Method for preparing ethylene and propylene and fluidized bed reaction-regeneration device
A fluidized bed reactor, regeneration device technology, applied in ethylene production, chemical instruments and methods, catalysts, etc., to achieve the effect of high yield
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Embodiment 1
[0065] Such as figure 1 As shown, the raw material comprising methanol enters the reactor reaction zone 10 through the reactor raw material feed line 12, contacts with the molecular sieve catalyst, reacts to generate a product containing low-carbon olefins, and carries the unborn catalyst into the reactor separation zone 11, and the gas phase product Entering the separation section, the catalyst enters the regenerator 3 for regeneration through the standby catalyst pipeline, and the regenerated catalyst returns to the reaction zone 10 through the regenerated catalyst pipeline. The outlet of the regenerated catalyst pipeline is provided with a catalyst distributor (not shown in the accompanying drawings), and the distributor is arranged radially and horizontally along the fluidized bed reactor 2, and the regenerated catalyst is evenly distributed in the radial direction of the reaction zone 10 of the fluidized bed reactor. to the plane.
[0066] The waiting catalyst pipeline i...
Embodiment 2
[0070] According to the conditions and steps described in [Example 1], the average amount of carbon deposited on the catalyst in the standby standpipe was 8wt%. The average amount of carbon deposited on the catalyst in the regeneration standpipe is 5wt%. The catalyst density in the riser is 500 kg / m3.
[0071] Fluidized bed reactors are of the turbulent fluidization type. The operating conditions of the reaction zone of the reactor are: the reaction pressure is 0.05MPaG, the reaction temperature is 550°C, the average density of the bed in the reaction zone is 50 kg / m3, and the methanol weight space velocity WHSV is 20h -1 .
[0072] The analysis and monitoring results show that the problem of "cross-gas" between the two devices has never occurred during a driving cycle, and the selectivity of low-carbon olefins is stable within 83±0.5%.
Embodiment 3
[0074] According to the conditions and steps described in [Example 1], the average amount of carbon deposited on the catalyst in the standby standpipe was 5 wt%. The average amount of carbon deposited on the catalyst in the regeneration standpipe is 1wt%. The catalyst density in the riser is 400 kg / m3.
[0075] The fluidized bed reactor is a fast fluidized type. The operating conditions of the reaction zone of the reactor are: the reaction pressure is 0.15MPaG, the reaction temperature is 480°C, the average density of the bed in the reaction zone is 150 kg / m3, and the methanol weight space velocity WHSV is 10h -1 .
[0076] The analysis and monitoring results show that the problem of "cross-gas" between the two devices has never occurred during a driving cycle, and the selectivity of low-carbon olefins is stable within 85±0.5%.
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