Hydrofining catalyst and preparation method thereof

Abstract

The invention discloses a hydrofining catalyst and a preparation method thereof, belonging to the field of catalysts used in the petroleum-chemical industry. The hydrofining catalyst disclosed herein comprises a carrier, an active component and an auxiliary agent, wherein the carrier is Ti-modified gamma-alumina, the active component comprises oxides of Mo, Co and Ni, and the auxiliary agent comprises oxides of rare earth. The catalyst is characterized in that: based on 100% of the total weight of the catalyst, Co (measured in CaO) in the active component accounts for 2.0-7.5% of the total weight of the catalyst, Mo (measured in MoO3) in the active component accounts for 4.0-18.0% of the total weight of the catalyst, Ni (measured in NiO) in the active component accounts for 0.2-5.0% of the total weight of the catalyst, the auxiliary agent accounts for 0.05-1.0% of the total weight of the catalyst, and the balance consists of the carrier. According to the invention, the catalyst prepared by the formula and the method disclosed in the invention can carry out hydrogenation on saturated monoolefine while the catalyst is used for carrying out hydrodesulfurization on oils, can be suitable for technical requirements of heavy oriention, changeable sulphur content, and high air speed of hydrogenation liquid for pyrolysis gasoline two-stage hydrogenated raw materials, and simultaneously, the catalyst has the advantages of low activation temperature and low loss of aromatics in the hydrogenation process.

Description

technical field [0001] A hydrorefining catalyst and a preparation method thereof belong to the field of petrochemical catalysts. Background technique [0002] During the steam cracking of hydrocarbons to produce olefins, the by-product C 5 above pyrolysis gasoline. Pyrolysis gasoline contains different degrees of unsaturated and easily oxidized hydrocarbons, such as diolefins and alkenyl aromatics. These compounds are prone to polymerization to form colloids, so that pyrolysis gasoline cannot be used directly. In industry, it is usually less than C in pyrolysis gasoline 5 , higher than C 9 After the fraction cut off, the middle distillate (C 6 ~C 8 ) is processed by a two-stage hydrogenation method. One-stage selective hydrogenation is mainly to remove diolefins, and then undergo two-stage hydrogenation to remove monoolefins and impurities such as S, N, and O, and then use them as raw materials for aromatics extraction. [0003] Since 1958, when UOP Corporation of th...

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Problems solved by technology

[0004] However, it has been found in practice that these catalysts require a high activation temperature, generally between 280 and 290°C, and the aromatics in the material are also likely to participate in the reaction during high-temperature hydrogenation, resulting in the saturation of some aromatics and affecting the economic benefits of subsequent aromatics extraction.

For example, the active ingredient of the second-stage LY-8602 catalyst for pyrolysis gasoline used in industry is MoO 3 , CoO, the carrier is γ-Al 2 o 3 , in practical industrial applications, the catalyst has poor activity in hydrogenation of saturated monoolefins, and cannot adapt to the industrial conditions of heavy hydrogenation feedstock, variable sulfur content, higher and higher space velocity of hydrogenation liquid, and high service temperature (Reactor inlet temperature above 280°C), at this temperature, the hydrogenation loss of aromatics is high

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