Pyrolysis gasoline C6-C8 fraction hydrofinishing catalyst and preparation method

Abstract

The invention relates to a pyrolysis gasoline C6-C8 fraction hydrofinishing catalyst. The catalyst takes molybdenum, cobalt, nickel and potassium as active components, and silicon oxide-aluminum oxideas a carrier. Measured by the total weight of the catalyst, the catalyst comprises 6-22% of molybdenum oxide, 0.1-2.2% of cobalt oxide, 4.0-7.2% of nickel oxide, 0.1-3.0% of potassium oxide, and 75-88w% of the silicon oxide-aluminum oxide carrier. In the carrier, mesopores account for 3-70% of total pores, and macropores account for 1.5-55% of the total pores. The catalyst has good colloid resistance and high arsenic resistant, sulphur resistant and water resistant abilities.

Description

technical field [0001] The invention relates to the field of oil refining and chemical industry, and relates to a catalyst for the second-stage refining treatment of pyrolysis gasoline and a preparation method thereof. Background technique [0002] With the improvement of ethylene production capacity, ethylene by-product pyrolysis gasoline also increases, and pyrolysis gasoline includes C5-C10 fractions. In the prior art, two-stage hydrogenation technology is generally used for the treatment of pyrolysis gasoline fractions. The first stage of pyrolysis gasoline is selective hydrogenation, and the purpose is to generate active components (such as alkynes, diolefins and alkenyl aromatics) therein. Corresponding monoolefins and alkyl aromatics, use noble metal hydrogenation catalysts or non-noble metal Ni-based catalysts to saturate these active unsaturated components in oil products at lower temperatures to reduce coking in the second-stage catalyst bed, thereby To ensure the...

AI Technical Summary

Problems solved by technology

CN1353168A discloses a catalyst suitable for the second-stage hydrofining of pyrolysis gasoline and its preparation method. The alumina precursor is used to add a high polymer and the IV subgroup metal to obtain a molded carrier after drying and roasting. Immerse in ammonia co-impregnation solution containing Mo, Co, and Ni active components, dry at 100-120°C, and activate at 400-700°C in air to obtain a catalyst, which can adjust the acidity and alkalinity of the carrier and inhibit the coking and deactivation speed of the catalyst. The low specific surface area of ​​the carrier leads to low hydrogenation activity of the catalyst

And pyrolysis gasoline when using Al 2 o 3 When used as a carrier, in the process of reducing nickel ions at high temperature, it is easy to cause the formation of nickel aluminate, thereby reducing the catalyst activity selectivity and poor catalyst stability