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    21.
    发明专利
    未知

    公开(公告)号：DE102004058887A1

    公开(公告)日：2006-06-08

    申请号：DE102004058887

    申请日：2004-12-06

    Applicant: BASF AG

    Inventor： GRAFMANS HORST ,  MAAS STEFFEN ,  WECK ALEXANDER ,  RUETTER HEINZ ,  SCHULZ MICHAEL ,  ROS KARL-HEINZ

    IPC: C07C231/02 ,  C07C233/05

    Abstract: A process for preparing N,N-dimethylacetamide (DMAC) by continuously reacting methyl acetate (MeOAc) with dimethylamine (DMA) in the presence of a basic catalyst, wherein MeOAc is used in the form of a methanolic solution and in the range from 0.0002 to 0.09 mol of catalyst per mole of MeOAc, and performing the reaction at a temperature in the range from 90 to 140° C. and at an absolute pressure in the range from 10 to 30 bar.

    24.
    发明专利
    未知

    公开(公告)号：DE10341614A1

    公开(公告)日：2005-04-28

    申请号：DE10341614

    申请日：2003-09-10

    Applicant: BASF AG

    Inventor： HUGO RANDOLF ,  JOURDAN SABINE ,  WENZ KIRSTEN ,  PREISS THOMAS ,  WECK ALEXANDER

    IPC: C07C209/48 ,  C07C211/27 ,  C07C253/24 ,  C07C253/34 ,  C07C209/82

    Abstract: A process for preparing xylylenediamine, comprising the steps of ammoxidizing xylene to phthalonitrile and hydrogenating the phthalonitrile, which comprises contacting the vaporous product of the ammoxidation stage directly with a liquid organic solvent or with molten phthalonitrile (quench), partly or fully removing components having a boiling point lower than phthalonitrile (low boilers) from the resulting quench solution or suspension or phthalonitrile melt and, after the low boiler removal and before the hydrogenation, removing products having a boiling point higher than phthalonitrile (high boilers).

    26.
    发明专利
    未知

    公开(公告)号：DE50103263D1

    公开(公告)日：2004-09-16

    申请号：DE50103263

    申请日：2001-12-07

    Applicant: BASF AG

    Inventor： BORCHERT HOLGER ,  SCHLITTER STEPHAN ,  FISCHER ROLF-HARTMUTH ,  ROESCH MARKUS ,  STEIN FRANK ,  RAHN RALF-THOMAS ,  WECK ALEXANDER ,  KAIBEL GERD

    IPC: C07B61/00 ,  C07D307/08 ,  C07D307/33

    Abstract: The present invention relates to a process for the gas-phase hydrogenation of C4-dicarboxylic acids and/or their derivatives over a catalyst based on copper oxide to give substituted or unsubstituted gamma-butyrolactone and/or tetrahydrofuran, which comprises, which a first reaction zone in which the C4-dicarboxylic acid and/or its derivatives is/are reacted to give a mixture comprising a substituted or unsubstituted gamma-butyrolactone as main product and a subsequent second reaction zone in which the substituted or unsubstituted gamma-butyrolactone present in the mixture from the first hydrogenation step is reacted at a temperature lower than the temperature in the first hydrogenation step to give substituted or unsubstituted tetrahydrofuran.

    27.
    发明专利
    未知

    公开(公告)号：DE10225926A1

    公开(公告)日：2003-12-24

    申请号：DE10225926

    申请日：2002-06-11

    Applicant: BASF AG

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

    IPC: C07B61/00 ,  C07C29/149 ,  C07C31/20 ,  C07C29/132 ,  C07D307/20 ,  C07D307/32

    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 10 to 100 bar into a first reactor or into a first reaction zone of a reactor and catalytically hydrogenating it in the gas phase to a product which contains mainly optionally alkyl-substituted gamma-butyrolactone; b) introducing the product stream obtained in this way into a second reactor or into a second reaction zone of a reactor at a temperature of from 140° C. to 260° C. and catalytically hydrogenating it in the gas phase to optionally alkyl-substituted 1,4-butanediol; steps a) and b) being carried out at the same pressure; c) removing the desired product from intermediates, by-products and any unconverted reactants; d) optionally recycling unconverted intermediates into one or both hydrogenation stages, said hydrogenation stages each using a catalyst which comprises =5% by weight, preferably from 5 to 95% by weight, in particular from 20 to 90% by weight, of an oxidic support, and the product mixture removed from the first hydrogenation stage being introduced without further purification into the second hydrogenation stage.

    METHOD FOR THE PRODUCTION OF 1,4- BUTANEDIOL
    28.
    发明专利
    METHOD FOR THE PRODUCTION OF 1,4- BUTANEDIOL 未知

    公开(公告)号：AU2003246407A1

    公开(公告)日：2003-12-22

    申请号：AU2003246407

    申请日：2003-06-10

    Applicant: BASF AG

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

    IPC: 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 10 to 100 bar into a first reactor or into a first reaction zone of a reactor and catalytically hydrogenating it in the gas phase to a product which contains mainly optionally alkyl-substituted gamma-butyrolactone; b) introducing the product stream obtained in this way into a second reactor or into a second reaction zone of a reactor at a temperature of from 140° C. to 260° C. and catalytically hydrogenating it in the gas phase to optionally alkyl-substituted 1,4-butanediol; steps a) and b) being carried out at the same pressure; c) removing the desired product from intermediates, by-products and any unconverted reactants; d) optionally recycling unconverted intermediates into one or both hydrogenation stages, said hydrogenation stages each using a catalyst which comprises =5% by weight, preferably from 5 to 95% by weight, in particular from 20 to 90% by weight, of an oxidic support, and the product mixture removed from the first hydrogenation stage being introduced without further purification into the second hydrogenation stage.

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