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    Removal and utilisation of carbon black formed in the cracking of hydrocarbons
    41.
    发明专利
    Removal and utilisation of carbon black formed in the cracking of hydrocarbons 未知

    公开(公告)号：GB893504A

    公开(公告)日：1962-04-11

    申请号：GB1023860

    申请日：1960-03-23

    Applicant: BASF AG

    Inventor： PLATZ ROLF ,  KROEPER HUGO

    IPC: C07C4/02 ,  C07C11/02

    Abstract: In the production of unsaturated hydrocarbons, e.g. ethylene or acetylene by cracking liquid or gaseous hydrocarbons in the gaseous phase with oxygen in a flame, carbon black produced is removed from the product by washing with a liquid hydrocarbon and the suspension is burned in the cracking chamber with an amount of oxygen capable of converting 1/3rd to 1/50th of the liquid hydrocarbon-carbon black mixture to carbon dioxide and water. In the drawing hydrocarbon enters the cracking chamber 1 by line 3 and oxygen by line 2. A liquid hydrocarbon quench is sprayed into the products at 4 and the products washed in scrubber 8 with liquid hydrocarbon. Liquid hydrocarbon containing carbon black collects in the sump of the scrubber and is cooled and recycled to the quench and the top of the scrubber, part being led off to the atomiser 12 with oxygen from line 2, a corresponding amount of fresh hydrocarbon being introduced from source 16.

    Process and apparatus for the dehydrogenation of hydrocarbons
    42.
    发明专利
    Process and apparatus for the dehydrogenation of hydrocarbons 未知

    公开(公告)号：GB853242A

    公开(公告)日：1960-11-02

    申请号：GB502959

    申请日：1959-02-13

    Applicant: BASF AG

    Inventor： KROEPER HUGO ,  PLATZ ROLF

    IPC: B01J8/26 ,  B01J8/28 ,  C07C4/06 ,  C07C5/32 ,  C07C5/333 ,  C07C5/367 ,  C10G11/18

    Abstract: In the catalytic dehydrogenation of hydrocarbons such as butanes, butenes, pentanes, pentenes, cyclohexane or petroleum naptha, using a fluidised bed of catalyst with simultaneous regeneration with an oxygen-containing gas, the regeneration bed is in communication only at its upper end with the cracking bed and, when the beds are side by side, ends a sufficient distance below the level of the cracking bed that sufficient exchange of catalyst occurs between the beds and the constitution and speed of the regenerating gas are regulated so that the oxygen is practically used up in the regeneration bed. The regeneration bed may be one or more tubes inside the cracking bed as shown in Fig. 1, or one or more coaxial annular spaces within the cracking bed. Alternatively an arrangement as shown in Fig. 3 may be used wherein the regeneration bed is wholly below the cracking bed, oxygen being introduced by pipe 14 and hydrocarbons by pipe 15 to distribution grid 16. Examples refer to the dehydrogenation of butylene or butane-butylene mixtures to butadiene of cyclohexane to benzene, of ethane to ethylene, of propane to propylene, of methyl butenes or methyl butene-isopentane mixtures to isoprene, of isobutane to isobutylene, and the cracking of a 40-80 DEG C. boiling range naphtha to ethylene, propylene, butylenes, pentylenes and light saturated hydrocarbons. A diluent gas or vapour may be added to the cracking or dehydrogenation reaction.

    44.
    发明专利
    未知

    公开(公告)号：FR1222886A

    公开(公告)日：1960-06-14

    申请号：FR786809

    申请日：1959-02-16

    Applicant: BASF AG

    Inventor： KROEPER HUGO ,  PLATZ ROLF

    IPC: B01J8/26 ,  B01J8/28 ,  C07C4/06 ,  C07C5/32 ,  C07C5/333 ,  C07C5/367 ,  C10G11/18

    Abstract: In the catalytic dehydrogenation of hydrocarbons such as butanes, butenes, pentanes, pentenes, cyclohexane or petroleum naptha, using a fluidised bed of catalyst with simultaneous regeneration with an oxygen-containing gas, the regeneration bed is in communication only at its upper end with the cracking bed and, when the beds are side by side, ends a sufficient distance below the level of the cracking bed that sufficient exchange of catalyst occurs between the beds and the constitution and speed of the regenerating gas are regulated so that the oxygen is practically used up in the regeneration bed. The regeneration bed may be one or more tubes inside the cracking bed as shown in Fig. 1, or one or more coaxial annular spaces within the cracking bed. Alternatively an arrangement as shown in Fig. 3 may be used wherein the regeneration bed is wholly below the cracking bed, oxygen being introduced by pipe 14 and hydrocarbons by pipe 15 to distribution grid 16. Examples refer to the dehydrogenation of butylene or butane-butylene mixtures to butadiene of cyclohexane to benzene, of ethane to ethylene, of propane to propylene, of methyl butenes or methyl butene-isopentane mixtures to isoprene, of isobutane to isobutylene, and the cracking of a 40-80 DEG C. boiling range naphtha to ethylene, propylene, butylenes, pentylenes and light saturated hydrocarbons. A diluent gas or vapour may be added to the cracking or dehydrogenation reaction.

    MANUFACTURE OF BUTANEDICARBOXYLIC ACID ESTERS
    48.
    发明专利
    MANUFACTURE OF BUTANEDICARBOXYLIC ACID ESTERS 未知

    公开(公告)号：CA1113491A

    公开(公告)日：1981-12-01

    申请号：CA298297

    申请日：1978-03-03

    Applicant: BASF AG

    Inventor： KUMMER RUDOLF ,  SCHNEIDER HEINZ-WALTER ,  PLATZ ROLF ,  MAGNUSSEN PETER ,  WEISS FRANZ-JOSEF

    IPC: C07C69/44 ,  B01J31/00 ,  C07B61/00 ,  C07C67/38 ,  C07C69/34

    Abstract: A process for the manufacture of butanedicarboxylic acid esters, whereina) an aqueous cobalt salt solution is treated, at from 50 to 200.degree.C and under a pressure of from 50 to 500 bars, with excess carbon monoxide and hydrogen in the presence of active charcoal laden with cobalt carbonyl,b) the resulting aqueous solution of cobalt carbonyl hydride is extracted with butadiene or with a hydrocarbon mixture containing butadiene and the aqueous phase is separated off,c) the butadiene, or butadiene-hydrocarbon mixture, containing cobalt carbonyl hydride, cobalt carbonyl and butenyl-cobalt tricarbonyl is reacted with carbon monoxide and an excess of an alkanol of 1 to 4 carbon atoms in the presence of from 0.5 to 2 moles, per mole of butadiene, of a tertiary nitrogen base having a pKa of from 3 to 11, at from 80 to 150.degree.C under a pressure of from 300 to 2,000 bars, andd) the resulting reaction mixture is freed from the tertiary nitrogen base contained therein, except for from 0.1 to 0.3 mole per mole of pentenoic acid ester, and from excess hydrocarbons, the pentenoic acid ester remaining in the reaction mixture is reacted with carbon monoxide and an excess of an alkanol of 1 to 4 carbon atoms at from 140 to 200.degree.C and under pressures of from 100 to 400 bars in the presence of the amounts of cobalt carbonyl and tertiary nitrogen base contained in the reaction mixture, and excess alkanol and free nitrogen base are then distilled off, ande) the reaction mixture which remains, and which contains cobalt catalyst, the butanedicarboxylic acid ester and by-products is treated with an oxidizing agent in an aqueous acid medium and the mixture is separated into an organic phase, from which the butanedicarboxylic acid ester is isolated by distillation, and into an aqueous phase containing cobalt salts. Butanedicarboxylic acid esters may be used for the manufacture of adipic acid and of nylons.

    MANUFACTURE OF BUTENEDIOL DIESTERS AND THEIR SECONDARY PRODUCTS
    49.
    发明专利
    MANUFACTURE OF BUTENEDIOL DIESTERS AND THEIR SECONDARY PRODUCTS 未知

    公开(公告)号：CA1095074A

    公开(公告)日：1981-02-03

    申请号：CA274099

    申请日：1977-03-16

    Applicant: BASF AG

    Inventor： WEITZ HANS M ,  PLATZ ROLF ,  HARTIG JUERGEN

    IPC: C07C69/16 ,  C07C27/00 ,  C07C27/02 ,  C07C31/20 ,  C07C67/00 ,  C07D307/08

    Abstract: O.Z. 31,903 In a process for the manufacture of butenediol-dicarboxylic acid esters by reacting butadiene with oxygen and a carboxylic acid in the presence of a noble metal catalyst containing platinum or palladium, the carboxylic acid is added to the reaction mixture in the form of the ester of the acid with a low molecular weight aliphatic alcohol such as methanol and the reaction is carried out under conditions under which the ester undergoes hydrolysis, or the hydrolysis is carried out before the main reaction. This enables the carboxylic acid obtained on further processing of the butenediol esters to be recycled.

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