a) introducing a gas stream of a C4-dicarboxylic acid or of a derivative thereof at from 200 to 300° C. and from 2 to 60 bar into a first reactor and catalytically hydrogenating it to a product which contains mainly optionally alkyl-substituted γ-butyrolactone;b) converting the product stream into the liquid phase;c) introducing the product stream obtained in this way into a second reactor at a temperature of from 100° C. to 240° C. and a pressure of from 20 to 250 bar and catalytically hydrogenating it in the liquid phase to optionally alkyl-substituted 1,4-butanediol;d) removing the desired product from by-products and any unconverted reactants;e) optionally recycling unconverted intermediates into one or both hydrogenation stages, said hydrogenation stages both using a catalyst which comprises ≦95% by weight, preferably from 5 to 95% by weight, in particular from 10 to 80% by weight, of CuO, and ≧5% by weight, preferably from 5 to 95% by weight, in particular from 20 to 90% by weight, of a support, said second reactor having a higher pressure than said first reactor, and the product mixture removed from said first reactor being introduced without further purification into said second reactor."/> Method for the production of 1,4- butane-diol by combined gas-phase and liquid-phase hydrogenation
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Method for the production of 1,4- butane-diol by combined gas-phase and liquid-phase hydrogenation

机译：气相和液相联合加氢生产1,4-丁二醇的方法

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The present invention relates to a process for preparing optionally alkyl-substituted 1,4-butanediol by two-stage catalytic hydrogenation in the gas phase of C4-dicarboxylic acids and/or of derivatives thereof having the following steps:a) introducing a gas stream of a C4-dicarboxylic acid or of a derivative thereof at from 200 to 300° C. and from 2 to 60 bar into a first reactor and catalytically hydrogenating it to a product which contains mainly optionally alkyl-substituted γ-butyrolactone;b) converting the product stream into the liquid phase;c) introducing the product stream obtained in this way into a second reactor at a temperature of from 100° C. to 240° C. and a pressure of from 20 to 250 bar and catalytically hydrogenating it in the liquid phase to optionally alkyl-substituted 1,4-butanediol;d) removing the desired product from by-products and any unconverted reactants;e) optionally recycling unconverted intermediates into one or both hydrogenation stages, said hydrogenation stages both using a catalyst which comprises ≦95% by weight, preferably from 5 to 95% by weight, in particular from 10 to 80% by weight, of CuO, and ≧5% by weight, preferably from 5 to 95% by weight, in particular from 20 to 90% by weight, of a support, said second reactor having a higher pressure than said first reactor, and the product mixture removed from said first reactor being introduced without further purification into said second reactor.
机译：本发明涉及一种在C 4 -二羧酸和/或其衍生物的气相中通过两步催化加氢制备任选烷基取代的1,4-丁二醇的方法脚步： a）引入C 4 -二羧酸或将其衍生物在200至300°C和2至60 bar的压力下进入第一反应器，并将其催化氢化为主要包含任选烷基取代的γ-丁内酯的产物; b）将产品流转换为液相; c）将以此方式获得的产品流引入在100℃至240℃的温度和20至250巴的压力下将第二反应器在液相中催化氢化为任选地烷基取代的1，4-丁二醇; d）从副产物和任何未转化的反应物中除去所需产物; e）回收未转换的内部介导进入一个或两个氢化阶段， 所述的氢化阶段均使用包含≤95重量％，优选5至95重量％的催化剂重量，特别是10至80重量％的CuO，和≥5重量％，优选5至95重量％，特别是20至90重量％的载体，所述第二反应器具有压力比所述第一反应器高，并且从所述第一反应器中除去的产物混合物无需进一步纯化即可引入所述第二反应器。

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