• 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:
    There is disclosed a catalyst for the hydrodemetallization of petroleum hydrocarbon streams containing asphaltenes and large quantities of metals. This catalyst consists essentially of a small amount of a single hydrogenation metal selected from the group consisting of metals from Group VIB of the Periodic Table of Elements and metals from Group VIII of the Periodic Table deposed on a large-pore alumina. The hydrogenation metal may be present in the elemental form, as an oxide, as a sulfide, or mixtures thereof. The catalyst is characterized by a surface area of at least 120 square meters per gram, a pore volume of at least 0.7 cc per gram, and an average pore diameter of at least 125 Angstrom units. Suitable examples of a hydrogenation metal are nickel and molybdenum. Also disclosed is a process for the hydrodemetallization of a hydrocarbon stream containing asphaltenes and a substantial amount of metals, which process comprises contacting said hydrocarbon stream in a reaction zone under suitable operating conditions and in the presence of hydrogen with the catalyst described hereinabove.
    公开号:SU1042621A3
    申请号:SU782635899
    申请日:1978-06-30
    公开日:1983-09-15
    发明作者:Дональд Хопкинс Пол；Ллойд Хенсли Альберт (Младший)
    申请人:Стандарт Ойл Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method of hydrodemetallization of a hydrocarbon feedstock selected from the group including crude oil, toppings, petroleum, petroleum residues, distillates, residues of bituminous sands extraction and liquid hydrocarbon feedstocks of coal origin in the presence of a catalyst, and can be used in oil refining The industry is known to hydrodemetallize a hydrocarbon feedstock in the presence of a catalyst containing 6–10% nickel oxide and 16–20% molybdenum trioxide supported on alumina l}. Closest to the invention is a method of hydrodemetallization of a hydrocarbon feedstock selected from the group that includes crude oil, stripped oil, petroleum residues, distillates, tar sands extraction residues and liquid hydrocarbon feedstock coal of 4-6th origin, and containing 15-30 wt. % of asphaltenes and 200–1000 ppm metal fluids (Ni, V), in the presence of a catalyst containing up to 20.5 wt.% molar trioxide and up to 6.0 wt. % of cobalt oxide deposited on large pore alumina at 371–455 s and at a pressure of 14–700 kg / cm 2 2. Odng1KO the percent of demetallization of hydrocarbon raw materials in the presence of such a catalyst is small and does not exceed 50 wt.% When the amount of metals on the catalyst reaches 56 wt.%. The purpose of the invention is to increase the degree of demetallization of hydrocarbon feedstock containing asphaltenes and metals. The goal is achieved according to the method of hydrodemetallization of hydrocarbon raw materials selected from the group including crude oil, stripped oil, oil residues, distillates, tar sands extraction residues and liquid hydrocarbon raw materials of coal origin and containing asphaltenes and metals, in the presence of a catalyst containing 1, 03, 0 wt.% Molybdenum trioxide and 97-99 wt.% Alumina and having a specific surface of 120–400 m; pore volume: 0.7–1.5; average particle diameter, 125–350 Å, at 371–482 ° С hydrogen partial pressure 35.1 211 kg / cm, the flow rate of the feed of the source of raw material is 178.1-1781 and the flow rate of the raw material is 0.2-2.5 hours. Example 1 To prepare a catalyst by hydrogenation demetallization, Kaiser Chemicals grade KSA alumina is used as a carrier. Alumina is made in the form of extrudates with a size of 3.2 mm and, in this form, is calcined under static conditions in air at 538 ° C for 1-2 hours. The calcined extrudate is then crushed to 14-20 mesh. Then a solution of ammonium paramolybdate is prepared, a solution of 120 g (, 0 in 250 ml of concentrated ammonium hydroxide. The resulting solution is then diluted with distilled water to a volume of 500 ml. In 1 ml of solution there is an equivalent of 0.2 g of MoO. 11 ml of the prepared solution is diluted 250 ml of distilled water are then applied, after which the resulting solution is added to 219 g (500 cm) of 14-20 mesh alumina. This amount of solution only wets all the alumina. The impregnated alumina is then calcined in still air at 538 ° C for one and a half hours. The catalyst contains 1.22% by weight of MoO based on the total weight of the catalyst. The characteristics of the physical properties of this catalyst are shown in Table 1. Comparative Example Preparing a catalyst containing both cobalt and molybdenum on high pore alumina Prepare a solution with cobalt and molybdenum compounds, for which 9.28 g of ammonium paramolybdate and 8.22 g of cobalt nitrate hexahydrate are dissolved in 150 ml of distilled water. The prepared solution is then used to impregnate 50 g of coarse alumina. The impregnated alumina is dried in a vacuum oven for 8 hours and calcined at 538s in still air for 1 hour. A catalyst is obtained, bearing 3.7% by weight of CaO and 13.3% by weight of MoO calculated on the total weight catalyst. Example 2. As a feedstock, oil residues are taken, respectively, designated as raw materials 1 and 2. Table. 2 shows the properties of these petroleum residues. The study of hydrogenation demetallization is carried out on a bench installation, in which pressure, reagent consumption and temperature are automatically maintained, the reactor is made of a thick-walled stainless steel pipe having an inner diameter of 9.5 mm. A thermocouple pocket is placed in the center of the reactor; its outer diameter is 3.2 mm. The reactor is heated by a steel electric heater. Hydrocarbon feedstock enters the installation of the pressure piston pump Rusk. The catalyst is located in a g reactor in the form of a layer with a height of 17.8-25.4 cm with a particle size of 14-20 mesh. Alandum particles with a size of 10-14 mesh are used as a carrier. In the experiments, the catalyst volume in the bed was 1116 cm. A layer of 10-14 mesh alandum particles was placed in the reactor. The second layer was 5.08 cm in height. The catalyst was placed in an annular gap between the pocket and the inner wall of the reactor (0 9 , 5 mm). Hydrocarbons and hydrogen are introduced into the reaction zone. To separate the liquid from the gas, the waste stream is passed through a separator. The liquid passes through the pressure regulating valve and is collected in containers for collecting liquid products, and the gas passes through the pressure control valve and then through the moisture absorber is sent to the outlet.
    In tab. 3 shows the process conditions for the proposed catalyst ee and the known.
    The characteristics of the activity of the catalysts obtained in these tests are presented in the graph. The activity is expressed as the percentage of vanadium and nickel extracted from the processed raw material, as a function of the metal content in the catalyst, determined as a percentage of the initial weight of the catalyst.
    The test results indicate that the catalyst has significant activity.
    If a known catalyst has an activity at the initial stages that is much better than the activity of the proposed one, then E increases the amount of deposited metal with the slope of the activity curve.
    corresponding to the known catalyst is much larger than the slope of the proposed catalyst, and at the time of deposition on each catalyst 50 weight. % metal known catalyst has a significantly greater demetallization activity than proposed.
    Example 3. For demetallization of stripped extract residues
    0 from bituminous shales, obtained after atmospheric distillation, use a catalyst prepared analogously to example 1, containing 1 weight. % MOD. The physical indicators of this catalyst are given in Table. one.
    The properties of the processed raw materials, designated as raw materials 3 ,. listed in Table. 2
    0
    The catalyst was tested in the described installation at 410 and and the space velocity equal to 1 and 2 hours. At 410 ° C and a space velocity of 2 hours, 28.5 wt. % demetallization of raw materials, accompanied by 39 wt.% desulfurization, 25.2% conversion of fractions with a boiling point above 538 ° C and a yield of 0.69 wt.%. from the raw material of hydrocarbon gas. Decreasing the volumetric rate to 1.0
    0, 60.8% demetallization of the raw material occurs, 44.0% conversion of the fractions with a boiling point above 538 ° C, while hydrocarbon gas is released in an amount of 1.19% by weight
    5 per raw material. With an increase in temperature up to and a space velocity of 1.0, a 69.0% demetallization is reached, a 52.0 conversion of fractions with a boiling point higher than 538 ° C, a 48.0% desulfurization, while the yield of hydrocarbon gas is 1, 86 wt.% From the feedstock.
    Table 1
    Light alumina
    Catalyst containing 1.22 wt. % molybdenum trioxide
    Catalyst containing 1.0 wt.% Molybdenum trioxide
    To alizator containing 3.7 wt.% Cobalt oxide and 13.5 wt.% Molybdenum trioxide (known method)
    205
    1.01
    195
    0.90 168 0.95
    138
    0.71
    Density, g / cm
    Content, weight,% Sulfur Nitrogen Hydrogen Carbon Asphaltenes
    The fractions with a boiling point of 553 ° С, wt.%
    table 2
    1,0014
    1.0246
    1,0451
    3.70
    4.52
    6.0
    0.62
    1.19
    0.62 10.22 0.38
    9.98 4.66 84.07 82.98 10.7 12.0
    31.1
    0.5
    32.0
    Ta b face 3
    权利要求:
    Claims (1)
    [1]
    METHOD FOR HYDROMETALLIZATION OF A HYDROCARBON RAW MATERIAL selected from the group consisting of crude oil, stripped oil, oil residues, distillates, extraction residues of tar sands and liquid hydrocarbon feedstocks of coal origin, and containing asphaltenes and metals, in the presence of a catalyst based on elevated molybdenum trioxide and molybdenum oxide temperature and pressure, characterized in that, in order to increase the degree of demetallization, a catalyst is used containing 1.0-3.0 wt.% molybdenum trioxide and 97-99 wt.% alumina Nia and having a specific surface area of 120-400 m 2 / g, a pore volume of 0,7-1,5 gM 3 / r, an average pore diameter of 125-350 A, and the process is conducted at a temperature of 371-482 ° C, a hydrogen partial pressure of 35 , 1-211 kg / cm g . the volumetric feed rate of hydrogen 178.1-1781 m 3 / m ' 3 ' raw materials and the volumetric feed rate of 0.2 0.2 2.5 hours 1 .
    SU ... 1042621
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    同族专利:
    公开号 | 公开日
    US4119531A|1978-10-10|
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    AU3720678A|1979-12-20|
    JPS6031542B2|1985-07-23|
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    引用文献:
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    US3712861A|1970-10-19|1973-01-23|Mobil Oil Corp|Upgrading a hydrocarbon utilizing a catalyst of metal sulfides dispersed in alumina|
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    GB1499297A|1976-06-29|1978-01-25|Kogan S|Catalyst for dehydrogenation of paraffin hydrocarbons to olefines and method of preparing such a catalyst|US4212729A|1978-07-26|1980-07-15|Standard Oil Company |Process for demetallation and desulfurization of heavy hydrocarbons|
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    US4394253A|1979-09-26|1983-07-19|Chevron Research Company|Hydrocarbons hydroprocessing with imogolite catalyst|
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    法律状态:
    优先权:
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