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    22.
    发明专利
    未知

    公开(公告)号：NO20024707L

    公开(公告)日：2003-04-07

    申请号：NO20024707

    申请日：2002-10-01

    Applicant: BASF AG

    Inventor： HEYDRICH GUNNAR ,  AUST NICOLA CHRISTIANE ,  PUETTER HERMANN ,  FISCHER ANDREAS ,  BOTZEN JOERG

    IPC: C07B61/00 ,  C07C41/50 ,  C07C43/303 ,  C07C47/198 ,  C07C41/56

    Abstract: The production of diacetals (I) of glyoxal (II) from aqueous glyoxal and monohydric alcohols (III) with an acid catalyst (IV) involves leaving a mixture of (III) and (II) in contact with (IV) until the content of (I) is at least 70% of the equilibrium concentration. production of diacetals (I) of glyoxal (II) from 40-75 wt% aqueous glyoxal and monohydric alcohols (III) with acid catalyst (IV) involves leaving a mixture of (III) and (II) (mol ratio = at least 15:1) and not more than 8 wt% water in contact with (IV) until the content of (I) is at least 70% of the equilibrium concentration (without distilling off more than 5 wt% of the alcohol).

    METHOD FOR THE PRODUCTION OF 1,4- BUTANE-DIOL BY COMBINED GAS-PHASE AND LIQUID-PHASE HYDROGENATION
    28.
    发明专利
    METHOD FOR THE PRODUCTION OF 1,4- BUTANE-DIOL BY COMBINED GAS-PHASE AND LIQUID-PHASE HYDROGENATION 未知

    公开(公告)号：AU2003274707A1

    公开(公告)日：2003-12-22

    申请号：AU2003274707

    申请日：2003-06-10

    Applicant: BASF AG

    Inventor： BOTTIKE NILS ,  FISCHER ROLF-HARTMUTH ,  WECK ALEXANDER ,  WINDECKER GUNTHER ,  HEYDRICH GUNNAR ,  HESSE MICHAEL ,  SCHLITTER STEPHAN ,  BORCHERT HOLGER ,  SCHUBERT MARKUS ,  ROSCH MARKUS

    IPC: B01J23/80 ,  C07B61/00 ,  C07C29/149 ,  C07C31/20

    Abstract: 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 C 4 -dicarboxylic acids and/or of derivatives thereof having the following steps: a) introducing a gas stream of a C 4 -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 gamma-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 =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.

    TWO-STAGE METHOD FOR PRODUCING BUTANDIOL IN TWO REACTORS
    29.
    发明专利
    TWO-STAGE METHOD FOR PRODUCING BUTANDIOL IN TWO REACTORS 未知

    公开(公告)号：AU2003238491A1

    公开(公告)日：2003-12-22

    申请号：AU2003238491

    申请日：2003-06-10

    Applicant: BASF AG

    Inventor： HESSE MICHAEL ,  SCHLITTER STEPHAN ,  BORCHERT HOLGER ,  SCHUBERT MARKUS ,  ROSCH MARKUS ,  BOTTKE NILS ,  FISCHER ROLF-HARTMUTH ,  WECK ALEXANDER ,  WINDECKER GUNTHER ,  HEYDRICH GUNNAR

    IPC: C07C29/149 ,  C07D315/00 ,  C07D307/33 ,  C07C31/20

    Abstract: The invention relates to a method for producing optionally akyl-substituted 1,4-butandiol by two-stage catalytic hydration in the gaseous phase of C4 dicarboxylic acids and/or the derivatives thereof with the steps of: a) introducing a gaseous flow of a C4 dicarboxylic acid or a derivative thereof at 200 to 300 °C and 2 to 60 bar in a first reactor and catalytic gas phase hydration to a mainly optionally alkyl-substituted gamma-butyrolactone containing product; b) introducing the product flow so obtained into a second reactor at a temperature of from 150 °C to 240 °C and a pressure of from 15 to 100 bar and catalytic gas phase hydration to optionally alkyl-substituted 1,4-butandiol; c) removing the desired product from the intermediates, byproducts and possibly not reacted educt; d) optionally returning non-reacted intermediates to one or both hydration stages, whereby in both hydration stages one catalyst each is used which comprises = 5 % by weight, preferably 5 to 95 % by weight, especially 20 to 90 % by weight of an oxidic carrier, the pressure prevailing in the second reactor is higher than in the first reactor, and the product mixture removed from the first reactor is introduced into the second reactor without further purifying it.

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