Coaxial segmented fluidized bed reactor for converting methanol and/or dimethyl ether to ethylene, propylene and aromatics and its reaction method
A fluidized bed reaction, dimethyl ether technology, applied in chemical instruments and methods, hydrocarbon production from oxygen-containing organic compounds, ethylene production, etc., can solve problems such as low yields of ethylene, propylene and aromatic hydrocarbons, and reduce the influence of diffusion. , the effect of expanding the airspeed adjustment range and promoting contact
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Embodiment 1
[0052] use as figure 1 device shown.
[0053] The diameter of the first reaction section of the reactor is 2 meters, and the height accounts for 30% of the total height of the reactor; the ratio of the diameter of the second reaction section to the diameter of the first reaction section is 1.2:1, and its height accounts for 55% of the total height of the reactor. %; The ratio of the diameter of the dilute phase section to the diameter of the second reaction section is 1.8:1, and its height accounts for 10% of the total height of the reactor. The height of the first transition section accounts for 3% of the total height of the reactor, and the height of the second transition section accounts for 2% of the total height of the reactor. A heat extractor is arranged outside the reactor, and the height of the heat extractor accounts for 30% of the height of the reactor. A heat extractor is arranged outside the regenerator, and the height of the heat extractor accounts for 80% of t...
Embodiment 2
[0060] use as figure 1 device shown.
[0061] The diameter of the first reaction section of the reactor is 1.5 meters, and the height accounts for 5% of the total height of the reactor; the ratio of the diameter of the second reaction section to the diameter of the first reaction section is 1.8:1, and its height accounts for 70% of the total height of the reactor. %; The ratio of the diameter of the dilute phase section to the diameter of the second reaction section is 2.5:1, and its height accounts for 20% of the total height of the reactor. The height of the first transition section accounts for 2% of the total height of the reactor, and the height of the second transition section accounts for 3% of the total height of the reactor. A heat extractor is arranged outside the reactor, and the height of the heat extractor accounts for 95% of the height of the reactor. A heat extractor is arranged outside the regenerator, and the height of the heat extractor accounts for 30% of ...
Embodiment 3
[0068] The device of Example 1 was used.
[0069] The reaction conditions of the reactor are: the temperature is 550°C, the reaction pressure in gauge pressure is 0 MPa, the weight space velocity of methanol is 10 (gram / hour) / gram catalyst, the mass ratio of catalyst circulation amount and methanol feed amount It is 40:1, and the average superficial gas velocity is 1 m / s. The temperature of the regenerator was 580°C. The content of char on the regenerated catalyst is 0.09% by weight based on the mass percentage of the catalyst.
[0070] The stripping medium is water vapor. The lifting medium is N 2 . The regeneration medium is air and O 2 mixture with a volume ratio of 8:2.
[0071] Using methanol as a raw material, the water content is 10% by weight. The mass ratio of propane: C4 and C5 and C6 non-aromatic in the circulating material is 2:8. The feed mass ratio of methanol and recycle material is 10:1.
[0072] A Ga-β catalyst is used.
[0073] The preparation steps...
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