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    11.
    发明专利
    未知

    公开(公告)号：DE1233858B

    公开(公告)日：1967-02-09

    申请号：DEB0055935

    申请日：1959-12-16

    Applicant: BASF AG

    Inventor： POEHLER DR GUENTER ,  WALDMANN DR HANS-JOACHIM ,  CORR DR HUBERT

    IPC: C07C45/82

    Abstract: Pure cyclohexanone is separated from mixtures, obtained by the oxidation of cyclohexane with oxygen followed by distilling off excess cyclohexane, by submitting the cyclohexane-free mixture to a multi-stage rectification process, one stage being carried out under a pressure of 300 mm. Hg. absolute to 5 atmospheres in order to remove low-boiling impurities such as amyl alcohol and aliphatic ketones, and another stage being carried out at a pressure of 1 to 300 mm. Hg. absolute whereby cyclohexanone is separated from cyclohexanol. These two stages may be conducted in either sequence. The difference in pressure between the two stages is preferably at least 300 mm. Hg. In an example, cyclohexane is oxidised with air, using cobalt naphthenate as catalyst, the reaction being carried out at a temperature of 140 DEG C. and a pressure of 25 atm. The oxidation-mixture is washed with water, and then re-oxidized. The oxidation-product is washed with water, then with caustic soda solution, then with water again. Excess cyclohexane is then removed from the mixture by distillation. The mixture is then submitted to rectification in the apparatus shown in the Figure. The mixture is first rectified under a pressure of 30 mm. Hg. absolute in column 2, which has sixty bubbletrays. With a reflux-ratio of 3:1 and a headtemperature of 63 DEG C., a cyclohexanonefraction is withdrawn through pipe 3 and condensed. The condensate is rectified under atmospheric pressure in column 4 using a reflux-ratio of 9 : 1. Low-boiling impurities are withdrawn through pipe 5. Cyclohexanone is withdrawn from the base of column 4, and is submitted to final purification in column 7, which is operated under a pressure of 30 mm. Hg. absolute. Pure cyclohexanone is obtained at the top of column 7. The residue withdrawn from the base of column 7 is returned to column 2 through pipe 10. The cyclohexanol fraction, withdrawn from the base of column 2, is distilled in column 12 at a pressure of 30 mm. Hg. absolute. Cyclohexanol, obtained as overhead-product from column 12, is passed over a copper catalyst, deposited on silicic acid, in dehydrogenator 17, which is maintained at 280 DEG to 320 DEG C. The cyclohexanone from the dehydrogenator may be passed via pipe 18 to column 2, or it may be freed from volatile by-products in column 20 and then passed via pipe 21 to column 7. In another example, the oxidation-mixture, already freed from cyclohexane, is first freed from low-boiling impurities by rectification under atmospheric pressure, and is then rectified at 30 mm. Hg. absolute to obtain pure cyclohexanone as distillate. Specifications 815,162 and 849,134 are referred to.

    13.
    发明专利
    未知

    公开(公告)号：DE1085165B

    公开(公告)日：1960-07-14

    申请号：DEB0052521

    申请日：1959-03-18

    Applicant: BASF AG

    Inventor： SUESSENGUTH DR HERMANN ,  MEIER DR HERMANN ,  CORR DR HUBERT ,  SIMON DR WALTER

    IPC: B01J23/34 ,  B01J23/50 ,  B01J23/70 ,  B01J37/08 ,  B01J37/14 ,  B01J37/18 ,  C07C209/36 ,  C07C209/48 ,  C07C209/72 ,  C07C241/02

    Abstract: A process for the hydrogenation of aromatic amino compounds and acyclic and carbocyclic compounds containing nitrogenous groups reducible to amino groups, wherein a hydrogenation of an aromatic ring to give a cycloaliphatic ring and a reduction of a nitrogenous group to give an amino group is achieved, comprises carrying out the hydrogenation in the absence of sulphur at a temperature between 40 DEG C. and 250 DEG C. under a pressure between 20 and 600 atmospheres in the liquid phase in the presence of at least one metal hydrogenation catalyst, the catalytic activity of which is impaired by sulphur, the catalyst having been sintered prior to the hydrogenation. The catalyst may contain, for example, silver, manganese, copper, iron, cobalt or nickel and may be prepared by sintering the oxide at 800 DEG C.-1,400 DEG C. and heating the sintered oxide with hydrogen at 250 DEG C.-600 DEG C. The catalyst may be supported on a carrier and promotors may be added. Aromatic amines may be hydrogenated at 200 DEG C.-250 DEG C. to give cycloaliphatic amines and other nitrogenous compounds containing, for example, nitro, nitroso, isonitroso and cyano groups may be hydrogenated at 60 DEG C.-150 DEG C. to give amino compounds. Other substituents such as aldehyde groups which are reduced and carboxylic, halogen, amino and alkoxy groups which are not reduced may also be present in the reactants. A list of suitable reactants is given. In the examples, ethylene diamine, cyclohexylamine, tolylene diamine, dimethyl hydrazine and isopropylamine are prepared.ALSO:Oxides of silver, manganese, copper, iron, cobalt or nickel are converted to the metal by sintering the oxide by heating for example, to a temperature within 20-60 DEG C. of the melting point and reducing the sintered oxide with a stream of hydrogen. Mixtures of metal oxides may be reduced after sintering to give alloys and in examples alloys of cobalt and aluminium and cobalt, nickel and aluminium are prepared.

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