WO1999065968A1 - Procede de production d'un polymere de tetrahydrofuranne - Google Patents
Procede de production d'un polymere de tetrahydrofuranne Download PDFInfo
- Publication number
- WO1999065968A1 WO1999065968A1 PCT/JP1999/003081 JP9903081W WO9965968A1 WO 1999065968 A1 WO1999065968 A1 WO 1999065968A1 JP 9903081 W JP9903081 W JP 9903081W WO 9965968 A1 WO9965968 A1 WO 9965968A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- heteropolyacid
- thf
- catalyst
- acid
- content
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/04—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers only
- C08G65/06—Cyclic ethers having no atoms other than carbon and hydrogen outside the ring
- C08G65/16—Cyclic ethers having four or more ring atoms
- C08G65/20—Tetrahydrofuran
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/04—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers only
- C08G65/06—Cyclic ethers having no atoms other than carbon and hydrogen outside the ring
- C08G65/08—Saturated oxiranes
- C08G65/10—Saturated oxiranes characterised by the catalysts used
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
- C08G65/2642—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds characterised by the catalyst used
- C08G65/2645—Metals or compounds thereof, e.g. salts
- C08G65/2666—Hetero polyacids
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/30—Post-polymerisation treatment, e.g. recovery, purification, drying
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S502/00—Catalyst, solid sorbent, or support therefor: product or process of making
- Y10S502/515—Specific contaminant removal
Definitions
- the present invention relates to a method for producing a polymer of tetrahydrofuran (hereinafter referred to as THF) using a heteropolyacid as a catalyst.
- THF tetrahydrofuran
- the present invention relates to a THF polymer (a homopolymer or copolymer of THF) using a specific compound, that is, a heteropolyacid having a low content of Al, Cr and free phosphoric acid as a catalyst.
- the present invention relates to a method for producing a polyether glycol containing
- Polyether glycol is an industrially useful polymer used as a main raw material of polyurethane used for polyurethane elastic fiber (spandex) and synthetic leather, an additive for oil, a softener, and the like.
- US Pat. No. 4,673,723 describes a method for removing a heteropolyacid catalyst.
- the catalyst performance of the heteropolyacid may be different due to a difference in the production lot of the heteropolyacid.
- the reaction conversion of THF to a polymer and the molecular weight stability of the polymer differ depending on the production lot of the heteropolyacid.
- reaction conversion rate is low, a large amount of energy is consumed in the polymerization of THF, which is not economically preferable.
- the amount of the heteropolyacid catalyst remaining in the THF polymer is large, The F polymer is depolymerized, and the molecular weight of the THF polymer changes with time.
- An adsorbent or the like is used to remove the heteropolyacid catalyst remaining in the THF, but the breakthrough time of the adsorbent gradually decreases, so that the adsorbent needs to be frequently replaced. Therefore, this method is not preferable from the economic point of view and the increase of industrial waste.
- An object of the present invention is to provide a method for polymerizing THF using a high-performance heteropolyacid catalyst when producing a THF polymer using a heteropolyacid catalyst. It is another object of the present invention to provide a method for polymerizing THF using a heteropolyacid whose catalytic performance does not change even if the production lot of the heteropolyacid is different. It is a further object of the present invention to provide a method for polymerizing THF using a heptane polyacid catalyst having a high reaction conversion.
- Another object of the present invention is to provide a method for polymerizing THF using a heteropolyacid catalyst having a low ratio remaining in the THF polymer.
- the present invention is a method for producing a tetrahydrofuran polymer using a heteropolyacid catalyst, wherein the content of A1 in the heteropolyacid is 4 ppm or less.
- the present invention also provides a method for producing a tetrahydrofuran polymer using a heteropolyacid catalyst, wherein the heteropolyacid is a heteropolyphosphoric acid having a free phosphoric acid content of 1 mol% or less. .
- a reaction conversion rate is high and a THF polymer can be produced with high yield. Further, by lowering the Cr element content, it is possible to obtain a polymer of less than 50 in colorless APHA.
- the heteropolyacid used as a catalyst contains impurities such as various metal elements derived from gemstones. Things exist.
- Phosphoric acid is used in excess to stably produce heteropolyphosphoric acid, a type of heteropolyacid.
- the resulting heteropolyphosphate contains free phosphoric acid that does not contribute to the formation of a crystal structure that is effective as a polymerization catalyst for THF.
- the present inventors focused on the impurity metal element and free phosphoric acid in the heteropolyacid, studied the relationship between the content of the metal element and free phosphoric acid, and the catalytic performance, and reached the present invention. is there.
- the polymerized THF polymer contains or reacts with the inorganic acid salt to form a certain organometallic compound, which covers the surface of the heteropolyacid, The catalytic activity decreases, or (2) A1 dissolves in the heteropolyacid in some form, resulting in a strong interaction with THF and a K eggin structure that is effective as a polymerization catalyst. It is assumed to be due to the change to a weak Dawson structure and a decrease in the proportion of the K eggin structure.
- This problem can be solved by setting the content of A1 in the heteropoly acid to 4 ppm or less, and a stable and high reaction conversion rate can be realized.
- Solid heteropoly acids identify the polarity of the molecule and adsorb it to the surface of the heteropoly acid or incorporate the molecule into the heteropoly acid crystal. This property is also observed during the catalytic reaction, and it is considered that the ring-opening polymerization reaction of THF includes a reaction occurring on the heteropolyacid catalyst surface and a reaction involving the inside of the crystal (bulk reaction). The latter reaction is a phenomenon that cannot be seen in conventional solid catalyst reactions, and is one of the specific properties of heteropolyacid as a catalyst.
- the contribution of the bulk reaction Although large, it is presumed that when A1 as an impurity is present in an amount exceeding 4 ppm, A1 is mixed into the crystal structure of the heteropolyacid and inhibits the bulk reaction. Therefore, it is presumed that the coordination of THF to the heteropolyacid catalyst via water is inhibited, and as a result, the reaction conversion in the ring-opening polymerization of THF is reduced.
- the content of A1 in the heteropolyacid is 4 ppm or less, a stable and high value can be obtained for the reaction conversion in THF ring-opening polymerization. Therefore, the A1 content in the heteropolyacid is 4 ppm or less, preferably 2 ppm or less.
- the Cr content in the heteropolyacid is preferably low.
- the heteropolyacid is colored, and when used as a catalyst, the resulting polymer may be colored.
- the heteropoly acid When the Cr in the heteropoly acid is 1 ppm or less, the heteropoly acid is not colored, and the obtained THF polymer is transparent without being colored.
- the Cr content in the heteropolyacid is 1 ppm or less, preferably 0.8 ppm or less.
- an extraction method using ether is known.
- an excess amount of an aqueous solution of a mixture of alkali phosphate or phosphoric acid and allylic tungstate (or allylicolymolybdate) is added while heating and stirring.
- the heteropolyphosphoric acid is produced by extracting with ether and separating it from salts and inorganic acids.
- this production method there is no purification step, and the resulting heteropolyacid contains impurities.
- the heteropolyacid suitable as a THF polymerization catalyst used in the present invention can be produced by the above-mentioned production method or other known production methods using a raw material raw material having a small amount of impurities, or can be obtained by regenerating a heteropolyacid obtained by a known method. It can be produced by purification by a method such as crystallization.
- the content of 81 and 1 to 1 in the heteropolyacid can be measured by a known method such as a fluorescent X-ray method and an atomic absorption method.
- Another impurity that has a significant effect on the catalytic performance of heteropolyacids is Free phosphoric acid content in polyphosphoric acid.
- a heteropolyphosphoric acid having a free phosphoric acid content of 1 mol% or less as a catalyst, the catalyst remaining rate in the THF polymer can be reduced, and depolymerization of the THF polymer can be prevented. . If the amount of free phosphoric acid in the polyphosphoric acid exceeds 1 mol%, the solubility of heteropolyphosphoric acid in polyether glycol increases, and the amount of catalyst remaining in the resulting polyether daricol increases. To increase.
- polyether glycol may be exposed to high temperatures in the purification step or the dehydration step when supplying it as a reaction raw material, or if it is stored for a long time, the polymerization product of THF Depolymerization occurs. As a result, the molecular weight and the molecular weight distribution change, and the desired polyester glycol cannot be obtained.
- U.S. Pat.No. 4,677,231 discloses that THF is polymerized to obtain a mixture of polyester glycol and THF, which has a higher boiling point than THF, and It is described that heteropolyphosphoric acid used as a catalyst can be efficiently separated by adding a hydrocarbon having 15 or less carbon atoms or a halogenated hydrocarbon which does not form an azeotrope. By using this method, it is possible to efficiently separate a reaction product using a heteropolyphosphate having a free phosphoric acid content of 1 mol% or less as a polymerization catalyst for THF.
- the hydrocarbon or halogenated hydrocarbon having 15 or less carbon atoms to be used includes, for example, n-heptane, octane, nonane, decane, pendecane, dodecane, cyclooctane, 1-chloro Examples include octane, chlorocyclohexane, and toluene.
- solvents such as heteropolyacids such as n-heptane, octane, nonane, decane, pendecane and dodecane are preferred because of their high ability to precipitate heteropolyacids.
- a solvent having 16 or more carbon atoms has a high boiling point and is difficult to separate and recover from polyether glycol, which is not preferable.
- the amount of the solvent used for separating and separating the heteropolyphosphoric acid varies depending on the amount of coexisting THF, but is usually from 1 to 50 times by weight, preferably from 2 to 20 times by weight of THF.
- an amount necessary to cause phase separation between the polyetherdiolicol and the solvent is added.
- the amount is 0.5 to 50 times by weight, preferably 1.0 times the weight of the polyether glycol. Use at 0 to 20 times the weight.
- a phase containing ether glycol Separate into a phase containing ether glycol.
- the temperature for mixing and phase separation (catalyst deposition) is within the temperature range where the polyether glycol does not solidify.
- Coalescer, hydrocyclone, centrifuge or filter filtration can be used to reduce the time required for phase separation.
- the solubility of the heteropolyphosphoric acid in the THF polymer is suppressed to a low level when used as a polymerization catalyst for THF.
- the polyphosphoric acid can be efficiently removed from the polymerization product.
- heteropolyphosphoric acid having a free phosphoric acid content of 1 mol% or less, an A1 content of 4 ppm or less, and a Cr content of 1 ppm or less as a catalyst.
- the heteropolyphosphoric acid suitable as a THF polymerization catalyst used in the present invention can be obtained by purifying a heteropolyphosphoric acid obtained by a known method by a method such as recrystallization.
- polyether glycol can be produced by homopolymerizing THF or using a cyclic ether or diol copolymerizable with THF as a comonomer.
- comonomers include oxetanes and oxetane derivatives, for example, cyclic ethers such as 3,3-dimethyloxetane, methyltetrahydrofuran, 1,3-dioxolane, tetrahydropyran, and / or ethylene glycol, propylene glycol, 1 1,3-butanediol, 1,5-pentanedionole, 1,6-hexanediol, neopentinoleglycol / le, diethylene glycol, dipropylene glycol, etc. Can be.
- cyclic ethers such as 3,3-dimethyloxetane, methyltetrahydrofuran, 1,3-dioxolane, tetrahydropyran, and / or ethylene glycol, propylene glycol, 1 1,3-butanediol, 1,5-pentanedionole, 1,6-hex
- the heteropolyacid used in the present invention comprises at least one oxide selected from the group consisting of Mo, W, and V, and an oxyacid of another element (eg, P, As, Ge, etc.). It is a general term for oxyacids formed by bonding, and preferably has an atomic ratio of the former to the latter of 2.5 to 12.
- heteropolyacids include heteropolyphosphoric acid such as phosphomolybdic acid, phosphotandastanoic acid, phosphomolybdotungstic acid, phosphomolybdovanadic acid, phosphomolybdo tangstovanadic acid, phosphotan dust vanadic acid, and phosphomolybdniobate. Acids, and germanium tungstic acid, arsenic molybdic acid, arsenic tandastanoic acid, and the like.
- the amount of the heteropoly acid used is not particularly limited, but if the amount of the heteropoly acid in the reaction system is small, the polymerization rate is low. Therefore, the amount is preferably 0.1 to 20 times, more preferably 0.5 to 5 times the weight of the monomer.
- the polymerization temperature of THF is high, the degree of polymerization tends to decrease due to depolymerization of the polymer.
- the polymerization temperature is preferably from 0 to 150 ° C, more preferably from 30 to 80 ° C.
- the reaction time varies depending on the amount of the catalyst and the reaction temperature, but is usually 0.5 to 20 hours.
- a solvent is not particularly required, but if necessary, an inert solvent may be added to the reaction.
- an inert solvent may be added to the reaction.
- a 300 ml container equipped with a stirrer and a reflux condenser was charged with 200 g of THF having a water content of 300 ppm, and heated in an electric furnace at 180 ° C to adjust the number of coordinated water. 100 g of telopolyacid were added. Table 1 shows the A1 content, Cr content, and free phosphoric acid content in this heteropolyacid. A 1 and C r content in X-ray fluorescence, in the free phosphoric acid is 3 1 P- NMR, were measured using a phosphoric acid Natoriumu as external standard. The reaction temperature was set to 60 ° C., and stirring was continued for 4 hours, and then the mixture was allowed to stand still at room temperature to separate a lower catalyst phase.
- THF was polymerized in the same manner as in Example 1 using phosphatic acid having an A1 content and a Cr content exceeding 4 ppm and 1 ppm, respectively.
- Table 1 summarizes the number average molecular weight, reaction conversion, and hue (APHA) of PTMG obtained at this time.
- Example 2 As in Example 1, 200 g of THF having a water content of 300 ppm was charged into a 300 ml vessel equipped with a stirrer and a reflux condenser, and heated in an electric furnace at 180 ° C. 100 g of the adjusted number of heteropolyphosphates was added. Table 2 shows the A1 content, the amount of free phosphoric acid, and the number of coordinated water in the heteropolyphosphate. After the reaction temperature was set to 60 and stirring was continued for 5 hours, the mixture was allowed to stand at room temperature and the lower catalyst phase was separated.
- Table 2 also shows the number average molecular weight (M n) and the reaction conversion obtained from the OH value measurement of the obtained PTMG.
- THF was polymerized in the same manner as in Example 6.
- the inlet pressure of the filtration increased 15 times in about 5 hours.
- the filtrate was a clear liquid, but the residual catalyst was as high as 50 ppm or more as shown in Table 1.
- the pore size of the filter was set to 1 ⁇ m, almost no pressure increase was observed, but the filtrate was not transparent and slightly turbid.
- the present invention is useful for production of polyether glycol used as a main raw material of polyurethane used for polyurethane elastic fiber (spandex) and synthetic leather, an additive for oil, a softener, and the like.
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyethers (AREA)
- Catalysts (AREA)
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE69920374T DE69920374T2 (de) | 1998-06-15 | 1999-06-09 | Verfahren zur herstellung von polytetrahydrofuran |
KR1020007001429A KR100358552B1 (ko) | 1998-06-15 | 1999-06-09 | 테트라히드로푸란 중합체의 제조 방법 |
EP99923980A EP1004610B1 (en) | 1998-06-15 | 1999-06-09 | Process for producing tetrahydrofuran polymer |
US09/502,485 US6414109B1 (en) | 1998-06-15 | 2000-02-11 | Process for producing tetrahydrofuran polymer |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP10/181351 | 1998-06-15 | ||
JP18135198A JP4831851B2 (ja) | 1998-06-15 | 1998-06-15 | ヘテロポリ酸を触媒としたthf重合体の製造方法 |
JP18329598A JP4831852B2 (ja) | 1998-06-16 | 1998-06-16 | ヘテロポリリン酸を触媒としてthf重合体を製造する方法 |
JP10/183295 | 1998-06-16 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/502,485 Continuation-In-Part US6414109B1 (en) | 1998-06-15 | 2000-02-11 | Process for producing tetrahydrofuran polymer |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1999065968A1 true WO1999065968A1 (fr) | 1999-12-23 |
Family
ID=26500580
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1999/003081 WO1999065968A1 (fr) | 1998-06-15 | 1999-06-09 | Procede de production d'un polymere de tetrahydrofuranne |
Country Status (7)
Country | Link |
---|---|
US (1) | US6414109B1 (ja) |
EP (1) | EP1004610B1 (ja) |
KR (1) | KR100358552B1 (ja) |
CN (1) | CN1105133C (ja) |
DE (1) | DE69920374T2 (ja) |
TW (1) | TW444032B (ja) |
WO (1) | WO1999065968A1 (ja) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB9828020D0 (en) * | 1998-12-18 | 1999-02-10 | Bp Chem Int Ltd | Synthesis of heteropolyacids |
DE10314648A1 (de) * | 2003-04-01 | 2004-10-14 | Basf Ag | Verfahren zur Herstellung von Tetrahydrofuran-Copolymeren |
DE102004012116A1 (de) * | 2004-03-12 | 2005-09-22 | Basf Ag | Verfahren zur Herstellung von Polytetrahydrofuran oder Tetrahydrofuran-Copolymeren |
KR100841603B1 (ko) * | 2007-02-16 | 2008-06-26 | 주식회사 효성 | 테트라히드로푸란 중합체의 제조방법 |
KR100824979B1 (ko) | 2007-02-16 | 2008-04-28 | 주식회사 효성 | 테트라히드로푸란 중합체의 제조방법 |
US11542442B1 (en) * | 2022-04-05 | 2023-01-03 | Saudi Arabian Oil Company | Hydrocracking process and system including separation of heavy poly nuclear aromatics from recycle with heteropoly acids |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS61123627A (ja) * | 1984-11-19 | 1986-06-11 | Asahi Chem Ind Co Ltd | ポリテトラメチレングリコ−ルの製法 |
JPH02196011A (ja) * | 1988-12-05 | 1990-08-02 | Sun Refining & Marketing Co | ヘテロポリ酸触媒の製造方法 |
JPH0570586A (ja) * | 1991-03-13 | 1993-03-23 | Basf Ag | ポリオキシアルキレングリコールの製造方法 |
JPH0741533A (ja) * | 1993-07-29 | 1995-02-10 | Nippon Shokubai Co Ltd | 高分子量ポリジオキソランの製法 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5452025A (en) * | 1977-09-28 | 1979-04-24 | Tokuyama Soda Co Ltd | Preparation of ester |
US4522934A (en) * | 1981-04-27 | 1985-06-11 | Atlantic Richfield Company | Vanadotungstomolybdophosphoric acid oxidation catalyst |
CA1216597A (en) | 1983-05-23 | 1987-01-13 | Atsushi Aoshima | Process for producing polyetherglycol |
US4658065A (en) | 1984-03-28 | 1987-04-14 | Asahi Kasei Kogyo Kabushiki Kaisha | Process for producing polyether polyol and a product |
CA1268481A (en) | 1984-11-13 | 1990-05-01 | Atsushi Aoshima | Process for purification of polyether |
EP0675146B1 (en) | 1993-07-29 | 2000-05-31 | Nippon Shokubai Co., Ltd. | High-molecular-weight polydioxolane and process for producing the same |
US5756604A (en) * | 1995-08-31 | 1998-05-26 | Hodogaya Chemical Co., Ltd. | Process for producing polyether, and process for recycling and reusing herteropolyacid |
JP3037612B2 (ja) * | 1996-04-12 | 2000-04-24 | ポリプラスチックス株式会社 | ポリアセタール共重合体の製造方法 |
-
1999
- 1999-06-08 TW TW088109557A patent/TW444032B/zh not_active IP Right Cessation
- 1999-06-09 EP EP99923980A patent/EP1004610B1/en not_active Expired - Lifetime
- 1999-06-09 KR KR1020007001429A patent/KR100358552B1/ko not_active IP Right Cessation
- 1999-06-09 CN CN99800941A patent/CN1105133C/zh not_active Expired - Lifetime
- 1999-06-09 WO PCT/JP1999/003081 patent/WO1999065968A1/ja active IP Right Grant
- 1999-06-09 DE DE69920374T patent/DE69920374T2/de not_active Expired - Lifetime
-
2000
- 2000-02-11 US US09/502,485 patent/US6414109B1/en not_active Expired - Lifetime
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS61123627A (ja) * | 1984-11-19 | 1986-06-11 | Asahi Chem Ind Co Ltd | ポリテトラメチレングリコ−ルの製法 |
JPH02196011A (ja) * | 1988-12-05 | 1990-08-02 | Sun Refining & Marketing Co | ヘテロポリ酸触媒の製造方法 |
JPH0570586A (ja) * | 1991-03-13 | 1993-03-23 | Basf Ag | ポリオキシアルキレングリコールの製造方法 |
JPH0741533A (ja) * | 1993-07-29 | 1995-02-10 | Nippon Shokubai Co Ltd | 高分子量ポリジオキソランの製法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP1004610A4 * |
Also Published As
Publication number | Publication date |
---|---|
EP1004610A4 (en) | 2003-06-04 |
DE69920374T2 (de) | 2005-06-30 |
CN1272856A (zh) | 2000-11-08 |
TW444032B (en) | 2001-07-01 |
KR100358552B1 (ko) | 2002-10-25 |
EP1004610A1 (en) | 2000-05-31 |
CN1105133C (zh) | 2003-04-09 |
US6414109B1 (en) | 2002-07-02 |
DE69920374D1 (de) | 2004-10-28 |
KR20010022827A (ko) | 2001-03-26 |
EP1004610B1 (en) | 2004-09-22 |
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