EP1132700B1 - Procédé et installation de séparation d'air par distillation cryogénique - Google Patents
Procédé et installation de séparation d'air par distillation cryogénique Download PDFInfo
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- EP1132700B1 EP1132700B1 EP01400413A EP01400413A EP1132700B1 EP 1132700 B1 EP1132700 B1 EP 1132700B1 EP 01400413 A EP01400413 A EP 01400413A EP 01400413 A EP01400413 A EP 01400413A EP 1132700 B1 EP1132700 B1 EP 1132700B1
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- column
- air
- oxygen
- process according
- fraction
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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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- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
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- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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Definitions
- the present invention relates to a method and an installation of air separation by cryogenic distillation according to the preamble of claim 1 and claim 15, respectively.
- Such a process and a such an installation are known from DE-A-1 199 293.
- US-A-4947649 discloses a solution where air is compressed for introduce it at least partially in a single column. Such a solution is not applicable only if it is desired to produce nitrogen at a significantly higher pressure atmospheric pressure, particularly in the case of integration with a gas turbine. Conversely, if the air pressure supplied by the turbine compressor gas is very high, it is not advisable to use this process because the distillation under high pressure (pressure greater than 15 bar) is very difficult and poses significant technological problems when we get closer to the pressure supercritical nitrogen (33 bar).
- the other disadvantage of the cycle described in this patent is that gaseous oxygen is produced at the same pressure as the air sent to the simple column.
- EP-A-0584420 relates to a simple column which produces oxygen and nitrogen with head condenser and two reboilers operating at between 5 and 20 bar. A reboilers is heated with compressed nitrogen at room temperature and then cooled.
- EP-B-0606 027 also describes a single column process for produce oxygen and / or nitrogen under pressure and at least one product liquid. Such a process is not interesting if one does not wish to produce products liquid. Indeed, the air pressure is eminently dependent on the amount of liquid produced. At zero or low liquid production, the air pressure is less than 3 bar abs, which poses problems in the design of the treatment in the head, which requires a huge amount of absorbent, making this process uneconomical.
- the US-A-5794458 also discloses a single-column air distillation process. The main complaint that can be made about such a scheme is that it includes a compressor cold compressing a fluid very rich in oxygen. Moreover, in a classical way, the air compression is performed in one or more compressors operating at the ambient temperature.
- DE-A-1199293 discloses a method of air distillation according to the preamble of the claim 1 wherein an air flow is separated in a single column and a flow of liquid oxygen is withdrawn in the vat from the column and vaporized by exchange of heat with a compressed cycle nitrogen flow rate in a cold compressor.
- a part compressed nitrogen in the cold compressor at between 30 and 40 atma serves to reboil the simple column. In this case it is necessary to warm the nitrogen to compress it before cooling it and liquefying it against the oxygen that vaporizes. This is expensive in energy and complicates the construction of the exchangers.
- US-A-5475980 discloses a double-column process for distillation of air which in an original way proposes to compress some of the air necessary for the distillation in a cold compressor.
- the disadvantage of such a solution is the complexity of the exchange line from which the cold fluid is extracted to compress before reintroduce.
- a cold compressor compresses a fluid whose oxygen content does not not exceed 30 mol%.
- Another advantage of such a scheme is that it is better in energy than the scheme described in US Patent 5794458 because the turbine of the invention being on a fluid entering the cold box and not a fluid coming out of the cold box, the amount of heat exchanged in the main heat exchanger is significantly lower from where less irreversibilities.
- Another aspect of the invention is to produce oxygen at a pressure greater than the pressure of the single column by compressing a liquid rich in oxygen (either by pump or by hydrostatic head) at a pressure greater than that of the single column and vaporizing it either by heat exchange indirect in a main heat exchanger or an external vaporizer, either by direct contact in a mixing column.
- the ambient temperature is defined by the temperature at the suction of the Main air compressor supplying the separation unit.
- FIGS. are schematic representations of facilities according to the invention.
- the air 1 is compressed in the compressor 3, cleaned in 5 and divided in two.
- Fraction 7 is partially cooled in exchanger 13 and sent to a turbine 15 in which it relaxes before being sent to the first column 17.
- the rest of the air 9 (about 35%) is overpressed in the booster 11 and then crosses the exchanger 13 where it condenses before being sent to the column after a subcooling step in the exchanger 35, a few trays above the injection point of the air of the turbine 15.
- the column operates at a pressure of between 1.2 and 1.3 bar abs, process which can be used up to pressures of 20 bar abs, preferably less than 10 bar abs.
- Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
- Nitrogen 25 from the top of the column warms up in the subcooler 35 before being divided in two. Part 31 is sent to the exchanger 13 where it heats up. The rest 29 is sent to the compressor 21 with an inlet temperature of - 182 ° C where it is compressed to 4.9 bar before to be sent to the reboiler of tank 19 of the first column 17. There it is condense and is returned to the top of the column to act as reflux. turbine 15 is coupled to the cold compressor 21.
- Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
- a cold booster 21 with several stages in series, each feeding an intermediate vaporizer or tank.
- the cold booster 21 may have several stages in series driven each by a turbine or combined for example via a single-turbine multiplier.
- Nitrogen 25 from the top of the column warms up in the subcooler 21 before being divided in two. Part 31 is sent to the exchanger 13 where it heats up. The rest 29 is sent to the compressor 21 with an inlet temperature of -182 ° C where it is compressed to 4.9 bar before to be sent to the reboiler of tank 19 of the first column 17. There it is condense and is returned to the top of the column to serve as reflux.
- the turbine 15 is coupled to the cold compressor 21.
- Figure 3 shows the case where the pressurized tank oxygen of the colone vaporizes by direct heat exchange in a mixing column.
- the air 1 is compressed in the compressor 3, purified at 5 and divided into two. Fraction 7 is partially cooled in exchanger 13 and sent to a turbine 15 in which it relaxes before being sent to the first column 17. The rest of the air 9 (about 25%) is overpressed in the booster 11 and then passes through the exchanger 13.
- the first column 17 operates at a pressure of between 3 and 20 bar.
- the air flow 9 does not liquefy in the exchanger but is sent in form gas in the vat of the mixing column. So the mixing column operates at a higher pressure than the first column 17. It is possible to envisage both columns at the same pressure or to operate the mixing column at the lowest pressure.
- the mixing column is fed at the top with oxygen pumped from the tank of the first column 17 but can be fed at the top by another flow less rich in oxygen than the flow pumped or in tank by air from a source other than the compressor 1.
- Nitrogen 25 from the top of the column warms up in the subcooler 21 before being divided in two. Part 31 is sent to the interchange 13 where it is warms. The remainder 29 is sent to the compressor 21 with an inlet temperature of -182 ° C where it is compressed to 4.9 bar before being sent to the tank reboiler 19 of column 17. There it condenses and is returned to the top of the column to serve as the reflux.
- the turbine 15 is coupled to the cold compressor 21.
- an exchanger 49 warms the pumped oxygen sent to the top of the column 47.
- the intermediate liquid flow of the mixing column is sent to the column 17 and the impure oxygen 48 withdrawn at the top of this one is sent to the exchanger 13.
- FIG. 4 illustrates the case where a flow enriched with argon from the column 17 feeds a mixture column 57 having a cooled head condenser 51 by an intermediate liquid of the first column 17. A fluid enriched in argon is withdrawn at the top of the 57 mixture column.
- Nitrogen 25 from the top of the column warms up in the subcooler 21 before being divided in two. Part 31 is sent to the interchange 13 where it is warms. The remainder 29 is sent to the compressor 21 with an inlet temperature of -182 ° C where it is compressed to 4.9 bar before being sent to the tank reboiler 19 of the first column 17. There he condenses and is sent back to the top of the column to serve of reflux.
- the turbine 15 is coupled to the cold compressor 21.
- Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
- FIG. 5 shows a Etienne column 67 fed in the tank with a flow rate liquid drawn off some trays below the air injection point 9 and at the same level that the air blown 7. This liquid is pressurized by the pump 63 before being sent to the Etienne column. The liquid formed at the top of the column Etienne 67 is sent in head of the first column 17.
- the Etienne column operating at 2.5 bar has a condenser head 61 cooled by part of the tank liquid 65 of the same column, the remainder of the liquid being sent to the column 17 below the injection point of the blown air 7.
- the relaxed liquid vaporizes in the condenser 61 before being sent some trays above condenser 19 of column 17.
- the turbine 15 is coupled to the compressor cold 21.
- Oxygen 27 is withdrawn in the bottom of the column, pressurized by the pump 23 and sent to the exchanger 13 where it vaporizes.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
- on soutire un produit gazeux riche en azote en tête de la première (la) colonne ;
- on comprime une fraction contenant au plus 30 % molaires d'oxygène extraite de la colonne dans un compresseur dont la température d'aspiration est inférieure à la température ambiante à une pression inférieure à 30 bar ab ;
- la pression de la première (la) colonne est entre 1,3 et 20 bar abs, de préférence entre 3 et 10 bar abs;
- la fraction comprimée contient au plus 19% molaires d'oxygène et au moins 81 % molaires d'azote, de préférence au moins 90% molaires d'azote ;
- au moins une partie de l'air est détendue dans une turbine avant de l'envoyer à la première (la) colonne ;
- la production de travail par la détente d'au moins une partie de l'air sert au moins partiellement à comprimer la fraction contenant au plus 30% d'oxygène en un ou plusieurs étage(s) de compression ;
- au moins une partie de l'air est comprimée à une haute pression, condensée et envoyée à la première (la) colonne ;
- une partie non-détendue de l'air est condensée en vaporisant un fluide interne ou extrait de la première colonne (Fig. 2) ;
- la vaporisation de la fraction liquide riche en oxygène s'effectue par contact direct dans une colonne auxiliaire dite de mélange (Fig. 3);
- une colonne auxiliaire destinée à la production d'argon est alimentée à partir de la première colonne (Fig. 4) ;
- on distille dans une colonne auxiliaire un liquide enrichi en oxygène extrait de la simple colonne pour produire une fraction plus riche en oxygène et une fraction appauvrie en oxygène réintroduites dans la première colonne (Fig. 5) ;
- au moins une partie de l'air destiné à une colonne de l'appareil vient du compresseur d'une turbine à gaz et/ou un gaz enrichi en azote provenant de la première (la) colonne est renvoyé au système de la turbine à gaz ;
- la pression d'entrée de la turbine à gaz est supérieure à 15 bar abs ;
- la pureté de l'oxygène gazeux produit est au moins 80% molaires, de préférence au moins 90% molaires ;
- la température d'aspiration du compresseur froid est inférieure à
- 100 °C ou de préférence inférieure à -150 °C ;
- on produit ou on ne produit pas de liquide comme produit final ;
- le débit d'air qui sert à vaporiser le liquide riche en oxygène se condense au moins partiellement et est envoyé à la première colonne ;
- l'appareil comprend une turbine alimentée par de l'air et la sortie de la turbine est reliée à la première colonne;
- le liquide pressurisé se vaporise dans une colonne de mélange ;
- l'appareil comprend une colonne de production d'argon alimentée à partir de la première colonne ayant un rebouilleur de cuve ;
- la colonne ayant un rebouilleur de cuve a au moins un condenseur intermédiaire ;
- la colonne ayant un rebouilleur de cuve n'a pas de condenseur de tête.
Claims (20)
- Procédé de séparation de l'air par distillation cryogénique dans un appareil comprenant au moins une colonne (17,47,57) comprenant les étapes de :comprimer de l'air, l'épurer et en envoyer au moins une partie (7,9) à une première (la) colonne (17) ;séparer à température cryogénique de l'air dans la colonne ;comprimer au moins une partie d'une fraction (25) contenant au plus 30% molaires d'oxygène extraite de la tête de la colonne dans un compresseur (21).refroidir au moins partiellement ladite fraction comprimée, la condenser dans un rebouilleur de cuve (19) de la première colonne et renvoyer la fraction condensée en tête de colonne, et,extraire une fraction liquide (33) riche en oxygène de la première colonne, la pressuriser à une pression supérieure à celle de la colonne (17) et la vaporiser pour former un produit gazeux sous pression riche en oxygène
- Procédé selon la revendication 1 dans lequel la fraction comprimée (25) contient au plus 19% molaires d'oxygène et au moins 81 % molaires d'azote.
- Procédé selon l'une des revendications 1 et 2 dans lequel au moins une partie (7) de l'air est détendue dans une turbine (15) avant de l'envoyer à la première (la) colonne.
- Procédé selon la revendication 3 dans lequel la production de travail par la détente d'au moins une partie de l'air sert au moins partiellement à comprimer la fraction contenant au plus 30 % d'oxygène en un ou plusieurs étage de compression.
- Procédé selon la revendication 1, 2 ,3 ou 4 dans lequel au moins une partie de l'air (9) est comprimée à une haute pression, condensée et envoyée à la première (la) colonne.
- Procédé selon la revendication 5 dans lequel une partie non-détendue de l'air est condensée en vaporisant un fluide interne ou extrait de la première colonne (Fig. 1,2).
- Procédé selon la revendication 1 à 6 dans lequel la vaporisation de la fraction liquide riche en oxygène s'effectue par contact direct dans une colonne auxiliaire dite de mélange (47)(Fig. 3).
- Procédé selon l'une des revendications 1 à 7 dans lequel une colonne auxiliaire (57) destinée à la production d'argon est alimentée à partir de la première colonne. (Fig. 4).
- Procédé selon l'une des revendications 1 à 8 dans lequel on distille dans une colonne auxiliaire un liquide enrichi en oxygène extrait de la simple colonne pour produire une fraction plus riche en oxygène et une fraction appauvrie en oxygène réintroduites dans la première colonne (Fig. 5).
- Procédé selon l'une des revendications 1 à 9 dans lequel au moins une partie de l'air destiné à une colonne de l'appareil vient du compresseur d'une turbine à gaz et/ou un gaz enrichi en azote provenant de la première (la) colonne est renvoyé au système de la turbine à gaz.
- Procédé selon la revendication 10 dans lequel la pression d'entrée de la turbine à gaz est supérieure à 15 bar abs.
- Procédé selon l'une des revendications 1 à 11 dans lequel la température d'aspiration du compresseur froid (21) est inférieure à -100 °C.
- Procédé selon la revendication 12 dans lequel la température d'aspiration du compresseur froid (21) est inférieure à -150 °C.
- Procédé selon l'une des revendications 1 à 13 dans lequel on produit ou on ne produit pas de liquide (78) comme produit final.
- Installation de séparation d'air par distillation dans au moins une première colonne (17) ayant un rebouilleur de cuve (19) comprenant des moyens (7) pour envoyer de l'air comprimé et épuré à la première (la) colonne, un compresseur (21) pour comprimer un gaz (25) contenant au plus 30% molaires d'oxygène provenant de la tête de la colonne, des moyens pour envoyer le gaz comprimé au rebouilleur de cuve, des moyens (33) pour renvoyer le gaz comprimé au moins partiellement condensé dans le rebouilleur de cuve (19) à la tête de la colonne, éventuellement des moyens pour enrichir le gaz comprimé en azote en amont du rebouilleur, des moyens (27) pour soutirer un liquide enrichi en oxygène en cuve de la colonne, des moyens (23) pour le pressuriser et des moyens (13,47) pour vaporiser le liquide pressurisé par échange de chaleur direct ou indirect caractérisé en ce qu'elle comprend des moyens pour vaporiser le liquide pressurisé par échange de chaleur direct ou indirect avec de l'air (9) destiné à la première colonne, et ence que le compresseur a une température d'entrée au plus 5°C plus chaude d'une température de la première (la) colonne et en ce que le compresseur a une température d'entrée inférieure à la température ambiante.
- Installation selon la revendication 15 comprenant une turbine de détentee d'air (15) et dans laquelle la sortie de la turbine est reliée à la première (la) colonne.
- Installation selon une des revendications 15 et 16 dans laquelle le liquide pressurisé se vaporise dans une colonne de mélange (47).
- Installation selon une des revendications 15 à 17 comprenant une colonne de production d'argon (57) alimentée à partir de la colonne (17) ayant un rebouilleur de cuve (19).
- Installation selon une des revendications 15 à 18 dans laquelle la colonne (17) ayant un rebouilleur de cuve (19) a au moins un condenseur intermédiaire (39).
- Installation selon une des revendications 15 à 19 dans laquelle la colonne (17) ayant un rebouilleur de cuve (19) n'a pas de condenseur de tête.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0002924A FR2806152B1 (fr) | 2000-03-07 | 2000-03-07 | Procede et installation de separation d'air par distillation cryogenique |
FR0002924 | 2000-03-07 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1132700A1 EP1132700A1 (fr) | 2001-09-12 |
EP1132700B1 true EP1132700B1 (fr) | 2005-10-26 |
Family
ID=8847820
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP01400413A Expired - Lifetime EP1132700B1 (fr) | 2000-03-07 | 2001-02-16 | Procédé et installation de séparation d'air par distillation cryogénique |
Country Status (8)
Country | Link |
---|---|
US (1) | US6484534B2 (fr) |
EP (1) | EP1132700B1 (fr) |
AR (1) | AR027970A1 (fr) |
BR (1) | BR0102482A (fr) |
CA (1) | CA2339392A1 (fr) |
DE (1) | DE60114269T2 (fr) |
ES (1) | ES2252164T3 (fr) |
FR (1) | FR2806152B1 (fr) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2830928B1 (fr) * | 2001-10-17 | 2004-03-05 | Air Liquide | Procede de separation d'air par distillation cryogenique et une installation pour la mise en oeuvre de ce procede |
US7296437B2 (en) * | 2002-10-08 | 2007-11-20 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for separating air by cryogenic distillation and installation for implementing this process |
EP2221315A1 (fr) * | 2003-12-04 | 2010-08-25 | Xencor, Inc. | Procédés de génération de protéines variantes avec un contenu amélioré de fil hôte et compositions associées |
EP1767884A1 (fr) * | 2005-09-23 | 2007-03-28 | L'Air Liquide Société Anon. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Procédé et dispositif pour la séparation cryogénique d'air |
US8397535B2 (en) * | 2009-06-16 | 2013-03-19 | Praxair Technology, Inc. | Method and apparatus for pressurized product production |
WO2012155318A1 (fr) * | 2011-05-13 | 2012-11-22 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de production d'oxygène à haute pression par distillation cryogénique |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1199293B (de) * | 1963-03-29 | 1965-08-26 | Linde Eismasch Ag | Verfahren und Vorrichtung zur Luftzerlegung in einem Einsaeulenrektifikator |
US3392536A (en) * | 1966-09-06 | 1968-07-16 | Air Reduction | Recompression of mingled high air separation using dephlegmator pressure and compressed low pressure effluent streams |
US5351492A (en) * | 1992-09-23 | 1994-10-04 | Air Products And Chemicals, Inc. | Distillation strategies for the production of carbon monoxide-free nitrogen |
US5379599A (en) * | 1993-08-23 | 1995-01-10 | The Boc Group, Inc. | Pumped liquid oxygen method and apparatus |
FR2721383B1 (fr) * | 1994-06-20 | 1996-07-19 | Maurice Grenier | Procédé et installation de production d'oxygène gazeux sous pression. |
US5832748A (en) * | 1996-03-19 | 1998-11-10 | Praxair Technology, Inc. | Single column cryogenic rectification system for lower purity oxygen production |
JP2875206B2 (ja) * | 1996-05-29 | 1999-03-31 | 日本エア・リキード株式会社 | 高純度窒素製造装置及び方法 |
US6082135A (en) * | 1999-01-29 | 2000-07-04 | The Boc Group, Inc. | Air separation method and apparatus to produce an oxygen product |
-
2000
- 2000-03-07 FR FR0002924A patent/FR2806152B1/fr not_active Expired - Fee Related
-
2001
- 2001-02-16 EP EP01400413A patent/EP1132700B1/fr not_active Expired - Lifetime
- 2001-02-16 DE DE60114269T patent/DE60114269T2/de not_active Expired - Lifetime
- 2001-02-16 ES ES01400413T patent/ES2252164T3/es not_active Expired - Lifetime
- 2001-03-05 CA CA002339392A patent/CA2339392A1/fr not_active Abandoned
- 2001-03-06 AR ARP010101047A patent/AR027970A1/es unknown
- 2001-03-07 US US09/799,735 patent/US6484534B2/en not_active Expired - Lifetime
- 2001-03-07 BR BR0102482-5A patent/BR0102482A/pt active Search and Examination
Also Published As
Publication number | Publication date |
---|---|
ES2252164T3 (es) | 2006-05-16 |
CA2339392A1 (fr) | 2001-09-07 |
DE60114269T2 (de) | 2006-07-20 |
FR2806152B1 (fr) | 2002-08-30 |
US20020134105A1 (en) | 2002-09-26 |
EP1132700A1 (fr) | 2001-09-12 |
AR027970A1 (es) | 2003-04-16 |
DE60114269D1 (de) | 2005-12-01 |
US6484534B2 (en) | 2002-11-26 |
BR0102482A (pt) | 2001-10-16 |
FR2806152A1 (fr) | 2001-09-14 |
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