Catalytic Conversion and Oligomerization of Feedstock Oil

Example 3

The test was conducted in accordance with the process flow shown in FIG. 3 using Feedstock oil C as a starting material for catalytic conversion on an equal-diameter riser reactor. Feedstock oil C was contacted with Catalyst C, and reacted in the riser reactor under conditions including a reaction temperature of 530° C., a reaction time of 3.5 seconds, a catalyst-to-oil weight ratio of 8, and a steam-to-oil weight ratio of 0.1 to obtain a spent catalyst and a reaction product. The spent catalyst was regenerated, and the regenerated catalyst was recycled to the riser reactor as the catalytic conversion catalyst. The reaction product was split according to distillation range in a product separation device to obtain dry gas, ethylene, propylene, propane, a fraction comprising C₄ olefin (with a C₄ olefin content of 85.0 wt %), butane, gasoline, diesel oil and slurry oil.

The fraction comprising C₄ olefin was fed to an oligomerization reactor for oligomerization, and the fraction comprising C₁₂ olefin (with a C₁₂ olefin content of 85.3 wt %) separated by a rectifying column was recycled to the riser reactor. The C₁₂ olefin recycled to the riser reactor for further cracking accounted for 14.17 wt % of the total catalytic conversion feedstock. The operating conditions and product distribution are listed in Table 5.

The operation was substantially the same as in Example 3, except that the catalytic conversion product was split according to distillation range in the product separation device to obtain dry gas, liquefied gas, propylene, gasoline, diesel oil and slurry oil, and the recycling of the catalytic conversion product was not performed. The operating conditions and product distribution are listed in Table 5.