Catalytic cracking apparatus and process
The present invention discloses catalytic cracking apparatus and process, which are useful for catalytic cracking of heavy oils with a high heavy oil conversion, a high propylene yield and low dry gas and coke yields.
1. A catalytic cracking process, comprising:
contacting a heavy feedstock and optionally an atomized steam with a catalyst containing a shape-selective zeolite having an average pore size of less than 0.7 nm in a first riser reactor to produce a first effluent comprising a first hydrocarbon product and a first coked catalyst;
separating said first hydrocarbon product from said first coked catalyst in a separation device disposed downstream from the first riser;
contacting a light feedstock and optionally an atomized steam with the catalyst containing a shape-selective zeolite having an average pore size of less than 0.7 nm in a second riser reactor to produce a second effluent comprising a second hydrocarbon product and a second coked catalyst;
separating said first product in a product separation system to obtain a cracked gas, a cracked gasoline, a cracked light cycle oil, and a cracked heavy oil;
feeding all or a part of the cracked heavy oil into the second riser, or into a fluidized bed reactor fluidly connected in series with said second riser reactor, or into both said second riser and said fluidized bed reactor;
feeding the second effluent into the fluidized bed reactor to continue reacting therein and obtaining a third effluent comprising a third hydrocarbon product and a third coked catalyst from the fluidized bed reactor.
2. The catalytic cracking process according to claim 1 , wherein said heavy feedstock comprises heavy hydrocarbons and/or hydrocarbon-rich animal or vegetable oils; wherein said light feedstock comprises gasoline fractions and/or C4 hydrocarbons; wherein said cracked heavy oil is a cracked heavy oil having an atmospheric distillation range of 330-550° C.
3. The catalytic cracking process according to claim 2 , wherein said light feedstock of gasoline fraction is an olefin-rich gasoline fraction which has an olefin content of 20-95 wt % and a final boiling point of not more than 85° C.; and said light feedstock of C4 hydrocarbon is an olefin-rich C4 hydrocarbon which has a C4-olefin content of more than 50 wt %.
4. The catalytic cracking process according to claim 2 , wherein said light feedstock comprises said cracked gasoline from said product separation system.
5. The catalytic cracking process according to claim 2 , further comprising feeding said first hydrocarbon product and said third hydrocarbon product into said product separation system for separation.
6. The catalytic cracking process according to claim 1 , wherein said first riser has a weight ratio between said atomized steam to said heavy feedstock of 2-50 wt %, a reaction pressure of 0.15-0.3 MPa, a reaction temperature of 480-600° C., a catalyst/oil ratio of 5-20, and a reaction time of 0.50-10 seconds.
7. The catalytic cracking process according to claim 1 , wherein said second riser reactor has a reaction temperature of 520-580° C., wherein said light feedstock comprises gasoline fractions, wherein said gasoline fractions to atomized steam ratio is 5-30 wt %, wherein said second riser has a catalyst/oil ratio of 10-30 and a reaction time of 0.10-1.5 seconds.
8. The catalytic cracking process according to claim 1 , wherein said fluidized bed reactor has a reaction temperature of 500-580° C., a weight hourly space velocity of 1-35 h −1 , and a reaction pressure of 0.15-0.3 MPa.
9. The catalytic cracking process according to claim 1 , wherein the fluidized bed has a catalyst to cracked heavy oil ratio of 1-50, a weight hourly space velocity of 1-20 h −1 , and an atomized steam to cracked heavy oil ratio of 5-20 wt %.
10. The catalytic cracking process according to claim 1 , wherein a weight ratio of said cracked heavy oil introduced into said second riser reactor and/or said fluidized bed reactor to said heavy feedstock introduced into said first riser reactor is 0.05-0.30:1.
11. The catalytic cracking process according to claim 1 , wherein said light feedstock comprises gasoline fractions, wherein a weight ratio of said gasoline fractions introduced into said second riser reactor to said heavy feedstock introduced into said first riser reactor is 0.05-0.20:1.
12. The catalytic cracking process according to claim 1 , further comprising: introducing said first coked catalyst into said fluidized bed reactor and introducing a catalyst from said fluidized bed into a stripper; or, introducing said first coked catalyst directly into the stripper.
13. The catalytic cracking process according to claim 1 , further comprising stripping said first coked catalyst and/or said third coked catalyst with steam in a stripper and introducing the stripping steam from said stripper into said fluidized bed reactor.
14. The catalytic cracking process according to claim 1 , wherein said light feedstock comprises C4 hydrocarbons, wherein said C4 hydrocarbons to atomized steam ratio is 10-40 wt %, wherein said second riser has a catalyst/oil of 12-40 and a reaction time of 0.50-2.0 seconds.
15. The catalytic cracking process according to claim 1 , wherein said light feedstock comprises gasoline fractions and C4 hydrocarbons, a weight ratio of C4 hydrocarbons in said light feedstock to said gasoline fractions in said light feedstock is 0-2:1.