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    Procedimiento de oxidación parcial en fase gaseosa catalizada de forma heterogénea de acroleína para dar ácido acrílico
    13.
    发明专利
    Procedimiento de oxidación parcial en fase gaseosa catalizada de forma heterogénea de acroleína para dar ácido acrílico 未知

    公开(公告)号：ES2545257T3

    公开(公告)日：2015-09-09

    申请号：ES04722172

    申请日：2004-03-20

    Applicant: BASF SE

    Inventor： DIETERLE MARTIN ,  PETZOLDT JOCHEN ,  MÜLLER-ENGEL KLAUS JOACHIM ,  ARNOLD HEIKO

    IPC: C07C57/055 ,  C07C51/25 ,  C07C57/05

    Abstract: Un procedimiento de oxidación parcial en fase gaseosa catalizada de forma heterogénea de acroleína para dar ácido acrílico, en el que se conduce una mezcla de partida de gas de reacción que contiene acroleína, oxígeno molecular y al menos un gas inerte, que está constituido en al menos el 20 % de su volumen por nitrógeno molecular, que contiene el oxígeno molecular y la acroleína en una relación molar de O2 : C3H4O >= 0,5, a una etapa de reacción a través de un relleno de catalizador en lecho fijo, que está dispuesta en dos zonas de reacción A, B dispuestas espacialmente consecutivas, siendo la temperatura de la zona de reacción A una temperatura en el intervalo de 230 a 320 ºC y la temperatura en la zona de reacción B también una temperatura en el intervalo de 230 a 320 ºC, y cuya masa activa es al menos un óxido multimetálico que contiene los elementos Mo y V, de modo que la zona de reacción A se extienda hasta una reacción de la acroleína del 45 al 85 % en moles y en un único paso de la mezcla de partida de gas de reacción a través de la totalidad del relleno de catalizador en lecho fijo la reacción de la acroleína sea >= 90 % en moles y la selectividad de la formación de ácido acrílico, con respecto a la acroleína reaccionada, sea >= 90 % en moles, correspondiendo la sucesión temporal en la que la mezcla de partida de gas de reacción atraviesa las zonas de reacción a la sucesión alfabética de las zonas de reacción, que está caracterizado porque a) la carga del relleno de catalizador en lecho fijo con la acroleína contenida en la mezcla de partida de gas de reacción es = 70 Nl de acroleína/l de relleno de catalizador en lecho fijo h, b) la actividad específica del volumen del relleno de catalizador en lecho fijo en la dirección de la corriente de la mezcla gaseosa de reacción a través del relleno de catalizador en lecho fijo es constante o al menos aumenta una vez, y c) la diferencia TmaxA - TmaxB, constituida por la temperatura más alta, TmaxA, que presenta la mezcla gaseosa de reacción dentro de la zona de reacción A y la temperatura más alta, TmaxB, que presenta la mezcla gaseosa de reacción dentro de la zona de reacción B es >= 0 ºC.

    Process for the long-term operation of a continuously operated heterogeneously catalyzed partial dehydrogenation of a hydrocarbon to be dehydrogenated
    16.
    发明专利
    Process for the long-term operation of a continuously operated heterogeneously catalyzed partial dehydrogenation of a hydrocarbon to be dehydrogenated 未知

    公开(公告)号：ZA200901384B

    公开(公告)日：2010-05-26

    申请号：ZA200901384

    申请日：2009-02-26

    Applicant: BASF SE

    Inventor： DIETERLE MARTIN ,  SCHINDLER GOETZ-PETER ,  MUELLER-ENGEL KLAUS JOACHIM ,  ADAMI CHRISTOPH ,  SCHEIDEL JENS ,  HORSTMANN CATHARINA

    IPC: B01J20100101 ,  C07C20100101

    Abstract: Preparation of dehydrogenated hydrocarbon, comprises providing a gaseous reaction mixture stream containing the hydrocarbon at an increased temperature through a catalyst bed system present in a reaction zone; and optionally supplying a volume flow of molecular oxygen, molecular hydrogen, water vapor and/or another inert gas that act as auxiliary gases for the dehydrogenation reaction, to the gaseous reaction mixture stream between its entry at the start of the catalyst bed system and its exit from the end of the catalyst bed system. Procedure for the long-term operation of a continuously-operated and heterogeneously-catalyzed partial dehydrogenation process of a hydrocarbon to be dehydrogenated to form a dehydrogenated hydrocarbon, comprises providing a gaseous reaction mixture stream containing the hydrocarbon in an initial molar volume (KW), at an increased temperature through a catalyst bed system, which is present in a reaction zone (RZ) and consist of many catalyst bed sections that are arranged serially along the flow direction of the gaseous reaction mixture stream, and as a whole consists a molar volume (M) of a dehydrogenation catalyst; where: at the time of operation t is t 0, the passage of the gaseous reaction mixture stream through first, second and last third portion of (M) along the flow direction output, proportions of A, B and C mol.% of (KW) of the hydrocarbon to be dehydrogenated are respectively converted to form dehydrogenated hydrocarbon, under the condition that A is greater than B and B is greater than C and during the passage of the gaseous reaction mixture stream through the catalyst bed system, a total (G) i.e. A+B+C mol.% of (KW) of the hydrocarbon to be dehydrogenated that is contained in this reaction mixture stream is dehydrogenated to form dehydrogenated hydrocarbon, and optionally supplying a volume flow of molecular oxygen, molecular hydrogen, water vapor and/or another inert gas that act as auxiliary gases for the dehydrogenation reaction, to the gaseous reaction mixture stream between its entry at the start of the catalyst bed system and its exit from the end of the catalyst bed system, where deactivation of the catalyst bed system that advances with increasing operating time within an operation time interval of greater than t 0 and less than t r is counteracted by varying the temperature profile of the gaseous reaction mixture stream within the catalyst bed system and/or the volume flow of the optionally supplied auxiliary gases for the dehydrogenation reaction, where t r is the operating time point at which the dehydrogenation is interrupted and the catalyst bed system is at first recovered after the operating time point of t 0, thus the variation is carried out in such a manner that with increasing operating time point, the proportion A decreases, the proportion B undergoes a maximum and the proportion C increases.

    Reactor from plated stainless steel for the continuous heterogeneously catalyzed partial dehydration of at least one hydrocarbon to be dehydrated, and corresponding method
    17.
    发明专利
    Reactor from plated stainless steel for the continuous heterogeneously catalyzed partial dehydration of at least one hydrocarbon to be dehydrated, and corresponding method 未知

    公开(公告)号：ZA200900538B

    公开(公告)日：2010-04-28

    申请号：ZA200900538

    申请日：2009-01-23

    Applicant: BASF SE

    Inventor： HECHLER CLAUS ,  RUPPEL WILHELM ,  SCHINDLER GOETZ-PETER ,  KLANNER CATHARINA ,  BASSLER HANS-JUERGEN ,  DIETERLE MARTIN ,  KLAPPERT KARL-HEINRICH ,  MUELLER-ENGEL KLAUS JOACHIM

    IPC: B01J20100101 ,  B32B20100101 ,  C07C20100101

    Abstract: Continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in the gas phase involves at least one catalyst bed disposed in the reaction chamber and with generation of a product gas comprising the at least one dehydrogenated hydrocarbon, unconverted hydrocarbon to be dehydrogenated and molecular hydrogen and/or steam, is dehydrogenated partially in an oxidative or non-oxidative manner to at least one dehydrogenated hydrocarbon, and at least one product gas stream is withdrawn continuously from the reaction chamber. Process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in the gas phase involves a reaction chamber enclosed by a shell which is in contact with the reaction chamber and has at least one first orifice for feeding at least one starting gas stream into the reaction chamber and at least one second orifice for withdrawing at least one product gas stream from the reaction chamber, at least one starting gas stream comprising at least one hydrocarbon to be dehydrogenated is fed continuously in the reaction chamber. The at least one hydrocarbon to be dehydrogenated is conducted through at least one catalyst bed disposed in the reaction chamber and with generation of a product gas comprising the at least one dehydrogenated hydrocarbon, unconverted hydrocarbon to be dehydrogenated and molecular hydrogen and/or steam, is dehydrogenated partially in an oxidative or non-oxidative manner to at least one dehydrogenated hydrocarbon, and at least one product gas stream is withdrawn continuously from the reaction chamber. The shell is manufactured from a composite material which, on its side B in contact with the reaction chamber, consists of steel B comprising (wt.%): chromium (18-30), nickel (9-37), silicon (1-4), aluminum (>=0-4), nitrogen (>=0-0.3), carbon (>=0-0.15), manganese (>=0-4), phosphorus (>=0-0.05), sulfur (>=0-0.05), and at least one rare earth metal (>=0-0.1), and iron and impurities resulting from production. The steel B, on its side A facing away from the reaction chamber, is plated either directly or via an intermediate layer of copper, and/or nickel, onto steel A comprising (wt.%): chromium (15-20), nickel (6-18), silicon (>=0-0.8), aluminum (>=0-0.8), nitrogen (>=0-0.3), carbon (>=0-0.15), molybdenum (>=0-4), manganese (>=0-2), titanium (>=0-0.8), niobium (>=0-1.2), vanadium (>=0-0.9), boron (>=0-0.1), phosphorus (>=0-0.05), sulfur (>=0-0.05), iron and impurities resulting from production, or a composition comprising (wt.%) Cr (19-23), Ni (30-35), Co (>=0-1), Si (>=0-1), Al (0.15-0.7), C (>=0-0.12), Mn (>=0-2), Cu (>=0-0.75), Ti (0.15-0.7), Nb (>=0-0.1), P (>=0-0.05), S (>=0-0.05) and iron and impurities resulting from production. An independent claim is included for a shell encloses an interior and has at least one first orifice for feeding at least one gas stream into the interior and at least one second orifice for withdrawing a gas stream fed to the interior beforehand via the at least one first orifice O1 from the interior. The shell is manufactured from a composite material which, on its side B in contact with the reaction chamber, consists of steel B on its side A facing away from the reaction chamber is plated either directly or via an intermediate layer of copper and/or nickel onto steel A.

    METHOD FOR THE HETEROGENEOUSLY CATALYSED PARTIAL GAS PHASE OXIDATION OR PROPYLENE TO FORM ACRYLIC ACID
    18.
    发明专利
    METHOD FOR THE HETEROGENEOUSLY CATALYSED PARTIAL GAS PHASE OXIDATION OR PROPYLENE TO FORM ACRYLIC ACID 未知

    公开(公告)号：ZA200806258B

    公开(公告)日：2009-12-30

    申请号：ZA200806258

    申请日：2008-07-18

    Applicant: BASF SE

    Inventor： HEILEK JORG ,  DIETERLE MARTIN ,  MULLER ENGLE KLAUS JOACHIM

    Abstract: Heterogeneously catalyzed partial gas phase oxidation of propylene to acrylic acid comprises introducing a reaction gas initial mixture (1) into a first reaction zone; reducing the temperature of the product gas mixture (1) by direct and/or indirect cooling, and adding a secondary gas to the product gas mixture (1); and subsequently introducing the product gas mixture (1), into a second reaction stage; and subsequently transferring the product gas mixture (2) containing acrylic acid in a first separation zone into the condensed phase and subsequently in a second separation zone. Heterogeneously catalyzed partial gas phase oxidation of propylene to acrylic acid comprises introducing a reaction gas initial mixture (1) containing propylene and molecular oxygen in a molar ratio of >=, 1 and at least an inert dilution gas in a first reaction stage, into a first reaction zone through at least a first catalyst bed at increased temperature, where the catalyst exhibit at least a multi-metal oxide (A) containing molybdenum, iron and bismuth as active mass, such that the propylene conversion during a single passage through the catalyst bed is >= 90 mol.% and the resulting selectivity of the acrolein- and acrylic acid by-product- formation is >= 80 mol.%; reducing the temperature of the product gas mixture (1) from the first reaction stage by direct and/or indirect cooling, and adding a secondary gas in the form of molecular oxygen and/or inert gas to the product gas mixture (1); and subsequently introducing the product gas mixture (1) as a reaction gas initial mixture (2) containing molecular oxygen and acrolein in a molar ratio of >= 0.5 and at least an inert dilution gas, in a second reaction stage at increased temperature by at least a second catalyst bed, whose catalysts exhibits multi-metal oxide (A1) containing at least an molybdenum and vanadium as active mass in such a way that the acrolein conversion during a single passage through the catalyst bed is >= 90 mol % and the selectivity of the acrylic acid formation over both the reaction stages is >= 70 mol %, with respect to converted propylene; subsequently transferring the product gas mixture (2) containing acrylic acid in a first separation zone into the condensed phase and subsequently in a second separation zone, where: the acrylic acid is separated from the condensed phase by application of at least a thermal separation process comprising at least a crystallization separation of the acrylic acid, and the reaction gas initial mixture (1) contains cyclopropane (up to 3 mol.%), with respect to the propylene.

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