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    Chloride addition during hydrogenation
    6.
    发明授权
    Chloride addition during hydrogenation 失效
    加氢期间的氯化物添加

    公开(公告)号：US3639227A

    公开(公告)日：1972-02-01

    申请号：US3639227D

    申请日：1969-11-17

    Applicant: CHEVRON RES

    Inventor： JACOBSON ROBERT L ,  SPURLOCK BURWELL

    IPC: B01J27/13 ,  C10G45/52 ,  C10L1/14 ,  C10L1/18 ,  C10L1/24 ,  C10G23/04

    CPC classification number: B01J27/13 ,  C10G2400/08 ,  C10L1/14 ,  C10L1/18 ,  C10L1/22 ,  C10L1/24 ,  C10L1/2437

    Abstract: A process for hydrogenation of an unsaturated hydrocarbon feedstock at an elevated temperature and pressure in a hydrogenation zone by (a) contacting the feedstock, in the presence of hydrogen, with a hydrogenating catalyst containing at least one noble metal on an alumina support and containing no essentially irreversibly sulfided metal (such as nickel, cobalt, or molybdenum), and (b) adding a chloride to the hydrogenation zone and reacting the chloride with the catalyst in an amount sufficient to increase hydrogenation activity of the catalyst.

    Abstract translation: 一种在氢化区中在升高的温度和压力下氢化不饱和烃原料的方法，是通过（a）在氢存在下使原料与含有至少一种贵金属的氢化催化剂在氧化铝载体上接触而不含 基本上不可逆地硫化的金属（例如镍，钴或钼），和（b）向氢化区加入氯化物并使氯化物与催化剂反应，其量足以提高催化剂的氢化活性。

    Regeneration procedure for sulfur-contaminated hydroconversion unit
    7.
    发明授权
    Regeneration procedure for sulfur-contaminated hydroconversion unit 失效
    硫化氢化液单元再生程序

    公开(公告)号：US3617523A

    公开(公告)日：1971-11-02

    申请号：US3617523D

    申请日：1969-10-16

    Applicant: CHEVRON RES

    Inventor： SPURLOCK BURWELL

    IPC: B01J23/96 ,  C10G35/085 ,  B01J11/04

    CPC classification number: C10G35/085 ,  B01J23/96 ,  Y10S502/517

    Abstract: A platinum group component catalyst, used in a hydroconversion unit comprising a plurality of reactors in series, is regenerated to remove carbonaceous matter from the catalyst without contaminating the catalyst with sulfur compounds by purging the hydroconversion unit of hydrocarbons, circulating an inert gas through the hydroconversion unit at a pressure of from 50 to 1000 p.s.i.g., controlling the inlet temperature in all but the terminal reactor to below about 500* F. while controlling the inlet temperature in the terminal reactor at from 500* to 700* F., then introducing an oxygen-containing gas into the terminal reactor to remove carbonaceous matter from the catalyst but insuring that the oxygen is discontinued when the exit stream from the terminal reactor contains more than about 0.1 volume percent oxygen.

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