WO2004060843A1 - アルコール及び/又はケトンの製造方法 - Google Patents
アルコール及び/又はケトンの製造方法Info
- Publication number
- WO2004060843A1 WO2004060843A1 PCT/JP2003/016722 JP0316722W WO2004060843A1 WO 2004060843 A1 WO2004060843 A1 WO 2004060843A1 JP 0316722 W JP0316722 W JP 0316722W WO 2004060843 A1 WO2004060843 A1 WO 2004060843A1
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- catalyst
- reaction
- amount
- reactor
- oxide catalyst
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C27/00—Processes involving the simultaneous production of more than one class of oxygen-containing compounds
- C07C27/10—Processes involving the simultaneous production of more than one class of oxygen-containing compounds by oxidation of hydrocarbons
- C07C27/12—Processes involving the simultaneous production of more than one class of oxygen-containing compounds by oxidation of hydrocarbons with oxygen
- C07C27/14—Processes involving the simultaneous production of more than one class of oxygen-containing compounds by oxidation of hydrocarbons with oxygen wholly gaseous reactions
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/14—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of germanium, tin or lead
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/24—Chromium, molybdenum or tungsten
- B01J23/28—Molybdenum
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
- C07C29/04—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
- C07C29/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/002—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by dehydrogenation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/28—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation of CHx-moieties
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
- C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
- C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
Definitions
- the present invention relates to a process for producing the corresponding alcohol and z or ketone from alkenes in the gas phase using an oxide catalyst in the presence of steam.
- Examples of the production of the corresponding alcohols and z or ketones from alkenes by gas phase reaction in the presence of steam include, for example, the production of acetone from propylene, the methyl ethyl ketone from 1-butene or 2-butene (MEK) And cyclohexanone from cyclohexene, and tert-butanol from isobutene. All of these products are industrially very important chemical substances as chemical starting materials and solvents.
- the prior art of the above reaction mainly includes a Picker-type reaction using a noble metal catalyst such as a palladium compound, and a reaction using a composite oxide catalyst of a non-noble metal such as molybdenum, tungsten, tin, and cobalt. No.
- Examples of the former Pecker-type reaction include the use of a catalyst in which palladium and Z or a palladium compound and copper chloride are supported on a carrier such as silica or alumina, in the presence of olefin, oxygen, and water vapor to form a carbonyl derivative.
- a catalyst in which palladium and Z or a palladium compound and copper chloride are supported on a carrier such as silica or alumina, in the presence of olefin, oxygen, and water vapor to form a carbonyl derivative.
- JP-A-49-72209 disclose the production of methylethyl ketone (MEK) from 1-butene using a catalyst in which palladium chloride and copper chloride are supported on silica. .
- a salted product is not used as a catalyst
- palladium is used as a catalyst in producing gaseous aldehydes or ketones by subjecting olefins to gas phase oxidation with oxygen or an oxygen-containing gas in the presence of steam.
- a catalyst in which a salt and a vanadyl salt are supported on activated carbon see, for example, JP-A-59-163335.
- Japanese Patent Application Laid-Open No. 59-163335 discloses an example in which acetone is produced from propylene using a catalyst in which palladium sulfate and vanadyl sulfate are supported on activated carbon.
- these catalysts use very expensive noble metals, and according to additional tests by the present inventors, both catalysts showed degradation of activity in a short time.
- an example of the latter without using a noble metal catalyst is that molybdic acid and fine particles of tin oxide uniformly distributed on a carrier and a catalyst consisting of power are used to convert olefin and oxygen in the presence of water vapor.
- a noble metal catalyst See, for example, Japanese Patent Publication No. 47-84046.
- acetone is produced from propylene using a catalyst in which tin dioxide and molybdenum trioxide are supported on silica.
- JP-A-49-61112 there is a description that MEK is produced from transbutene using a catalyst in which tin dioxide, molybdenum trioxide and sodium are supported on silica.
- Another method is to use a similar catalyst and alternately contact a gas consisting of olefin and water vapor containing a small amount of oxygen in the reaction raw material with a gas containing a large amount of oxygen (see, for example, — See 3 4 6 52 2).
- Examples of the publication of Japanese Examined Patent Publication No. 493-134652 include production of MEK from n-butene using a catalyst in which tin dioxide and molybdenum trioxide are supported on silica.
- the present invention relates to a reaction for producing a corresponding alcohol and / or ketone from an alkene in a gas phase using an oxide catalyst in the presence of water vapor, the production of a carbonaceous substance that accumulates on the catalyst during the reaction. It is an object of the present invention to provide a production method in which the selectivity of a target product (alcohol and Z or ketone) is significantly improved while suppressing the production.
- the present inventors have conducted intensive studies in order to solve the above-mentioned problems. It has been found that using a catalyst containing oxides of butene and / or tin and (b) controlling the amount of carbonaceous material on the catalyst to a specific range may be suitable for the purpose, The present invention has been accomplished based on this finding.
- the present invention relates to a manufacturing method described below.
- the oxide catalyst is the oxide catalyst
- the accumulation amount of the carbonaceous substance on the oxide catalyst is controlled in a range of 0.1 to 10% by mass
- the oxide catalyst used for the reaction is withdrawn from the reactor, and the oxide catalyst is regenerated in the presence of an oxygen-containing gas. (1) above or using a catalyst circulation system that returns the product catalyst to the reactor again
- the amount of the oxide catalyst returned to the reactor is in the range of 0.5 to 100, and is described in any one of the above items (3) to (5). the method of.
- Atomic ratio of molybdenum to tin in the oxide catalyst X ⁇ Mo / (S n + Mo);
- Mo is the number of molybdenum atoms in the oxide catalyst
- Sn is the number of tin atoms in the oxide catalyst.
- the raw material containing 1-butene and Z or 2-butene as an alkene contains at least one or more selected from the group consisting of isopten, butadiene, tert-butylalcohol, methinolate tert-butylether, The method described in (14) above.
- the catalyst used in the method of the present invention is a catalyst containing an oxide of molybdenum and / or tin. These oxides may be used alone, but by using both molybdenum and tin oxides as a mechanically mixed and Z or composite oxide, the catalytic activity and selectivity of the target product can be improved. It is effective and more preferable. Further, oxides of other elements can be added in order to further improve the catalytic activity and the selectivity of the target product.
- Elements belonging to the fourth, fifth, sixth, eighth, ninth, tenth, tenth, eleventh, fourteenth, and fifteenth groups of the periodic table are preferred, and more preferably,
- the Group 4 elements are titanium and zirconium, the Group 5 elements are vanadium and niobium, the Group 6 elements are tungsten and chromium, the Group 8 elements are iron, and the Group 9 elements are cobalt.
- Group 10 elements are nickel, Group 11 elements are copper, Group 14 elements are lead, and Group 15 elements are bismuth, antimony, and phosphorus.
- the periodic table referred to here is the Periodic Table of the Group 18 elements described on page 56 of the Basic Handbook of Chemical Chemistry, I revised 4th edition (edited by The Chemical Society of Japan, Maruzen, 1993). If it is a trace amount, an oxidized product of an alkali metal such as sodium, potassium or rubidium or an alkaline earth metal such as magnesium, calcium or barium may be further added.
- these acids are used by being supported on a suitable carrier.
- a suitable carrier inorganic oxides such as silica, silica alumina, alumina, titania, silica titania, zirconia, and silica zirconia are preferable, and silica is particularly preferable.
- clay such as kaolin or talc may be added to increase the mechanical strength of the catalyst.
- the oxide catalyst contains an oxide of molybdenum and tin
- ⁇ Force S preferably in the range other than 0.29 and 0.51; more preferably in the range 0 ⁇ X ⁇ 0.50 (excluding 0.29); 0.011 ⁇ X ⁇ 0.24 Is more preferable, the range of 0.05 ⁇ X ⁇ 0.24 is still more preferable, and the range of 0.08 ⁇ X ⁇ 0.15 is particularly preferable.
- the catalyst preparation mainly includes 1) a step of preparing a catalyst raw material solution, 2) a step of drying the catalyst raw material solution, and a step of calcining the catalyst precursor.
- the term “oxide” includes the complex oxide.
- a salt or compound that forms an oxide at 200 to 100 ° C. is used.
- commercially available oxides can be used as they are.
- one or more of the raw materials is sufficiently dissolved in water or a suitable solvent at 20 to 80 ° C.
- the liquid property of the solution may be controlled to be acidic or alkaline! / ,.
- hydrogen peroxide or the like may be added.
- the raw material solution may be dried as it is, it is preferable that the raw material solution is sufficiently mixed with a powder, a solution, a sol, a gel, or the like containing a carrier component, in order to be supported on an appropriate carrier as described above.
- the oxide material when nitrate, sulfate, chloride, or the like is used as the oxide material, corrosive gas is generated in the subsequent firing step, so that it is preferable to add ammonia water to convert to hydroxide.
- the liquid property of the mixed solution may be adjusted to an acidic alkaline property.
- the catalyst raw material solution (hereinafter, the term “catalyst raw material solution” also includes the case where a carrier component is included) is obtained by removing the solvent by force drying to obtain a catalyst precursor, followed by calcination, etc. And converting the catalyst into an acid catalyst.
- the method for drying the catalyst raw material solution is not particularly limited.
- a method in which the solvent is removed from the catalyst raw material solution under reduced pressure at 50 to 90 ° C. by an evaporator and then dried at 50 to 150 ° C. for 1 to 48 hours in a vacuum dryer A method of spraying and drying the catalyst raw material solution on a hot plate heated to 50 to 300 ° C. with a nozzle, a method of drying using a spray drier (spray hot air drier), and the like.
- Industrially spray Drying with one drier is preferred.
- the spray drier is a hot air drier consisting of a drying chamber, a raw material liquid fog section, hot air intake * exhaust section, and a dry powder recovery section.
- Preferred spray drying conditions are as follows.
- the catalyst raw material solution is supplied using a pump. Then, it is sprayed into the drying chamber by a rotary atomizer (centrifugal atomizer), pressurizing nozzle, two-fluid nozzle (gas atomizer), etc.
- the sprayed droplets of the catalyst raw material solution are brought into contact with hot air controlled at an inlet temperature of 150 to 500 ° C. in countercurrent or cocurrent to evaporate the solvent, and are recovered as a dry powder.
- firing is performed in an electric furnace at 400 to 100 ° C. for 0.5 to 48 hours under a flow of an inert 1 ′′ raw gas such as nitrogen and a Z or oxygen-containing gas.
- treatment may be performed with steam at 150 to 500 ° C for 0.5 to 48 hours before or after calcination.
- the catalyst of the present invention is formed into a columnar shape, a cylindrical shape, a spherical shape, or the like by a known molding method such as tablet molding, extrusion molding, spray molding or the like, depending on the type of the reaction, and then subjected to the reaction.
- the shaping may be performed on the catalyst precursor or may be performed after calcination.
- the reaction of the present invention is carried out in a fluidized bed reaction mode, the catalyst raw material solution is dried using a spray drier and shaped.
- Particularly preferred is a method of obtaining the catalyst precursor and calcining the mixture at 500 to 800 ° C. for 1 to 24 hours while flowing an oxygen-containing gas.
- the catalyst used in the reaction of the present invention is a catalyst in which the accumulated amount of carbonaceous material (defined below) on the catalyst during the reaction is controlled in the range of 0.1 to 10% by mass.
- the carbonaceous material mentioned here is a heavy material mainly composed of carbon, which accumulates on the catalyst by a chemical reaction via an organic compound, and accumulates without scattering from the catalyst during the reaction.
- heavy substances that accumulate on the catalyst when producing the corresponding alcohol and Z or ketone from the alkene, or by contact with a highly reactive organic compound separately from the reaction are highly reactive organic compound separately from the reaction.
- the range of the amount of carbonaceous material accumulated on the catalyst needs to be controlled in the range of 0.1 to 10% by mass as described above, and preferably 0.3 to 8% by mass. And more preferably 0.3 to 5% by mass, and still more preferably 0.5 to 5% by mass. %, Particularly preferably 1 to 5% by mass. If the amount of accumulated carbonaceous material is less than 0.1% by mass, the effect of suppressing the formation of carbonaceous material due to the reaction described below tends to be insufficient, and if it exceeds 10% by mass, the catalytic activity is insufficient. It tends to be.
- the amount of carbonaceous material accumulated on the catalyst is defined by the following formula, using a CHN coder used for organic elemental analysis to measure the carbon mass of the catalyst in which the carbonaceous material is accumulated.
- Amount of carbonaceous material accumulated on the catalyst (% by mass) BZ (A— B) XI 0 0
- the analysis conditions of the CHN coder could be the general measurement conditions of the CHN coder, but specifically, Samples of several mg to several tens of mg (depending on the amount of carbonaceous material accumulated on the catalyst) were analyzed in a helium stream containing a certain amount of oxygen gas in a combustion furnace at 850 ° C. The organic component is burned, and the mass of carbon is measured from the combustion gas.
- the method of controlling the amount of carbonaceous material accumulated on the catalyst can be controlled within the above range by selecting appropriate reaction conditions represented by the reaction conditions described in the present specification, for example.
- the catalyst when regenerating the catalyst after the reaction in which the carbonaceous substance has accumulated on the catalyst, for example, by selecting appropriate regeneration conditions typified by the regeneration conditions described in this specification, the catalyst is again subjected to the reaction.
- the amount of carbonaceous material accumulated on the regenerated catalyst By controlling the amount of carbonaceous material accumulated on the regenerated catalyst, the amount of carbonaceous material accumulated on the catalyst in the reactor can be controlled within the above range.
- the reaction to produce the corresponding alcohol and z or ketone from the alkene is performed by circulating the catalyst between the fluidized bed reactor and the regenerator, return from the regenerator to the reactor under the following regeneration conditions It is preferable to control the amount of carbonaceous material accumulated on the catalyst within the above range. That is, the oxygen gas concentration is maintained at 100 to 550 ° C. for 10 seconds to 10 hours in an atmosphere containing oxygen gas having an oxygen gas concentration of 10 to 21% by volume.
- the temperature is more preferably from 270 to 550 ° C, and particularly preferably from 270 to 500 ° C. Below 270 ° C, the recovery of catalytic activity tends to be inadequate when the reaction conditions used are severe, and above 550 ° C, the carbonaceous material on the catalyst is completely (Ie, below the lower limit of the range specified in the present invention).
- lattice oxygen of an oxide catalyst is used as an oxygen source during the reaction.
- treatment under the above-mentioned regeneration conditions is preferable because lattice oxygen can be replenished at the same time.
- Another method is to control the amount of carbonaceous material accumulated on the catalyst by contacting the catalyst with a reactive organic compound such as aromatic hydrocarbons or gens under appropriate processing conditions. (For example, treatment at 130 to 500 ° C. in a gaseous atmosphere of the above compound is preferable).
- reaction conditions, regeneration conditions, treatment conditions, etc. are appropriately selected, and the amount of carbonaceous material accumulated on the catalyst can be controlled within the range of 0.1 to 10% by mass during the reaction. is important.
- a fresh catalyst or a catalyst that has little or no carbonaceous material accumulated on the catalyst ie, a catalyst in which the amount of carbonaceous material accumulated on the catalyst falls below the lower limit of the range specified by the present invention
- the yield of the target product with respect to the supplied alkene that is, the selectivity of the target product in the product
- the yield of the target product with respect to the supplied alkene is significantly reduced because the amount of the carbonaceous substance generated by the reaction and accumulated in the catalyst is extremely large.
- the catalyst of the present invention in which the amount of carbonaceous material accumulated is controlled to be in a specific range can significantly suppress the accumulation of carbonaceous material produced by the reaction on the catalyst, and consequently the target product Can be greatly improved. Moreover, the productivity of the target product can be made comparable to that of a fresh catalyst by using the catalyst of the present invention.
- the catalyst is frequently regenerated in an atmosphere containing oxygen gas in order to maintain catalytic activity. Must. This is because it is necessary to supplement the lattice oxygen of the oxide catalyst used as the oxygen source for the reaction.
- the method of the present invention is a reaction in which a raw material containing an alkene is brought into contact with an oxide catalyst in a gas phase in the presence of steam to carry out a reaction and produce a corresponding alcohol and Z or ketone from the alkene.
- the present inventors first produced an alcohol by a hydration reaction between the alkene and water vapor, and then produced the alcohol and gaseous molecular oxygen or solid oxygen (ie, It is presumed that ketones are formed by the oxidative dehydrogenation reaction with the lattice oxygen of the oxide catalyst).
- the alkene contained in the reaction raw material preferably includes propylene, 1-butene, 2-butene (cis and / or trans), pentene, hexene, cyclohexene, heptene, otaten, cyclootaten and the like. More preferred are propylene, 1-butene, 2-butene (cis and Z or trans) and cyclohexene, and particularly preferred are 1-butene and 2-butene (cis and / or trans). These may be used alone or in combination of two or more.
- Butaje switch (1, 2-butadiene and / or 1, 3-butadiene) by extraction from C 4 fraction obtained by thermal cracking of naphtha for industrial or C 4 Rafuine one toe 1 except the, C 4 raffinate an 1 is reacted with H 2 0 or methanol, C 4 raffinate one 2 except converted to the tert- butyl alcohol or methyl-tert- Buchirue one ether
- Isobuten included is a useful raw material.
- 1 mol or less preferably 0.5 mol or less, more preferably 0.1 mol or less, particularly preferably 1 mol or less per mol of 1-butene and Z or 2-butene.
- Isobutene, butadiene, tert-butyl alcohol, methyl-tert-butyl ether and the like may be contained within the range of 0.05 mol or less. This is a beneficial feature that can reduce raw material refining costs.
- a gas inert to the reaction such as nitrogen gas, argon gas, carbon dioxide gas, methane gas, ethane gas, propane gas, butane gas or the like may be mixed and brought into the reaction raw material as a diluting gas or carrier gas.
- the amount of steam supplied to the reactor / the amount of alkene supplied to the reactor is preferably in the range of 0.05 to 10.0, and more preferably in the range of 0.2 to 5.0. And particularly preferably in the range of 0.5 to 2.0. If the molar ratio is less than 0.05, the reaction rate tends to decrease, and if the molar ratio is too high, the reaction rate tends to increase. Extra energy is needed.
- Molecular oxygen may or may not be present in the above reaction. As described above, the present inventors presume that when molecular oxygen is not present in the gas phase, lattice oxygen of the oxide catalyst is used as the oxygen source for the reaction.
- the amount of oxygen gas supplied to the reactor / the amount of alkene supplied to the reactor is preferably in the range of 0.0 to 5.0, more preferably 0.0 to 1.0. Within the range, more preferably within the range of 0.0 to 0.5, and particularly preferably within the range of 0.0 to 0.3. Excess oxygen tends to decrease the selectivity of the desired product in the product.
- the molar ratio of 0.0 means that molecular oxygen is not present and lattice oxygen of the oxide catalyst is used for the reaction. In the reaction of the present invention, it is most preferable that this molecular oxygen is not present.
- WH SV weight hourly space velocity
- Weight space velocity (WHSV) is defined by the following equation.
- WHS V (Hr — 1 ) Alkene supply amount (KgZHr) / catalyst amount (Kg)
- the preferred range of the reaction temperature varies depending on the raw material, but generally 130 to 500 ° C. is preferred.
- the temperature is more preferably from 200 to 450 ° C, and particularly preferably from 230 to 350 ° C.
- the reaction pressure is not particularly limited. It is preferably from 0.01 to 1 MPa, more preferably from 0.03 to 0.5 MPa, and particularly preferably from 0.05 to 0.3 MPa.
- the reaction system used in the method of the present invention includes a fixed bed reaction system, a moving bed reaction system, a fluidized bed reaction system and the like.
- a fluidized bed reaction system in which the reaction temperature can be easily controlled is preferable.
- the catalyst used for the reaction is continuously or intermittently withdrawn to the regenerator while the reaction is carried out in a fluidized bed reaction method, regenerated under the conditions described above, and the catalyst returned from the regenerator to the reactor is returned to the reactor. Replenish the lattice oxygen.
- the amount of the oxide catalyst returned to the reactor / the amount of the alkene supplied to the reactor is preferably 0.5 to 100, more preferably 2 to 100, and particularly preferably. Is from 100 to 100. If the mass ratio is less than 0.5, the steady-state activity of the catalyst tends to be low, and if it is 100 or more, the effect of increasing the steady-state activity of the catalyst tends to be small.
- the catalyst In the fluidized bed reactor or the catalyst regenerator, the catalyst is continuously or intermittently supplied or discharged, so the internal catalyst is stirred by the flowing gas, but the amount of carbonaceous material accumulated on the catalyst May result in a local distribution of In such a case, a homogeneous sample is obtained as much as possible by sampling the catalyst from the line that extracts the catalyst from the reactor to the regenerator or the line that returns the catalyst from the regenerator to the reactor, and accumulates on the catalyst. By measuring the amount of carbonaceous material collected, the amount of carbonaceous material accumulated on the catalyst in the reactor or from the regenerator to the reactor is defined. Specifically, it is preferable to sample at least 1 g of the catalyst and at least three samples, measure the amount of each carbonaceous substance, and take the arithmetic average.
- Figure 1 shows a schematic diagram of a fluidized bed reactor and a catalyst regenerator. That is, sampling the catalyst from S 2 of S l catalyst recycle line 2 in and withdrawing the catalyst drawing lines 1, measuring the carbonaceous material amount accumulated on the catalyst.
- the carbonaceous material amount accumulated on the catalyst in the reactor is from 0.1 to 1 0 wt 0/0, so preferably 0. It I is controlled to a range of 3-5 wt% , According, if carbonaceous or material weight in the range of the average is the range of the carbonaceous material of the sample from the S 1 beauty S 2 samples from S E and / or S 2. Alcohol and / or ketone is recovered from the reaction mixture containing alcohol and / or Z or ketone obtained by the above-mentioned reaction by known recovery, separation and purification operations such as cooling, distillation and extraction. it can. Unreacted alkenes can be recycled as needed after separation from the reaction mixture and recycled as necessary.
- the recovered water obtained after cooling or liquefying all or part of the steam supplied to the reaction can be reused in the reaction even if it contains a certain amount of reaction by-products.
- recovered water containing by-products such as acetone and acetic acid by-produced by the reaction of 1-butene can be reused in the reaction. This is a useful feature that can greatly reduce the burden of wastewater treatment.
- the reaction mixture when producing MEK from 1-butene and / or 2-butene, the reaction mixture is cooled and the MEK and water vapor are condensed. After gas-liquid separation, MEK is recovered from the pseudo-liquor by distillation. All or part of the recovered water, including by-products after the recovery of MEK, is recycled back to the reactor as steam.
- the non-condensed gas phase is compressed and cooled to liquefy and recover the MEK entrained in the gas phase, and unreacted 1-butene and / or 2-butene is separated from light gases such as carbon dioxide, Recycle the reactor.
- FIG. 1 is a schematic diagram of a reactor and a regenerator when the reaction of the present invention is carried out by a fluidized bed reaction by a catalyst circulation system. Among them, 1 indicates the catalyst extraction line, and 2 indicates the catalyst recycling line.
- the analyzer used and the analysis conditions are described below.
- Catalyst B having a different composition was prepared in substantially the same manner as in Reference Example 1.
- the composition of this catalyst B is SnO. 48% by mass, Mo 0 3 1 1% by mass 1 %, Si 0 2 4 1% by mass Was.
- the Mo / (Sn + Mo) atomic ratio of this catalyst B was 0.19, and it had a smooth spherical shape suitable for a fluidized bed catalyst and had sufficient mechanical strength.
- Catalyst C having a different composition was prepared in substantially the same manner as in Reference Example 1. This set configuration of Catalyst C, S n O 2 65% by mass, M o O 3 5% wt%, and the S i O 2 30% by weight.
- the Mo / (Sn + Mo) atomic ratio of this catalyst C was 0.07, and it had a smooth spherical shape suitable for a fluidized bed catalyst and had sufficient mechanical strength.
- Catalyst D was prepared in substantially the same manner as in Reference Example 1. The composition of this catalyst D is
- Mo / (Sn + Mo) of the fluidized bed catalyst is preferably less than 0.50, more preferably 0.24 or less.
- Catalyst E composed of acid and Cr and Mo was prepared in substantially the same manner as in Reference Example 1 except that chromium trichloride hexahydrate was used in place of stannic salt pentahydrate.
- the composition of this catalyst E is, C r 2 O 3 42 wt%, Mo Og 1 7% wt%, and the S i O 2 41 weight 0/0.
- the Mo / (Cr + Mo) atomic ratio of this catalyst E was 0.18, and it had a smooth spherical shape suitable for a fluidized bed catalyst and had sufficient mechanical strength.
- Catalyst F composed of oxides of Ti and Mo was prepared in substantially the same manner as in Reference Example 1, except that tetrachloride titanium was used instead of stannic salt pentahydrate.
- the composition of this catalyst F is, T i O 2 44 weight 0/0, M o O 3 1 7% by weight 0/0, S I_ ⁇ 2 39 weight 0 /. Met.
- the catalyst F had a Mo / (T i + Mo) atomic ratio of 0.18, had a smooth spherical shape suitable for a fluidized bed catalyst, and had sufficient mechanical strength.
- Catalyst G consisting solely of Sn oxidized product was prepared in substantially the same manner as in Reference Example 1 except for removing the molybdate ammonium.
- the composition of this catalyst G is Sn_ ⁇ 2 45 mass %, And Si0 2 55% by mass.
- This catalyst G had a smooth sphere suitable for a fluidized bed catalyst, and had sufficient mechanical strength.
- Catalyst H was prepared in substantially the same manner as in Reference Example 1, except that alumina sol was used as a part of the carrier.
- the composition of the catalyst H is, S N_ ⁇ 2 51 mass 0/0, Mo 0 3 7 wt%, S 1_Rei 2 28 wt%, and the A 1 2 0 3 14 mass 0/0.
- This catalyst H had a Mo Z (S n + Mo) atomic ratio of 013, had a smooth spherical shape suitable for a fluidized bed catalyst, and had a higher mechanical strength than a carrier having only a sily force.
- a reactor consisting of a fluidized bed reactor and a catalyst regenerator as shown in Fig. 1 is charged with catalyst A, and the reaction and catalyst regeneration are continuously performed while circulating catalyst A between the reactor and the regenerator.
- the fluidized bed reaction was carried out in a manner.
- the reaction temperature was 250 ° C.
- a gas mixture of air and N 2 was supplied to the regenerator.
- the regeneration temperature was 320 ° C.
- the ratio of the amount of catalyst circulated (that is, the amount of catalyst returning from the regenerator to the reactor) for one supplied feedstock is 15 (mass ratio), and the amount of carbonaceous material accumulated on the catalyst returning from the regenerator to the reactor is 3 It was 5% by mass.
- the above reaction was continued for about 10 hours, and a part of the result of the reaction for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- the amount of ME K generated (Cmo 1): The amount of ME K generated in one hour
- 2-Butene a product of the 1-butene isomerization reaction, was treated as an unreacted product because it can be reused as a raw material.
- the by-products in the table C_ ⁇ 2, co, acetone, acetic acid, butyl alcohol, is 5 or more oligomers first class carbon.
- the carbonaceous substance selectivity in the table is the selectivity of the carbonaceous substance newly generated by the reaction.
- Example 1 Except that the regeneration temperature was set at 600 ° C., a fluidized bed reaction using a catalyst circulation system was performed under substantially the same conditions as in Example 1. At this time, the accumulated amount of the carbonaceous substance on the catalyst returned to the reactor from the regenerator was 0.03% by mass, and the carbonaceous substance on the catalyst was almost completely removed. The above reaction was continued for about 10 hours, and a part of the reaction results for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 1 From a comparison between Example 1 and Comparative Example 1, the amount of MEK produced was controlled by controlling the amount of carbonaceous material accumulated on the catalyst returning from the regenerator to the reactor in the range of 0.1 to 10% by mass. Nevertheless, it can be seen that the suppression of the formation of new carbonaceous materials greatly improved the selectivity of MEK.
- Example 2 the value of the MEK selectivity excluding the generated carbonaceous material, which indicates the purity of the generated MEK, is extremely high, indicating that the separation and purification of MEK are easy.
- Example 2 the value of the MEK selectivity excluding the generated carbonaceous material, which indicates the purity of the generated MEK, is extremely high, indicating that the separation and purification of MEK are easy.
- a catalyst-circulating fluidized bed reaction was performed under substantially the same conditions as in Example 1 except that the amount of air supplied to the regenerator was reduced. At this time, the accumulated amount of carbonaceous material on the catalyst returning to the reactor from the regenerator was 3.3% by mass.
- the above reaction was continued for about 10 hours, and a part of the reaction results for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- the regeneration temperature was set at 280 ° C, and the catalyst
- the fluidized bed reaction of the catalyst circulation system was performed under almost the same conditions as in Example 1 except that the ratio of the circulation amount was set to 60 (mass ratio). At this time, the accumulated amount of carbonaceous material on the catalyst returning from the regenerator to the reactor was 3.7% by mass.
- the above reaction was continued for about 10 hours, and a part of the reaction results for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 5 Example in which the amount of accumulated carbonaceous material is 0.5% by mass using catalyst B
- Example 7 (Example of reusing a reaction recovery solution containing a reaction by-product)
- a fluidized bed reaction using a catalyst circulation system was carried out under substantially the same conditions as in Example 1 except that the residual liquid obtained by distilling and separating MEK from the reaction solution of Example 1 was used instead of water.
- This residue contained 4% by mass of acetic acid as a by-product and 0.5% by mass of high-boiling components.
- the accumulated amount of the carbonaceous substance on the catalyst returning from the regenerator to the reactor was 3.5% by mass.
- the above reaction was continued for about 10 hours, and a part of the reaction results for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 8 Example in which the raw material is changed to C 4 rough rice 1 to 2
- Example 10 (Example using Mo, Cr oxidizing catalyst E)
- a fluidized bed reaction using a catalyst circulation system was carried out under substantially the same conditions as in Example 1 except that the catalyst E was used. At this time, the accumulated amount of the carbonaceous substance on the catalyst returned to the reactor from the regenerator was 3.3% by mass.
- the above reaction was continued for about 10 hours, and a part of the reaction results for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 11 (Example using Mo, Ti acid catalyst F)
- a fluidized bed reaction of a catalyst circulation system was performed under substantially the same conditions as in Example 1 except that catalyst F was used. At this time, the accumulated amount of the carbonaceous substance on the catalyst returned to the reactor from the regenerator was 3.7% by mass. The above reaction was continued for about 10 hours, and a part of the reaction result for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 12 (Example using catalyst G containing only Sn oxide)
- Example 13 Example using a silica-alumina catalyst
- a fluidized bed reaction using a catalyst circulation system was performed under substantially the same conditions as in Example 1 except that the catalyst H was used. At this time, the accumulated amount of the carbonaceous substance on the catalyst returned from the regenerator to the reactor was 4.2% by mass. The above reaction was continued for about 10 hours, and a part of the reaction result for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 14 Example of pretreating catalyst to accumulate carbonaceous material
- a pretreatment device was provided between the regenerator and the reactor, and the reaction was performed in substantially the same manner as in Example 1.
- the regeneration temperature was 600 ° C., and the amount of carbonaceous material accumulated on the catalyst from the regenerator to the pretreatment device was almost completely removed as in Comparative Example 1.
- This catalyst was treated in a pretreatment device with 30 volumes of benzene 0 /. , 1, 2-, 1, 3-butadiene 20 volume 0 /.
- Was accumulated carbonaceous material on the catalyst is contacted with gas and 3 5 0 ° C consisting of N 2 5 0 Capacity%.
- the amount of carbonaceous material accumulated on the catalyst returning from the pretreatment device to the reactor was 2.0% by mass.
- the above reaction was continued for about 10 hours, and a part of the reaction results for an arbitrary hour is shown in Table 1. The reaction results were almost constant during the reaction.
- Example 1 A 0.13 3.5 15 0.0 2.0 320 632 86 4 10 95.6 Comparative Example 1 A 0.13 0.03 15 0.0 2.0 600 624 50 4 4S 92.6 Example 2 A 0.13 3.3 15 0.0 2.0 320 520 90 4 6 95.7 Example 3 A 0.13 3.1 15 0.0 1.0 320 648 91 3 6 96.8 Example 4 B 0.19 3.7 60 0.0 2.0 280 616 85 5 10 94.4 Example 5 B 0.19 0.5 15 0.0 2.5 500 376 70 5 25 93,3 Example 6 C 0.07 2.5 0.5 0.2 2.0 280 500 86 10 4 89.6 Example 7 A 0.13 3.5 15 0.0 2.0 320 640 86 4 10 95.6 Example 8 A 0.13 '4.5 15 0.0
- Catalyst Catalyst composition anti] 3 ⁇ 4, 3 ⁇ 4 To catalyst circulation amount ⁇ 2 Steam regeneration MEK MEK By-product Carbonaceous material MEK * 1
- Example 11 In Example 11 only, the total value of MEK and butanol is shown. That is, the amount of MEK production is the sum of MEK 305 mmo 1 and butal 331 mmo 1.
- the production method of the present invention has an effect of suppressing the accumulation of carbonaceous substances on a catalyst during a reaction when producing a corresponding alcohol and / or ketone from an alkene in a gas phase using an oxide catalyst. Therefore, the selectivity of the target product can be greatly improved. Therefore, it is possible to suppress the loss of the raw material alkene due to the generation of carbonaceous materials and to reduce the utility cost required for catalyst regeneration, etc., and to provide a method for producing the target product with extremely high productivity.
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Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
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US10/541,367 US7291755B2 (en) | 2003-01-06 | 2003-12-25 | Process for producing alcohol and/or ketone |
JP2004564523A JP4547270B2 (ja) | 2003-01-06 | 2003-12-25 | アルコール及び/又はケトンの製造方法 |
EP03786307A EP1582510A4 (en) | 2003-01-06 | 2003-12-25 | PROCESS FOR PRODUCING ALCOHOL AND / OR KETONE |
AU2003296112A AU2003296112A1 (en) | 2003-01-06 | 2003-12-25 | Process for producing alcohol and/or ketone |
Applications Claiming Priority (2)
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JP2003000110 | 2003-01-06 | ||
JP2003-000110 | 2003-01-06 |
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WO2004060843A1 true WO2004060843A1 (ja) | 2004-07-22 |
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PCT/JP2003/016722 WO2004060843A1 (ja) | 2003-01-06 | 2003-12-25 | アルコール及び/又はケトンの製造方法 |
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US (1) | US7291755B2 (ja) |
EP (1) | EP1582510A4 (ja) |
JP (1) | JP4547270B2 (ja) |
KR (1) | KR100636570B1 (ja) |
CN (1) | CN1735578A (ja) |
AU (1) | AU2003296112A1 (ja) |
TW (1) | TWI293291B (ja) |
WO (1) | WO2004060843A1 (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1714954A1 (en) * | 2004-02-10 | 2006-10-25 | Maruzen Petrochemical Co., Ltd. | Method for producing alcohol and/or ketone |
CN104470875A (zh) * | 2012-05-09 | 2015-03-25 | 链解决方案公司 | 一种通过非催化的化学反应生成含氧化合物的方法 |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7482497B2 (en) * | 2007-06-27 | 2009-01-27 | H R D Corporation | Method of making alcohols |
US7491856B2 (en) | 2007-06-27 | 2009-02-17 | H R D Corporation | Method of making alkylene glycols |
US8581007B2 (en) | 2011-04-04 | 2013-11-12 | Exxonmobil Chemical Patents Inc. | Use of steam to reduce coking and/or metal dusting |
CN108369162B (zh) * | 2015-12-16 | 2021-08-27 | 环球油品公司 | 用于催化剂取样的方法和装置 |
CN108002967B (zh) * | 2017-11-28 | 2021-01-29 | 万华化学集团股份有限公司 | 一种惕各醛衍生物的制备方法 |
US11091701B2 (en) * | 2019-01-10 | 2021-08-17 | Saudi Arabian Oil Company | Conversion of olefinic naphthas by hydration to produce middle distillate fuel blending components |
KR102325331B1 (ko) * | 2019-12-20 | 2021-11-10 | 한화토탈 주식회사 | 터트-부탄올로부터 이소부틸렌의 제조방법 |
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GB1240858A (en) * | 1967-10-07 | 1971-07-28 | Stamicarbon | Process for the preparation of ketones and/or aldehydes from olefins |
GB1324717A (en) * | 1969-11-12 | 1973-07-25 | Stamicarbon | Process for the preparation of alkanones from olefins |
US3987104A (en) * | 1972-06-12 | 1976-10-19 | Stamicarbon B.V. | Process for preparing saturated ketones and a catalyst for realizing the process |
EP0614872A1 (en) * | 1993-03-12 | 1994-09-14 | Nippon Shokubai Co., Ltd. | Process for removal of solid organic matters |
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US3636156A (en) * | 1968-04-25 | 1972-01-18 | Idemitsu Petrochemical Co | Process for the direct production of ketones from olefins |
US4022837A (en) * | 1970-07-24 | 1977-05-10 | Chevron Research Company | Production of ketones from alkenes, hydrated molybdenum(VI) oxide and water |
JPS478046U (ja) | 1971-02-23 | 1972-09-29 | ||
JPS5211782B2 (ja) | 1972-08-03 | 1977-04-02 | ||
JPS5320485B2 (ja) | 1972-11-22 | 1978-06-27 | ||
US4560804A (en) * | 1982-09-21 | 1985-12-24 | Exxon Research & Engineering Co. | Catalytic process for the manufacture of ketones |
US4737482A (en) * | 1983-07-25 | 1988-04-12 | Exxon Research & Engineering Co. | Catalysts for oxidation of olefins to ketones |
JPS59163335A (ja) | 1983-03-09 | 1984-09-14 | Tokuyama Soda Co Ltd | オレフイン類の気相酸化方法 |
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2003
- 2003-12-25 US US10/541,367 patent/US7291755B2/en not_active Expired - Lifetime
- 2003-12-25 KR KR1020057012608A patent/KR100636570B1/ko active IP Right Grant
- 2003-12-25 EP EP03786307A patent/EP1582510A4/en not_active Withdrawn
- 2003-12-25 CN CNA200380108304XA patent/CN1735578A/zh active Pending
- 2003-12-25 WO PCT/JP2003/016722 patent/WO2004060843A1/ja active Application Filing
- 2003-12-25 JP JP2004564523A patent/JP4547270B2/ja not_active Expired - Fee Related
- 2003-12-25 AU AU2003296112A patent/AU2003296112A1/en not_active Abandoned
- 2003-12-30 TW TW092137509A patent/TWI293291B/zh not_active IP Right Cessation
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GB1240858A (en) * | 1967-10-07 | 1971-07-28 | Stamicarbon | Process for the preparation of ketones and/or aldehydes from olefins |
GB1324717A (en) * | 1969-11-12 | 1973-07-25 | Stamicarbon | Process for the preparation of alkanones from olefins |
US3987104A (en) * | 1972-06-12 | 1976-10-19 | Stamicarbon B.V. | Process for preparing saturated ketones and a catalyst for realizing the process |
EP0614872A1 (en) * | 1993-03-12 | 1994-09-14 | Nippon Shokubai Co., Ltd. | Process for removal of solid organic matters |
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1714954A1 (en) * | 2004-02-10 | 2006-10-25 | Maruzen Petrochemical Co., Ltd. | Method for producing alcohol and/or ketone |
EP1714954A4 (en) * | 2004-02-10 | 2008-02-13 | Maruzen Petrochem Co Ltd | PROCESS FOR PRODUCING ALCOHOL AND / OR KETONE |
CN104470875A (zh) * | 2012-05-09 | 2015-03-25 | 链解决方案公司 | 一种通过非催化的化学反应生成含氧化合物的方法 |
CN104470875B (zh) * | 2012-05-09 | 2016-08-17 | 链解决方案公司 | 一种通过非催化的化学反应生成含氧化合物的方法 |
Also Published As
Publication number | Publication date |
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US20060173220A1 (en) | 2006-08-03 |
EP1582510A4 (en) | 2006-07-05 |
KR100636570B1 (ko) | 2006-10-19 |
EP1582510A1 (en) | 2005-10-05 |
AU2003296112A1 (en) | 2004-07-29 |
JPWO2004060843A1 (ja) | 2006-05-11 |
TWI293291B (en) | 2008-02-11 |
JP4547270B2 (ja) | 2010-09-22 |
KR20050088246A (ko) | 2005-09-02 |
CN1735578A (zh) | 2006-02-15 |
US7291755B2 (en) | 2007-11-06 |
TW200418780A (en) | 2004-10-01 |
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