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    • 37. 发明授权
    • Process for the preparation of a hydrogenation catalyst
    • 制备氢化催化剂的方法
    • US5817592A
    • 1998-10-06
    • US590455
    • 1996-01-23
    • Daniel HeinekeHeinz-Walter SchneiderAlfred Thome
    • Daniel HeinekeHeinz-Walter SchneiderAlfred Thome
    • B01J23/42B01J23/96B01J37/16B01J38/64C01B21/14B01J21/18B01J23/16B01J27/185
    • B01J23/42B01J37/16C01B21/1418
    • A process for the preparation of a hydrogenation catalyst by reduction of platinum in an oxidation stage of not less than 2 in an aqueous medium in the presence of a carboniferous support, optionally following partial poisoning with a sulfur, arsenic, tellurium, or antimony-containing compound, using a reducing agent, in which the reducing agent used is an ammonium or phosphonium salt of the general formula I �XR.sup.4 !.sub.n Y I in which X stands for N or P, R stands for hydrogen, C.sub.1 --C.sub.18 alkyl, C.sub.5 --C.sub.10 cycloalkyl, phenyl radical, and also a C.sub.1 --C.sub.4 alkyl radical substituted by phenyl, the phenyl radicals being mono-to tri-substituted by C.sub.1 --C.sub.6 alkyl, halogen, nitro or amino, if desired, provided that the radicals R may be the same or different but cannot simultaneously denote hydrogen, if X is P, n is an integer of 1 to 3, and Y is an organic anion which can reduce platinum in an oxidation stage other than zero to platinum in the oxidation stage of zero.
    • 一种通过在含水载体的存在下在水性介质中在不少于2的氧化阶段还原铂的氢化催化剂的方法,任选地在用硫,砷,碲或含锑的部分中毒后 化合物,使用还原剂,其中所用的还原剂是通式I [XR4] nYinin的铵盐或鏻盐,其中X代表N或P,R代表氢,C1-C18烷基,C5-C10环烷基 苯基,以及被苯基取代的C1-C4烷基,如果需要,苯基由C1-C6烷基,卤素,硝基或氨基单取代至三取代,条件是基团R可以相同 或不同,但不能同时表示氢,如果X为P,n为1至3的整数,Y为有机阴离子,在氧化阶段为零的情况下,铂可以在除氧以外的氧化阶段中还原为铂。
    • 38. 发明授权
    • Method for the complete hydrodechlorination of chlorinated hydrocarbons
    • 氯代烃完全加氢脱氯的方法
    • US5811628A
    • 1998-09-22
    • US504628
    • 1995-07-20
    • Klaus WeberRainer SchoedelPeter BirkeReinhard GeyerUlrich NeumannWerner HaertwigGerhard VogelWilli SattelmayerRudolf SchumannAnette Hoppe
    • Klaus WeberRainer SchoedelPeter BirkeReinhard GeyerUlrich NeumannWerner HaertwigGerhard VogelWilli SattelmayerRudolf SchumannAnette Hoppe
    • A62D3/00B01D53/86B01J23/96B01J38/10B01J38/12C07C1/26B01J20/34
    • B01J38/12B01D53/8662B01J23/96B01J38/10
    • A method for the hydrodechlorination of a reaction gas primarily composed of chlorinated hydrocarbons is carried out sequentially. A first step is advantageously carried out in a tubular reactor filled with catalyst and cooled externally, to maintain a temperature within a preferred range of 80.degree. to 230.degree. C. and a radial temperature difference of not more than 40.degree. C. Hydrogen is added to the tubular reactor with a hydrogen excess in a preferred range of 1.1 to 1.5 relative to the reaction gas, based on the stoichiometric consumption. The catalyst is present in a catalyst loading in a preferred range of 0.1 to 1.5 v/vh based on the volume of reaction gas. A fixed bed reactor is advantageously used for a second step, optimally connected in straight transit with the output of the reactor of the first step. The full-space reactor is maintained at a temperature within a preferred range of 200.degree. to 300.degree. C. and a hydrogen excess relative to the stoichiometric consumption is in a preferred range of 2 to 100. Catalyst is present in a preferred amount related to a volume of catalyst in step one according to a ratio in a range of 2:1 to 10:1. The dechlorination is preferably carried out at pressures between 1 and 50 bar. A method is further provided for regenerating deactivated catalysts without accumulation of dioxin in the waste gas, achieved by a reducing treatment, followed by an oxidizing treatment at a temperature at or above the last operating temperature of the catalyst.
    • 依次进行主要由氯代烃组成的反应气体的加氢脱氯的方法。 第一步有利地在填充有催化剂的管式反应器中进行并在外部冷却,以将温度保持在80℃至230℃的优选范围和不超过40℃的径向温度差。加入氢气 基于化学计量消耗,相对于反应气体,相对于反应气体,优选范围为1.1〜1.5的氢过渡到管式反应器。 基于反应气体的体积,催化剂以0.1至1.5v / vh的优选范围存在于催化剂负载中。 固定床反应器有利地用于第二步骤,最佳地连续地与第一步骤的反应器的输出相连。 全空间反应器保持在200℃至300℃的优选范围内的温度,相对于化学计量消耗的氢过量在优选的范围为2至100.催化剂以优选的量存在 根据比例在2:1至10:1的范围内的步骤1中的催化剂体积。 脱氯优选在1至50巴之间的压力下进行。 还提供一种方法,用于再生失活的催化剂,而不会在废气中积聚二恶英,通过还原处理实现,然后在等于或高于催化剂的最后操作温度的温度下进行氧化处理。