP1966554 B1 EP 1966554B1 EP 06842175 A EP06842175 A EP 06842175A EP 1966554 B1 EP1966554 B1 EP 1966554B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- line
- column
- section
- exchange
- exchange line
- 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.)
- Active
Links
- 238000004821 distillation Methods 0.000 title claims description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 35
- 239000007788 liquid Substances 0.000 claims description 17
- 229910052757 nitrogen Inorganic materials 0.000 claims description 16
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 9
- 229910052782 aluminium Inorganic materials 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 4
- 239000004411 aluminium Substances 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 239000010935 stainless steel Substances 0.000 claims description 4
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 2
- 238000001577 simple distillation Methods 0.000 claims 1
- 238000010926 purge Methods 0.000 description 14
- 241000897276 Termes Species 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000012217 deletion Methods 0.000 description 2
- 230000037430 deletion Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000001629 suppression Effects 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Images
Classifications
-
- 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
- F25J3/04624—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 integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
-
- 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
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
-
- 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
-
- 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
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
-
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
-
- 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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
-
- 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
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface
Definitions
- the cold box is higher, but much less wide because the exchanger is above the column, which results in a significant gain.
- a compressed air flow 1 is purified in a purification unit (not shown) and sent to the hot end of an exchange line 3.
- the exchange line comprises a conventional heat exchange section 3A and a section 3B of deflegmation. The two sections are contiguous and the exchange line is a plate and finned heat exchanger.
- the air 1 cools in the exchange line to the cold end of the section 3A, then leaves the exchange line to be sent to the base of a single distillation column 7.
- the column 7 contains packings structured or trays 9.
- the air separates into an oxygen-enriched flow 11 and a nitrogen-enriched flow.
- the oxygen-enriched flow 11 is withdrawn in liquid form from column 7 and sent to the cold end of section 3B.
- the nitrogen-enriched gas exits directly from the top of the column in the passages of section 3B.
- the exchange line 3 has the same width as the head of the column 7 and is welded to the ferrule of the column (by a round-square or round-rectangular adapter piece).
- the frigories necessary for distillation are provided by liquid nitrogen liquor 13 from storage in a manner known as described in US Pat. EP-A-0452177 .
- an air turbine 5 or vaporized rich liquid may be provided.
- Section 3B includes two nitrogen passages for a rich liquid passage.
- the rich liquid vaporizes entirely in this section 3B of the exchange line 3 so that it is completely converted into a gas 15.
- Section 3A of the exchange line is composed of the classic main exchange line.
- the nitrogen gas 17 and the vaporized rich liquid 15 heat up against the incoming air 1.
- the exchange line 3 is preferably copper or aluminum and the column 7 will be stainless steel. If the exchange line is aluminum and the stainless steel column, provide a joint junction (s) between the two. Otherwise the exchange line 3 and the column 7 may be aluminum.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
- La présente invention concerne un appareil de séparation d'air par distillation cryogénique, en particulier pour la production d'azote, conformément au préambule de la revendication 1 et connu du document
US-6351969-B1 Un générateur d'azote décrit dansUS-A-5899093 comprend une ligne d'échange où se refroidit l'air à distiller, une colonne de distillation où l'air est séparé en un débit riche en azote en tête de colonne et en un débit enrichi en oxygène en cuve de colonne. Pour fournir du reflux, une partie du débit riche en azote est envoyé à un rebouilleur-condenseur où il se condense par échange de chaleur avec le débit enrichi en oxygène. Alternativement l'azote peut se condenser dans un déphlegmateur. Le liquide riche partiellement vaporisé dans le déphlegmateur est envoyé à un séparateur de phases et le liquide formé dans le séparateur circule de nouveau vers le déphlegmateur. La présente invention vise à supprimer le condenseur-rebouilleur à bain, qui impose des contraintes : - de coût d'investissement, notamment pour assurer une recirculation de liquide
- de concentration des impuretés (CnHm, N2O, CO2,...)
- de purge liquide
- de maintien de niveau
- de mesure de niveau
- Selon un objet de l'invention, il est prévu un appareil selon la revendication 1.
- Selon des objets facultatifs :
- l'appareil comprend des moyens de biberonnage et/ou de détente d'air ou de liquide riche vaporisé ;
- la conduite pour envoyer de l'air comprimé, épuré et refroidi de la ligne d'échange à la colonne de distillation est connectée au bout froid de la section d'échange de chaleur ;
- l'appareil comprend des moyens de redistribution des passages entre la section d'échange de chaleur et la section de déflegmation ;
- la ligne d'échange est en cuivre ou en aluminium et/ou la colonne de distillation est en acier inoxydable ;
- la ligne d'échange et la colonne de distillation sont en aluminium ;
- la ligne d'échange est un échangeur à plaques et à ailettes brasées.
- L'invention propose d'intégrer la fonction « vaporisation-condensation » dans l'échangeur principal en utilisant la partie la plus froide de l'échangeur comme déphlegmateur afin d'y condenser l'azote. Les intérêts de l'invention sont les suivants :
- Il y a une purge « naturelle » du liquide riche, qui est peu concentré par vaporisation (à l'image d'un appareil à pompe).
- Comme on n'a plus besoin de purge de liquide de déconcentration, ceci permet :
- ∘ de supprimer les équipements qui y sont associés, dont la fosse à cailloux (ou pot de purge) nécessaire du fait d'une purge régulière et dont les équipements qui permettent de s'assurer de la fiabilité et l'effectivité de la purge,
- ∘ un gain de puissance frigorifique (pour un appareil biberonné, la consommation d'azote liquide est fortement réduite d'où une réduction du coût opératoire),
- ∘ d'alléger le suivi opération de cette purge « critique » en terme de sécurité.
- Suppression de la mesure de niveau, des pinces de mises à chauds des prises d'impulsion, des éventuels bulleurs et de la jauge de niveau et allégement suivi opération de cette mesure « critique » en terme de sécurité.
- Suppression du pot de recirculation.
- Le surcoût sur échangeur est marginal, voire nul si on convertit une partie du gain de la puissance frigorifique dans une ligne d'échange un peu moins performante (et donc moins grande).
- La boite froide est plus haute, mais beaucoup moins large car l'échangeur est au-dessus de la colonne, ce qui se traduit par un gain important.
- L'invention sera décrite en plus de détail en se référant à la figure qui représente un appareil de séparation d'air selon l'invention.
- Un débit d'air 1 comprimé est épuré dans une unité d'épuration (non-illustrée) et envoyé au bout chaud d'une ligne d'échange 3. La ligne d'échange comprend une section 3A d'échange de chaleur classique et une section 3B de déphlegmation. Les deux sections sont contiguës et la ligne d'échange est un échangeur à plaques et à ailettes brasées.
- L'air 1 se refroidit dans la ligne d'échange jusqu'au bout froid de la section 3A, puis sort de la ligne d'échange pour être envoyé en base d'une simple colonne de distillation 7. La colonne 7 contient des garnissages structurés ou des plateaux 9.
- L'air se sépare en un débit 11 enrichi en oxygène et un débit enrichi en azote. Le débit enrichi en oxygène 11 est soutiré sous forme liquide de la colonne 7 et envoyé au bout froid de la section 3B.Le gaz enrichi en azote sort directement de la tête de la colonne dans les passages de la section 3B. De préférence la ligne d'échange 3 a la même largeur que la tête de la colonne 7 et est soudée à la virole de la colonne (par une pièce d'adaptation rond-carré ou rond-rectangulaire).
- Les frigories nécessaires à la distillation sont fournies par biberonnage d'azote liquide 13, provenant d'un stockage de manière connue décrite dans
EP-A-0452177 . Alternativement ou additionnellement une turbine d'air 5 ou de liquide riche vaporisé peut être prévue. - La section 3B comprend deux passages d'azote pour un passage de liquide riche. Le liquide riche se vaporise entièrement dans cette section 3B de la ligne d'échange 3 de sorte qu'il est entièrement transformé en gaz 15. L'azote se condense en partie : la partie condensée retombe par gravité dans la colonne pour servir de reflux, la ligne d'échange 3 étant installée au-dessus de la colonne par soudage direct. Le reste de l'azote gazeux 17 continue son ascension à travers toute la ligne d'échange 3.
- La section 3A de la ligne d'échange est composée de la ligne d'échange principale classique. L'azote gazeux 17 et le liquide riche vaporisé 15 se réchauffent face à l'air entrant 1.
- Pour optimiser la ligne d'échange 3, au niveau de l'interface entre les deux sections, on pourra ré-affecter les doubles passages azote de la section 3B de déphlegmation entre l'azote à réchauffer et l'air à refroidir de la section 3A. Ceci peut être réalisé par entrée/sortie de fluide (boite de distribution), ou, de façon préférentielle, par redistribution interne (utilisation de barres et de tôles séparatrices perforées).
- La ligne d'échange 3 est de préférence en cuivre ou en aluminium et la colonne 7 sera en acier inoxydable. Si la ligne d'échange est en aluminium et la colonne en acier inoxydable, il faut prévoir une (des) jonction(s) mixte(s) entre les deux. Sinon la ligne d'échange 3 et la colonne 7 peuvent être en aluminium.
Claims (6)
- Appareil de séparation d'air par distillation cryogénique pour la production d'azote comprenant :a) une ligne d'échange (3) qui est un échangeur à plaques et à ailettes braséesb) une simple colonne de distillation (7) contenant des plateaux et/ou des garnissages structurésc) une conduite (1) pour envoyer de l'air comprimé et épuré à la ligne d'échanged) une conduite pour envoyer de l'air comprimé, épuré et refroidi de la ligne d'échange à la colonne de distillatione) une conduite (11) pour soutirer un liquide enrichi en oxygène de la colonne et pour l'envoyer à la ligne d'échange et la ligne d'échange comprenant deux sections contiguës qui sont une section de déphlegmation (3B) et une section d'échange de chaleur (3A) ; la section de déphlegmation est connectée à la colonne et à la conduite de liquide enrichi en oxygène et la section d'échange de chaleur est connectée à la conduite d'air et à la section de déphlegmation, la ligne d'échange (3) étant située au-dessus de la colonne de distillation (7),caractérisé en ce que la section de déphlegmation (3B) est fixée à la tête de la colonne (7), et la colonne et la section de déphlegmation sont agencées de sorte que le gaz enrichi en azote sort directement de la tête de la colonne dans les passages de cette section.
- Appareil selon la revendication 1 comprenant des moyens de biberonnage (13) et/ou de détente d'air (5) ou de liquide riche vaporisé.
- Appareil selon la revendication 1 ou 2 dans lequel la conduite pour envoyer de l'air comprimé, épuré et refroidi de la ligne d'échange à la colonne de distillation est connectée au bout froid de la section d'échange de chaleur (3A).
- Appareil selon l'une des revendications précédentes comprenant des moyens de redistribution des passages entre la section d'échange de chaleur et la section de déphlegmation.
- Appareil selon l'une des revendications précédentes dans lequel la ligne d'échange (3) est en cuivre ou en aluminium et/ou la colonne de distillation (7) est en acier inoxydable.
- Appareil selon l'une des revendications précédentes dans lequel la ligne d'échange (3) et la colonne de distillation (7) sont en aluminium.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL06842175T PL1966554T3 (pl) | 2005-12-20 | 2006-12-15 | Urządzenie do rozdzielania powietrza za pomocą destylacji kriogenicznej |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0553971A FR2895069B1 (fr) | 2005-12-20 | 2005-12-20 | Appareil de separation d'air par distillation cryogenique |
PCT/FR2006/051366 WO2007074276A2 (fr) | 2005-12-20 | 2006-12-15 | Appareil de separation d'air par distillation cryogenique |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1966554A2 EP1966554A2 (fr) | 2008-09-10 |
EP1966554B1 true EP1966554B1 (fr) | 2018-08-15 |
Family
ID=36660838
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP06842175.9A Active EP1966554B1 (fr) | 2005-12-20 | 2006-12-15 | Appareil de séparation d'air par distillation cryogénique |
Country Status (9)
Country | Link |
---|---|
US (1) | US20080271481A1 (fr) |
EP (1) | EP1966554B1 (fr) |
JP (1) | JP5074416B2 (fr) |
CN (1) | CN101341370B (fr) |
DK (1) | DK1966554T3 (fr) |
ES (1) | ES2689041T3 (fr) |
FR (1) | FR2895069B1 (fr) |
PL (1) | PL1966554T3 (fr) |
WO (1) | WO2007074276A2 (fr) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2026025A1 (fr) * | 2007-07-30 | 2009-02-18 | Linde Aktiengesellschaft | Procédé et dispositif de production d'azote sous haute pression par séparation cryogénique d'air dans une colonne simple |
FR2929384A1 (fr) * | 2008-03-27 | 2009-10-02 | Air Liquide | Appareil de separation d'air comprenant une simple colonne de distillation |
WO2009063146A1 (fr) * | 2008-03-28 | 2009-05-22 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Echangeur de chaleur et appareil de séparation d'air par distillation cryogénique incorporant un tel échangeur |
FR2973486B1 (fr) * | 2011-03-31 | 2013-05-03 | Air Liquide | Procede de separation d'air par distillation cryogenique |
WO2020150988A1 (fr) * | 2019-01-25 | 2020-07-30 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Processus et appareil pour fournir un gaz de secours sous pression |
Family Cites Families (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1472402A (en) * | 1973-07-18 | 1977-05-04 | Cryoplants Ltd | Air separation |
JP2716762B2 (ja) * | 1988-12-12 | 1998-02-18 | 大同ほくさん株式会社 | 高純度窒素ガス製造装置 |
FR2660741A1 (fr) | 1990-04-10 | 1991-10-11 | Air Liquide | Procede et installation de production d'azote gazeux, et systeme de fourniture d'azote correspondant. |
FR2665755B1 (fr) * | 1990-08-07 | 1993-06-18 | Air Liquide | Appareil de production d'azote. |
FR2675568B1 (fr) * | 1991-04-19 | 1993-07-16 | Air Liquide | Procede de separation cryogenique de melanges contenant de l'oxygene et garnissages organises pour la mise en óoeuvre de ce procede. |
FR2690231B1 (fr) * | 1992-04-17 | 1994-06-03 | Air Liquide | Echangeur de chaleur a ruissellement et installation de distillation d'air comportant un tel echangeur. |
US5275004A (en) * | 1992-07-21 | 1994-01-04 | Air Products And Chemicals, Inc. | Consolidated heat exchanger air separation process |
US5410885A (en) * | 1993-08-09 | 1995-05-02 | Smolarek; James | Cryogenic rectification system for lower pressure operation |
JP3957842B2 (ja) * | 1997-11-25 | 2007-08-15 | 大陽日酸株式会社 | 窒素製造方法及び装置 |
US5899093A (en) * | 1998-05-22 | 1999-05-04 | Air Liquide Process And Construction, Inc. | Process and apparatus for the production of nitrogen by cryogenic distillation |
US6079223A (en) * | 1999-05-04 | 2000-06-27 | Praxair Technology, Inc. | Cryogenic air separation system for producing moderate purity oxygen and moderate purity nitrogen |
US6125656A (en) * | 1999-11-03 | 2000-10-03 | Praxair Technology, Inc. | Cryogenic rectification method for producing nitrogen gas and liquid nitrogen |
US6237366B1 (en) * | 2000-04-14 | 2001-05-29 | Praxair Technology, Inc. | Cryogenic air separation system using an integrated core |
US6295836B1 (en) * | 2000-04-14 | 2001-10-02 | Praxair Technology, Inc. | Cryogenic air separation system with integrated mass and heat transfer |
US6351969B1 (en) * | 2001-01-31 | 2002-03-05 | Praxair Technology, Inc. | Cryogenic nitrogen production system using a single brazement |
JP4520667B2 (ja) * | 2001-07-17 | 2010-08-11 | 大陽日酸株式会社 | 空気分離方法および装置 |
EP1300640A1 (fr) * | 2001-10-04 | 2003-04-09 | Linde Aktiengesellschaft | Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air |
US6907751B2 (en) * | 2002-07-30 | 2005-06-21 | Air Products And Chemicals, Inc. | Liquid distributor |
JP4230213B2 (ja) * | 2002-12-24 | 2009-02-25 | 大陽日酸株式会社 | 空気液化分離装置及び方法 |
-
2005
- 2005-12-20 FR FR0553971A patent/FR2895069B1/fr not_active Expired - Fee Related
-
2006
- 2006-12-15 PL PL06842175T patent/PL1966554T3/pl unknown
- 2006-12-15 JP JP2008546547A patent/JP5074416B2/ja active Active
- 2006-12-15 ES ES06842175.9T patent/ES2689041T3/es active Active
- 2006-12-15 WO PCT/FR2006/051366 patent/WO2007074276A2/fr active Application Filing
- 2006-12-15 CN CN2006800479541A patent/CN101341370B/zh active Active
- 2006-12-15 EP EP06842175.9A patent/EP1966554B1/fr active Active
- 2006-12-15 US US12/097,641 patent/US20080271481A1/en not_active Abandoned
- 2006-12-15 DK DK06842175.9T patent/DK1966554T3/en active
Non-Patent Citations (1)
Title |
---|
None * |
Also Published As
Publication number | Publication date |
---|---|
CN101341370B (zh) | 2011-09-14 |
FR2895069A1 (fr) | 2007-06-22 |
CN101341370A (zh) | 2009-01-07 |
PL1966554T3 (pl) | 2018-11-30 |
WO2007074276A2 (fr) | 2007-07-05 |
FR2895069B1 (fr) | 2014-01-31 |
US20080271481A1 (en) | 2008-11-06 |
ES2689041T3 (es) | 2018-11-08 |
WO2007074276A3 (fr) | 2007-09-13 |
JP2009520176A (ja) | 2009-05-21 |
JP5074416B2 (ja) | 2012-11-14 |
EP1966554A2 (fr) | 2008-09-10 |
DK1966554T3 (en) | 2018-10-15 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP1966554B1 (fr) | Appareil de séparation d'air par distillation cryogénique | |
CA2788759C (fr) | Appareil et procede de separation d'un melange contenant du dioxyde de carbone par distillation | |
FR2991442A1 (fr) | Appareil et procede de separation cryogenique d'un melange de monoxyde de carbone et de methane ainsi que d'hydrogene et/ou d'azote | |
EP2149021B1 (fr) | Capacité de stockage, appareil et procédé de production de monoxyde de carbone et/ou d'hydrogène par séparation cryogénique intégrant une telle capacité | |
CA2865991C (fr) | Procede et appareil de separation d'un melange contenant du dioxyde de carbone par distillation | |
EP2694898B1 (fr) | Procédé et appareil de séparation d'air par distillation cryogénique | |
EP1078212B1 (fr) | Installation de distillation d'air et boite froide correspondante | |
EP2440871A2 (fr) | Appareil et procédé de séparation d'air par distillation cryogénique | |
EP1146300B1 (fr) | Echangeur vaporiseur-condenseur du type à bain | |
EP3058297B1 (fr) | Procédé et appareil de séparation d'air par distillation cryogénique | |
EP2132509B1 (fr) | Procédé et appareil de séparation d'air par distillation cryogénique | |
FR3102548A1 (fr) | Procédé et appareil de séparation d’air par distillation cryogénique | |
FR3110686A1 (fr) | Procédé de fourniture d’oxygène et/ou d’azote ainsi que d’argon à une zone géographique | |
FR2930328A1 (fr) | Procede et appareil de separation d'air par distillation cryogenique | |
FR2930331A1 (fr) | Procede et appareil de separation d'air par distillation cryogenique | |
FR2990019A1 (fr) | Procede et appareil de separation d'air par distillation cryogenique | |
WO2005047790A2 (fr) | Procede et installation d'enrichissement d'un flux gazeux en l'un de ses constituants | |
WO2009136077A2 (fr) | Procede et appareil de separation d'air par distillation cryogenique | |
WO2022162041A1 (fr) | Procédé et appareil de séparation d'un débit riche en dioxyde de carbone par distillation pour produire du dioxyde de carbone liquide | |
FR3119884A1 (fr) | Procédé de séparation d’air par distillation cryogénique | |
FR2926355A1 (fr) | Colonne de separation d'un melange de monoxyde de carbone et d'azote par distillation cryogenique et appareil incorporant une telle colonne. | |
FR2929384A1 (fr) | Appareil de separation d'air comprenant une simple colonne de distillation | |
WO2009130430A2 (fr) | Procede et appareil de separation d'air par distillation cryogenique | |
FR2787562A1 (fr) | Procede et installation de distillation d'air avec production d'argon | |
FR2947042A1 (fr) | Echangeur principal d'un appareil de separation d'air et procede de refroidissement d'air utilisant un tel echangeur |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 20080612 |
|
AK | Designated contracting states |
Kind code of ref document: A2 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR |
|
17Q | First examination report despatched |
Effective date: 20100820 |
|
DAX | Request for extension of the european patent (deleted) | ||
GRAP | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOSNIGR1 |
|
INTG | Intention to grant announced |
Effective date: 20180405 |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: DAVIDIAN, BENOIT |
|
GRAS | Grant fee paid |
Free format text: ORIGINAL CODE: EPIDOSNIGR3 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: EP Ref country code: GB Ref legal event code: FG4D Free format text: NOT ENGLISH Ref country code: AT Ref legal event code: REF Ref document number: 1030269 Country of ref document: AT Kind code of ref document: T Effective date: 20180815 |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FG4D Free format text: LANGUAGE OF EP DOCUMENT: FRENCH |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R096 Ref document number: 602006056116 Country of ref document: DE |
|
REG | Reference to a national code |
Ref country code: RO Ref legal event code: EPE |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: T3 Effective date: 20181008 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: TRGR |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2689041 Country of ref document: ES Kind code of ref document: T3 Effective date: 20181108 |
|
REG | Reference to a national code |
Ref country code: NL Ref legal event code: MP Effective date: 20180815 |
|
REG | Reference to a national code |
Ref country code: LT Ref legal event code: MG4D |
|
REG | Reference to a national code |
Ref country code: SK Ref legal event code: T3 Ref document number: E 28540 Country of ref document: SK |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BG Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20181115 Ref country code: NL Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 Ref country code: IS Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20181215 Ref country code: LT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 Ref country code: GR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20181116 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: IE Payment date: 20181210 Year of fee payment: 13 Ref country code: SE Payment date: 20181219 Year of fee payment: 13 Ref country code: SK Payment date: 20181127 Year of fee payment: 13 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LV Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: EE Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R097 Ref document number: 602006056116 Country of ref document: DE |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed |
Effective date: 20190516 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: MC Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20181215 Ref country code: SI Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: MM4A |
|
REG | Reference to a national code |
Ref country code: BE Ref legal event code: MM Effective date: 20181231 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20181215 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20181231 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: PT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: CY Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20180815 Ref country code: HU Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO Effective date: 20061215 |
|
REG | Reference to a national code |
Ref country code: FI Ref legal event code: MAE |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: EBP Effective date: 20191231 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: EUG |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: RO Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20191215 Ref country code: FI Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20191215 |
|
REG | Reference to a national code |
Ref country code: SK Ref legal event code: MM4A Ref document number: E 28540 Country of ref document: SK Effective date: 20191215 |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: UEP Ref document number: 1030269 Country of ref document: AT Kind code of ref document: T Effective date: 20180815 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SK Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20191215 Ref country code: SE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20191216 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DK Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20191231 |
|
P01 | Opt-out of the competence of the unified patent court (upc) registered |
Effective date: 20230523 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GB Payment date: 20231220 Year of fee payment: 18 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: IT Payment date: 20231221 Year of fee payment: 18 Ref country code: FR Payment date: 20231221 Year of fee payment: 18 Ref country code: DE Payment date: 20231214 Year of fee payment: 18 Ref country code: CZ Payment date: 20231208 Year of fee payment: 18 Ref country code: AT Payment date: 20231221 Year of fee payment: 18 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: PL Payment date: 20231211 Year of fee payment: 18 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: ES Payment date: 20240126 Year of fee payment: 18 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: CH Payment date: 20240102 Year of fee payment: 18 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: TR Payment date: 20231214 Year of fee payment: 18 |