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    • 15. 发明专利
      ES2344414T3 PROCEDIMIENTO PARA LA OBTENCION DE BUTADIENO. 未知
    • PROCEDIMIENTO PARA LA OBTENCION DE BUTADIENO.
    • ES2344414T3
    • 2010-08-26
    • ES04804421
    • 2004-12-30
    • BASF SE
    • JOHANN THORSTEN , SCHINDLER GOTZ-PETER , BRODHAGEN ANDREAS , CRONE SVEN , BENFER REGINA , HILL THOMAS
    • C07C5/333 , C07C5/48 , C07C11/167
    • 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.
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Espacenet 法律信息 同族专利 专利引用
    • 17. 发明专利
      DK1836146T3  未知
    • DK1836146T3
    • 2009-10-19
    • DK06700188
    • 2006-01-04
    • BASF SE
    • CRONE SVEN , MACHHAMMER OTTO , SCHINDLER GOETZ-PETER , BORGMEIER FRIEDER
    • C07C5/327 , C07C7/04 , C07C7/11
    • 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.
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Espacenet 法律信息 同族专利 专利引用
    • 18. 发明专利
      DE102006060509A1 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
    • 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
    • DE102006060509A1
    • 2008-06-26
    • DE102006060509
    • 2006-12-19
    • BASF SE
    • OLBERT GERHARD , CORR FRANZ , CRONE SVEN
    • B01J8/02 , C07B35/04 , C07C5/333 , C07C11/06 , C07C11/08
    • 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.
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