Dual-seal-head controllable water heat removing reactor

Abstract

The invention discloses a dual-seal-head controllable water heat removing reactor. The top of a main cylinder body is connected with a lower flange; the bottom of the main cylinder body is connected with a lower outer seal head; the upper flange is connected with the lower flange; one end of a catalyst filling pipe is connected between an upper inner seal head and a gas distribution cylinder, and the other end of the catalyst filling pipe sequentially penetrates through a baffle and an upper external seal head; one end of a water guide pipe is communicated between the baffle and the upper outer seal head, and the other end of the water guide pipe sleeves a heat exchange pipe internally; a pipe body of the heat exchange pipe is positioned in a gas distribution cylinder; an outlet of the heat exchange pipe is formed between the baffle and the upper inner seal head; a cylinder body of a gas collecting cylinder is positioned in the gas distribution cylinder; an outlet of the gas collecting cylinder is connected with a gas outlet. The heat exchange pipe is buried in a catalyst bed layer so as to remove reaction heat in the catalyst bed layer timely, and the defects of short service life, easiness in overtemperature, multiple auxiliary reactants, difficulty in bed layer temperature control, long driving time, difficulty of scaling up, high running energy consumption, high project investment and the like in the prior art can be solved.

Description

technical field [0001] The invention relates to a fixed-bed catalyst, a conversion, synthesis and hydrogenation reactor in a gas phase state, in particular to a double-head controllable water transfer heat reactor. Background technique [0002] The CO shift reactor is a widely used reactor in the chemical industry. During this period, people have made many improvements to the shift reactor, from the original full axial to full radial, and achieved good results in the resistance of the catalyst bed. effect, but the catalyst bed is still an adiabatic reaction. The catalyst bed is divided into several beds, and indirect heat exchange or water cooling is adopted between each bed. This kind of indirect heat exchange recovery transformation system has the disadvantages of low thermal energy grade, low recovery efficiency of sensible heat and latent heat, easy overheating of the catalyst, simultaneous transformation and side reactions such as methanation, etc. [0003] Coal-to-eth...

AI Technical Summary

Problems solved by technology

This indirect heat exchange recovery transformation system has low thermal energy grade, low recovery efficiency of sensible heat and latent heat, easy overheating of the catalyst, simultaneous transformation and side reactions such as methanation, etc.

[0003] Coal-to-ethylene glycol carbonylation reactor currently uses a ф25X2 tube to fill the catalyst, and water outside the tube to remove heat. A column and tube reactor is composed of thousands of axial ф21 cylindrical catalyst beds, and the gas distribution is uneven. Uniformity, many side reactants, large catalyst bed resistance, large thermal stress, equipment leakage, a 200,000-ton / year ethylene glycol plant carbonylation reactor requires 6 shell-and-tube reactors to operate in parallel, and the project investment major defect

[0004] The esterification hydrogenation reactor for coal-to-ethylene glycol currently uses ф38X2 tubes to fill catalysts, and water outside the tubes to remove heat. A column-tube reactor is composed of thousands of axial ф34 cylindrical catalyst beds, and the gas distribution Inhomogeneity, many side reactants, large catalyst bed resistance, large thermal stress, equipment leakage, large engineering investment and other defects

[0005] At present, the reaction of coal to natural gas adopts the heat transfer method of n adiabatic beds + n waste superheated boilers, and it is necessary to increase the reactant water vapor to suppress the reaction of the first and second adiabatic beds, and configure the circulating gas at the same time, otherwise Flying temperature phenomena in the first and second adiabatic beds, high operating energy consumption, large equipment investment, large system resistance and other defects

[0006] At present, there is no large-scale equipment in operation for the Fischer-Tropsch synthesis reaction of coal-to-oil and coal-to-paraffin, and some of the small-scale Fischer-Tropsch synthesis reactors in operation are also tubular reactors, filled with Fe (or Co) catalysts. In the ф76X4 tube, there are still defects such as uneven gas distribution, overheating, carbon deposition, low yield of long-carbon paraffins, large resistance, equipment leakage, and difficulty in large-scale expansion.

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