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    • 1. 发明授权
    • Manufacture of predominantly straight-chain aldehydes
    • 主要生产直链醛
    • US3941848A
    • 1976-03-02
    • US382277
    • 1973-07-24
    • Rudolf KummerHans-Juergen NienburgHeinz HohenschutzMax StrohmeyerTheo Teutsch
    • Rudolf KummerHans-Juergen NienburgHeinz HohenschutzMax StrohmeyerTheo Teutsch
    • B01J31/00B01J38/00C07B61/00C07C45/00C07C45/50C07C47/02C07C67/00C07C45/08
    • C07C45/50
    • An improvement in the process for the manufacture of predominantly straight-chain aldehydes by hydroformylation of olefinically unsaturated compounds of 2 to 20 carbon atoms with carbon monoxide and hydrogen in which, in a first stage, aqueous cobalt solutions are treated with carbon monoxide and hydrogen at temperatures of 50.degree. to 200.degree.C and pressures of 100 to 400 atmospheres in the presence of active charcoal, zeolites or basic ion exchangers which are charged with cobalt carbonyl, in a second stage cobalt carbonyl-hydride is extracted from the reaction mixtures thus obtained, at temperatures of 20.degree. to 180.degree.C and pressures of 1 to 400 atmospheres, by means of olefinically unsaturated compounds which must be water-insoluble and liquid under the conditions used, the aqueous phase is separated off and the organic phase is transferred to a third stage and in this stage, after introducing olefinically unsaturated compounds if the latter have only been used partially for the extraction, the hydroformylation is carried out at temperatures of 70.degree. to 170.degree.C and pressures of 100 to 400 atmospheres, the improvement being that the extraction in the second stage is carried out as a co-current extraction whilst maintaining turbulent flow.
    • 通过用一氧化碳和氢气将2-20个碳原子的烯属不饱和化合物加氢甲酰化制备主要是直链醛的方法的改进,其中在第一阶段中用一氧化碳和氢处理含钴水溶液 在由此得到的反应混合物中提取在第二阶段钴羰基氢化物中,在活性炭,沸石或带有羰基钴的碱性离子交换剂存在下,在50〜200℃的温度和100〜400个大气压的压力 在20〜180℃的温度和1〜400个大气压的压力下,通过烯烃不饱和化合物,在所用的条件下必须是不溶于水和液体的,分离出水相,将有机相转移到 在第三阶段,在这一阶段,如果后者仅部分用于前者,则引入烯属不饱和化合物 牵引,加氢甲酰化在70〜170℃的温度和100〜400个大气压的压力下进行,其改进在于,在保持湍流的同时进行第二阶段的萃取。
    • 6. 发明授权
    • Continuous production of ethanol and plural stage distillation of the
same
    • 连续生产乙醇和多级蒸馏相同
    • US4454358A
    • 1984-06-12
    • US337683
    • 1982-01-07
    • Rudolf KummerVolker TaglieberHeinz-Walter Schneider
    • Rudolf KummerVolker TaglieberHeinz-Walter Schneider
    • C07C29/132B01J31/00B01J31/20C07B61/00C07C27/00C07C27/04C07C29/149C07C29/80C07C29/92C07C31/08C07C67/00B01D3/00
    • C07C29/80C07C29/149C07C67/08C07C67/36C07C67/54Y02P20/52Y10S203/06Y10S203/20
    • Ethanol is produced continuously via the carbonylation of methanol, by(a) carbonylating methanol, in a reactor R, in the presence of a carbonyl complex of a metal of group VIII of the periodic table and of a halogen compound,(b) separating, in a distillation column D1, the reactor discharge, into a top fraction comprising methyl acetate, methanol, dimethyl ether and an organohalogen compound, and into a bottom fraction comprising water, small quantities of acetic acid and the catalyst, if the latter is not in a fixed bed, the residence time being so adjusted that the greater part of the acetic acid reacts with the methanol present to give methyl acetate,(c) separating the top fraction from D1, in a distillation column D2, into a top fraction comprising small quantities of methyl acetate, methanol, dimethyl ether and the organo-halogen compound, and a bottom fraction comprising methyl acetate and methanol, and recycling the top fraction to reactor R,(d) distilling off, via the top of distillation column D3, the greater part of the water from the bottom fraction from D1and removing this water from circulation, and recycling to reactor R the bottom fraction consisting of small quantities of water, acetic acid and the catalyst,(e) using hydrogen to hydrogenate, in the hydrogenation reactor H, the bottom fraction from D2, in a conventional manner, to give a mixture of methanol and ethanol, and(f) separating the mixture into ethanol and methanol in a distillation column D4, and recycling the methanol to reactor R.
    • 通过(a)在反应器R中羰基化甲醇,在周期表第VIII族金属的羰基络合物和卤素化合物的存在下,连续生产乙醇,(b)分离, 在蒸馏塔D1中,反应器排出成为包含乙酸甲酯,甲醇,二甲醚和有机卤素化合物的顶级馏分,并进入包含水,少量乙酸和催化剂的底部馏分,如果后者不在 固定床,停留时间如此调节,使得大部分乙酸与存在的甲醇反应得到乙酸甲酯,(c)将蒸馏塔D2中的顶馏分与D1分离成包含小分子的顶馏分 数量的乙酸甲酯,甲醇,二甲醚和有机卤素化合物,以及包含乙酸甲酯和甲醇的底部馏分,并将顶部馏分再循环到反应器R中,(d)通过顶部o蒸馏 f蒸馏塔D3,来自D1的底部馏分的大部分水从循环中除去,并且将反应器R再循环到由少量水,乙酸和催化剂组成的底部馏分,(e)使用氢气 以常规方式在氢化反应器H中将来自D2的塔底馏分氢化,得到甲醇和乙醇的混合物,和(f)将混合物在蒸馏塔D4中分离成乙醇和甲醇,并将甲醇再循环至 反应器
    • 9. 发明授权
    • Preparation of butanedicarboxylic acid esters
    • 丁烷二羧酸酯的制备
    • US4259520A
    • 1981-03-31
    • US2329
    • 1979-01-10
    • Rudolf KummerHeinz-Walter SchneiderFranz-Josef Weiss
    • Rudolf KummerHeinz-Walter SchneiderFranz-Josef Weiss
    • C07C67/38
    • C07C67/38
    • In a process for the preparation of butanedicarboxylic acid esters by(a) reacting butadiene or hydrocarbon mixtures containing butadiene with carbon monoxide and a C.sub.1 -C.sub.4 -alkanol in the presence of a tertiary nitrogen base and a cobalt carbonyl catalyst at from 80.degree. to 150.degree. C. under superatmospheric pressure,(b) removing the greater part of the tertiary nitrogen base together with any excess hydrocarbon and(c) reacting the resulting pentenoic acid ester, in the presence of the catalyst remaining in the reaction mixture, and in the presence of the remaining amount of tertiary nitrogen base, with carbon monoxide and a C.sub.1 - to C.sub.4 -alkanol at from 140.degree. to 200.degree. C. under superatmospheric pressure, to give the butanedicarboxylic acid ester, the improvement wherein the reaction mixture in stage c) is substantially free from dissolved butadiene or butadiene bonded to the catalyst.Butanedicarboxylic acid esters may be used for the preparation of polymers.
    • 在(a)将叔丁基或含有丁二烯的烃混合物与一氧化碳和C 1 -C 4烷醇在叔氮碱和羰基钴催化剂存在下反应制备丁烷二羧酸酯的方法中, (b)将大部分叔氮碱与任何过量的烃一起除去,和(c)使所得戊烯酸酯在残留在反应混合物中的催化剂存在下反应,并在 在超大气压下,在140℃至200℃下存在剩余量的叔氮碱,一氧化碳和一种C 1 -C 4烷醇,得到丁烷二羧酸酯,其中阶段c中的反应混合物 )基本上不含结合到催化剂上的溶解的丁二烯或丁二烯。 丁二羧酸酯可用于制备聚合物。