EP2285484A1 - Procede de neutralisation d'une zeolithe cationique - Google Patents
Procede de neutralisation d'une zeolithe cationiqueInfo
- Publication number
- EP2285484A1 EP2285484A1 EP09765986A EP09765986A EP2285484A1 EP 2285484 A1 EP2285484 A1 EP 2285484A1 EP 09765986 A EP09765986 A EP 09765986A EP 09765986 A EP09765986 A EP 09765986A EP 2285484 A1 EP2285484 A1 EP 2285484A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- organic solvent
- zeolite
- inert gas
- anhydrous organic
- separation
- 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.)
- Withdrawn
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/18—Synthetic zeolitic molecular sieves
- B01J20/186—Chemical treatments in view of modifying the properties of the sieve, e.g. increasing the stability or the activity, also decreasing the activity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/026—After-treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
- C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
- C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
- C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves
- C10G25/05—Removal of non-hydrocarbon compounds, e.g. sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/38—Base treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/08—Jet fuel
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/22—Higher olefins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
Definitions
- cationic zeolites as adsorbents. Their principle is based on a selectivity of shape or size, or on a particular affinity of one of the constituents of the charge for the cations. Insofar as the process does not involve any chemical reaction, these are to be avoided. Any conversion of feedstock compounds leads to a drop in yield and can also be at the origin of the formation of coke precursors, thus causing premature aging of the adsorbent. These undesirable phenomena are all the more frequent as the zeolite has active surface sites which are most often acidic sites.
- cationic zeolites which do not have, a priori, any Bronsted acid sites, should not have a strong activity. Nevertheless, in certain cases, they have non-negligible activities characterized by reactions involving acidic sites.
- zeolites In order to obtain very little or even non-reactive zeolites, it is necessary either to find a particular mode of preparation such as, for example, activation under a reducing atmosphere such as NH 3 which makes it possible to neutralize the protons as soon as they are formed (H. Siegel, R. Scholler, B. Staudte, JJ Van Dun, WJ Mortier, Zeolites, 1987, 7, 372), or find a way to neutralize the detected activity.
- a reducing atmosphere such as NH 3
- the neutralization is the only option possible when it comes to working with a commercially supplied zeolite.
- the invention relates to a method for neutralizing a cationic zeolite exchanged at least partially with one or more mono- and / or multivalent cations.
- the neutralization process comprises at least the steps of dissolving a basic salt in an anhydrous organic solvent, degassing this solution by bubbling a dry inert gas, suspending the zeolite in this solution under dry inert gas , filtration and washing of the solid with an anhydrous organic solvent and calcination in the presence of oxygen and in a dry gas stream.
- the invention also relates to the use of neutralized zeolites for the separation or purification of hydrocarbon feeds.
- the invention relates to a method for neutralizing a cationic zeolite exchanged at least partially with one or more mono- and / or multivalent cations, said exchanged cationic zeolite being preferably of X, Y, A, ⁇ or MFI type, said method of neutralization comprising at least the following steps:
- anhydrous organic solvent preferably an anhydrous alcohol, very preferably anhydrous ethanol
- the multivalent cation (s) are generally divalent or trivalent cations and are generally alkaline earth or lanthanide cations.
- the monovalent cation (s) are generally alkaline cations.
- the steps a), b), c), d) and e) of the neutralization process can generally be carried out under the operating conditions described below.
- Step a) Step a) is that of dissolving a basic salt in an anhydrous organic solvent.
- concentration of the basic salt is generally greater than 0.01 mol / l, preferably between 0.01 mol / l and 5 mol / l, the temperature between 20 and 60 ° C.
- the stage is generally carried out with stirring at a speed of between 500 and
- Step b) is that of degassing the solution obtained at the end of step a) by bubbling a dry inert gas, preferably dry argon, and maintaining the solution under dry inert gas, preferably dry argon.
- a dry inert gas preferably dry argon
- Step c) is that of suspending the zeolite in the solution prepared in b), under dry inert gas, preferably dry argon, and with stirring at a speed generally of between 500 and 700 rpm , the temperature generally being between 20 and 40 ° C. and the duration of the step generally being between 1 to 24 hours.
- Step d) is that of filtration and washing of the solid obtained at the end of step c) with an anhydrous organic solvent, preferably an anhydrous alcohol, very preferably anhydrous ethanol.
- an anhydrous organic solvent preferably an anhydrous alcohol, very preferably anhydrous ethanol.
- the volume of the anhydrous organic solvent used is generally at least equal to that used during the ion exchange step.
- step d) the solid obtained at the end of step d) can be stored without risk of evolution of its acid-base characteristics.
- Step e) is that of calcination of the solid obtained at the end of step d) in the presence of oxygen, at a temperature generally of between 200 and 600 ° C., preferably between 300 and 550 ° C., for a period of generally between 1 and 20 hours, preferably between 10 and 15 hours, in a dry gas stream of between 3 and 8 I. h -1 .g -1 , preferably under a stream of dry compressed air.
- the exchange rate obtained in the mono- and / or multivalent cation (s) is generally verified by inductively coupled plasma atomic emission spectrometry (ICP-AES).
- the cationic zeolite thus prepared can be used in any process for the separation or purification of hydrocarbon feeds.
- Potential applications include separation of paraxylene from an aromatic C8 cut, separation of linear paraffins from a kerosene cut, separation of linear paraffins / branched paraffins from a gasoline cut, separation of paraffins / olefins, removal of mercaptans from natural gas, desulphurization of FCC gasolines, denitrogenation of C4-C6 feedstocks for oligomerization.
- This suspension is carried out in a three-necked balloon. b) degassing of the suspension prepared in a) for a few minutes by bubbling argon, then maintaining it under an inert atmosphere of argon but without bubbling c) stirred with magnetic stirring at 500 rpm and under heating in a bath of silicone oil at 150 ° C. for 24 h.
- the three-neck flask is surmounted by a reflux refrigerant system to prevent evaporation of solution during the experiment d) samples of 0.05 ml at regular time intervals and analysis thereof by column gas chromatography PONA (Paraffin, Olefin, Naphtene, Aromatic) with a diameter of 200 ⁇ m, a film thickness of 0.5 ⁇ m and a length of 50 m.
- PONA Paraffin, Olefin, Naphtene, Aromatic
- 1-dodecene From the chromatograms, the composition of each sample is determined in 1-dodecene and its different isomers (2-dodecene, 3-dodecene, 4-dodecene, 5-dodecene and 6-dodecene) from which the conversion is calculated.
- 1-dodecene according to the following equation:
- the curve of the conversion to 1-dodecene can then be plotted as a function of the reaction time, the slope of the tangent at the first points of this curve corresponding to the initial speed of the isomerization reaction of 1-dodecene and reflecting the initial activity of the zeolite tested, that is to say its number of active sites vis-à-vis a reaction involving acid sites.
- An NaCaY zeolite with an exchange rate of approximately 25% is prepared by ion exchange according to the prior art from a NaY zeolite in the form of a powder in an aqueous medium.
- approximately 10 g of the zeolite are directly suspended in 1 l of CaCb solution at 0.6 g / l (solution prepared from CaCl 2 .2H 2 O from Aldrich).
- the flask is heated by means of a silicone bath at 60 ° C. and the suspension is kept under magnetic stirring.
- a refrigerant system is adapted to avoid evaporation of the suspension during exchange.
- the exchange lasts approximately 7 hours.
- the zeolite After exchanging the zeolite is filtered, washed with distilled water and dried in an oven at 110 ° C. Then, it is dehydrated under a stream of nitrogen (3 lh '1 .g zeo r 1 ) in a tube furnace 450 0 C for 2 h so as to remove the adsorbed water in the zeolite during the exchange.
- This zeolite denoted NaCaY-26%, is subjected to two basic washes, one in an aqueous medium and the other in anhydrous ethanol according to the present invention.
- zeolite For washing with an aqueous alkaline solution, 10 g of zeolite are suspended in 250 ml of a solution prepared by dissolving 4.1 g of NaOH pellets in 1 l of distilled water (concentration 0.1 mol / l). l) and the system is placed under magnetic stirring at 500 rpm for 4h at room temperature and the solid is filtered and activated under a stream of nitrogen at 45O 0 C for 2 hours in column. The recovered solid is denoted NaCaY-26% -NaOH 0.1 M (water).
- Basic washing in an alcoholic medium is carried out as described in the present invention.
- a basic solution of NaOH is prepared by dissolving 4.1 g of NaOH pellets in 1 l of anhydrous ethanol after argon bubbling in. this one. Then, 10 g of zeolite are suspended in 250 ml of this solution. The whole is stirred magnetically at 500 rpm at 25 0 C for 4 h. After filtration and recovery of the solid, it is calcined at 550 ° C. for 2 h under a stream of dry compressed air. The recovered solid is denoted NaCaY-26% -NaOH 0.1 M (ethanol).
- the residual acidity of these three solids, NaCaY-26%, NaCaY-26% -NaOH 0.1 M (water) and NaCaY-26% -NaOH 0.1 M (ethanol) is determined by a transformation model reaction.
- an olefin (1-dodecene) that characterizes weak activities.
- the differences in the activity of the three NaCaYs with each other and with the starting NaY are presented in FIG. 1 which shows the variation of the 1-dodecene conversion as a function of time for the NaY (starting zeolite), NaCaY-26. % (solid not treated with a basic solution), NaCaY-26% - 0.1M NaOH (water) and NaCaY-26% -NaOH 0.1M (ethanol).
- the activity of the NaCaY zeolite is not reduced when it undergoes an alkaline wash in an aqueous medium, but is when it is subjected to washing of the same type in a nonaqueous alcoholic medium (initial rates of reaction, conversion and number of products formed very close). The activity becomes even lower than that of the starting zeolite NaY.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Geology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Materials Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0802950A FR2931704B1 (fr) | 2008-05-28 | 2008-05-28 | Procede de neutralisation d'une zeolithe cationique |
PCT/FR2009/000530 WO2009153424A1 (fr) | 2008-05-28 | 2009-05-05 | Procede de neutralisation d'une zeolithe cationique |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2285484A1 true EP2285484A1 (fr) | 2011-02-23 |
Family
ID=40231245
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP09765986A Withdrawn EP2285484A1 (fr) | 2008-05-28 | 2009-05-05 | Procede de neutralisation d'une zeolithe cationique |
Country Status (4)
Country | Link |
---|---|
US (1) | US20110071333A1 (fr) |
EP (1) | EP2285484A1 (fr) |
FR (1) | FR2931704B1 (fr) |
WO (1) | WO2009153424A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA2803904C (fr) | 2010-07-26 | 2014-01-28 | Sortwell & Co. | Procede de dispersion et d'agregation de composants de suspensions minerales et polymeres anioniques multivalents a poids moleculaire eleve pour agregation d'argile |
US8721896B2 (en) | 2012-01-25 | 2014-05-13 | Sortwell & Co. | Method for dispersing and aggregating components of mineral slurries and low molecular weight multivalent polymers for mineral aggregation |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1547623A (fr) * | 1967-10-12 | 1968-11-29 | Raffinage Cie Francaise | Procédé de purification des isooléfines |
GB1266781A (fr) * | 1969-02-20 | 1972-03-15 | ||
US3888939A (en) * | 1973-09-28 | 1975-06-10 | Universal Oil Prod Co | Process for separating olefins by adsorption |
DE3806932A1 (de) * | 1988-03-03 | 1989-09-14 | Vaw Ver Aluminium Werke Ag | Verfahren zur modifizierung eines zeoliths |
US5292990A (en) * | 1988-12-07 | 1994-03-08 | Exxon Research & Engineering Co. | Zeolite composition for use in olefinic separations |
US5206195A (en) * | 1990-05-31 | 1993-04-27 | Kanebo Ltd. | Stablized synthetic zeolite and a process for the preparation thereof |
US5329057A (en) * | 1991-04-19 | 1994-07-12 | The Dow Chemical Company | Process for the cyclodimerization of 1,3-butadienes to 4-vinylcyclohexenes |
FR2690856B1 (fr) * | 1992-05-06 | 1995-01-06 | Inst Francais Du Petrole | Catalyseur à base de zéolithe omega renfermant au moins un métal des groupes IIA, IVB, IIB ou IVA et son utilisation en isomérisation d'une coupe C8 aromatique. |
US5914013A (en) * | 1995-01-31 | 1999-06-22 | The Regents Of The University Of California | Selective thermal and photooxidation of hydrocarbons in zeolites by oxygen |
WO2002042245A1 (fr) * | 2000-11-21 | 2002-05-30 | Exxonmobil Chemical Patents Inc. | Procede de produciton d'olefines legeres |
CN101134760B (zh) * | 2006-08-31 | 2010-05-12 | 上海医药工业研究院 | 去除粉末状头霉素c中色素的方法 |
-
2008
- 2008-05-28 FR FR0802950A patent/FR2931704B1/fr not_active Expired - Fee Related
-
2009
- 2009-05-05 US US12/994,202 patent/US20110071333A1/en not_active Abandoned
- 2009-05-05 WO PCT/FR2009/000530 patent/WO2009153424A1/fr active Application Filing
- 2009-05-05 EP EP09765986A patent/EP2285484A1/fr not_active Withdrawn
Non-Patent Citations (1)
Title |
---|
See references of WO2009153424A1 * |
Also Published As
Publication number | Publication date |
---|---|
FR2931704B1 (fr) | 2012-05-04 |
US20110071333A1 (en) | 2011-03-24 |
FR2931704A1 (fr) | 2009-12-04 |
WO2009153424A1 (fr) | 2009-12-23 |
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