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    11.
    发明专利
    未知

    公开(公告)号：BRPI0710208A2

    公开(公告)日：2011-05-24

    申请号：BRPI0710208

    申请日：2007-03-22

    Applicant: BASF SE

    Inventor： SCHUBERT MARKUS ,  MUELLER ULRICH ,  KIENER CRISTOPH ,  TEICH FRIEDHELM ,  CRONE SVEN ,  SIMON FALK ,  PASTRE JOERG

    IPC: C07C7/13 ,  B01D53/02 ,  B01J20/22 ,  C07C11/06 ,  C10L3/10

    Abstract: The invention relates to a method for commercially obtaining propene from a gas flow containing propene and at least one additional hydrocarbon. Said method comprises the following steps; (a) the gas flow is brought into contact with an adsorber containing a porous metalorganic framework material containing at least one at least bidentate organic compound which is co-ordinately bound to at least one metal ion, said adsorber being charged with propene; and (b) the propene is released from the adsorber charged with the propene. The invention further relates to the use of a porous metalorganic framework material for commercially obtaining propene from a gas flow containing propene and at least one additional hydrocarbon.

    PROCEDIMIENTO PARA LA OBTENCION DE BUTADIENO.
    13.
    发明专利
    PROCEDIMIENTO PARA LA OBTENCION DE BUTADIENO. 未知

    公开(公告)号：ES2344414T3

    公开(公告)日：2010-08-26

    申请号：ES04804421

    申请日：2004-12-30

    Applicant: BASF SE

    Inventor： JOHANN THORSTEN ,  SCHINDLER GOTZ-PETER ,  BRODHAGEN ANDREAS ,  CRONE SVEN ,  BENFER REGINA ,  HILL THOMAS

    IPC: C07C5/333 ,  C07C5/48 ,  C07C11/167

    Abstract: Procedimiento para la obtención de butadieno a partir de n-butano, con los siguientes pasos: A) Preparación de un flujo de gas de alimentación que contiene n-butano; B) Suministro del flujo de gas de alimentación que contiene n-butano a, al menos, una primera zona de deshidrogenación y una deshidrogenación no oxidativa, catalítica, de n-butano, obteniendo un flujo de gas de productos b que contiene n-butano, 1-buteno, 2-buteno, butadieno, hidrógeno, componentes secundarios de bajo punto de ebullición y, eventualmente, vapor de agua; C) Suministro del flujo de gas b de la deshidrogenación catalítica no oxidativa y de un gas que contiene oxígeno a, al menos, una segunda zona de deshidrogenación y una deshidrogenación oxidativa de 1-buteno y 2-buteno, obteniéndose un flujo de gas c que contiene n-butano, 2-buteno, butadieno, hidrógeno, componentes secundarios de bajo punto de ebullición y vapor de agua, que contiene una proporción mayor de butadieno que el flujo de gas de producto b; D) Separación de hidrógeno, de los componentes secundarios de bajo punto de ebullición y del vapor de agua, obteniendo un flujo de gas de productos C4 d que consiste, esencialmente, en n-butano, 2-buteno y butadieno; E) Separación del flujo de gas de productos C4 d en un flujo de retorno e1 que consiste, esencialmente, en n-butano y 2-buteno, y un flujo e2 conformado, esencialmente por butadieno, a través de la destilación extractiva, y retorno a la zona de deshidrogenación del flujo de retorno e1 a la primera zona de deshidrogenación; E) eventualmente, suministro parcial o completo del flujo e2 que consiste, esencialmente, en butadieno a la zona de hidrogenación selectiva y la hidrogenación selectiva de butadieno hasta obtener 1-buteno y/o 2-buteno, obteniendo un flujo f que contiene 1-buteno y 2-buteno; G) eventualmente, suministro del flujo f que contiene 1-buteno y 2-buteno a una zona de destilación y separación de un flujo de producto de valor g1, obteniendo un flujo g2 que contiene 2-buteno; H) eventualmente, retorno a la primera zona de deshidrogenación del flujo g2 que contiene 2-buteno.

    15.
    发明专利
    未知

    公开(公告)号：DK1836146T3

    公开(公告)日：2009-10-19

    申请号：DK06700188

    申请日：2006-01-04

    Applicant: BASF SE

    Inventor： CRONE SVEN ,  MACHHAMMER OTTO ,  SCHINDLER GOETZ-PETER ,  BORGMEIER FRIEDER

    IPC: C07C5/327 ,  C07C7/04 ,  C07C7/11

    Abstract: A process for preparing propene from propane, comprising the steps: A) a feed gas stream a comprising propane is provided; B) the fed gas stream a comprising propane, if appropriate steam and, if appropriate, an oxygenous gas stream are fed into a dehydrogenation zone and propane is subjected to a dehydrogenation to propene to obtain a product gas stream b comprising propane, propene, methane, ethane, ethene, carbon monoxide, carbon dioxide, steam, if appropriate hydrogen and, if appropriate, oxygen; C) product gas stream b is cooled, if appropriate condensed and steam is removed by condensation to obtain a steam-depleted product gas stream c; D) product gas stream c is contacted in a first absorption zone with a selective, inert absorbent which selectively absorbs propene to obtain an absorbent stream d1 laden substantially with propene and a gas stream d2 comprising propane, methane, ethane, ethene, carbon monoxide, carbon dioxide and hydrogen; E) if appropriate, the absorbent stream d1 is decompressed to a lower pressure in a first desorption zone to obtain an absorbent stream e1 laden substantially with propene and a gas stream e2 comprising propene, and gas stream e2 is recycled into the first absorption zone, F) from the absorbent stream d1 or e1 laden substantially with propene, in at least one second desorption zone, by decompression, heating and/or stripping the absorbent stream d1 or e1, a gas stream f1 comprising propene is released and the selective absorbent is recovered.

    Reactor for continuous oxide hydrogenation of feed gas flow of saturated hydrocarbons on moving catalyst bed, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating deflector plates
    16.
    发明专利
    Reactor for continuous oxide hydrogenation of feed gas flow of saturated hydrocarbons on moving catalyst bed, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating deflector plates 未知

    公开(公告)号：DE102006060509A1

    公开(公告)日：2008-06-26

    申请号：DE102006060509

    申请日：2006-12-19

    Applicant: BASF SE

    Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

    IPC: B01J8/02 ,  C07B35/04 ,  C07C5/333 ,  C07C11/06 ,  C07C11/08

    Abstract: The reactor (1) for continuous oxide hydrogenation of a feed gas flow (2) of saturated hydrocarbons, which are previously mixed with a gas flow (3) containing oxygen, on a moving catalyst bed (4) arranged between two concentric cylindrical holding devices (5, 6) in the longitudinal direction of the reactor by leaving a central inner space and an intermediate space, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating disk-type deflector plates arranged in the central inner space. The reactor (1) for a continuous oxide hydrogenation of a feed gas flow (2) of saturated hydrocarbons, which are previously mixed with a gas flow (3) containing oxygen, on a moving catalyst bed (4) arranged between two concentric cylindrical holding devices (5, 6) in the longitudinal direction of the reactor by leaving a central inner space and an intermediate space between the moving catalyst bed and an inner envelope of the reactor to obtain a reaction gas mixture, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating disk-type deflector plates arranged in the central inner space, and annular deflector plates arranged in the intermediate space between the moving catalyst bed and the inner envelope of the reactor. Each reactor sections comprise a mixing device, which is arranged in the direction of flow of the reaction gas mixture upstream of the moving catalyst bed. The mixing device is formed from two or three successively arranged rows of tubes having turbulence generators on the outer side of the tubes, which narrow the cross-section for the passage of the feed gas flow to 1/3-1/6 of the free cross-section. The oxygen-containing gas flow is guided through the tubes and sprayed into the feed gas flow through holes in the tubes in addition to a perforated plate mounted upstream of the tubes and a further perforated plate mounted downstream of the tubes. The tubes are ribbed tubes with the turbulence generators. The holes in rib gears are arranged between the ribs of the ribbed tubes. The ribbed tubes have 100-300 circulations of the ribs per meter length of the ribbed tubes, are formed from tubes with cylindrical outer circumference and are welded in spiral-shaped manner on the outer circumference along a strip longitudinal edge from a longitudinal strip containing ribs, which are notched under the formation of segments with exception of a rib base. An outer diameter of the tubes is 20-50 mm. A ratio of the height of the ribs to the outer diameter of the tubes is 1/10:1/2. The segments are distorted against the rib base in an angle. A thickness of the ribs is 0.3-1.5 mm and a width of the segments is 4-8 mm. The second row of the ribbed tubes is arranged in a gap to the first row of the ribbed tubes. The third row of the ribbed tubes is arranged in a gap to the second row of the ribbed tubes. The diameter of the holes in the upstream perforated plate is smaller than the half of the small distance of the ribs between two sequential circulations on each other. A ratio of the perforated plate thickness to the diameter of the holes in the perforated plate is 0.75:2.0. The diameter of the holes in the downstream perforated plate is larger or same to the diameter of the holes in the upstream perforated plate. The upstream perforated plate is arranged in a distance to flowing level of the first row of the ribbed tubes through the feed gas flow according to 7-20 times of the diameter of the holes in the upstream perforated plate. Two holes per rib gear are arranged between the ribs at diametrically opposite positions of the rib gears with small distance to the adjacent ribbed tubes in the row of the ribbed tubes. A ratio of the holes in the upstream perforated plate is defined as sum of the free surfaces of the holes in the upstream perforated plate related to the entire cross-section area vertical to the supply direction of the feed gas flow to the mixing device of = 0.3. The downstream perforated plate is spaced from the flowing level of the ribbed tubes around 0.5-2 times of the diameter of the ribbed tubes to the last row of the ribbed tubes. A distance of the downstream perforated plate for entering the reaction mixture into the catalyst bed is 5-20 times of the diameter of the holes in the downstream perforated plate. An independent claim is included for a procedure for continuous oxide hydrogenation of a feed gas flow of saturated hydrocarbons.

    СПОСОБ РЕГЕНЕРАЦИИ АДСОРБЕРА С ВОЗВРАТОМ ПРОДУКТА
    17.
    发明专利
    СПОСОБ РЕГЕНЕРАЦИИ АДСОРБЕРА С ВОЗВРАТОМ ПРОДУКТА 未知

    公开(公告)号：EA037477B1

    公开(公告)日：2021-04-01

    申请号：EA201790641

    申请日：2014-10-09

    Applicant: BASF SE

    Inventor： WAGNER HANS-GUENTER ,  BAYER CHRISTOPH ,  KARRER LOTHAR ,  RUETTER HEINZ ,  PIETZ PATRIK ,  CRONE SVEN ,  EGGERSMANN MARKUS ,  WONG KAM WING

    IPC: C10G25/00 ,  B01D53/04 ,  C07B63/00 ,  C10G25/12

    Abstract: Изобретениеотноситсяк способурегенерацииадсорбера (A1). Адсорбер (A1) регенерируютпутемконтактас газовымпотоком (S2), ивыходящийизадсорбера (A1) поток, содержащийконденсатпотока (S2) иорганическуюкомпозицию (OC1), собираютв устройстве. Послерегенерацииадсорбера (A1) поток (S2) вадсорбере (A1) замещаютполностьюили, какминимум, частичносодержимымустройства. Затемв адсорбер (A1) подаетсяорганическаякомпозиция, содержащая, какминимум, одинолефин, какминимум, одиналкани, какминимум, односоединение, содержащеекислороди/илисеру.

    Procedimiento de intercambio de calor para la regeneración de un adsorbedor
    18.
    发明专利
    Procedimiento de intercambio de calor para la regeneración de un adsorbedor 未知

    公开(公告)号：ES2733399T3

    公开(公告)日：2019-11-28

    申请号：ES14903801

    申请日：2014-10-09

    Applicant: BASF SE

    Inventor： WAGNER HANS-GUENTER ,  BAYER CHRISTOPH ,  KARRER LOTHAR ,  RUETTER HEINZ ,  PIETZ PATRIK ,  CRONE SVEN ,  EGGERSMANN MARKUS ,  WONG KAM WING ,  KIRCHNER GUENTHER ,  ZIMMER GABRIELE

    IPC: B01J20/34

    Abstract: Procedimiento para la regeneración de un adsorbedor (A) que comprende las siguientes etapas a) a d): a) calentar una corriente (S1) en al menos dos unidades de intercambio de calor (HEU1) y (HEU2), b) regenerar un adsorbedor (A) mediante el contacto con la corriente (S1) obteniendo, como flujo de salida del adsorbedor (A), una corriente (S2), c) hacer pasar la corriente (S2) a través de la unidad de intercambio de calor (HEU2), en el que la temperatura de la corriente (S2) alimentada a la unidad de intercambio de calor (HEU2) es mayor que la temperatura de la corriente (S1) alimentada a la unidad de intercambio de calor (HEU2) con el fin de transferir el calor de la corriente (S2) a corriente (S1), d) hacer pasar la corriente (S2) a través de la unidad de intercambio de calor (HEU1), en el que la temperatura de la corriente (S2) alimentada a la unidad de intercambio de calor (HEU1) es mayor que la temperatura de la corriente (S1) alimentada a la unidad de intercambio de calor (HEU1) con el fin de transferir el calor de la corriente (S2) a la corriente (S1), en el que i) las etapas c) y d) pueden ejecutarse en paralelo dividiendo la corriente (S2) en dos partes, ii) la etapa c) va seguida por la etapa d) y la temperatura de la corriente (S2) alimentada a la unidad de intercambio de calor (HEU2) es mayor o igual que su temperatura cuando se alimenta a la unidad de intercambio de calor (HEU1) y/o iii) temporalmente sólo una de las etapas c) y d) se lleva a cabo y en el que la regeneración del adsorbedor en la etapa b) comprende las siguientes etapas componentes b1) a b5): b1) calentar el adsorbedor (A) mediante el contacto con la corriente gaseosa (S1), en el que la corriente gaseosa (S1) se condensa dentro del adsorbedor, b2) calentar el adsorbedor (A) mediante el contacto con la corriente gaseosa (S1) hasta una temperatura en el intervalo de 230 a 270ºC sin ninguna condensación de la corriente gaseosa (S1) dentro del adsorbedor, b3) regenerar el absorbedor (A) a una temperatura en el intervalo de 230 a 270ºC mediante el contacto con la corriente gaseosa (S1), b4) enfriar el absorbedor mediante el contacto con la corriente gaseosa (S1), y b5) enfriar el absorbedor (A) mediante el contacto con la corriente líquida (S1) hasta una temperatura por debajo de 80ºC, preferiblemente hasta una temperatura en el intervalo de 40 a 60ºC, y en la etapa b), la etapa b1) va seguida por b2), seguida por b3), seguida por b4) y seguida por b5) y el calentamiento del adsorbedor no excede de 60ºC/h y la temperatura de la corriente gaseosa (S1) no es de más de 100ºC, mayor que el adsorbedor (A), especialmente durante la etapa de calentamiento b1) y/o b2) y la temperatura de la corriente gaseosa u opcionalmente líquida (S1) no es de más de 100ºC menor que el adsorbedor, especialmente durante las etapas de enfriamiento b4) y/o b5) y en el que la corriente (S1) se origina a partir de una composición orgánica que se ha purificado anteriormente mediante el mismo adsorbedor (A) o mediante un adsorbedor adicional similar durante el modo de operación del respectivo adsorbedor.

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