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    1.
    发明专利
    未知

    公开(公告)号：FR1500050A

    公开(公告)日：1967-11-03

    申请号：FR65840

    申请日：1966-06-17

    Applicant: BASF AG

    Inventor： BUSCHMANN KARL ,  EDER KURT ,  SCHMULDER PAUL

    IPC: B01F23/10 ,  C01B3/36

    Abstract: 1,141,888. Making fuel gas. BADISCHE ANILIN- & SODA-FABRIK A.G. 17 June, 1966 [18 June, 1965], No. 27161/66. Heading C5E. An apparatus for mixing gaseous and vaporous hydrocarbons with air or oxygen, optionally with steam, for flameless catalytic partial combustion reactions, comprises inner and outer tubes 1, 7 respectively, a spindle 2 in the tube 1 carrying guide blades 3 and a member 4, and a mechanism 5 connected to the spindle 2 for axial adjustment thereof to enable the member 4 to regulate the outlet cross-section of the tube 1. The mechanism 5 may be automatically controlled, e.g. by a device 9 responsive to the pressure difference across the tubes 1, 7. Hydrocarbon is delivered by the tube 7, and air &c., with or without steam, by the tube 1, the amount of air &c. being thus controlled to match the richness of the hydrocarbon. The tubes 1, 7 lead to a diffuser 8 which communicates with a catalyst chamber.

    Flameless cracking of gaseous and/or liquid vaporisable hydrocarbons having from twoto thirty carbon atoms
    3.
    发明专利
    Flameless cracking of gaseous and/or liquid vaporisable hydrocarbons having from twoto thirty carbon atoms 未知

    公开(公告)号：GB1129114A

    公开(公告)日：1968-10-02

    申请号：GB4854165

    申请日：1965-11-16

    Applicant: BASF AG

    Inventor： KNOBLOCH WALTER ,  NONNENMACHER HELMUT ,  RALL WOLFGANG ,  SCHMULDER PAUL

    IPC: B01J23/70 ,  C01B3/38 ,  C01B3/40

    Abstract: 1,129,114. Making combustible gas. BADISCHE ANILIN- & SODA-FABRIK A.G. 16 Nov., 1965 [17 Nov:, 1964], No. 48541/65. Heading C5E. A process for the flameless catalytic cracking of gaseous and liquid vaporizable hydrocarbons having 2 to 30 C atoms per molecule with steam and insufficient O 2 for complete combustion, optionally with CO 2 , to produce H 2 and CO, utilizes a catalyst which has been calcined at 1300‹ to 1400‹ C., and comprises cobalt on a carrier material of MgO, optionally with Al 2 O 3 .The process allows feedstocks containing up to 1 g. of sulphur per Kg. of feed to be cracked without a pretreatment. Feeds mentioned are gasoline fractions (B.P.R. 40‹ to 160‹ C.) and gas oils (B.P.R. 65‹ to 360‹ C.), and gaseous hydrocarbons containing up to 90 vol. per cent unsaturates. The reactants are preheated, and the process may be performed at atmospheric or superatmospheric pressure. A conventional Pt catalyst may precede the CO catalyst. Details of the main catalyst are: cobalt content, 3 to 40% b.w. (preferably 5 to 25%) and ZrO 2 or an alkali metal compound may be added to the carrier, e.g. from 0À5 to 10% b.w. Two specific examples are described.

    Flameless reaction of liquid hydrocarbons to form carbon monoxide and hydrogen
    7.
    发明专利
    Flameless reaction of liquid hydrocarbons to form carbon monoxide and hydrogen 未知

    公开(公告)号：GB1049749A

    公开(公告)日：1966-11-30

    申请号：GB3396863

    申请日：1963-08-28

    Applicant: BASF AG

    Inventor： BUSCHMANN KARL ,  EDER KURT ,  SCHMULDER PAUL

    IPC: C01B3/38

    Abstract: A process for making a mixture of hydrogen and carbon monoxide comprises reacting vaporizable liquid hydrocarbons with amounts of oxygen insufficient for complete combustion over a platinum catalyst in a first stage and completing the reformation of the hydrocarbons by reaction with steam and carbon dioxide over a nickel catalyst in a second stage, the reaction mixture, prior to contacting the platinum catalyst, being passed through a layer of an inert granular material of poor thermal conductivity which is free from heavy metals and heavy metal compounds. Granular materials mentioned are ceramics, highly pored alumina, aluminium silicate, or blocks of porous magnesium oxide. The process is carried out in an apparatus similar to that described in Specification 834,595. Steam and/or carbon dioxide may be reacted in the first stage, e.g. after mixing with the hydrocarbons, e.g. light naphthas, and with the oxygen, and after the mixtures have been preheated, e.g. to 200 DEG to 400 DEG C. The steam and carbon dioxide required for the second stage are provided by the reaction in the first state.ALSO:A process for making a mixture of hydrogen and carbon monoxide comprises reacting vaporizable liquid hydrocarbons with amounts of oxygen insufficient for complete combustion over a platinum catalyst in a first stage and completing the reformation of the hydrocarbons by reaction with steam and carbon dioxide over a nickel catalyst in a second stage, the reaction mixture, prior to contacting the platinum catalyst, being passed through a layer of an inert granular material of poor thermal conductivity which is free from heavy metals and heavy metal compounds. Granular materials mentioned are ceramics, highly pored alumina, aluminium silicate, or blocks of porous magnesium oxide. The process is carried out in an apparatus similar to that described in Specification 834,595. Steam and/or carbon dioxide may be reacted in the first stage, e.g. after mixing with the hydrocarbons (e.g. light naphthas), and with the oxygen, and after the initial materials have been preheated, e.g. to 200 DEG to 400 DEG C. The steam and carbon dioxide required for the second stage are provided by the reaction in the first stage.

    Production of fuel gas and synthesis gases
    9.
    发明专利
    Production of fuel gas and synthesis gases 未知

    公开(公告)号：GB972263A

    公开(公告)日：1964-10-14

    申请号：GB3414762

    申请日：1962-09-06

    Applicant: BASF AG

    Inventor： EDER KURT ,  SCHMULDER PAUL

    IPC: C01B3/30 ,  C01B3/38

    Abstract: A process for the production of fuel gases and synthesis gases by cracking gaseous and liquid hydrocarbons, e.g. natural gas, in a heated fluidized bed, in the presence of catalysts containing Gp. 8 metals or compounds of the metals with or without the addition of steam and/or CO2, heat necessary for cracking being produced by partial combustion of the initial materials with the oxygen and/or oxygen-containing gases, wherein the catalyst is replenished by the introduction of a decomposable compound of the catalytically active metal into the fluidized bed. The catalyst may be nickel, cobalt, or platinum, and is preferably nickel or nickel compounds. Examples of the decomposable materials are nickel nitrates, carbonates and acetates in aqueous solution, and nickel carbonyl in alcoholic solution. These solutions may be sprayed into the beds through one or more nozzles with compressed nitrogen or gaseous hydrocarbons. The temperature may be between 700 DEG and 1000 DEG C. The fluidized bed may be of magnesite, sillimanite sand, or corundum sand, and the hydrocarbons and steam may be the fluidizing agent. A portion of the initial material may be precombusted with oxygen containing gas in a separate chamber and the resulting hot gases may be used as the fluidizing agent.

    Continuous Catalytic Cracking of Gaseous and/or Vaporisable Hydrocarbons
    10.
    发明专利
    Continuous Catalytic Cracking of Gaseous and/or Vaporisable Hydrocarbons 未知

    公开(公告)号：GB1156156A

    公开(公告)日：1969-06-25

    申请号：GB5041866

    申请日：1966-11-10

    Applicant: BASF AG

    Inventor： BUSCHMANN KARL ,  KNOBLOCH WALTER ,  SCHMULDER PAUL ,  SCHWEITZER ARMIN

    IPC: A47F3/04 ,  C01B3/38

    Abstract: 1,156,156. Making combustible gas. BADISCHE ANILIN- & SODA-FABRIK A.G. 10 Nov., 1966 [11 Nov., 1965], No. 50418/66. Heading C5E. In a process for continuously cracking gaseous and/or vaporizable hydro-carbons, e.g. methane, natural gas, and liquefied low boiling hydrocarbons, with steam and optionally with oxygen, to produce H 2 - and CO-containing gases, the feed is passed through a bed of catalyst located in the annular space between inner and outer concentric tubes, the bed being heated by direct firing of the walls of both the tubes. The source of heat for the inert tube is one or more burners, preferably a single longitudinal burner, at one end of the tube, and several burners normal to the external wall of the outer tube. The tubes may be cylindrical or conical, and may be corrugated on the faces contacting the catalyst, which is preferably nickel and may contain alkali metal oxides. Preferred temperatures are 700‹ to 900‹ C., and pressures up to 50 atmos are mentioned. The object of the invention is to prevent a temperature gradient across the catalyst.

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