Methyl alcohol deep-processing bed gradient directional temperature-control reaction device and reaction method thereof

Abstract

The invention discloses a methyl alcohol deep-processing bed gradient directional temperature-control reaction device. The methyl alcohol deep-processing bed gradient directional temperature-control reaction device comprises a cylinder, and a fin constant temperature tube component and / or a corrugated tube component and / or a trapezoid tube component which is installed in the cylinder. The outer wall of the cylinder corresponding to the fin constant temperature tube component and / or the corrugated tube component and / or the trapezoid tube component is provided with multiple feeding ports. The feeding ports stretched into the inner wall of the cylinder are provided with a gas distributor. The cylinder is divided to multiple layers of feeding layers by the feeding ports. After a raw material enters through the feeding port of one layer of the feeding layer on the fin constant temperature tube component and / or the corrugated tube component and / or the trapezoid tube component, a reaction temperature of the feeding layer is controlled. The cylinder is fixed on a skirt, and the lower end of the skirt is provided with a bottom plate. The methyl alcohol deep-processing bed gradient directional temperature-control reaction device has the advantage of acquiring multiple hydrocarbon products with different compositions by controlling a reaction bed temperature curve through the feeding ports in different horizontal planes. The invention further discloses a reaction method of the methyl alcohol deep-processing bed gradient directional temperature-control reaction device.

Description

technical field [0001] The invention relates to the field of chemical process flow, more specifically it is a methanol deep processing bed layer gradient orientation temperature control reaction device. The invention also discloses a reaction method with a methanol deep processing bed gradient directional temperature control reaction device. Background technique [0002] There are various reactors in the process of exothermic reaction. In order to ensure the reaction conditions and the performance of different catalysts, the working principles of the reactors are different. [0003] Existing reactors include fixed-bed reactors, fluidized-bed reactors and multi-tubular reactors; fixed-bed reactors have the following disadvantages in actual production: (1) the released heat cannot be removed from the reactor well to produce fly (2) seriously affect the stability of the reaction product; (3) seriously affect the service life of the catalyst, so that the regeneration cycle of t...

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Problems solved by technology

[0003] Existing reactors include fixed-bed reactors, fluidized-bed reactors and multi-tubular reactors; fixed-bed reactors have the following disadvantages in actual production: (1) the released heat cannot be removed from the reactor well to produce fly (2) seriously affect the stability of the reaction product; (3) seriously affect the service life of the catalyst, so that the regeneration cycle of the catalyst is shortened; the fluidized bed reactor has the following disadvantages in actual production: (1) in the reaction product Entrained catalyst; (2) It is necessary to separate the catalyst entrained in the reaction product, which increases the investment cost of the equipment; (3) The catalyst in the fluidized bed is in a moving state, and the movement will cause the catalyst to be broken, and the powder catalyst is not easy to separate from the reaction product. Catalyst loss is large

The multi-tubular reactor has the following disadvantages in actual production: (1) using ordinary tubes, due to the strong exothermic reaction, the temperature difference between the tube side and the shell side is too large, and only materials with large specific heat capacity can be used to remove heat; (2 ) heat cannot meet the raw material heating demand of continuous feeding after the heat is removed; (3) less heat is removed, and the bed will be overheated, which will affect the effective use of the catalyst; (4) increasing the number of heat exchange tubes can remove a large amount of heat, not It affects the effective use of the catalyst, but adding heat exchange tubes will greatly increase the equipment cost; (5) There is a gas distributor at the feed, which affects the complete regeneration of the catalyst; therefore, the existing three reactors cannot be separated and complete satisfies the relatively efficient use of the catalyst in the reactor

[0004] Existing reactors have relatively high requirements for raw materials and less raw materials for conversion, and cannot use a wide range of cheap hydrocarbon raw materials including waste diesel oil, waste engine oil, etc.; a reactor can usually only convert one kind of raw material, and the production efficiency Low equipment utilization rate; the reactor cannot make maximum use of the reaction heat, resulting in waste of resources; at the same time, the temperature control of the existing reactor is relatively difficult, and one reactor can only produce products of one component at the same time, and cannot Simultaneous production of products with multiple components

As far as the inventor knows, existing reactors and reaction methods cannot control the reaction temperature in the reactor in a directional manner, and the use of common catalysts cannot achieve the catalytic effect of the desired product

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