WO2006109667A1 - 2,7-ジメチルナフタレンの精製方法 - Google Patents
2,7-ジメチルナフタレンの精製方法 Download PDFInfo
- Publication number
- WO2006109667A1 WO2006109667A1 PCT/JP2006/307321 JP2006307321W WO2006109667A1 WO 2006109667 A1 WO2006109667 A1 WO 2006109667A1 JP 2006307321 W JP2006307321 W JP 2006307321W WO 2006109667 A1 WO2006109667 A1 WO 2006109667A1
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- WO
- WIPO (PCT)
- Prior art keywords
- dimethylnaphthalene
- purifying
- raw material
- solvent
- material oil
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Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/373—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation
- C07C5/393—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation with cyclisation to an aromatic six-membered ring, e.g. dehydrogenation of n-hexane to benzene
- C07C5/41—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
- C07C15/20—Polycyclic condensed hydrocarbons
- C07C15/24—Polycyclic condensed hydrocarbons containing two rings
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2729—Changing the branching point of an open chain or the point of substitution on a ring
- C07C5/2732—Catalytic processes
- C07C5/2737—Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
- C07C2523/04—Alkali metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/18—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type
Definitions
- the present invention relates to a method for efficiently separating 2,7-dimethylnaphthalene from a raw oil containing a mixture of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene, and particularly, separation and purification with high purity.
- the present invention relates to a method for separating 2,7-dimethylnaphthalene, which is difficult to achieve.
- This 2,7-dimethyl naphthalene is oxidized to 2,7-naphthalenedicarboxylic acid, or it is esterified to dimethyl 2,7-naphthalenedicarboxylic acid, which has excellent heat resistance and physical strength. It is extremely useful as a raw material for high performance polyester.
- Dimethylnaphthalene (hereinafter sometimes referred to as "DMN") has 10 isomers.
- organic compounds are purified by operations such as distillation, crystallization, adsorption, or a combination of these methods.
- Conventional methods for separating dimethylnaphthalene mixtures include crystallization and separation using an adsorbent! / Speak.
- 2,7-dimethylnaphthalene (hereinafter sometimes referred to as “2,7-DMN”) is selectively precipitated from a dimethylnaphthalene isomer mixture using ethyl alcohol as a solvent, and low melting point DMNs are obtained.
- Patent Document 1 By filtration while maintaining the liquid state (see Patent Document 1), or by treating the DMN isomer mixture containing 2,7-DMN with methanol, followed by crystallization separation and 2,7-DMN (See Patent Document 2), a method for obtaining 2,7-DMN with high purity from raw material oil containing DMN isomer by pressure crystal (see Patent Document 3), and DMN isomer mixture
- Patent Document 4 a method of adsorbing and separating 2,7-DMN and 2,6-dimethylnaphthalene with high selectivity by using zeolite having a 10-membered ring as an adsorbent is known (see Patent Document 4). It has been.
- 1,7-DMN 2,7-dinaphthane from mixtures such as 2,7-dimethylnaphthalene and 1,7-dimethylnaphthalene
- Patent Document 1 Japanese Patent Laid-Open No. 9 124520
- Patent Document 2 JP-A-48-22448
- Patent Document 3 Japanese Patent Laid-Open No. 4-120027
- Patent Document 4 Japanese Patent Laid-Open No. 1-224336
- the present invention solves the above problems, and an object of the present invention is to produce 2,7-dimethylnaphthalene with a high purity and a high yield from a dimethylnaphthalene isomer mixture at a low production cost and a simple constitution.
- the object of the present invention is to provide an industrially stable production method.
- the present inventors have determined that 2,7-dimethyl by adsorption separation from a raw material oil containing 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene.
- the separation of naphthalene the adsorption power of 1,7-dimethylnaphthalene to a specific adsorbent is used, and by using an appropriately selected adsorbent, the non-adsorbed 2,7-dimethylnaphthalene It was found that selective separation is possible.
- 2,7-dimethylnaphthalene can be separated and purified with high purity by using L-type zeolite as the adsorbent and using aliphatic hydrocarbons or alicyclic hydrocarbons as the developing solvent. Reached Ming.
- the present invention includes a step of contacting a raw material oil containing a mixture of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene with L-type zeolite together with a developing solvent to adsorb 1,7-dimethylnaphthalene. This is a method for purifying 2,7-dimethylnaphthalene.
- 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene can be produced with a simple structure.
- the 2,7-dimethylnaphthalene can be separated efficiently and with high purity from the dimethylnaphthalene mixture, and it has great industrial significance.
- the method for purifying 2,7-dimethylnaphthalene according to the present invention comprises contacting a raw material oil containing a mixture of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene with L-type zeolite together with a developing solvent. , 7-dimethylnaphthalene adsorbing step (A) is included.
- the feedstock containing a mixture of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene used for purification in the present invention is a combined amount of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene. Is preferably 70% by weight or more.
- the method for producing a feedstock containing a mixture of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene is not limited, but can be obtained by the following feedstock production process (D) with the following steps (1) to (3) I prefer that.
- Process (1) is a process for the conversion of para-xylene and 1,3-butadiene to 5-paratolyl-2-pentene
- process (2) is from 5-paratolyl-2-pentene to 1,7-dimethylnaphthalene.
- step (3) 1,7-dimethylnaphthalene is isomerized to give 2,7-dimethylnaphthalene.
- Various methods can be used for the isomerization in the isomerization step (3), but it can be performed relatively easily by using a solid acid catalyst or the like.
- a feedstock containing 70% by weight or more of the combined amount of 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene can be easily obtained. It can be obtained.
- Examples of the step (1) include the following.
- 1,3-Butadiene is introduced and a batch reaction is performed. After completion of the reaction, cool, transfer to another glass container, supply sulfuric acid aqueous solution with stirring and let stand. This supernatant is distilled under reduced pressure. Supply to the column, distill off the low boiling fraction, extract the bottom liquid, and extract 5-paratoluyl-2-pentene while extracting the high boiling fraction in the high boiling power distillation column with increased vacuum.
- Examples of the step (2) include the following.
- reaction liquid after removing heptane is supplied to a vacuum glass distillation column, and low-boiling fraction and high-boiling fraction are withdrawn, and 98% pure 1,7-DMN is withdrawn from the middle stage of the distillation tower.
- Examples of the step (3) include the following.
- a feedstock containing a mixture of 1J-DMN and 2,7-DMN is preferably selected as 1,7-DMN strength zeolite by contacting it with L-type zeolite together with a developing solvent that is organic solvent strength. Adsorbed selectively (adsorption process (A)).
- Examples of the developing solvent suitably used in the present invention include aliphatic hydrocarbons (straight and branched) and alicyclic hydrocarbons, and those having 6 to 14 carbon atoms are preferable.
- Examples include n-hexane, n-heptane, n-octane, isooctane, n-nonane, n-decane, n-undecane, n-dodecane, cyclohexane, decalin, and methylcyclohexane.
- a substance having a greatly different boiling point from 2,7-dimethylnaphthalene is preferable. It is a force that can use a distillation method to separate the developing solvent later.
- aliphatic hydrocarbons and alicyclic hydrocarbons may be used alone or in combination. Further, aliphatic hydrocarbons and alicyclic hydrocarbons may be used in combination.
- the L-type zeolite used in the present invention has a SiO ZA10 ratio (molar ratio) power of .2 to 7.0.
- L-type zeolite Preferably, in the range of 5.6 to 7.0. Further, it preferably has a one-dimensional pore having a diameter of 0.7 nm (oxygen 12-membered ring), and the type of pore system is preferably three-dimensional.
- L-type zeolite include KL-type zeolite, and examples of commercially available KL-type zeolite include “HS-500” (SiO ZA10 ratio (molar ratio) 6.0) manufactured by Wako Pure Chemical Industries, Ltd.
- L-type zeolite, KL type power, KL type zeolite is selected from among alkali metals or alkaline earth metals such as sodium, lithium, rubidium, cesium, norium, L-type zeolite substituted with one or more of metal ions such as calcium, magnesium, strontium and lanthanum can be used.
- These zeolites may be used as they are, or may be used after steam treatment, alkali treatment, acid treatment, ion exchange, and the like.
- the shape is preferably molded into a spherical shape, a noodle shape or a cylindrical shape.
- the present invention allows the raw material oil to flow through the adsorption layer filled with the L-type zeolite at the same time as the development. It is preferable to carry out by a method in which a solvent is passed through or a method in which the developing solvent is added to the raw material oil in advance and passed through the adsorption layer.
- the developing solvent may be used in an amount of 1 to 200 times, preferably 5 to 150 times, more preferably 10 to L00 times the total amount of dimethylnaphthalene in the raw material oil.
- the amount of liquid passing through the adsorption layer is preferably in the range of 0.1 to 10.
- the temperature of the adsorption layer at the time of liquid passage is preferably in the range of 10 to 200 ° C, more preferably in the range of 20 to 150 ° C.
- 1,7-dimethylnaphthalene is selectively adsorbed, and a liquid mainly containing 2,7-dimethylnaphthalene and a developing solvent is distilled out. This distillate is expanded by distillation, etc. By separating the open solvent, 2,7-dimethylnaphthalene of high purity can be obtained (developing solvent separation step (C)).
- dimethylnaphthalene adsorbed on zeolite (mainly 1,7-dimethylnaphthalene) is desorbed and separated to recover Z.
- aromatic hydrocarbons from the viewpoint of elimination time and the like, for example, benzene, toluene, orthoxylene, paraxylene, metaxylene, ethylbenzene, jetylbenzene and the like.
- the amount of the desorption solvent used is preferably 1 to 200 times by weight with respect to the total amount of dimethylnaphthalene in the raw material oil.
- the liquid flow rate at this time is preferably in the range of 0.05 to 20.
- the temperature of the adsorption layer at the time of liquid passage is in the range of 10 to 200 ° C, preferably 20 to 150 ° C.
- the recovered 1,7-dimethylnaphthalene can be recycled as a raw material for the isomerization step (3).
- the adsorption step (A) and the desorption step (B) in the present invention may be performed in various ways such as a fixed bed, a fluidized bed, and a moving bed that may be performed in any of a batch type, a continuous type, and a semi-notch type.
- a fixed bed a fluidized bed
- a moving bed that may be performed in any of a batch type, a continuous type, and a semi-notch type.
- it is preferable to use the simulated moving bed method see, for example, Japanese Patent Laid-Open No. 8-217700), which is an established technology.
- the present invention will be described in more detail with reference to examples. However, the present invention is not limited to these examples.
- the raw materials and target products were analyzed by gas chromatography.
- the part shown below means a weight part.
- reaction mixture was cooled, transferred to another glass container, and 50 parts of 10% aqueous sulfuric acid solution was supplied with stirring and allowed to stand.
- the yield per para-xylene reacted with 5-paratolyl-2-pentene was 82%.
- This supernatant was fed to a 23 kPa distillation column at a rate of 63 parts Zhr to distill off the low boiling fraction.
- the bottom liquid was extracted, and 5-paratoluyl-2-pentene was extracted at 10 parts Zhr while extracting a high boiling fraction at 2 parts Zhr in a 5 kPa high boiling cut distillation column.
- the reaction solution was continuously supplied to a stainless steel cylindrical dehydrogenation reactor filled with 40 parts of 1% platinum Z activated carbon catalyst (manufactured by NE Chemcat).
- the reaction temperature was 280 ° C.
- the dehydrogenation reaction was carried out while simultaneously supplying 20 parts Zhr of n-heptane as a diluent solvent.
- n-heptane was recovered by supplying to a glass distillation column whose pressure was reduced to 19 kPa.
- the n-heptane-removed reaction solution was supplied to a glass distillation column depressurized to 13 kPa, and the low-boiling fraction was extracted at 0.05 part Zhr and the high-boiling fraction was extracted at 0.3 part Zhr. 9.4 parts of 98% pure 1,7-DMN was extracted from the middle column of the distillation column.
- KL-type zeolite manufactured by Wako Pure Chemical Industries, Ltd., "HS-500", SiO ZA1 0 ratio as an adsorbent
- Example 2 The same raw material oil (100 g) used in Example 1 and KL type zeolite (15 g) were contacted at 40 ° C. in a vessel equipped with a stirrer. After 2 hours, filter the zeolite and distill n-heptane. As a result of separation, 2,7-dimethylnaphthalene having a purity of 99.2% was obtained with a recovery rate of 40%.
- the adsorbent zeolite is NaY-type zeolite (manufactured by Wako Pure Chemical Industries, Ltd., HS-320), SiO /
- Example 2 The same procedure as in Example 1 was carried out except that the adsorbent zeolite was ZSM-5 proton type (manufactured by NU Chemcat Co., Ltd.), SiO ZA10 ratio (molar ratio) 26). In this case 1,7
- 2,7-dimethylnaphthalene is efficiently and highly purified from a dimethylnaphthalene mixture containing 1,7-dimethylnaphthalene and 2,7-dimethylnaphthalene with a simple structure. And the industrial significance is extremely great.
- the 2,7-dimethylnaphthalene acidified to 2,7-naphthalenedicarboxylic acid or the esterified to 2,7-naphthalenedicarboxylic acid dimethyl has excellent heat resistance and physical strength. It is extremely useful as a raw material for high-performance polyester.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2007512942A JP4919086B2 (ja) | 2005-04-06 | 2006-04-06 | 2,7−ジメチルナフタレンの精製方法 |
DE602006010843T DE602006010843D1 (de) | 2005-04-06 | 2006-04-06 | Verfahren zur aufreinigung von 2,7-dimethylnaphthalin |
EP06731269A EP1873133B1 (en) | 2005-04-06 | 2006-04-06 | Method of purifying 2,7-dimethylnaphthalene |
US11/910,774 US8124825B2 (en) | 2005-04-06 | 2006-04-06 | Method of purifying 2,7-dimethylnaphthalene |
CN2006800156352A CN101171215B (zh) | 2005-04-06 | 2006-04-06 | 2,7-二甲基萘的精制方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2005109737 | 2005-04-06 | ||
JP2005-109737 | 2005-04-06 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2006109667A1 true WO2006109667A1 (ja) | 2006-10-19 |
Family
ID=37086943
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2006/307321 WO2006109667A1 (ja) | 2005-04-06 | 2006-04-06 | 2,7-ジメチルナフタレンの精製方法 |
Country Status (7)
Country | Link |
---|---|
US (1) | US8124825B2 (ja) |
EP (1) | EP1873133B1 (ja) |
JP (1) | JP4919086B2 (ja) |
KR (1) | KR20080024109A (ja) |
CN (1) | CN101171215B (ja) |
DE (1) | DE602006010843D1 (ja) |
WO (1) | WO2006109667A1 (ja) |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62240632A (ja) * | 1986-04-11 | 1987-10-21 | Mitsui Petrochem Ind Ltd | ジメチルナフタレン異性体の分離方法 |
JPH01224336A (ja) * | 1988-03-04 | 1989-09-07 | Idemitsu Kosan Co Ltd | ジメチルナフタレン異性体の分離方法 |
JPH026320A (ja) * | 1988-01-04 | 1990-01-10 | Exxon Chem Patents Inc | ゼオライトl及びその製造方法 |
JPH05213787A (ja) * | 1992-02-06 | 1993-08-24 | Nikko Kyodo Co Ltd | 2,6−ジメチルナフタレンの分離方法 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3668267A (en) * | 1970-01-30 | 1972-06-06 | Sun Oil Co | Separation of 2,7-dimethylnaphthalene from 2,6-dimethylnaphthalene with molecular sieves |
US3775500A (en) * | 1972-08-09 | 1973-11-27 | Sun Research Development | Preparation of 2,7-dimethylnaphthalene |
JP2766059B2 (ja) * | 1990-09-12 | 1998-06-18 | 財団法人石油産業活性化センター | 2,7―ジメチルナフタレンの分離方法 |
JPH08217700A (ja) * | 1995-02-13 | 1996-08-27 | Chiyoda Corp | パラキシレンの分離方法 |
JPH09124520A (ja) * | 1995-11-08 | 1997-05-13 | Cosmo Sogo Kenkyusho:Kk | 2,7−ジメチルナフタレンの分離回収法 |
US6057487A (en) * | 1997-12-30 | 2000-05-02 | Chevron Chemical Company | Method for producing 2,6-DMN from mixed dimethylnaphthalenes by crystallization, adsorption and isomerization |
DE60002513T2 (de) * | 1999-02-22 | 2004-04-08 | Mitsubishi Gas Chemical Co., Inc. | Verfahren zur Herstellung von Dimethyltetralin |
CN100584808C (zh) * | 2004-12-24 | 2010-01-27 | 三菱瓦斯化学株式会社 | 二甲基萘异构体的分离方法 |
-
2006
- 2006-04-06 JP JP2007512942A patent/JP4919086B2/ja not_active Expired - Fee Related
- 2006-04-06 EP EP06731269A patent/EP1873133B1/en not_active Expired - Fee Related
- 2006-04-06 US US11/910,774 patent/US8124825B2/en not_active Expired - Fee Related
- 2006-04-06 KR KR1020077025708A patent/KR20080024109A/ko active IP Right Grant
- 2006-04-06 DE DE602006010843T patent/DE602006010843D1/de active Active
- 2006-04-06 CN CN2006800156352A patent/CN101171215B/zh not_active Expired - Fee Related
- 2006-04-06 WO PCT/JP2006/307321 patent/WO2006109667A1/ja active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62240632A (ja) * | 1986-04-11 | 1987-10-21 | Mitsui Petrochem Ind Ltd | ジメチルナフタレン異性体の分離方法 |
JPH026320A (ja) * | 1988-01-04 | 1990-01-10 | Exxon Chem Patents Inc | ゼオライトl及びその製造方法 |
JPH01224336A (ja) * | 1988-03-04 | 1989-09-07 | Idemitsu Kosan Co Ltd | ジメチルナフタレン異性体の分離方法 |
JPH05213787A (ja) * | 1992-02-06 | 1993-08-24 | Nikko Kyodo Co Ltd | 2,6−ジメチルナフタレンの分離方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP1873133A4 * |
Also Published As
Publication number | Publication date |
---|---|
CN101171215A (zh) | 2008-04-30 |
CN101171215B (zh) | 2011-09-21 |
EP1873133A1 (en) | 2008-01-02 |
US20100113853A1 (en) | 2010-05-06 |
EP1873133A4 (en) | 2008-12-03 |
JPWO2006109667A1 (ja) | 2008-11-13 |
KR20080024109A (ko) | 2008-03-17 |
EP1873133B1 (en) | 2009-12-02 |
DE602006010843D1 (de) | 2010-01-14 |
US8124825B2 (en) | 2012-02-28 |
JP4919086B2 (ja) | 2012-04-18 |
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