Production increasing method for propylene
A technology of propylene and products, which is applied in the direction of ethylene production, bulk chemical production, and hydrocarbon production from oxygen-containing organic compounds. It can solve the problems of low selectivity and low propylene yield, and achieve the reduction of secondary reactions and radial distribution Homogeneous, less agglomerated effect
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Embodiment 1
[0018] The reaction is carried out in a gas-solid co-current downflow fluidized bed reactor, the feed is methanol, the catalyst is SAPO-34, the temperature of reactor A is 470°C, the pressure is 0.1MPa, the residence time is 5 seconds, and the ratio of catalyst to raw material is 4. The carbon four and above components in the reaction product of reactor A enter into reactor B, wherein the temperature of reactor B is 510°C, the pressure is 0.1MPa, the residence time is 8 seconds, the weight ratio of catalyst to hydrocarbon is 5, and the regenerator temperature is It is 530°C. The conversion rate of methanol was 99.8%. Among the hydrocarbon products, ethylene accounted for 52% and propylene accounted for 31%.
Embodiment 2
[0020] The reaction is carried out in a gas-solid co-current downflow fluidized bed reactor, the feed is methanol, the catalyst is SAPO-34, the temperature of reactor A is 450°C, the pressure is 0.02MPa, the residence time is 3 seconds, and the ratio of catalyst to raw material is 5. The carbon four and above components in the reaction product of reactor A enter into reactor B, wherein the temperature of reactor B is 560°C, the pressure is 0.2MPa, the residence time is 5 seconds, the weight ratio of catalyst to hydrocarbon is 1, and the regenerator The temperature is 580°C. The methanol conversion rate was 100%, and among the hydrocarbon products, ethylene accounted for 49% and propylene accounted for 36%.
Embodiment 3
[0022]The reaction is carried out in a gas-solid co-current downflow fluidized bed reactor, the feed is dimethyl ether, the catalyst is SAPO-34, the temperature of reactor A is 560 ° C, the pressure is 0.5 MPa, and the residence time is 15 seconds. The catalyst and raw materials The ratio is 26, and the carbon four and above components in the reaction product of reactor A enter into reactor B, wherein the temperature of reactor B is 620°C, the pressure is 0.4MPa, the residence time is 20 seconds, and the weight ratio of catalyst to hydrocarbon is 0.6, The regenerator temperature was 550°C. The conversion rate of dimethyl ether was 100%. Among the hydrocarbon products, ethylene accounted for 47% and propylene accounted for 28%.
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