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Continuous reaction regeneration device utilizing vulcanization catalyst to perform alkane dehydrogenation

A technology for alkane dehydrogenation and reaction regeneration, which is applied in catalyst regeneration/reactivation, physical/chemical process catalyst, catalyst activation/preparation, etc. , The effect of reducing heat dissipation loss and improving production efficiency

Inactive Publication Date: 2014-07-16
CHINA UNIV OF PETROLEUM (EAST CHINA)
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The existence of this phenomenon of catalyst loss limits the use of too expensive catalysts and toxic catalysts in circulating fluidized bed reactors.
Catalysts are too expensive, making the process uneconomical; catalysts are poisonous, causing environmental disaster
[0006] Therefore, for the reaction system of propane and butane dehydrogenation to corresponding olefins, if a circulating fluidized bed is used, neither a supported Pt catalyst can be used because it is too expensive, nor can a toxic supported Cr 2 o 3 Catalysts, because lost catalysts will pollute the environment, even if they can all be recovered, there are still problems in harmless disposal

Method used

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  • Continuous reaction regeneration device utilizing vulcanization catalyst to perform alkane dehydrogenation
  • Continuous reaction regeneration device utilizing vulcanization catalyst to perform alkane dehydrogenation
  • Continuous reaction regeneration device utilizing vulcanization catalyst to perform alkane dehydrogenation

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Experimental program
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Effect test

Embodiment 1

[0054] The feed rate of the propane raw material is 5kg / h, and the raw material contains hydrogen sulfide, and its content is 0.5wt% in terms of sulfur. After the raw material is preheated by the heating furnace, it enters the reactor through a ring pipe equipped with multiple nozzles. There are two layers of distribution plates inside, and the opening ratio is 45%. The reaction temperature is 590°C, and the axial superficial gas velocity under the actual reaction conditions in the reactor is 0.5m / s; the reacted catalyst then enters the regenerator, and the temperature in the regenerator is controlled at 750°C, and the supplementary fuel of the catalyst For diesel, the temperature of the regenerator is controlled by the amount of diesel, and the average residence time of the catalyst in the regenerator is 9 minutes. Then the regenerated catalyst enters the pre-sulfurizer built into the reactor through the regenerated inclined pipe, with an average residence time of 5 minutes. ...

Embodiment 2

[0057] The raw material of this embodiment contains isobutane, and its composition is as shown in Table 1. During the dehydrogenation reaction, the reaction temperature is 560 ° C, and the axial superficial gas velocity in the reactor is 0.35m / s. In addition to the above differences, See embodiment 1 for other technological processes and process parameters. The product distribution after catalytic dehydrogenation is shown in Table 2, the conversion rate of isobutane is 65.59wt%, and the selectivity of isobutene is 84.51wt%.

Embodiment 3

[0059] Propane (composition in the propane raw material is as shown in Table 1) the feed rate of raw material is 5kg / h, contains hydrogen sulfide in the raw material, and its content is 1.0wt% in sulfur, raw material is preheated to 400 ℃ through heating furnace, passes The loop pipe with multiple nozzles enters the reactor, and two layers of distribution plates are arranged in the reactor, and the opening ratio is 45%. The reaction temperature is 650°C, and the axial superficial gas velocity under the actual reaction conditions in the reactor is 0.02m / s; the reacted catalyst then enters the regenerator, and the temperature in the regenerator is controlled at 550°C, and the supplementary fuel of the catalyst For diesel, the temperature of the regenerator is controlled by the amount of diesel, and the average residence time of the catalyst in the regenerator is 9 minutes. Then the regenerated catalyst enters the built-in presulfurizer of the reactor through the regenerated incl...

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Abstract

The invention relates to a continuous reaction regeneration device utilizing a vulcanization catalyst to perform alkane dehydrogenation. The continuous reaction regeneration device comprises a reactor, a catalyst regenerator and a catalyst pre-vulcanizer. The reactor and the catalyst regenerator are connected by a catalyst generation inclined tube and a catalyst lifting conveying pipe, and the catalyst regenerator and the catalyst pre-vulcanizer are connected through a regeneration inclined pipe. The catalyst pre-vulcanizer consists of an inlet and an outlet, and the outlet is directly communicated with the reactor. The regeneration device can realize a successive process of dehydrogenation reaction, catalyst regeneration and afterburning as well as catalyst prevulcanization, thus greatly improving the production efficiency of the device.

Description

technical field [0001] The invention relates to a continuous reaction regeneration device for alkane dehydrogenation, in particular to a continuous reaction regeneration device for alkane dehydrogenation using a sulfurized catalyst. Background technique [0002] The heat of reaction for dehydrogenation of propane and butane into corresponding olefins is around 120kJ / mol, which is a strong endothermic reaction. In addition, during the catalytic dehydrogenation reaction of propane and butane, the catalyst will be deactivated by carbon deposition. Some catalysts need to be regenerated by charring within tens of minutes, and some catalysts need to be regenerated by charring within tens of hours. For such a reaction system, a fixed bed reactor is used. First, the heat transfer efficiency of the catalyst bed is low, which is inconvenient to provide heat for the reaction in time; second, the catalyst needs to be frequently burnt and regenerated. The temperature of the layer, and b...

Claims

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Application Information

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IPC IPC(8): C07C5/333C07C11/06C07C11/09B01J38/02B01J37/20
CPCY02P20/584
Inventor 李春义王国玮孙楠楠孙亚楠
Owner CHINA UNIV OF PETROLEUM (EAST CHINA)
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