• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Composition of matter suitable as a catalyst (base) in hydroprocessing comprising a crystalline aluminosilicate zeolite and a binder wherein the crystalline aluminosilicate comprises a modified Y zeolite having a unit cell size below 24.35 ANGSTROM , a degree of crystallinity which is at least retained at increasing SiO2/Al2O3 molar ratios, a water adsorption capacity (at 25 DEG C and a p/po value of 0.2) of at least 8% by weight of modified zeolite and a pore volume of at least 0.25 ml/g wherein between 10% and 60% of the total pore volume is made up of pores having a diameter of at least 8 nm. The invention also relates to hydroconversion catalysts and processes based on said compositions of matter.
    公开号:SU1641184A3
    申请号:SU874202636
    申请日:1987-05-27
    公开日:1991-04-07
    发明作者:Хук Аренд；Хейзинга Том；Эрнест Максвелл Ян
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    oo-and
    The invention relates to a catalyst for the conversion of hydrocarbons, in particular for the hydrocracking of a heavy hydrocarbon oil product, as well as methods for the hydrocracking of a heavy hydrocarbon oil product.
    The aim of the invention is to increase the catalyst selectivity in middle distillates and the yield of the latter due to the use of
    lit. modified zeolite Y with the indicated characteristics, as well as due to a certain quantitative composition of the catalyst.
    Example 1
    a) Preparation of the modified zeolite composition / binding additive.
    Ammonium ultra stable zeolite having cells of 24.57 A in size, sodium oxide content 0.12% by mass.
    B cm
    and the molar ratio Si02 / Al203 is about 6, subjected to ion exchange treatment with 0.2 M aluminum sulfate for 1 hour under countercurrent conditions. After that, the resulting material is subjected to heat treatment in a stream for 1 h at 700 ° C. The annealed material obtained has a cell size of 24.30 A and a molar ratio of SiO2 /
    ten
    / A1203, equal to 6.85
    The resulting material is then subjected to ion exchange treatment with 0.66 M aluminum sulfate for 1 h under countercurrent conditions, after which it is bare. treatment with 1 M ammonium nitrate is blowing under the same conditions. This treatment is carried out once. The resulting modified zeolite Y has cells.
     at
    24.33 A in size and the molar ratio of the 20 rolling device Si02 / Al, 0 - - nr 466
    thirty
    35
    1-2 for equal to 9.85. g of modified zeolite U having cells of 24.33 A in size, molar ratio Si02 / Al203 equal to 9.85, degree of moisture absorption (at 25–25 ° C and ratio P / P0 equal to 0.2) 11.3 wt. %, pore volume 0.40 ml / g, while 18% of the total pore volume is occupied by pores with a diameter of more than 8 nm, annealing losses (550 ° C) 14.1 wt.%, mixed with 135 g of hydrated alumina c Annealing losses of 25.8 wt0%. Next, a solution of 5 g of acetic acid and 302.6 g of water is added to the resulting mixture. After stirring the mixture obtained, it is pressed in a Bonnot press and 1.5 mmo squeezes are obtained.

    with
    n
    , 70
    d
    Viscosity, cSt, at temperature, ° С:
    100
    60
    RCT, mas
    Initial boiling point, ° С
    The volume of boiling,%, at a temperature, ° C:
    10/20
    30/40
    50/60
    70/80
    90
    Final boiling point, ° С
    dried for 2 hours; annealed at 500 ° C. The resulting water pore 0.66 ml
    b Cooking
    50 g of marc, described as described, are dried during the period when the thief, who received the thief, soaked them, prepared shivan 214.3 g of scoop (14 wt0% composition 150 g of water, and 137 g tungsten (69.5 wt fram) and 8 g of water. P undergo a process for 1 h with approx.
    holding pots containing 2 hours at 120 ° C for 1 hour at 500 ° C, the mash contains 2.6 NiO) and 8.2% w / w in the final catalyst 77.5% by weight,% modified Y and 22.5% by weight s (estimated by total and binding additive
    c) Experiments
    Described katali in the process of hydro-gas oil, having n holding sulfur and azo properties: Content, May.%:
    86.2 13.8 0.826
    4.87 (ASTM-D 445) 12.43 (ASTM-D 445) 0.05 (ASTM-D 542)
    205
    332/370 392/410 428/448 467/492 525
    598
    0

    0 device
    0
    five
    five
    dried for 2 hours at 120 ° C and finally annealed for 2 hours at 500 ° C. The resulting product has a water pore volume of 0.66 ml / g.
    b Preparation of the catalyst.
    50 g of the marc prepared according to the described method are dried for 1 hour at 450 ° C before they are soaked with 33 ml of the solution, which is obtained from 25 g of the solution prepared by stirring 214.3 g of nickel nitrate solution (14 wt0 % is nickel), 150 g of water, and 137 g of ammonium meta-tungsten (69.5% by weight is tungsten) and 8 g of water. The impregnated composition is subjected to a homogenization process for 1 hour with the use of rolled products. Finally, the squeezes containing metal are dried for 2 hours at 120 ° C and annealed for 1 hour at 500 ° C. The resulting catalyst contains 2.6 mas nickel (3.8% NiO ) and 8.2 wt.% tungsten (10% W03). The finished catalyst contains i 77.5 wt.% modified zeolite U and 22.5 wt.% binder additive (estimated from the total amount of zeolite and binder additive per dry basis).
    c) Cracking Experiments.
    The described catalyst is tested in the process of hydrocracking of vacuum gas oil having a slight content of sulfur and nitrogen and the following properties: Content, wt.%:
    86.2 13.8 0.826
    4.87 (ASTM-D 445) 12.43 (ASTM-D 445) 0.05 (ASTM-D 542)
    205
    332/370 392/410 428/448 467/492 525
    598
    51
    The catalyst is initially subjected to preliminary sulfide treatment by slow heating in an atmosphere of hydrogen sulfide / hydrogen (10 vol.%) To 370 ° C. The catalyst was tested at a volume dilution of 1: 1, SiC particles, 0.2 mm in size, under the following operating conditions: processing speed 1.1 kg / l "h, partial pressure H2 1.4 bar, total pressure 130 bar, ratio gas / feed 1000 nl / kg „The experiment was carried out in one stage.
    During the cracking of the raw material, the catalyst action is expressed in 70% of the transformations of the fraction 300 C after the catalyst becomes stable. The required temperature of a 70% conversion of the 300 ° fraction is 318 ° C. At the same time, products are obtained, by weight%.
    C, -C47
    С j- at temperature, ° С:
    13046
    130-300 47 The consumption of hydrogen is
    ., 2%.
    Example 2. The hydrocracking experiment described in example 1 was repeated to transform 70% of the fraction with a boiling point of 180 ° C. The required 70% conversion of the 180 ° C fraction was 324 ° C.
    C 4 11
    С с- at temperateReg, ° С:
    6521
    65-18068
    The consumption of hydrogen is
    ., 3%.
    PRI me R 3 (comparative). An ultra stable zeolite, whose cells have dimensions of 24.56 A, the degree of moisture absorption is 24% by weight at 25 ° C and a P / P0 ratio of 0.2, a pore volume of 0.38 ml / g, with 8% of the total volume pores occupy pores having a diameter of more than 8 nm, are treated with hydrated alumina and a solution of nickel nitrate and ammonium metavolphramate, thereby obtaining a catalyst containing 2.6 wt.% nickel (3.8 NiO) and 8.2 wt.% tungsten (10% WO,).
    46
    The catalyst used for comparison is subjected to a preliminary sulfide treatment, as described in Example 1c, and charged with the same raw material. After stabilization, the required temperature is 70%, the conversion of the 300 ° C fraction is 325 ° C0.
    c ci13
    With with - at temperatures в, VS:
    13057
    130-30030
    The consumption of hydrogen is 1.5 May%.
    Comparative catalyst is tested in the cracking process of Example 2. The required temperature for conversion is 325 ° C0. In this case, products are obtained, wt%: C4-C4.16
    Se - at a temperature of - p1, ° С :,
    6526
    65-18058
    The consumption of hydrogen is 1.5 wt.%
    PRI me R 4. Ammonium ultra stable zeolite of type Y, cell size 24.57 A, sodium oxide content 0.12 mass% and molar ratio Si02 / Al203 of approximately 6, is subjected to ion exchange with 0.2 M sulfate aluminum for 1 h under reflux conditions. After this, the treated material is calcined in this way.
    0
    in the presence of water vapor for 1 hour at 700 ° C “Received
    The calcined material has a cell size of 24.30 A and is characterized by a Si02 / Al203 molar ratio of 6.85 (the degree of crystallinity of the material, the rial is taken as 100) 0
    The resulting material is then subjected to ion exchange with 0.16 M aluminum sulphate for 1 hour under reflux with the floor following treatment with 1 M ammonium nitrate under the same conditions. This treatment is repeated once more. The resulting modified zeolite Y has a cell size of 24.32 A and is characterized by a Si02 / A1203 molar ratio of 10.2. The degree of crystallinity of the material is 11b. A modified zeolite with a cell size of 24.32 A and a molar ratio of Si02 / Al203 of 10.2 has a degree of moisture absorption (at 25 ° C and P / P № 0.2) 10 , 6 wt.%, The pore volume of nitrogen is 0.47 ml / g, at which 27% of the total pore volume are pores with a diameter of more than 8 nm and a loss on obzolivanie (550 ° C) is 21 wt.%
    The zeolite is combined with alumina by a compound method, analogous method,
    described in example 1a, so that the ratio between the zeolite and alumina is 80:20
    EXAMPLE 5 Catalysis- containing a combination of zeolite / alumina, nickel, molybdenum, platinum, palladium, tungsten and cobalt is obtained. "The preparation is carried out by immersion, co-grinding and ion exchange using the processes of conventional processing technology.
    The compositions of the resulting catalysts are given in table. one"
    Example 6. The described catalysts are used in the hydrocracking experiments of the raw material of Example 1c. The conditions for the nickel / modibdic and nickel / tungsten catalyst are the same as those for the catalyst described in Example 1c. The conditions for the platinum / palladium catalyst are similar, the only difference is that the H2S partial pressure is 0.2 bar instead of 1.4 bar. In addition, there is no pre-acification.
    The results of the experiments are given in Table 2.
    Example 7. Some of the catalysts are tested in a hydrocracking experiment using vacuum gas oil having characteristics; at С180 ° С boils out 0.1 wt%, at 180-370 ° С boil up 30.7 wt.%, at С boil 69.2 wt.%. The catalysts are pre-subjected to arassing. Then they are tested at a volume dilution of 1: 1, SiC particles of 0.1 mm in size under the following conditions: total pressure 60 bar, H2S / feed ratio 240 nl / kg, H2S / feed ratio 30 nl / kg NH3 / feedstock 1.8 nl / kg and a volumetric rate of 1.8 kg / Lh. The partial pressure of hydrogen, therefore, is 53 bar. The temperature is set to achieve the same conversion.
    None of the 370 ° C4 materials, i.e., such, for which the 55.4% fraction does not undergo transformation. The results are shown in Table. 3
    Example The catalyst (preliminarily prepared) of Example 1 is used in the hydrocracking of a distillate in the vapor phase, obtained after preliminary catalytic hydrocracking, having the following boiling characteristics: Initial boiling point,
    Volume of boiling out,% temperature, ° С: 10/20 30/40 50/60 70/80 90 End point of the boiling point,
    at
    321
    377/404 426/445 461/479 499/520 572
    neither
    620
    5 o
    0
    v
    five
    five
    The required 65% conversion temperature of the 370 ° C fraction is 328 ° C.
    You get the following products, wt „%:
    Ct-C4.4
    Cg. at temperature, С:
    15033
    150-37063
    Thus, the proposed method allows to increase the selectivity of the used catalyst with respect to middle distillates and, therefore, to increase their yield from 34.0 wt.% By a known method to 38.0 wt.% „
    权利要求:
    Claims (2)
    [1]
    Invention Formula
    i
    1 o Catalyst for hydrocracking a heavy hydrocarbon oil product containing a type Y zeolite, the hydrogenating component is nickel oxide and a metal oxide of group VI, or platinum and palladium, a binder is aluminum oxide, characterized in order to increase the selectivity of the catalyst in middle distillates there; as a type Y zeolite, it contains a modified zeolite Y with elemental cells of 24.32–24.33 A, with a degree of crystallinity that is maintained with an increase in the molar ratio of silica to alumina
    mini, water absorption capacity at 25 ° C and a value of 2, where P is the partial pressure of water vapor, MPa, P0 is the water saturation pressure at 25 ° C, MPa, equal to 10.6-11.3 wt.% with a pore volume of 0 , 4-0,47 ml, the pore volume being pores with a diameter of more than 8 nm, as a metal of the sixth group, oxide oxide or tungsten oxide, and the catalyst contains these components in the following quantity, wt%:
    Modified 67.0-79.4
    zeolite Y
    The hydrogenating component is nickel oxide
    Molybdenum oxide or
    tungsten
    Platinum and Palladium
    Alumina
    [2]
    2. The method of hydrocracking heavy hydrocarbon oil by contacting the latter at a temperature of 314–405 ° C, a pressure of 60–130 bar, a bulk feed rate of 1.1–1.8 kg / l ч h with a catalyst containing type U zeolite, which hydrogenates component - nickel oxide metal oxide of group VI or platinum and palladium, binder - alumina oxide, 3-5.0
    6.3-10.3 0.8 Else
    Component of group VIII NiO NiO NiO NiO Component group VIW03
    left; wt.%:
    component
    Group VIII 3.3
    WO,
    MoO, MoO,
    component
    group VI 10.3 10.3 6.3 9.4 modified type U zeolite alumina oxide
    Moo,
    3.3 3.3 5.0 5.0
    9.4 67.0 69.1 72.3 68.5 68.5
    neither
    19.4 17.3 18.1 17.1 17.1 19.8
    5 o
    five
    Neither with medium distillates, characterized in that, in order to increase the yield of middle distillates, a catalyst is used which contains, as a type Y zeolite, a modified zeolite Y with elemental cells 24.32-24.33 A with a degree of crystallinity remaining at an increase in the molar ratio of silicon dioxide to aluminum oxide, water adsorption capacity at 25 ° C and a value of, 2, where P is the partial pressure of water vapor, MPa; P is the saturation pressure of water at a temperature of 25 ° C, MPa, equal to 10.6-11.3 wt.%, With a pore volume of 0.40-0.47 ml / g, with 18-27% of the pore volume being pores with a diameter greater than 8 nm, as a metal of group VI, molybdenum oxide or tungsten oxide in the following ratio, wt.%:
    Modified zeolite U67,0-79,4
    Hydrogenating component - nickel oxide 3.3-5.0 molybdenum oxide
    or tungsten 6.3-10.3 Platinum and palladium 0.8 Alumina Else
    Table 1
    Soo
    Pt / Pd
    MoO, MoO,
    Moo,
    0.3 Pt-f + 0.5 Pd
    79.4
    The temperature required to convert the 70% fraction to 300 ° C, ° C
    Obtaining product, wt.%;
    Su at a temperature of 0 C:
    328 314
    325
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB868613132A|GB8613132D0|1986-05-30|1986-05-30|Hydrocarbon conversion catalysts|
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