• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
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  • 优先权
    • 专利摘要:
    Hydrocarbon oils of which more than 70% by volume boils above 360 DEG C, which have a C5 asphaltene content of less than 2.5% by weight and of which the total vanadium and nickel content is 5-150 ppmw, are demetellized by contacting them at elevated temperature and pressure and in the presence of hydrogen with a catalyst containing as metal with hydrogenation activity exclusively molybdenum in a quantity of more than 2.0 parts by weight per 100 parts by weight of porous carrier, which catalyst has such an average pore diameter (p) and average particle diamter (d) that the relation: 7.0.10<-><3>.(PH2)<2> > p/d<0.5> > 1.4.10<-><3>.(PH2)<2>, where PH2 represents the hydrogen partial pressure used (p in nm, d in mm, PH2 in bar), is fulfilled.
    公开号:SU1225493A3
    申请号:SU813287901
    申请日:1981-05-27
    公开日:1986-04-15
    发明作者:Ван Дер Эйк Хуно；Матиас Хендрикус Дирке Якобус
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    catalytic demetallization of heavy hydrocarbon feedstock before its conversion.
    but with hydrogen from top to bottom through vertically located
    The fixed cylinder reactor The purpose of the invention is a semi-5 catalyst bed at 375 ° C, P 60,
    Improved quality of raw materials for catalytic processes.
    Example. 15 catalysts (1-15) are used to demetallize six types of hydrocarbon feedstocks (A-F). Demetallization is carried out on-.
    four
    four
    6
    four
    1.5
    0.5
    1.5
    one
    3
    four
    0.5 2.5 10
    Moe
    Moe
    Moe
    Moe
    Moe
    Ni / 2V
    Ni / 6V
    Ni / 4Mo
    Ni / 8Mo
    Cr
    W
    Ni / 2V
    Mo
    Mo
    SiO,
    SiO.,
    SiO,
    SiO,
    SiO,
    Sio
    Sio
    Sio
    Al, 0 SiO
    SiO.
    SiO,
    Sio
    SiO,
    Raw material A is obtained by flash evaporation of the residue after atmospheric distillation of South American crude oil and deasphalting of the resulting residue with butane.
    Raw B is a mixture of distillate after instant evaporation and deasphally with hydrogen from top to bottom through vertically located
    75 or 150 bar, the space velocity is 2 KG KG .. and the ratio between hydrogen and raw materials is 1000. The properties of the catalysts, which are used in the sulfide form, with the exception of catalyst 12, are listed in Table. one.
    Table 1

    11 60 10 10 12 10
    9 10 13 11 11 11 60
    9 10
    1.5

    1.5
    3.0 1.5 1p5 1.5 1.5 1.5 1/5 1.5 1.5 1.5 1.5 1.5
    9.0 49.0 8.2 5.8 9.8 8.2 7.3 8.2 10.6 9.0 9.0 9.0 49.0 7.3 8.2
    tizatsii. Raw material B is obtained from the residue of atmospheric distillation of South African crude oil by sequential evaporation and deasphalting of the raw material at a ratio obtained under production conditions.
    150
    150 60
    150 60150 60 75 75 60 60
    D
    Continuation of table. 3


    3.2
    4.0
    10 ,, 2 1,9 4,8 0,4 3,6 3 ,, 1 3,1 3,8
    1.7
    0.6
    2.4
    6.0
    1.0
    2.5
    0.15
     3) -
    2 „0
    Oh 15
    0.1
    0.15
    0.25
    0.1
    0.2
    0.15
    0.1
    0.1
    0.1
    0.15
     As a result of low activity o; determine the value of M,
    Pszzde the mode of operation of catalysts is estimated on the basis of M „„ „,
    , -flL4r.v,
    K,, K,.; and ps
    .ottc is the maximum amount of MZ-T2l.p (vanadium and nickel), expressed 8,% ;;: mass amount of fresh catalyst J which can be ad-:; orbited from the pores of the catalyst particles,
    To catalr / congestion activity, height-in kg-kg. after half the life of the catalyst (in units of the amount of adsorbed M2 gall), the K value is calculated by the formula
     2 1p
    May .. h, mln, dl
    Vanadium raw materials
    May..h, i-Fn. for
    vanadium tzprodukteK, |. - activity of catarrh of congestion; expressed in kg. , after half the service life of the catalyst (in units of quantity a /; sorbed metal)., The value is calculated by the formula
    catalyst 12 is impossible
    May., h, ppm for Zn nickel in the feedstock
    ma.ch about per million, for nickel in the product
     The consumption of hydrogen is expressed by the formula
    Hydrogen consumption
    May, h, per million. spent hydrogen
    X 100%
    May, h, processed raw materials:
    The behavior of the catalyst is considered to be xopoJui-tMj if, during demetallization of raw material A under the specified conditions, the following estimated indicators are provided by the reaction committee: M. .. 30% maso | K, Z., 0 kg. kg dh; KM, 1.5 kg, kg, hydrogen consumption is less than O, 2%.
    Among the experiments 1-24 listed in table. 3j experiments 1J 3, 4 ,. 14, 16 and 19, 21-24 were carried out according to the proposed method. In these experiments, when demetallizing heavy hydrocarbon feedstocks, catalysts were used, containing hydrogenated as the metal active in the mouth, exclusively molybdenum in an amount greater than 2.0 mph . on May 100, h porous carrier. Starting from a particular p / d, Pj is applied within the range prescribed by the ratio. In experiments 1, 3, 4 and 14, carried out with raw material A, the estimated indicators relating to, K, K (,; and hydrogen consumption and characterizing a good catalyst, were fully satisfied. A satisfactory behavior of the catalyst was also observed in experiments 16 and 19,
    Experiments 2, 5-13, 15, 17, 18 and 20 are comparative. In experiments 2, 5-13 and 15, carried out with raw material A, at least one estimated
    indicator for M,
    ladks
     . and hydrogen consumption.
    In experience 2, the PU is too low
    WHAT leads to low K values
    and K
    In experiment 5 applied catalyst with a low content of molybdenum; In experiments 6, 7, 10, 11, and 15, catalysts were used which contain, instead of molybdenum, nickel / vanadium, nickel / vanadium, chromium, tungsten, and nickel / vanadium, respectively; in experiment 12, a caliser was used that does not contain a component in the form of a metal. In all these experiments, the estimated values for K and Cc are not met; characterized by a good demetallization catalyst,
    In experiments 8 and 9, catalysts containing nickel in addition to molybdenum were used; in carrying out these experiments is not satisfied
    Compiled by E. Gorlov Editor A. Lezhnin Tehred M. Moregtal
    Order 1972/63 Circulation 482 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow. Zh-35, Raushsk nab, 4/5
    Production and printing company, Uzhgorod, st. Project, 4
    indicator for hydrogen consumption and, moreover, K and K indicators are not met,
    M.
    maize
    necessary for a good demetallization catalyst.
    Although in experiments 5-12 and 15, the value of Р Tajtoe is applied, that for the ratio, the catalyst satisfies the ratio of 7.0.10 (P) 1.4 V10-i (Рц) 2, unsatisfactory results are still obtained, that when conducting - the experiments cited used
    5 catalysts that do not meet the requirement: the catalyst must contain, as a metal having activity with respect to hydrogenation, only molybdenum in an amount exceeding 2.0 May, h, per 100 May, h, porous carrier,
    In Test 17, an excessively high P was used to demetalize a high boiling hydrocarbon feedstock.
    5 which results in a low max.
    Although in test 20 a catalyst was used containing
    only molybdenum in an amount greater than 2.0 mach. h, and 100 May, h, of a porous carrier, as well as an experiment was conducted with a P value that is in the range dictated by the particular p / d °, however, unsatisfactory results were obtained ( -. Lemo low N. and Kj;). This is due to the fact that in test 20, raw material B was used as a feedstock, which does not belong to the group of heavy hydrocarbon raw materials,
    Proofreader A. T sko
    权利要求:
    Claims (3)
    [1]
    1. METHOD FOR DEMETALLIZING HEAVY-HYDROCARBON RAW MATERIAL, 76-100 r L of which boils at a temperature above 360 ° C, containing asphaltenes and 9-85 parts of nickel and vanadium per 1 million parts by weight, by contacting the raw material at elevated temperature and pressure in the presence of hydrogen and a catalyst containing, as a hydrogenating compound, molybdenum in the form of a metal, oxide and / or sulfide in an amount of 2.5-10 parts by weight molybdenum per 100 m.h. porous silicon dioxide, characterized in that, in order to obtain improved quality raw materials for catalytic processes, use raw materials containing 0,092,4 may L With -asphaltenes, and the catalyst has a pore size and an average particle diameter at which the ratio
    7.0 1 (r 3 x (P Hj ) 2 P / jSl, 4 -10- '(P „) 2 where P and is the partial pressure of hydrogen, bar;
    p is the average pore size of the catalyst β , nm; ® d - average particle size of the catalyst, mm
    [2]
    2. The method of pop. 1, characterized in that as the starting material using a mixture obtained by mixing distillates of atmospheric or vacuum distillation and deasphalting deasphalting residues of distillation of oil.
    [3]
    3. The method of pop. 1, characterized in that it is carried out at 375 ° C, a partial pressure of hydrogen of 60-150 bar and a volumetric feed rate of 2 hours *.
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    同族专利:
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    MY8500921A|1985-12-31|
    FI70920B|1986-07-18|
    NO162971C|1990-03-14|
    JPH0253478B2|1990-11-16|
    ZA813550B|1982-08-25|
    ES502521A0|1982-10-01|
    DE3161111D1|1983-11-10|
    NO162971B|1989-12-04|
    PH17039A|1984-05-17|
    BR8103315A|1982-02-16|
    ES8300133A1|1982-10-01|
    NZ197216A|1983-05-31|
    NO811805L|1981-11-30|
    EP0041284B1|1983-10-05|
    FI811634L|1981-11-30|
    MX158451A|1989-02-02|
    EP0041284A1|1981-12-09|
    DK232481A|1981-11-30|
    AR226598A1|1982-07-30|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US4069140A|1975-02-10|1978-01-17|Atlantic Richfield Company|Removing contaminant from hydrocarbonaceous fluid|
    GB1550684A|1975-08-28|1979-08-15|Mobil Oil Corp|Demetalation-desulphurisation catalyst and the preparation and use thereof|
    NL7607551A|1976-07-08|1978-01-10|Shell Int Research|METHOD FOR THE METALIZATION OF HYDROCARBON OILS.|
    NL187026C|1976-07-08|1991-05-01|Shell Int Research|METHOD FOR THE METALIZATION OF HYDROCARBON OILS.|
    US4227995A|1978-12-06|1980-10-14|The Lummus Company|Demetallization of hydrocarbon feedstock|CA1258439A|1984-04-16|1989-08-15|Karl-Heinz W. Robschlager|Process for the catalytic conversion of heavyhydrocarbon oils|
    US4832829A|1987-04-27|1989-05-23|Intevep S.A.|Catalyst for the simultaneous hydrodemetallization and hydroconversion of heavy hydrocarbon feedstocks|
    GB8722839D0|1987-09-29|1987-11-04|Shell Int Research|Hydrocracking of hydrocarbon feedstock|
    US7384537B2|2000-10-24|2008-06-10|Jgc Corporation|Refined oil and process for producing the same|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL8003092|1980-05-29|
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