US 12,435,284 B2
Fluidized catalytic conversion method for producing low-carbon olefins from hydrocarbons
Youhao Xu, Beijing (CN); Yanfen Zuo, Beijing (CN); Xin Wang, Beijing (CN); Mingyuan He, Beijing (CN); Youxin Sha, Beijing (CN); and Xuhui Bai, Beijing (CN)
Assigned to CHINA PETROLEUM & CHEMICAL CORPORATION, Beijing (CN); and SINOPEC RESEARCH INSTITUTE OF PETROLEUM PROCESSING CO., LTD., Beijing (CN)
Appl. No. 18/260,707
Filed by CHINA PETROLEUM & CHEMICAL CORPORATION, Beijing (CN); and SINOPEC RESEARCH INSTITUTE OF PETROLEUM PROCESSING CO., LTD., Beijing (CN)
PCT Filed Jun. 24, 2021, PCT No. PCT/CN2021/101927
§ 371(c)(1), (2) Date Jul. 7, 2023,
PCT Pub. No. WO2022/147972, PCT Pub. Date Jul. 14, 2022.
Claims priority of application No. 202110031551.4 (CN), filed on Jan. 11, 2021; application No. 202110245789.7 (CN), filed on Mar. 5, 2021; and application No. 202110296896.2 (CN), filed on Mar. 19, 2021.
Prior Publication US 2024/0059989 A1, Feb. 22, 2024
Int. Cl. C10G 69/04 (2006.01)
CPC C10G 69/04 (2013.01) [C10G 2300/1088 (2013.01); C10G 2300/4006 (2013.01); C10G 2300/4012 (2013.01); C10G 2300/4081 (2013.01); C10G 2400/20 (2013.01)] 19 Claims
OG exemplary drawing
 
1. A fluidized catalytic conversion method for producing light olefins from hydrocarbons, comprises the following steps:
1) introducing an olefin-rich feedstock into a first reaction zone of a fluidized catalytic conversion reactor, contacting with a catalytic conversion catalyst having a temperature of 650° C. or higher, and reacting under first catalytic conversion conditions, wherein the olefin-rich feedstock has an olefin content of 50 wt % or more;
2) introducing a heavy feedstock into a second reaction zone of the fluidized catalytic conversion reactor downstream of the first reaction zone, contacting with the catalytic conversion catalyst from the first reaction zone after the reaction of step 1), and reacting under second catalytic conversion conditions;
3) separating an effluent of the fluidized catalytic conversion reactor to obtain a reaction product vapor and a spent catalyst, and separating the reaction product vapor to obtain ethylene, propylene, butylene, a first catalytic cracking distillate oil and a second catalytic cracking distillate oil; an initial boiling point of the first catalytic cracking distillate oil is in a range of more than 20° C. to less than 140° C., a final boiling point of the second catalytic cracking distillate oil is in a range of more than 250° C. to less than 550° C., and a cut point between the first catalytic cracking distillate oil and the second catalytic cracking distillate oil is in a range of 140° C. to 250° C.;
4) separating the first catalytic cracking distillate oil to obtain an olefin-rich stream having a C5+ olefin content of at least 50 wt %; and
5) recycling at least a part of the olefin-rich stream to step 1) for further reaction,
wherein the first catalytic conversion conditions include:
a reaction temperature of 600-800° C.;
a reaction pressure of 0.05-1 MPa;
a reaction time of 0.01-100 seconds; and
a weight ratio of the catalytic conversion catalyst to the olefin-rich feedstock of (1-200): 1; and
the second catalytic conversion conditions include:
a reaction temperature of 400-650° C.;
a reaction pressure of 0.05-1 MPa;
a reaction time of 0.01-100 seconds; and
a weight ratio of the catalytic conversion catalyst to the heavy feedstock of (1-100): 1, wherein the fluidized catalytic conversion method further comprises:
7) recycling at least a part of the butylene separated in step 3) to the catalytic conversion reactor upstream of a position at which the olefin-rich feedstock is introduced to contact with the catalytic conversion catalyst for reaction under third catalytic conversion conditions that include:
a reaction temperature of 650-800° C.,
a reaction pressure of 0.05-1 MPa,
a reaction time of 0.01-10 seconds, and
a weight ratio of the catalytic conversion catalyst to the butylene of (20-200):1.