Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
  • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
  • B01D53/75—Multi-step processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
  • B01D53/86—Catalytic processes
  • B01D53/8659—Removing halogens or halogen compounds
  • B01D53/8662—Organic halogen compounds
• • 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
  • C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
• • 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
  • C10G35/00—Reforming naphtha
  • C10G35/04—Catalytic reforming
• • 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
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
  • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
• • 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
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
  • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
  • C10G45/10—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing platinum group metals or compounds thereof
• • 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
  • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
  • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
  • C10G69/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
  • B01D2253/10—Inorganic adsorbents
  • B01D2253/104—Alumina
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/10—Noble metals or compounds thereof
  • B01D2255/102—Platinum group metals
  • B01D2255/1021—Platinum
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/10—Noble metals or compounds thereof
  • B01D2255/102—Platinum group metals
  • B01D2255/1023—Palladium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/202—Alkali metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/204—Alkaline earth metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/20—Halogens or halogen compounds
  • B01D2257/204—Inorganic halogen compounds
  • B01D2257/2045—Hydrochloric acid
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/20—Halogens or halogen compounds
  • B01D2257/206—Organic halogen compounds
  • B01D2257/2064—Chlorine
• • 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

Definitions

• the present invention relates to a purification process by removing chlorine in the form of hydrogen chloride and organochlorine compounds.
• One of the aims of catalytic reforming is to obtain hydrocarbons having an increased octane number. It is established that the octane number of a hydrocarbon is greater when it is branched, cyclic or even aromatic. Thus, the reactions of cyclization and aromatisation of hydrocarbons will be favored.
• chlorinated bimetallic heterogeneous catalysts are based on alumina and comprise, most often, platinum and another metal such as for example tin, rhenium, or iridium.
• the presence of chlorine in said catalysts is important because, added to the alumina, it ensures the overall acidity of the system and participates in the redispersion of platinum over time, thereby stabilizing the catalytic activity of the catalyst.
• Catalytic reforming also produces hydrogen.
• hydrogen is a particularly valuable product, particularly through its use in hydrotreatments, which are increasingly being developed with the aim of improving the protection of the environment.
• the gaseous effluents are mainly composed of hydrogen, light hydrocarbons such as methane, ethane, and the like; general traces of hydrogen chloride and water. It is therefore important to be able to remove all traces of hydrogen chloride from these effluents, for example on alumina-based solids, and then to recycle and therefore use purified hydrogen, still in refinery.
• regenerative or new generation processes have recently been developed and are growing in the field. These processes operate at a pressure close to 0.3 to 1.5 MPa, or even less.
• the object of the present invention is to provide an improved process for the efficient removal of chlorinated compounds and hydrogen chloride more particularly, contained in a gas or a liquid.
• Another object of the present invention is to provide a process using a composition which will substantially reduce, or even eliminate, the formation of oligomers, and in particular chlorinated oligomers called "green oils” or “green oils", downstream of the processes. regenerative reforming or new generation.
• An advantage of the present invention is that the removal of chlorinated compounds makes it possible in particular to avoid the harmful formation of NH 4 Cl as well as corrosion problems related to chlorine. Another advantage of the present invention is that the removal of the chlorinated compounds makes it possible to protect the catalysts of the downstream units, in particular the catalyst of the benzene hydrogenation unit.
• Patent Application EP1053053 describes a process for eliminating, reducing, and / or eliminating halogenated compounds contained in a gas or a liquid, in which the gas or the liquid is brought into contact with a composition obtained by depositing on an alumina of at least one compound comprising at least one element selected from alkalis followed, after the deposition, calcining the alumina at a temperature of at least 600 ° C.
• the patent application EP0948995 describes a process for removing halogenated compounds contained in a gas or a liquid in which the gas or the liquid is brought into contact with a composition comprising a hydrated alumina and / or alumina and at least one selected metallic element. in the group consisting of metals of groups VIII, IB and / or HB.
• the invention relates to a process for purification by removing chlorine in the form of hydrogen chloride and organochlorine compounds by contacting, in the presence of hydrogen, at least part of the effluent of a reforming zone with production of aromatics, dehydrogenation, isomerization or hydrogenation, said part of the effluent comprising olefins, hydrogen chloride and organochlorine compounds, a zone of éiimination comprising a sequence of two masses, the 1 st weight being a mass comprising at least one metal from group VIII deposited on an inorganic support, the 2nd mass being a hydrogen chloride adsorbent.
• group VIIl corresponds to group VIII according to the classification CAS corresponds to the metals of columns 8 to 10 according to the new IUPAC classification (CRC Handbook of Chemistry and Physics, editor CRC press, editor-in-chief DR Lide, 81 st edition, 2000-2001).
• olefin corresponds to mono-olefins and / or diolefins.
• the invention relates to a process for purification by removing chlorine in the form of hydrogen chloride and organochlorine compounds by contacting, in the presence of hydrogen, at least part of the effluent of a reforming zone with production of aromatics, dehydrogenation, isomerization or hydrogenation, said part of the effluent comprising olefins, hydrogen chloride and organochlorine compounds, on an elimination zone comprising a sequence of two masses, the 1 st mass being a mass comprising at least one group VIII metal deposited on an inorganic support, the 2nd mass being a hydrogen chloride adsorbent.
• At least a part of the effluent of the reforming zone circulates through a liquid gas separator, said separator leading to a flow of hydrogen-rich gas (A) and to a liquid effluent (B), said liquid effluent being sent to a stabilization zone, said stabilization zone leading to at least two fractions, a first light fraction (C) and a first heavy fraction (D), said first section being heavy sent to a fractionation column leading to the production of at least two sections, a second light section (E1) withdrawn at the top of the column, optionally a section (E2) withdrawn between the column head and the feed of the column, each of the sections (E1) and (E2) can be sent to a hydrogenation zone of benzene, and a second heavy section (F).
• the area of purification is placed on any flow from the separator liquid gas, the stabilizer column or fractionator.
• the purification zone is placed on the stream of hydrogen-rich gas (A), on the liquid effluent (B) or on at least one of the sections (E1) or (E2).
• hydrogen is added during the contacting of at least a part of the effluent of a reforming zone, of aromatics production, dehydrogenation, isomerization or hydrogenation.
• the two masses of the capture zone are generally either loaded in the same reactor or in two different reactors.
• the first mass is generally the catalytic mass and the second mass is generally the hydrogen chloride adsorbent.
• the two masses are arranged in the same reactor and the first mass is generally disposed at the head of the capture zone. It then occupies a volume corresponding generally to 10 to 60% of the total volume of said zone.
• the second mass when the second mass is saturated, it is discharged separately while deflecting the feedstock to be treated to a third reactor comprising a hydrogen chloride adsorbent.
• the selected Group VIII metal will preferably be palladium and / or platinum. These metals are deposited on the support using the methods known to those skilled in the art, namely by impregnation of aqueous solutions of soluble salts of palladium and platinum. For example, if the Group VIII metal is palladium, it can be introduced by aqueous or organic solution impregnation techniques of a palladium precursor.
• This precursor may for example be a mineral compound such as palladium chloride, palladium nitrate, palladium tetramine dihydroxide, palladium tetramine chloride or an organometallic compound such as for example palladium bis-z-allyl or palladium bis- acetylacetonate.
• the palladium is deposited preferably in crust, that is to say on the surface of the catalyst grains, for example cylindrical or extruded beads, with a penetration into the grains included in a peripheral layer not exceeding, for example, 80% of the radius of the balls or cylinders.
• the thickness of the crust is generally between 100 and 700 micrometers.
• the catalyst is generally dried at about 120 0 C, then calcined at temperatures generally between 150 and 700 0 C.
• the palladium or platinum content is generally between 0.1 and 1% by weight and preferably between 0.2 and 0.6% by weight.
• the inorganic support used may be chosen from alumina, silica, silica-alumina, silica-magnesia, titanium oxide, alumino-silicates such as zeolites, all these solids being taken alone or mixed with one another.
• Alumina will preferably be used.
• the second mass may be chosen from all those known to effectively adsorb hydrogen chloride. They may consist of one or more alkaline or alkaline earth compounds deposited on an alumina with a specific surface area generally between 50 and 400 m 2 / g. They may also include mixed oxides, especially those based on copper and / or zinc.
• the alkali or alkaline earth content is generally between 0.5% and 70% by weight and preferably between 2% and 35% by weight relative to the total weight of the composition.
• the deposition of the alkaline and alkaline earth elements can be achieved by any method known to those skilled in the art for example by impregnation of the alumina with an aqueous solution of soluble salts of alkali or alkaline earth. After impregnation, the mass is dried and calcined appropriately, the calcination temperature generally being between 300 and 900 ° C.
• the second mass may be in any form allowing the greatest accessibility and therefore the greatest possible adsorption capacity of hydrogen chloride.
• beads or extrudates which may be of any form, for example in the form of trilobates, may be used.
• the average diameter of the balls and extrudates will be as small as possible, for example between 1 and 5 mm, while being careful not to cause excessive head losses in the reactor.
• the Feffluent portion of the treated reforming zone generally contains between 0.1 and 50 ppm by weight of chlorinated compounds counted as chlorine.
• the elimination zone is operated in the presence of hydrogen, preferably with a molar ratio of hydrogen to chlorine of greater than 5, very preferably with a molar ratio of hydrogen to chlorine of between 5 and 10 6 , at a temperature of between 25 and 35O 0 C, preferably between 35 and 200 0 C, preferably between 130 and 180 ° C and at a pressure between 0.2 and 5 MPa, preferably between 0.5 and 4MPa, preferably between 1 and and 3 MPa.
• the space velocities of the gases to be purified expressed in TPN volume hourly flowrate of the gas divided by the mass volume, GHSV are generally between 50 and 2000 h -1 and preferably between 100 and 100 h -1 .
• the space velocities of the liquids to be purified are generally between 1 and 50 and preferably between 2 and 40 h -1 .
• the hydrogen may be present initially in the hydrocarbon feedstock to be treated. Particularly in liquid fillers in dissolved form from 100 ppm molar. Hydrogen can also be added during the contacting of at least a portion of the effluent of a reforming zone, of aromatics production, dehydrogenation, isomerization or hydrogenation.
• Figure 1 shows the treatment of the effluent of the reforming zone.
• At least a portion of the effluent from the reforming zone flows via the line (1) through a liquid gas separator (10), said separator leading to a flow of hydrogen-rich gas (A) flowing via the line (2). ) and a liquid effluent (B) flowing via the line (3), said liquid effluent is sent via line (3) at a stabilizing zone (11), said stabilization zone leading to at s least two fractions, a first light cut (C) circulating via line (4) and a first heavy cut (D) flowing via line (5), said first heavy cut being sent via line (5) to a fractionating column (12) leading at the production of at least two cuts, a second light cut (E1) withdrawn at the top of the column and flowing via line (6), optionally a cut (E2) withdrawn between the column head and the feed of the column and flowing via the line (7), each of the cuts (E1) and (E2) being able to be sent a benzene hydrogenation zone and a second heavy fraction (F) circulates via the line
• An alumina prepared according to the method of preparation described in the patent application EP1053053 is used. It is in the form of balls of 2 to 5 mm and has a specific surface of 349 m 2 / g.
• Sodium is first incorporated by so-called dry impregnation with a solution of NaNO 3 so as to obtain 6.7% by weight of sodium after drying at 100 ° C. and calcination at 82 ° C.
• Diolefin content 1000 ppm wt
• Chlorine content (ex organochlorine): 2 ppm by weight (2)
• This reformate is circulated at a flow rate of 2 liters per hour, which corresponds to a liquid space velocity of 20 h -1
• the reactor is operated at a temperature of 140 ° C. and under a pressure of 1 MPa.
• This reactor is operated for 1000 hours.
• a mass B comprising 0.3% by weight of palladium deposited on alumina is prepared.
• the palladium is deposited by so-called dry impregnation from Pd (NO 3 ) 2 .
• the alumina is in the form of beads 3 mm in average diameter, it has a specific surface area of 120 m 2 / g.
• the mass is dried at 120 ° C. and then calcined at 450 ° C. This gives a palladium deposit which remains crusted on the ball. The thickness of this crust is 300 microns.
• a second mass C is prepared according to the method of preparation described in the patent application EP1053053 comprising 6.7% Na after impregnation of NaNO 3 and calcination at 82O 0 C of an alumina equivalent to that described in Example 1.
• Example 1 The operation is carried out with the same liquid charge and under the same conditions as those of Example 1. This reactor is operated for 1000 hours. and the olefin and chlorine contents are measured after 200 hours, 800 hours, and 1000 hours.
• the light cut (called light reformate containing most of the benzene) from the fractionation column is treated before being sent to a hydrogenation zone of benzene.
• This cup is named E1 in the description.
• Mono-olefin content 1.0% by weight
• Diolfin content 1000 ppm by weight
• Chlorine content (eg organochlorine): 1.5 ppm wt (2)
• the two reactors are run for 1000 hours and the olefins and chlorine contents are measured after 500 and 1000 hours.
• the behavior of the mass A is compared with that of the combination of masses B and C.
• Example 2 In one case the charged reactor is used as in Example 1 and in the other case the arrangement of Example 2.
• Example 2 It is observed that the mass A of Example 1, after 1000 hours, removes the HCl not by adsorption but by addition to the olefins present. On the contrary, the arrangement of Example 2 with masses B and C continues to eliminate almost completely HCI by avoiding the formation of organochlorines through the almost complete hydrogenation of olefins present.

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• 2008
  • 2008-04-25 FR FR0802345A patent/FR2930559B1/fr active Active
• 2009
  • 2009-03-27 JP JP2011505546A patent/JP5567552B2/ja active Active
  • 2009-03-27 KR KR1020107023640A patent/KR101671531B1/ko active Active
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