A catalytic conversion system

Abstract

The invention discloses a catalytic conversion system, which comprises reaction equipment, catalyst circulation equipment and catalyst regeneration equipment. The reaction equipment comprises a pre-lifting section, a riser, a stripping section and a dense phase fluidized bed which are arranged from bottom to top in the vertical direction. A spent catalyst outlet of the reaction equipment is communicated with a spent catalyst inlet of the regeneration equipment through the catalyst circulation equipment. A regenerated catalyst outlet of the regeneration equipment is communicated with a regenerated catalyst inlet of the reaction equipment through the catalyst circulation equipment. According to the catalytic conversion system, size of equipment, especially diameter of a reactor, is reduced; a filter effectively filters out catalyst dust carried by a reaction product, thus providing convenience for subsequent processing; and nature loss of the catalyst is reduced.

Description

technical field [0001] The present invention relates to a catalytic conversion system. Background technique [0002] The reactor is one of the cores of the process. The existing catalytic conversion equipment in industrial production includes fixed-bed reactors, moving-bed reactors, dense-phase fluidized-bed reactors, and riser reactors. Taking the catalytic cracking reaction as an example, the above reactors have all been industrialized. [0003] A fixed bed reactor refers to a reactor in which the catalyst bed remains stationary while the gas and liquid reactants flow through the catalyst bed in the reactor during the reaction. In industrial production, the reactors used in hydrogenation catalytic reactions are often fixed-bed reactors. Although the diameter and height of the fixed-bed reactor are not strictly limited, considering factors such as fluid distribution, production cost, and safety, the height / diameter ratio usually used in reactor design is 2.5-12. Early ca...

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Problems solved by technology

[0005] The dense-phase fluidized bed reactor belongs to the category of bubbling bed and turbulent bed, and its superficial linear velocity is generally 0.2-1.5m / s, and its space velocity is 2-10h -1 , so the reaction residence time is generally relatively long. Due to the low linear velocity of the dense-phase fluidized bed reactor, there is often back-mixing, which affects product distribution and quality. On the other hand, the diameter of the reactor is relatively large

For example, it is generally believed that the reaction of MTO is a reaction in which the number of molecules increases, and the low reaction pressure is conducive to the direction of chemical equilibrium to generate low-carbon olefins. Considering engineering factors, a process similar to catalytic cracking is usually still used, and the reactor adopts dense-phase fluidization Bed reactor, the reaction pressure is also similar to the catalytic cracking process, that is, 0.1 ~ 0.3MPa (gauge pressure), but the problem is that the size of the reactor is too large

Since the existing MTO unit uses a cyclone separator similar to catalytic cracking, the natural loss of the catalyst during the production process is unavoidable, especially when the catalyst fine powder with a particle size of ≦20 μm increases, which will affect the subsequent Product separation has adverse effects and is also detrimental to the reuse of catalysts

In addition, the generated olefins stay in the reactor for a long time, and the hydrogen transfer reaction increases, which is also very unfavorable for the production of low-carbon olefins

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