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    Oxidation catalyst containing vanadium and titanium
    38.
    发明专利
    Oxidation catalyst containing vanadium and titanium 未知

    公开(公告)号：GB1140264A

    公开(公告)日：1969-01-15

    申请号：GB2178166

    申请日：1966-05-17

    Applicant: BASF AG

    Inventor： FRIEDRICHSEN WILHELM ,  GOEHRE OTTO

    IPC: B01J23/22 ,  B01J23/24 ,  B01J23/68 ,  B01J23/84 ,  B01J23/89 ,  B01J37/02 ,  C07C51/215 ,  C07C51/25 ,  C07C51/265 ,  C07C51/31

    Abstract: 1,140,264. Oxidation of hydrocarbons. BADISCHE ANILIN- & SODA-FABBIK A.G. 17 May, 1966 [18 May, 1965], No. 21781/66. Heading C2C. [Also in Division B1] Aromatic hydrocarbons may be oxidized to carboxylic acids, for example o-xylene may be oxidized to phthalic anhydride+maleic anhydride, using a catalyst consisting of an inert porous carrier coated with a 0À02 to 2 mm. thick layer of a composition containing 1% to 15% by weight of vanadium pentoxide and 85% to 99% by weight of titanium dioxide, the catalyst containing from 0À05% to 3% by weight of vanadium pentoxide. In the examples, vapour phase o-xylene and air are passed over the catalyst in a tube heated by a salt-bath, the reaction temperature being: (1), (4), and (5) 400‹ C.; (2) and (7) 390‹ C.; (3) 380‹ C.; (6) 410‹ C. Also mentioned are oxidation of propylene to acetic acid; butene-(1 butene-(2) or butadiene-(1,3) to maleic acid; benzene to maleic acid; naphthalene to phthalic acid; toluene to benzoic acid; methyl naphthalenes to naphthoic acids; durene to pyromellitic acid.

    Production of phthalic anhydride
    39.
    发明专利
    Production of phthalic anhydride 未知

    公开(公告)号：GB1082326A

    公开(公告)日：1967-09-06

    申请号：GB5151664

    申请日：1964-12-18

    Applicant: BASF AG

    Inventor： FRIEDRICHSEN WILHELM ,  GOEHRE OTTO

    IPC: B01J21/06 ,  B01J23/04 ,  B01J23/22 ,  C07C51/265 ,  C07C51/31

    Abstract: Naphthalene or o-xylene is oxidized to phthalic anhydride with oxygen or gases containing same at 250 DEG to 420 DEG C. in the vapour phase in contact with a supported catalyst containing a vanadium compound and at least one alkali metal pyrosulphate such that the V content (calculated as V2O5) is 0.5 to 15% and at least 50% but not more than 90% of the V is present as V4+ and at least 10% as V5+. Maleic anhydride is mentioned as a by-product.ALSO:A supported catalyst containing a mixture of V2O5 and an alkali metal pyrosulphate in which at least 50% and not more than 90% of the vanadium is present as V4+ and at least 10% is present as V5+ is prepared by mixing V2O5 and alkali metal pyrosulphate with particles of TiO2 at a temperature of more than 500 DEG C. at which the mixture is molten. Additionally the catalyst may contain P2O5, MoO3, WO3, AlPO4, C, H2SiO3, Ce2O3, Al2O3, pumice, a natural or synthetic silicate, silica gel, Ag2O or CuO. Preferably the carrier has a low surface area, e.g. 2-50 sq. m/gm.

    Tube reactors
    40.
    发明专利
    Tube reactors 未知

    公开(公告)号：GB1004234A

    公开(公告)日：1965-09-15

    申请号：GB4888263

    申请日：1963-12-11

    Applicant: BASF AG

    Inventor： POEHLER GUENTER ,  WEGERICH ANTON ,  GOEHRE OTTO ,  GIEHNE HELLMUT

    IPC: B01J8/06 ,  B01J19/24 ,  C07C45/00

    Abstract: A catalytic dehydrogenation reactor, e.g. for dehydrogenating paraffins and naphthenes comprises a plurality of tubes each having a diameter of at least 70 mm. arranged in a reactor so as to leave a central free space and baffles arranged perpendicularly to the tubes and alternately at the reactor wall and in the central space to deflect a gaseous heating medium which is passed between the tubes in the same direction as reactants are passed through the tubes. The ratio of diameter to length of the tubes may be 12-17 : 1000 with a diameter of 70-120 mm. and a length of 5-12 m. The free space in the centre of the reactor may be 7-25% of the total cross-sectional area. The baffles are alternate central circular baffles occupying 25-60% of the total cross-sectional area extending into the section containing tubes and outer annular baffles occupying 50-75% of the total area. The baffles, particularly in the tubed area, may have perforations, e.g. 3-10 mm. in diameter. The tubes may be spaced 15-60 mm. from each other. Heating medium is preferably introduced by an annular duct 2 surrounding the reactor. The medium is divided into two streams by a baffle 9 which flow in opposite directions round the reactor and enter the reactor through slots which increase in size in the direction of flow. The heating medium is withdrawn by a similar duct 5 and is reheated and re-used. The ducts 2 and 5 may have a cross-sectional area 5-20% that of the reactor.ALSO: A catalytic dehydrogenation reactor e.g. for converting alcohols to ketones comprises a plurality of tubes each having a diameter of at least 70 mm. arranged in a reactor so as to leave a central free space and baffles arranged perpendicularly to the tubes and alternately at the reactor wall and in the central space to deflect a gaseous heating medium which is passed between the tubes in the same direction as reactants are passed through the tubes. The ratio of diameter to length of the tubes may be 12-17 : 1,000 with a diameter of 70-120 mm. and a length of 5-12 cm. The free space in the centre of the reactor may be 7-25% of the total cross sectional area. In Fig. 1 the baffles 4 are alternate central circular baffles occupying 25-60% of the total cross-sectional area extending into the section containing tubes and outer annular baffles occupying 50-75% of the total area. The baffles, particularly in the tubed area, may have perforations, e.g. 3-10 mm. in diameter. The tubes may be spaced 15-60 mm. from each other. Heating medium is preferably introduced by an annular duct 2 surrounding the reactor. The medium is divided into two streams by a baffle 9 which flow in opposite directions round the reactor and enter the reactor through slots which increase in size in the direction of flow. The heating medium is withdrawn by a similar duct 5 and is reheated and reused. The ducts 2 and 5 may have a cross-sectional area 5-20% that of the reactor. In examples cyclohexanol is converted to cyclohexanone and sec.-butanol to methyl ethyl ketone.

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