• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Water dealkylation catalysts of petroleum fractions containing monoalkylated or polyalkylated aromatic hydrocarbons including at least one metal of group VIII deposited in a proportion of from 0.1 to 5% by weight on a spinel, and having deposited in a proportion of from 0.1 to 5% by weight on a spinel, and having improved properties of activity, selectivity and stability, characterized in that the carrier is a mixed spinel of the formula (MxM'1-x)Al2O4 wherein M is a bivalent base metal of group VIII such as nickel, iron and cobalt and M' is a bivalent metal belonging to groups 2a, 7b, 1b or 2b such as magnesium, manganese, copper and zinc. The mol. ratio M/M' may vary from 0.5:1 to 50:1, preferably from 1:1 to 20:1.
    公开号:SU982529A3
    申请号:SU792739105
    申请日:1979-03-19
    公开日:1982-12-15
    发明作者:Дюпре Даниель；Гран Мишель
    申请人:Елф Юньон (Фирма)；
    IPC主号:
    专利说明:

    Whether 0.6% of rhodium or its mixtures with noble metal VI of group 11 are deposited in a ratio of 5: 1. The metals are introduced by impregnating the support with an aqueous or acidic solution of the salt of the selected metal. After impregnation, the catalyst is dried and then calcined in air. Before reaction, it is reduced by hydrogen current at 400-550С. After reconstitution, the catalyst is treated with a stream of water vapor at 400 ° C for a period of time from 5 minutes to 15 hours, preferably from 1/4 hour to 4 hours. The resulting catalysts are tested in the process of toluene dealkylation. The dealkylation is carried out at 400-BOOC, preferably at 420-550 ° C under a pressure of 0-80 bar, preferably O-bO bar. The spatial hourly rate of toluene is 0.1-10 hours, preferably 0.3-4 hours. The molar ratio of water to toluene at the feed level is 2-20, preferably 4-10. The proposed catalyst has a high activity in the toluene dealkylation reaction with good selectivity, as well as high stability: the catalyst performance remains unchanged for 400 hours without any changes in operating conditions. Example 1. A catalyst containing 0.6% by weight of rhodium / Nig, Mgu Al deposited on mixed spinel is prepared as follows: 258 g of aluminum nitrate AlCNQ dissolved in 500 cm of purified permutite filter with continuous stirring (combined) molecular weight 375.1 g 50 g nickel nitrate NiCNO 1-bN.O (theoretical molecular weight 290.8) and 43 g magnesium nitrate: (N03) 2 .6HiO (theoretical molecular weight 255.4 g). Dissolution is carried out with a heat of 2 hours. Then metal hydroxides precipitate as follows: when very energetic Ammonia is added to the stirring until the first flakes of hydroxides appear, which then do not dissolve. The precipitation is completed by adding a 2N ammonia solution to a pH of 6.5. , in the course of nickel, which manifests itself in the appearance of an intensely blue color of the solution. The co-precipitated precipitates are filtered through a Büchnor funnel under vacuum. The combined precipitate is dried under vacuum for 36 hours, then it is passed into 500 cm of purified water by the permuta filter. Filtered again, dried at 160 ° C under vacuum for 48 hours. Calcined for 1 hour for 1 hour, then for 2 hours. Get solid black and gray. The transformation into spinel is carried out by calcining the support for 3 hours, then for 15 minutes. Then it is cooled in a desiccator. The solid gets a blue color, intermediate between the dark blue color of the spinel. and white spinel, 56.5 g of solid are obtained, which corresponds to more than 98% of the theoretical yield. 0.55 g of hydrated rhodium chloride (39-40% rhodium) is dissolved in 15 cm of a 0.1 N solution of acetic acid. 35 g of mixed spinel (Mg, Ni) is immersed in this solution. Stir continuously for 5 minutes, then leave in air for 1 hour. The volume of the solution is calculated so that all the liquid is absorbed. Then the catalyst is dried for 4 hours, then calcined in two stages: for 30 minutes with a gradual increase in temperature to, then for 30 minutes at. Then the catalyst is cooled in a desiccator. 20 g of the catalyst prepared in this way is placed in a dynamic fixed bed reactor and tested under the following conditions: bed temperature pressure b bar (relative pressure 5 bar) J OOC (volume of toluene per unit volume of catalyst per hour) 0.9; the molar ratio of I2 O / toluene 8; after 23 hours of operation, the molar yield of benzene with respect to the passed toluene is 0, bb; with respect to converted toluene, the benzene yield is 0.81. Examples 2-5. These examples are given to compare the characteristics of the proposed catalysts with those of catalysts containing rhodium deposited on simple spinels of the type or. (in the latter case, Rh is introduced directly into the spinel). The experiments were carried out under a pressure of 2 bar, the temperature of the catalyst bed was 4–5 ° C, the volume of toluene per unit volume of catalyst per hour (TOC) was 0.9; molar ratio ILjtO; toluene 8.0. The results are shown in Table. one.
    Catalyst 2 is the most active of the rhodium catalysts obtained by precipitation of rhodium on simple spinel; it is tested for 200 hours to assess its stability (Table 2). The test was carried out under the following conditions: temperature,; TOC-0.90; the molar ratio Hj O: toluene 8; pressure 2 bar. Catalyst 2 has good activity, stability.
    Example 6. Catalyst 1 is tested under the conditions described in example 1 (438C, TOC 0.9;: toluene 8) at different pressures.
    The results are shown in Table. 2
    The activity of catalyst 1, according to the invention, corresponds to the activity of β-catalyst containing 0.6% rhodi on simple spinel. Selectivity and stability of his improved. For example, at a pressure of 6 bar, when operating for 9-360 hours without changing the operating parameters, no deactivation is observed.
    Example 7. A catalyst is obtained, with a content of 0.6% rhodium deposited on mixed spinel io, 75 MRop-S AL2.04 (catalyst 6), according to example 1, by adding such amounts of nickel and magnesium salts that satisfy the stoichometric ratio N / MC-3 (for 258 g of aluminum nitrate, 75 g of nitrate-nickel and 21.5 g of magnesium nitrate are taken). 10 g of the catalyst thus obtained are tested at, a pressure of 2 bar, 90 the H 0: toluene ratio of 8.
    The results are shown in Table. 3
    The catalyst b according to the invention combines high activity with good selectivity. Its stability is also high.
    Example 8. For the evaluation of catalyst 6 under production conditions in which the determining stability of TopaiAi is sufficient stability and maximum possible sensitivity, it is tested at 39bc (Table 4),
    This table indicates the selectivity of catalyst 6 with a conversion degree of 40-50%. This selectivity
    0 is significantly limited by the appearance in products of significant quantities of xylenes (0.8-2% in the liquid hydrocarbon phase),
    Examples 9-15. These examples 5 are given for the evaluation of catalyst b under different operating conditions (Table 5).
    Examples 16-19. In accordance with Example 7, bimetallic catalysts containing 0.5% rhodium and 0.1% of another metal of group VII are deposited on mixed spinel from nickel, magnesium and aluminum by adding the corresponding 5 metal salts for impregnation. The carrier is chosen the same as in Example 7, with reference to Mi / Mo

    The results are shown in Table. b. 0 Bimetallic catalysts of rhodium-platinum, rhodium-palladium to rhodium iridium have good selectivity, of these bimetallic catalysts the most stable catalysts are rhodium-iridium.
    P & M 20. Replacing spinels. Part of nickel with magnesium leads to the production of catapysis with high rates in the process of water. He is dealkylated with toluene. Carriers are prepared in accordance with Example 1 by replacing the magnesium salt with a stoichiometric amount of metal sue M, where M- is manganese, copper or zinc.
    The results are shown in Table. 7
    Table 1
     This catalyst is obtained by impregnation of - γ-gcncanozem with such amount of nickel and rhodium salts, so that the Ni / Rh ratio is 0.5 and the rhodium content in the catalyst is 0.6 wt.%, Then the catalyst is calcined at high temperature (900, then 1000 ° С ), as in example 1 „
    (6.6% per mix. Catalyst and experience conditions
    0.6% Rh HaNi ,,, Mg
    vvh "0.90
    JlO.-.
    - 8 toluene
    2v6ap
    Table 3
    Table
    b 24
    50.8
    91.5 47.3 93.5
    50
    44.9
    95.7 0Q 41.2 96.0 Continuous Strength, | . h 1 Conversion, I Selectivity, ... „.„ ...%
    396
    (re)
    Table 5
    44.9
    0.90
    95.7
    50
    100.6% Pvh on
    V-v.
    110.6% Rh on
    Thu Cu, a5AIi04
    120, Rh on
    Ni, Znx, .. ABO. 426
    0, Y-460, 6% Rh on
     26 2
    权利要求:
    Claims (2)
    [1]
    1. The patent of France 2169875, cl. C 07 C 3/00, published. 1976.
    [2]
    2. US patent 4013734,
    cl. 260-672, publ. 1977 (prototype)
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    同族专利:
    公开号 | 公开日
    FR2420517B1|1980-08-29|
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    CA1124703A|1982-06-01|
    IT7921127D0|1979-03-20|
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    GB2016298B|1982-10-13|
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    US4233186A|1980-11-11|
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    引用文献:
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    US3691247A|1970-09-28|1972-09-12|Phillips Petroleum Co|Selectively removing monoalkylbenzenes from mixtures thereof with dialkylbenzenes|
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    US4013734A|1973-12-14|1977-03-22|Exxon Research And Engineering Company|Novel catalyst and its use for steam hydroconversion and dealkylation processes|US4495304A|1980-07-29|1985-01-22|Atlantic Richfield Company|Catalyst for conversion of hydrocarbons|
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    JPH0153717B2|1980-07-29|1989-11-15|Atoranchitsuku Ritsuchifuiirudo Co|
    US4495305A|1980-07-29|1985-01-22|Atlantic Richfield Company|Catalyst for conversion of hydrocarbons|
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    US4546093A|1984-07-05|1985-10-08|China Petrochemical Development Corp.|Preparation of catalyst system for the synthesis of 2-6-xylenol|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR7807987A|FR2420517B1|1978-03-20|1978-03-20|
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