Process for preparing 1,3-alkanediol from epoxide derivative

Abstract: The present invention relates to a process for preparing 1,3-alkanediol through carbonylation of an epoxide derivative, which comprises (a) reacting an epoxide derivative with alcohol and carbon monoxide in a solvent at a temperature of from 30 to 150 °C and at a pressure of from 50 to 3000 psig under the catalyst system consisting of an effective amount of a cobalt catalyst and an effective amount of a promoter to convert 3-hydroxyester and derivatives thereof in an amount of from 2 to 95 % by weight, (b) separating said reaction product and solvent from the catalyst and promoter, (c) reacting said reaction product and solvent with hydrogen at a temperature of from 30 to 350°C and at a pressure of from 50 to 5000 psig under a catalyst system for hydrogenation to prepare a hydrogenation product mixture including 1,3-alkandiol, and (d) recovering 1,3-alkandiol from the hydrogenation product mixture.

Description: Field of the Invention The present invention relates to a process for preparing a 1,3-alkanediol through carbonylation of an epoxide derivative. More specifically, the present invention relates to a process for preparing 1,3-alkanediol, which comprises reacting an epoxide derivative with alcohol and carbon monoxide under the catalyst system consisting of a cobalt catalyst and a promoter to convert 3-hydroxyester, and adding hydrogen to the3-hydroxyester to prepare 1,3-alkanediol. Background of the Invention An epoxide derivative can be easily converted into a difunctional compounds through carbonylation, which is used as an intermediate for preparing an organic compound. In particular, as 3-hydroxyester derivative has two functional groups, it is used as solvents, resins, coating materials, materials for medical substances, an intermediate for preparing alkanediol which is used for preparing polyester, etc. The alkanediol is used as an intermediate for coating materials or synthetic organic compounds. 1,3-diol is a representative of alkandiol. As shown in the following scheme, 1,3-diol is prepared by hydroformylating an epoxide derivative to prepare 3-hydroxyaldehyde derivative and adding hydrogen to the 3-hydroxyaldehyde derivative to convert the aldehyde groups into alcohol groups. The scheme for preparing 1,3-diol above was disclosed in U.S. Patent Nos. 5,770,776, 5,723,389 and 5,731,478. On the other hand, in a known process for synthesizing 3-hydroxyaldehyde showing a high selectivity under a low temperature and a low pressure, there are used a cobalt catalyst and phosphine oxide ligand as a promoter. However, when phosphine oxide ligand is used as a promoter, the recovery and regeneration of the catalyst become complicated. U.S. Patent No. 5,770,776 discloses a process for preparing 1,3-propanediol comprising the steps of (a) contacting ethylene oxide with carbon monoxide and hydrogen in a non-water-miscible solvent in the presence of an effective amount of a non-phosphine-ligated cobalt catalyst and an effective amount of a catalyst promoter. (b) adding an aqueous liquid to said intermediate product mixture and extracting into said aqueous liquid a major portion of the 3-hydroxypropanal so as to provide a first aqueous phase and a first organic phase, (c) separating the first aqueous phase from the first organic phase, (d) adding fresh non-water-miscible solvent to the first aqueous phase and extracting into such solvent a portion of any cobalt catalyst or cobalt-containing derivative thereof present in such aqueous phase, to provide asecond aqueous phase and a second organic phase, (e) separating the second aqueous phase from the second organic phase, (f) passing the first organic phase and the second organic phase to the process step (a), (g) contacting the second aqueous phase with hydrogen, and (h) recovering 1.3-propanediol. U.S. Patent Nos. 5,723,389 and 5,731,478 disclose a process for preparing an alkanediol comprising the steps of (a) contacting an ethylene oxide with carbon monoxide and hydrogen in a non-water-miscible solvent in the presence of an effective amount of a non-phosphine-ligated cobalt or rhodium catalyst and an effective amount of a cobalt or rhodium porphyrin promoter, (b) adding an aqueous liquid to said intermediate product mixture and extracting into said aqueous liquid a major portion of the hydroxyaldehyde so as to provide an aqueous phase and an organic phase, (c) separating the aqueous phase from the organic phase, (d) contacting the aqueous phase with hydrogen in the presence of a hydrogenation catalyst, and (e) recovering the alkanediol. U.S. Patent Nos. 5,135,901 and 4,973,741 disclose another process for obtaining the 3-hydroxyester derivative from the epoxide derivatives. In this process, there is synthesized methyl 3-hydroxypropionate from ethylene oxide by using rhodium and ruthenium as catalysts in the presence of carbon monoxide and alcohol. However, in this process, in spite of the use of expensive catalysts, the yield of the 3-hydroxypropionate is as low as 60%, and by-products are produced in considerable amounts. Further, there is another known process for obtaining a 3-hydroxyester by hydroesterification of the epoxide. In this process also, the yield is as low as 40-60% [(1) Dalcanali, E.; Foa, M. Synthesis 1986, 492. (2) Heck, R. F., J. Am. Chem. Soc., 1963, 85, 1460. (3) Eismann, J. L.; Yamartino, R. L.; Howard, Jr. J. F., J. Org. Chem. 1961, 2102.]. The reason why the yield is so low is that the isomerization reaction of the starting material readily occurs. Meanwhile, U.S. Patent Nos. 5,310,948 and 5,359,081 relate to a carbonylation of the epoxide, in which the epoxide and carbon monoxide are reacted in the presence of cobalt and pyridine derivatives. The final product is mainly β -lacton, and the by-product is the 3-hydroxyester. In preparation of 1,3-alkanediol for preparing polyester, if 3-hydroxyaldehyde is used as intermediate, the quality of polyester becomes lower because of formation of oligomers and acetals as by-products. On the other hand, if 3-hydroxyester is used as intermediate, a lower yield and a high cost of catalyst will arise. An effective catalyst system for preparing a 3-hydroxyester derivative from an ethylene oxide through hydroesterification has not been developed yet, and a method of obtaining 1,3-alkanediol in a high yield has not been developed yet. Accordingly, the present inventors have developed a process for preparing 1,3-alkanediol in a high yield by synthesizing 3-hydroxyester as an intermediate from an epoxide derivative through hydroesterification and reacting the 3-hydroxyester with hydrogen and a catalyst system for the hydroesterification. Objects of the Invention An object of the present invention is to provide a novel process for preparing 1,3-alkanediol, which comprises reacting an epoxide derivative with alcohol and carbon monoxide under the catalyst system consisting of a cobalt catalyst and a promoter to convert 3-hydroxyester, and adding hydrogen to the3-hydroxyester to prepare 1,3-alkanediol. Another object of the invention is to provide a new catalyst system for preparing 3-hydroxyester in a high yield by reacting an epoxide derivative with alcohol and carbon monoxide, which consists of a cobalt catalyst and an imidazole or a derivative thereof as promoter. A further object of the invention is to provide a process for preparing 1,3-alkanediol using a new catalyst system for preparing 3-hydroxyester in a high yield by reacting an epoxide derivative with alcohol and carbon monoxide, which consists of a cobalt catalyst and an imidazole or a derivative thereof as promoter. A further object of the invention is to provide a process for preparing 1,3-alkanediol in a lower cost by using an imidazole or a derivative thereof as promoter. In achieving the above objects, the present invention is characterized as follows. Summary of the Invention The present invention relates to a process for preparing 1,3-alkanediol through carbonylation of an epoxide derivative, which comprises (a) reacting an epoxide derivative with alcohol and carbon monoxide in a solvent at a temperature of from 30 to 150 °C and at a pressure of from 50 to 3000 psig (446 to 20786 kPa (absolute)) under the catalyst system consisting of an effective amount of a cobalt catalyst and an effective amount of a promoter selected from imidazole, pyrrole, pyrazine, pyrimidine, derivatives thereof and mixtures thereof to convert 3-hydroxyester and derivatives thereof in an amount of from 2 to 95% by weight, (b) separating said reaction product and solvent from the catalyst and promoter, (c) reacting said reaction product and solvent with hydrogen at a temperature of from 30 to 350 °C and at a pressure of from 50 to 5000 psig (446 to 34576 kPa (absolute)) under a catalyst system for hydrogenation to prepare a hydrogenation product mixture including 1,3-alkandiol, and (d) recovering 1,3-alkandiol from the hydrogenation product mixture. Detailed Description of the Invention The present invention relates to a process for preparing 1,3-alkanediol through carbonylation of an epoxide derivative. An epoxide derivative reacts with alcohol and carbon monoxide in a solvent at a temperature of from 30 to 150 °C and at a pressure of from 50 to 3000 psig (446 to 20786 kPa (absolute)) under the catalyst system consisting of an effective amount of a cobalt catalyst and an effective amount of a promoter selected from imidazole, pyrrole, pyrazine, pyrimidine, derivatives thereof and mixtures thereof to convert 3-hydroxyester and derivatives thereof. In this invention, this step is called as "hydroesterification". The reaction product and solvent is separated from the catalyst and promoter. The reaction product and solvent reacts with hydrogen at a temperature of from 30 to 350 C and at a pressure of from 50 to 5000 psig (446 to 34576 kPa (absolute)) under a catalyst system for hydrogenation to prepare a hydrogenation product mixture including 1,3-alkandiol. In this invention, this step is called as "hydrogenation". 1,3-allcandiol is recovered from the hydrogenation product mixture. In the present invention, an effective catalyst system is employed to maximize the production yield of 3-hydroxyester when an epoxide derivative carries out hydroesterification. The catalyst system consists of a cobalt catalyst and a catalyst promoter. A representative example of the cobalt catalyst is Co 2 (CO) 8 . The cobalt catalyst may be a compound of Co 2 (CO) 8 and an organic compound selected from the group consisting of imidazole, pyrrole, pyrazine, pyrimidine, a derivative thereof, and a mixture thereof. It is preferable to use an organic compound which is not bonded to a phosphine compound. It is preferable to use the cobalt catalyst and promoter at a ratio of up to 1 : 100. In the present invention, it is also preferable to use an imidazole derivative as a promoter as shown in the following formula (I): wherein R 15 , R 16 , and R 17 are independently hydrogen; branched aliphatic hydrocarbon having up to 10 carbon atoms; linear aliphatic hydrocarbon having up to 10 carbon atoms; saturated cyclohydrocarbon having up to 10 carbon atoms; cycloaliphatic hydrocarbon having up to 10 carbon atoms; aromatic aliphatic hydrocarbon having up to 10 carbon atoms; F; Cl; alkoxy of C 1-3 ; OH; OH group-containing branched aliphatic hydrocarbon having up to 10 carbon atoms; OH group-containing linear aliphatic hydrocarbon having up to 10 carbon atoms; OH group-containing saturated cyclohydrocarbon having up to 10 carbon atoms; OH group-containing cycloaliphatic hydrocarbon having up to 10 carbon atoms; or OH group-containing aromatic aliphatic hydrocarbon having up to 10 carbon atoms. An appropriate solvent is used in the hydroesterification in the presence of alcohol. The hydroesterification is carried out at a temperature of from 30 to 150 °C, preferably from 40 to 120 °C and at the CO pressure of from 50 to 3000 psig (446 to 34576 kPa (absolute). preferably from 100 to 1500 psig (790 to 10444 kPa (absolute)) The epoxide derivative usable in this invention is shown as the following formula (II): wherein R, and R, are independently hydrogen; linear aliphatic hydrocarbon having up to 20 carbon atoms; branched aliphatic hydrocarbon having up to 20 carbon atoms; saturated cycloaliphatic hydrocarbon having up to 20 carbon atoms; cycloaliphatic hydrocarbon having up to 20 carbon atoms; aromatic aliphatic hydrocarbon having up to 20 carbon atoms; hydrocarbon having up to 20 carbon atoms substituted hydrogen on the carbon chain for F or Cl or Br; aromatic hydrocarbon having up to 20 carbon atoms with no substituted group or aromatic hydrocarbon having up to 20 carbon atoms substituted hydrogen on the aromatic ring for F, Cl, amine group, nitrile group, or alkoxy group. The desirable examples of the epoxide derivatives include ethylene oxide, propylene oxide, 1-butene oxide, 1-pentene oxide, 1-heptene oxide, 1-octene oxide, 1-nonene oxide, 1-decene oxide, 2-methyl-propylene oxide, 2-methyl-1-butene oxide, 2-methyl-1-octene oxide, 2-methyl-nonene oxide, 2-methyl-1-decene oxide, 2-methyl-1-butene oxide, 2-methyl-1-pentene oxide, 2-methyl-1-hexene oxide, 2-ethyl-1-heptene oxide, 2-ethyl-1-octene oxide, 2-ethyl-1-nonene oxide, 2-ethyl-1-decene oxide, epifluorohydrin, epichlrorohydrin, epibromohydrin, glycidol, methyl gltcidate, ethyl glycidate, t-butyl glycidate, allyl benzene oxide, styrene oxide, etc. The alcohol of the present invention is expressed by R'OH. Here, R' is a a saturated linear hydrocarbon having up to 20 carbon atoms, an unsaturated linear hydrocarbon having up to 20 carbon atoms; a hydrocarbon having up to 20 carbon atoms having branches, a cyclohydrocarbon having up to 20 carbon atoms, an aromatic hydrocarbon having up to 20 carbon atoms, or a linear hydrocarbon including an aromatic group. Preferably R' is methyl, ethyl, isopropyl, cyclohexyl, phenyl or benzyl. The solvent of the present invention may be an ether, a substituted aromatic compound, or an acetate. Of course, the alcohol itself may be used as a solvent. The ether available in this invention is represented as the following formula (III), (IV) or (V): R 3 ―O―R 4 wherein R 3 , R 4 , R 5 , R 6 , and R 7 are saturated aliphatic hydrocarbon having up to 10 carbon atoms; having no branches; branched aliphatic hydrocarbon having up to 10 carbon atoms; saturated cyclohydrocarbon having up to 10 carbon atoms; cycloaliphatic hydrocarbon having up to 10 carbon atoms; or aromatic aliphatic hydrocarbon having up to 10 carbon atoms; m is an integer of 1 to 10; and n is an integer of 2 to 5. The substituted aromatic compound available in this invention is represented as the following formula (VI): where R 8 , R 9 , R 10 , R 11 , R 12 and R 13 are hydrogen; saturated aliphatic hydrocarbon of C 1-4 having no branches; branched aliphatic hydrocarbon of C 1-4 ; F; Cl; or alkoxy group of C 1∼3 . 3-hydroxyester and derivatives thereof are obtained through hydroesterification of the epoxide derivative. The 3-hydroxyester and derivatives thereof according to the present invention are represented by the following formula (VII) or (VIII): wherein R 1 and R 2 are hydrogen; linear aliphatic hydrocarbon having up to 20 carbon atoms; branched aliphatic hydrocarbon having up to 20 carbon atoms; saturated cycloaliphatic hydrocarbon having up to 20 carbon atoms; cycloaliphatic hydrocarbon having up to 20 carbon atoms; aromatic aliphatic hydrocarbon having up to 20 carbon atoms; hydrocarbon having up to 20 carbon atoms substituted hydrogen on the carbon chain for F or Cl or Br; aromatic hydrocarbon having up to 20 carbon atoms with no substituted group; or aromatic hydrocarbon having up to 20 carbon atoms substituted hydrogen on the aromatic ring for F, Cl, amine group, nitrile group, or alkoxy group, and R' is a saturated linear hydrocarbon having up to 20 carbon atoms, an unsaturated linear hydrocarbon having up to 20 carbon atoms, a hydrocarbon having up to 20 carbon atoms having branches, a cyclohydrocarbon having up to 20 carbon atoms, an aromatic hydrocarbon of having up to 20 carbon atoms, or a linear hydrocarbon including an aromatic group. As shown in formulae (VII) and (VIII), the 3-hydroxyester and derivatives thereof are difunctional so as to be available for an intermediate for synthesizing an organic compound or for a coating material. The reaction product and solvent is separated from the catalyst and promoter. The separation of the reaction product and solvent is carried out by vacuum distillation or by extracting into water, which will depend on the solvent. When an ether of Formula (III) or a substituted aromatic compound of Formula (IV) is used as solvent, the reaction product of 3-hydroxyester derivative is extracted into water. When an ether of Formula (IV) or (V) or a lower alcohol such as methyl alcohol, ethyl alcohol and isopropyl alcohol is used as solvent, the reaction product is separated under vacuum distillation. When a higher alcohol than isopropyl alcohol is used as solvent, the reaction product is separated by extracting into water. When extracting into water, 3-hydroxyester and derivatives thereof are extracted into the water layer by adding water of 100 °C or lower to the reaction production mixture in the presence of carbon monoxide at a pressure of from 20 to 3000 psig (239 to 20786 kPa (absolute). The extracts react with hydrogen at a temperature of from 30 to 350 °C and at a pressure of from 50 to 5000 psig (446 to 34576 kPa (absolute)) under a catalyst system for hydrogenation to prepare a hydrogenation product mixture including 1,3-alkandiol. In this invention, this step is called as "hydrogenation". The hydrogenation can be carried out without extraction of the reaction product. The separated catalyst and promoter can be recycled to the hydroesterification in partial or in total. The 3-hydroxyester derivative is hydrogenated under a catalyst system to produce 1,3-alkanediol. The catalyst system comprises copper chromate or Pd/C. The hydrogenation process is carried out at the temperature of from 50 to 250 °C and at the pressure of from 200 to 3000 psig (1480 to 20786 kPa (absolute)). Finally, 1,3-alkandiol is recovered from the hydrogenation product mixture. The separation and hydrogenation of the reaction product and the hydrogenation can be easily carried out by an ordinary skilled person in the art to which the present invention pertains. The present invention will be more thoroughly understood by the below described actual examples. These examples are not intended to limit the scope of the present invention, but are just for specifically presenting the present invention to help understanding the present invention. Examples Examples 1-10: Hydroesterification of Ethylene Oxide with Catalyst of Co 2 (CO) 8 in Imidazole At room temperature, a 450 ml Parr reactor was filled with a solvent and 5 mmole of Co 2 (CO) 8 . The reactor was filled with CO gas at 500 psig (3549 kPa (absolute)), heated to 80 °C and agitated for one hour. Then the reactor was cooled to room temperature and imidazole as promoter was added to the reactor. Ethylene oxide was added to the reactor and CO was added at a predetermined pressure. The reactor was heated to a temperature as shown in Table 1 at a pressure as in Table 1 for the time as in Table 1. During reaction, the reaction product was sampled using a tube. As product, methyl 3-hydroxypropionate (3-HPM) was analyzed with a GC. The reaction conditions and the resulting data are shown in Table 1. Imidazole of 20 mmole as promoter was used in Examples 1-7 and 9, 40 mmole in Example 8, and 30 mmole in Example 10. Ethylene oxide of 500 mmole was used in Examples 1-8 and 10, and 1.4 mmole in Example 9. In Example 7, tetraglyme was used besides methyl alcohol. Example Temp. (°C) Pressure (bar) (kPa) Time (hrs) MeOH (ml) Conversion Rate(%) Yield (%) Selectivity(mole%) 3-HPM 3-HPM AA DMA ME Dimer 1 70 34 (3400) 3 200 78.09 65.66 84.08 2.71 9.44 1.10 2.66 2 70 50 (5000) 3 200 68.23 59.68 87.47 7.77 0.20 2.38 2.17 3 70 80 (8000) 3 200 65.66 58.65 89.33 4.50 0.59 2.47 3.11 4 60 50 (5000) 3 200 45.19 40.20 88.96 8.45 0.39 2.19 0 5 75 50 (5000) 3 200 78.62 66.01 83.97 0.03 10.98 1.92 3.10 6 80 50 (5000) 3 200 91.61 71.86 78.45 9.44 6.51 2.63 2.97 7 80 34 (3400) 2 100 - 82.44 - - - - - 8 80 34 (3400) 4 250 - 70.1 - - - - - 9 80 34 (3400) 4 200 - 66.4 - - - - - 10 75 60 (6000) 3 150 95.27 88.90 93.31 1.78 0.32 0.98 3.61 Comparative Examples 1-2: Hydroesterification of Ethylene Oxide with Catalyst of Co 2 (CO) 8 Comparative Example 1 was conducted in the same manner as in Example 1 except that 4 mmole of 3-hydroxypyridine was used as promoter instead of imidazole and except the reaction conditions. 1 mmole of Co 2 (CO) 8 was used and 200 mmole of ethylene oxide was used. The reaction conditions of Comparative Example 1 were shown in Table 2. Comparative Example 2 was conducted in the same manner as in Example 1 except that Co 2 (CO) 8 as catalyst was used without any catalyst promoter. 2.5 mmole of Co 2 (CO) 8 was used and 650 mmole of ethylene oxide was used.The reaction conditions of Comparative Example 2 were shown in Table 2. the resulting data were shown in Table 2. In Comparative Example 1 using a pyridine derivative, 3-HPM was obtained in a high yield, but by-products such as acetaldehyde was produced in a significant amount. In Comparative Example 2 not using a catalyst promoter, the yield of 3-HPM was very low. Comparative Example Temp (°C) Pressure (bar) (kPa) Time (hrs) MeOH (ml) Conversion Rate(%) Yield (%) Selectivity(mole%) 3-HPM 3-HPM AA DMA ME Dimer 1 75 60 (6000) 4 40 92.07 81.08 88.07 8.43 - 2.28 1.22 2 75 60 (6000) 4 120 - 20.6 - - - - - Examples 11-14 Examples 11-14 were conducted in the same manner as in Example 1 except the epoxide derivative. As shown in Table 3, in Examples 11-14, propylcne oxide, butylenes oxide, epichlorohydrin, and glycidol as epoxide derivative were used, respectively. 5 mmole of Co 2 (CO) 8 , 10 mmole of catalyst promoter, 500 mmole of epoxide derivative, and 200 ml of ethyl alcohol as solvent was used. The reactor was kept at 80 °C and at 34 bar (3400 kPa) for 4 hours. The products and yields of Examples 11-14 were shown in Table 3. Example Epoxide Product Yield(%) 1 propylene oxide- methyl 3-hydroxybutanoate 60.56 2 butylene oxide methyl 3-hydroxypentanoate 53.70 3 epichlorohydrin methyl 3-hydroxy4-chlorobutanoate 66.17 4 glycidol 3-hydroxy γ -butyrolacton 62.50 Example 15 To a 45 ml Parr reactor were 1 g of 3-hydroxy propionate and 10 ml of methyl alcohol added to dissolve the 3-hydroxy propionate. To the reactor was 0.5 g of copper chromate as catalyst added. Hydrogen was introduced to the reactor at 1500 psig (34576 kPa (absolute) and the reactor was agitated and heated to 180 °C. After reaction for 15 hours, the reactor was cooled to room temperature. The product was analyzed with a GC. Conversion rate to 3-hydroxy propionate was about 5 %, and selectivity to 1,3-propandiol was about 3 %. The present invention has an effect to provide a novel process for preparing 1,3-alkanediol, in which 3-hydroxyester is prepared in a high yield by reacting an epoxide derivative with alcohol and carbon monoxide under a catalyst system consisting of a cobalt catalyst and an imidazole or a derivative thereof as promoter. Further, the present invention has an effect to provide a process for preparing 1,3-alkanediol in a lower cost by using an imidazole or a derivative thereof as promoter.

Claims: A process for preparing 1,3-alkanediol through carbonylation of an epoxide derivative, which comprises: (a) reacting an expoxide derivative with alcohol and carbon monoxide in a solvent at a temperature of from 30 to 150 °C and at a pressure of from 50 to 3000 psig (446 to 20786 kPa(absolute)) under the catalyst system consisting of an effective amount of a cobalt catalyst and an effective amount of promoter selected from imidazole, pyrrole, pyrazine, pyrimidine, derivates thereof and mixtures thereof to convert 3-hydroxyester and derivatives thereof; (b) separating said reaction product and solvent from the catalyst and promoter; (c) reacting said reaction product and solvent with hydrogen at a temperature of from 30 to 350 °C and at a pressure of from 50 to 5000 psig (446 to 34576 kPa(absolute)) under a catalyst system for hydrogenation to prepare a hydrogenation product mixture including 1,3-alkandiol; and (d) recovering 1,3-alkandiol from the hydrogenation product mixture. The process as claimed in Claim 1, wherein said separating step (b) is conducted under vacuum distillation. The process as claimed in Claim 1, wherein said separating step (b) is conducted by extracting 3-hydroxyester and derivatives thereof into a water layer by adding water at a temperature of 100°C or lower to the reaction production mixture in the presence of carbon monoxide at a pressure of from 20 to 3000 psig (239 to 20786 kPa(absolute)). The process as claimed in any of Claims 1 to 3, wherein said catalyst and promoter are recycled to the step (a) for hydroesterification in partial or in total. The process as claimed in any of Claims 1 to 4, wherein said cobalt catalyst is Co 2 (CO) 8 . The process as claimed in any of Claims 1 to 5, wherein said cobalt catalyst and promoter are employed at a ratio of up to 1:100. The process as claimed in any of Claims 1 to 6, wherein said promoter is an imidazole derivative represented by the following formula (I): wherein R 15 , R 16 , and R 17 are independently hydrogen; branched aliphatic hydrocarbon having up to 10 carbon atoms; linear aliphatic hydrocarbon having up to 10 carbon atoms; saturated cyclohydrocarbon having up to 10 carbon atoms; cycloaliphatic hydrocarbon having up to 10 carbon atoms; aromatic aliphatic hydrocarbon having up to 10 carbon atoms; F; Cl; alkoxy of C 1-3 ; OH; OH group-containing branched aliphatic hydrocarbon having up to 10 carbon atoms; OH group-containing linear aliphatic hydrocarbon having up to 10 carbon atoms; OH group-containing saturated cyclohydrocarbon having up to 10 carbon atoms; OH group-containing cycloaliphatic hydrocarbon having up to 10 carbon atoms; or OH group-containing aromatic aliphatic hydrocarbon having up to 10 carbon atoms. The process as claimed in Claim 7, wherein said promoter is an imidazole. The process as claimed in any of Claims 1 to 8, wherein said reacting step (a) is conducted at a temperature of from 40 to 120°C. The process as claimed in any of claims 1 to 9, wherein said reacting step (a) is conducted at a pressure of from 100 to 1500 psig (790 to 10444 kPa(absolute)). The process as claimed in any of Claims 1 to 10, wherein said epoxide derivative is represented by the following formula (II): wherein R 1 and R 2 are independently hydrogen; linear aliphatic hydrocarbon having up to 20 carbon atoms; branched aliphatic hydrocarbon having up to 20 carbon atoms; saturated cycloaliphatic hydrocarbon having up to 20 carbon atoms; cycloaliphatic hydrocarbon having up to 20 carbon atoms; aromatic aliphatic hydrocarbon having up to 20 carbon atoms; hydrocarbon having up to 20 carbon atoms substituted hydrogen on the carbon chain for F or Cl or Br; aromatic hydrocarbon having up to 20 carbon atoms with no substituted group or aromatic hydrocarbon having up to 20 carbon atoms substituted hydrogen on the aromatic ring for F, Cl, amine group, nitrile group, or alkoxy group. The process as claimed in any of Claims 1 to 11, wherein said alcohol is represented by R'OH, wherein R' is a saturated linear hydrocarbon having up to 20 carbon atoms, an unsaturated linear hydrocarbon having up to 20 carbon atoms; a hydrocarbon having up to 20 carbon atoms having branches, a cyclohydrocarbon having up to 20 carbon atoms, an aromatic hydrocarbon having up to 20 carbon atoms, or a linear hydrocarbon including an aromatic group. The process as claimed in any of Claims 1 to 12, wherein said solvent is represented by the following formula (III), (IV) or V): R 3 ―O―R 4 wherein R 3 , R 4 , R 5 , R 6 , and R 7 are saturated aliphatic hydrocarbon having up to 10 carbon atoms; having no branches; branched aliphatic hydrocarbon having up to 10 carbon atoms; saturated cyclohydrocarbon having up to 10 carbon atoms; cycloaliphatic hydrocarbon having up to 10 carbon atoms; or aromatic aliphatic hydrocarbon having up to 10 carbon atoms; m is an integer of 1 to 10; and n is an integer of 2 to 5. The process as claimed in any of claims 1 to 12, wherein said solvent is an acetate. The process as claimed in any of Claims 1 to 12, wherein said solvent is an alcohol represented by R'OH, wherein R' is a saturated linear hydrocarbon having up to 20 carbon atoms, an unsaturated linear hydrocarbon having up to 20 carbon atoms, a hydrocarbon having up to 20 carbon atoms having branches, a cyclohydrocarbon having up to 20 carbon atoms, an aromatic hydrocarbon having up to 20 carbon atoms or a linear hydrocarbon including an aromatic group. The process as claimed in any of Claims 1 to 12, wherein said solvent is a substituted aromatic compound represented by the following formula (VI): where R 8 , R 9 , R 10 , R 11 , R 12 and R 13 are hydrogen; saturated aliphatic hydrocarbon of C 1-4 having no branches; branched aliphatic hydrocarbon of C 1-4 ; F; Cl; or alkoxy group of C 1-3 . The process as claimed in any of Claims 1 to 16, wherein said reaction product includes 3-hydroxyester and derivatives thereof represented by the following formula (VII) or (VIII): wherein R 1 and R 2 are hydrogen; linear aliphatic hydrocarbon having up to 20 carbon atoms; branched aliphatic hydrocarbon having up to 20 carbon atoms; saturated cycloaliphatic hydrocarbon having up to 20 carbon atoms; cycloaliphatic hydrocarbon having up to 20 carbon atoms; aromatic aliphatic hydrocarbon having up to 20 carbon atoms; hydrocarbon having up to 20 carbon atoms substituted hydrogen on the carbon chain for F or Cl or Br; aromatic hydrocarbon having up to 20 carbon atoms with no substituted group; or aromatic hydrocarbon having up to 20 carbon atoms substituted hydrogen on the aromatic ring for F, Cl, amine group, nitrile group, or alkoxy group, and R' is a saturated linear hydrocarbon having up to 20 carbon atoms, an unsaturated linear hydrocarbon having up to 20 carbon atoms, a hydrocarbon having up to 20 carbon atoms having branches, a cyclohydrocarbon having up to 20 carbon atoms, an aromatic hydrocarbon of having up to 20 carbon atoms, or a linear hydrocarbon including an aromatic group. The process as claimed in any of claims 1 to 17, wherein said catalyst system of said step (c) is copper chromate or Pd/C. The process as claimed in any of claims 1 to 18, wherein said step (c) is conducted at the pressure of hydrogen of from 200 to 3000 psig (1480 to 20786 kPa(absolute)). The process as claimed in any of Claims 1 to 19, wherein said step (c) is conducted at the temperature of from 50 to 250°C.

Inventors: CHEN BYUNG-SOON, LEE BYEONG-NO, CHEN, BYUNG-SOON, LEE, BYEONG-NO
Applicants: DAVY PROCESS TECHN LTD, DAVY PROCESS TECHNOLOGY LIMITED
Application year: 2000
Main classification: C07C67
IPC codes: C07C67, C07C29