초록 ▼

The invention relates to a method for hydrogenation of aromatic urethanes, which contain one or more aromatic rings and one or more urethane groups bonded directly and/or indirectly to one aromatic ring or to different aromatic rings, using hydrogen in the presence of a supported catalyst, which con

The invention relates to a method for hydrogenation of aromatic urethanes, which contain one or more aromatic rings and one or more urethane groups bonded directly and/or indirectly to one aromatic ring or to different aromatic rings, using hydrogen in the presence of a supported catalyst, which contains ruthenium as active metal. The catalyst support of the catalyst to be used according to the invention has a BET surface ranging from larger than 30 m 2 /g to smaller than 70 m 2 /g and more than 50% of the pore volume of the catalyst support is represented by macropores with a pore diameter of larger than 50 nm and less than 50% is represented by mesopores with a pore diameter of 2 to 50 nm. The method is suitable in particular for hydrogenation of dibutyl 4,4′-methylenedicarbanilate to dibutyl 4,4′-methylenedicyclohexylcarbamate with a trans-trans isomer content of <30%, preferably of <20%, particularly preferably of 5 to 15%.

대표청구항 ▼

1. A method for hydrogenation of an aromatic urethane, which contain one or more aromatic rings and one or more urethane groups bonded directly and/or indirectly to one aromatic ring or to different aromatic rings, by reacting the aromatic urethane with hydrogen in the presence of a supported cataly

1. A method for hydrogenation of an aromatic urethane, which contain one or more aromatic rings and one or more urethane groups bonded directly and/or indirectly to one aromatic ring or to different aromatic rings, by reacting the aromatic urethane with hydrogen in the presence of a supported catalyst, which contains as active metal, applied on a support, ruthenium alone or together with at least one metal of the subgroups of Groups I, VII or VIII of the Periodic Table, the proportion of active metal being 0.01 to 20 wt % relative to the supported catalyst, and wherein the catalyst support has a BET surface ranging from larger than 30 m 2 /g to smaller than 70 m 2 /g and more than 50% of the pore volume of the catalyst support is represented by macropores with a pore diameter of larger than 50 nm and less than 50% is represented by mesopores with a pore diameter of 2 to 50 nm. 2. The method according to claim 1, characterized in that the active metal applied on the catalyst has a depth of penetration into the support ranging from 20 to 500 μm. 3. The method according to claim 1, characterized in that the ratio of the surface area of the active metal, determined by CO pulse chemisorption, to that of the catalyst support, determined by the BET method, is larger than 0.01. 4. The method according to claim 1, characterized in that the support material is selected from the group consisting of crystalline and amorphous oxides and crystalline and amorphous silicates. 5. The method according to claim 1, characterized in that the catalyst support has a BET surface ranging from 32 to 67 m 2 /g, a depth of penetration of the active metal into the support ranges from 50 to 200 μm, and the Ru content ranges from 0.2 to 3 wt % relative to the catalyst, and at least 55% of the pore volume of the catalyst support is represented by macropores and less than 45% is represented by mesopores. 6. The method according to claim 1, characterized in that the hydrogenation step is carried out in a suspension or fixed-bed hydrogenation reactor in continuous or batchwise operation, at a temperature ranging from 20 to 250° C., and a hydrogen partial pressure ranging from 1 to 30 MPa. 7. The method according to claim 1, characterized in that the hydrogenation step is carried out in a fixed-bed reactor. 8. The method according to claim 1, characterized in that there is used a supported catalyst whose active metal, ruthenium, was applied onto a support by spraying the support with a dilute ruthenium solution, at a temperature of at least 80° C., with subsequent heat treatment and activation of the catalyst by reduction in a hydrogen-containing gas. 9. The method according to claim 1, characterized in that the compounds hydrogenerated are selected from dialkyl 4,4′-methylenedicarbanilate, dialkyl 2,4′-methylenedicarbanilate, dialkyl 2,2′-methylenedicarbanilate and polynuclear methylene-bridged alkyl carbanilates (PMDU) as well as mixtures thereof,dialkyl 4,4′-methylene-3,3′-dicarbanilate, dialkyl 2,4′-methylene-3,3′-dicarbanilate, dialkyl 2,2′-methylene-3,3′-dicarbanilate as well as mixtures thereof,dialkyl 1,2-phenyldicarbamate, dialkyl 1,3-phenyldicarbamate and dialkyl 1,4-phenyldicarbamate as well as mixtures thereof,dialkyl 2,4-toluenedicarbamate, dialkyl 2,6-toluenedicarbamate as well as mixtures thereof,dialkyl 1,6-naphthalenedicarbamate,and the urethanes corresponding to the compounds abbreviated as MXDI and TMXDI, 10. The method according to claim 1, characterized in that there is hydrogenated a dialkyl 4,4′-(C 1 to C 4 )alkanedicarbanilate and/or a 2,4′-isomer and/or 2 , 2 -isomer or mixtures thereof. 11. The method according to claim 10, characterized in that there is hydrogenated a dibutyl 4,4′-methylenedicarbanilate or an isomer or a mixture thereof. 12. The method according to claim 1, characterized in that hydrogenation products with a trans-trans isomer content of <30% are synthesized from bridged binuclear starting products. 13. The method according to claim 1, for hydrogenation of dibutyl 4,4′-methylenedicarbanilate to dibutyl 4,4′-methylenedicyclohexylcarbamate with a trans-trans isomer content of <30%. 14. The method according to claim 1, characterized in that the hydrogenation step is performed in a solvent or solvent mixture of alcohols and/or ethers. 15. The method according to claim 14, characterized in that the alcohols correspond to the alcohol group of the urethane. 16. The method according to claim 14, characterized in that the alcohols and/or ethers include n-butanol and tetrahydrofuran. 17. The method according to claim 1, characterized in that the active metal applied on the catalyst has a depth of penetration into the support ranging from 25 to 250 μm. 18. The method according to claim 1, characterized in that the ratio of the surface area of the active metal, determined by CO pulse chemisorption, to that of the catalyst support, determined by the BET method, is in a range of from 0.03 to 0.3. 19. The method according to claim 1, characterized in that the support material is selected from the group consisting of Al 2 O 3 , SiO 2 , TiO 2 , ZrO 2 , MgO, ZnO and aluminosilicates. 20. The method according to claim 1, characterized in that the aromatic urethane is free of one or more of sulfur, phosphorus and chlorine.