System and method for preparing propylene by catalytic dehydration of methanol
A technology for catalytic dehydration and methanol, which is applied in the direction of chemical instruments and methods, catalysts, molecular sieve catalysts, etc., can solve the problems of methanol coking loss, slow reaction rate, and large heat release, so as to avoid frequent switching, slow coking rate, and reduce The effect of energy consumption
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Embodiment 1
[0053] Such as figure 1 As shown, a reaction process for methanol to light olefins using a fluidized bed includes a dehydration reactor 100, a catalyst regenerator 200, a heating furnace 300, a heat exchanger 400 and a separation unit 500, and the dehydration reactor 100 is regenerated with the catalyst The device 200 is a fluidized bed reactor; the dehydration reactor 100 is equipped with 40 tons of HZSM-5 high silicon molecular sieve catalyst with a silicon-aluminum ratio of 200. Feed stream 10 is methanol and water at flow rates of 200 and 130 t / h, respectively. The higher olefin fraction 90 contains C4-C6 hydrocarbons, and the flow rate is 270 tons / hour. The raw material stream is mixed with the high-carbon olefin fraction 90, and after passing through the heat exchanger 400 and the heating furnace 300, the temperature rises to 400° C., and enters the dehydration reactor 100 for reaction. Due to the exothermic reaction, the reaction temperature in the dehydration reactor...
Embodiment 2
[0055] Such as figure 1 As shown, a reaction process for methanol to light olefins using a fluidized bed includes a dehydration reactor 100, a catalyst regenerator 200, a heating furnace 300, a heat exchanger 400 and a separation system 500, and the dehydration reactor 100 is regenerated with the catalyst The device 200 is a fluidized bed reactor; the dehydration reactor 100 is equipped with 7 tons of HZSM-5 molecular sieve catalyst with a silicon-aluminum ratio of 200. Feed stream 10 is methanol and water with flow rates of 200 t / h and 130 t / h, respectively. The higher olefin fraction 90 contains C4-C6 hydrocarbons, and the flow rate is 200 tons / hour. The raw material stream 10 is mixed with the high carbon olefin fraction, after passing through the heat exchanger 400 and the heating furnace 300, the temperature rises to 400° C., and enters the dehydration reactor 100 for reaction. Due to the exothermic reaction, the reaction temperature in the dehydration reactor 100 was 4...
Embodiment 3
[0057] Such as figure 1 As shown, a reaction process for methanol to light olefins using a fluidized bed includes a dehydration reactor 100, a catalyst regenerator 200, a heating furnace 300, a heat exchanger 400 and a separation system 500, and the dehydration reactor 100 is regenerated with the catalyst The device 200 is a fluidized bed reactor; the dehydration reactor 100 is equipped with 60 tons of HZSM-5 molecular sieve catalyst with a silicon-aluminum ratio of 200. Feed stream 10 is methanol and water with flow rates of 200 t / h and 150 t / h, respectively. The higher olefin fraction 90 contains C4-C6 hydrocarbons, and the flow rate is 300 tons / hour. The raw material stream 10 is mixed with the high-carbon olefin fraction 90, and after passing through the heat exchanger 400 and the heating furnace 300, the temperature rises to 330° C., and enters the dehydration reactor 100 for reaction. Due to the exothermic reaction, the reaction temperature in the dehydration reactor 1...
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