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    METHOD FOR THE CATALYTIC DECOMPOSITION OF N2O
    11.
    发明专利
    METHOD FOR THE CATALYTIC DECOMPOSITION OF N2O 未知

    公开(公告)号：CA2329871C

    公开(公告)日：2008-10-07

    申请号：CA2329871

    申请日：1999-04-15

    Applicant: BASF AG

    Inventor： FETZER THOMAS ,  BAIER MICHAEL ,  HESSE MICHAEL ,  BURGER GERT ,  SCHUMACHER VOLKER

    IPC: B01D53/94 ,  C01B21/26 ,  B01D53/86 ,  B01J23/80 ,  C01B21/38 ,  C01B21/40

    Abstract: In the reactor for the catalytic oxidation of ammonia into nitrogen oxides, which in the direction of flow contains, in this order, a precious-metal gauze catalyst and a heat exchanger, a catalyst for the decomposition of N20 is positioned between the precious-metal gauze catalyst and the heat exchanger. According to said method for the catalytic decomposition of N20 in a gaseous mixture obtained during the production of nitric acid by catalytic oxidation of ammonia, on a catalyst intended for the decomposition of N20, the hot gas mixture obtained as a result of the catalytic oxidation of ammonia is brought into contact with the catalyst used for the decomposition of N20 before being cooled.

    METODO PARA PRODUCIR ANHIDRIDO DE ACIDO FTALICO.
    13.
    发明专利
    METODO PARA PRODUCIR ANHIDRIDO DE ACIDO FTALICO. 未知

    公开(公告)号：ES2280728T3

    公开(公告)日：2007-09-16

    申请号：ES03706423

    申请日：2003-02-04

    Applicant: BASF AG

    Inventor： STORCK SEBASTIAN ,  ROSOWSKI FRANK ,  BAIER MICHAEL ,  TENTEN ANDREAS ,  WOLF HANS-JOSEF

    IPC: C07C51/265 ,  C07D307/89 ,  B01J23/22 ,  B01J35/00 ,  C07B61/00 ,  C07C51/31 ,  C07C63/16

    Abstract: Un proceso para preparar anhídrido de ácido ftálico mediante oxidación en fase gaseosa de xileno, naftaleno o mezclas de los mismos en un reactor de haz de tubos, termostatizado mediante un agente de transferencia de calor por sobre tres o más catalizadores anulares soportados en lechos fijos, ubicados en capas, donde el proceso se lleva a cabo de tal modo que la temperatura máxima en la segunda capa de catalizador en la dirección de flujo es de 10 hasta 40ºC más baja que la temperatura máxima en la primera capa de catalizador, la temperatura máxima en la tercera capa desde la entrada de gas es desde 30 hasta 100ºC más baja que en la primera zona de catalizador y la temperatura máxima en la primera zona de catalizador es menor que 470ºC.

    18.
    发明专利
    未知

    公开(公告)号：ES2196390T3

    公开(公告)日：2003-12-16

    申请号：ES97953761

    申请日：1997-12-09

    Applicant: BASF AG

    Inventor： HEINEKE DANIEL ,  BAIER MICHAEL ,  DEMUTH DIRK ,  HARTH KLAUS

    IPC: B01J21/06 ,  B01J23/14 ,  B01J23/24 ,  B01J23/26 ,  B01J23/36 ,  B01J23/40 ,  B01J23/62 ,  C07C5/333 ,  C07C11/02 ,  C07C11/06

    Abstract: Olefinically unsaturated hydrocarbons are prepared from corresponding paraffinic hydrocarbons, in particular propylene is prepared from propane, by dehydrogenation over a catalyst comprising an oxide of a transition metal of group IV B of the Periodic Table, eg. TiO 2 or ZrO 2 , and possibly at least one element selected from among elements of transition group VIII, eg. palladium, platinum or rhodium, and/or an element of transition group VI, eg. chromium, molybdenum or tungsten, and/or rhenium and/or tin and possibly a compound of an alkali metal or alkaline earth metal, a compound of main group III or transition group III or zinc.

    METHOD FOR PRODUCING PHTHALIC ANHYDRIDE
    19.
    发明专利
    METHOD FOR PRODUCING PHTHALIC ANHYDRIDE 未知

    公开(公告)号：AU2003208789A1

    公开(公告)日：2003-09-09

    申请号：AU2003208789

    申请日：2003-02-04

    Applicant: BASF AG

    Inventor： ROSOWSKI FRANK ,  BAIER MICHAEL ,  TENTEN ANDREAS ,  WOLF HANS-JOSEF ,  STORCK SEBASTIAN

    IPC: C07D307/89 ,  B01J23/22 ,  B01J35/00 ,  C07B61/00 ,  C07C51/265 ,  C07C51/31 ,  C07C63/16

    Abstract: Production of phthalic anhydride by gas-phase oxidation of o-xylene or naphthalene in a tubular reactor involves using three or more different catalyst beds with controlled hot-spot temperatures. A method for the production of phthalic anhydride (I) by gas-phase oxidation of xylene and/or naphthalene in a thermostatted tube-bank reactor on 3 or more solid-bed catalysts in 3 different layers involves carrying out the process in such a way that the peak temperature (T2) in the second catalyst layer (in the direction of flow) is up to 50 degrees C below the peak temperature (T1) in the first layer and the peak temperature (T3) in the third layer is 30-100 degrees C below T1.

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