Control method of coke-burning regeneration of deactivated catalyst in methanol-to-olefins process
A deactivated catalyst, methanol-to-olefin technology, applied in catalyst regeneration/reactivation, physical/chemical process catalyst, molecular sieve catalyst, etc., can solve the problem of low yield of low-carbon olefins, etc. Yield, the effect of reducing carbon difference
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Embodiment 1
[0017] On the fluidized bed reaction-regeneration cycle device, the catalyst is SAPO-34, the regeneration temperature is 650℃, the regeneration medium is compressed air, the combustion medium is methane and hydrogen, the volume ratio of methane to hydrogen is 5:1, and the auxiliary combustion chamber The oxygen concentration in the outlet gas is 17.5% by volume, the carbon difference between the spent catalyst and the regenerated catalyst can be stabilized at about 2.2% by weight, the regeneration temperature changes within the control value (650°C) ±5°C, the dilute phase temperature of the regenerator is consistent with the density The difference in phase temperature is around 80°C, and no CO tail-ignition has been found. The regenerated catalyst enters the reactor and is mixed with the spent catalyst and contacts with the methanol feedstock. The reaction temperature is 450° C., and the yield of low-carbon olefins is 82.69% by weight.
Embodiment 2
[0019] On the fluidized bed reaction-regeneration cycle device, the catalyst is SAPO-34, the regeneration temperature is 650℃, the regeneration medium is compressed air, the combustion medium is light diesel, the ignition and ignition temperature is 370℃, and the gas in the auxiliary combustion chamber outlet gas The oxygen concentration is 5% by volume, the carbon difference between the spent catalyst and the regenerated catalyst can be stabilized at about 0.8% by weight, the regeneration temperature changes within the control value (650°C) ±7°C, the difference between the dilute phase temperature and the dense phase temperature of the regenerator The value is around 110°C and no CO tail-ignition has been found. The regenerated catalyst enters the reactor and is mixed with the spent catalyst and contacts with the methanol raw material. The reaction temperature is 450° C., and the yield of low-carbon olefin is 80.24% by weight.
Embodiment 3
[0021] On the fluidized bed reaction-regeneration cycle device, the catalyst is SAPO-34, the regeneration temperature is 650℃, the regeneration medium is a mixture of nitrogen and oxygen, the volume ratio of nitrogen and oxygen is 3:1, the combustion medium is propane, and the combustion is assisted. The oxygen concentration in the outlet gas of the chamber is 20% by volume, the carbon difference between the spent catalyst and the regenerated catalyst can be stabilized at about 2.5% by weight, the regeneration temperature changes within the control value (650°C) ±10°C, and the dilute phase temperature of the regenerator is equal to The difference in dense phase temperature is about 68°C, and no CO tail-ignition has been found. The regenerated catalyst enters the reactor and is mixed with the spent catalyst and contacts with the methanol feedstock. The reaction temperature is 450° C., and the yield of low-carbon olefin is 80.03% by weight.
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