US 11,873,457 B2
Catalytic conversion process and system for producing gasoline and propylene
Xuhui Bai, Beijing (CN); Yanfen Zuo, Beijing (CN); Youhao Xu, Beijing (CN); Yibin Luo, Beijing (CN); Xingtian Shu, Beijing (CN); Xieqing Wang, Beijing (CN); and Xin Wang, Beijing (CN)
Assigned to CHINA PETROLEUM & CHEMICAL CORPORATION, Beijing (CN); and RESEARCH INSTITUTE OF PETROLEUM PROCESSING, SINOPEC, Beijing (CN)
Appl. No. 17/442,055
Filed by CHINA PETROLEUM & CHEMICAL CORPORATION, Beijing (CN); and RESEARCH INSTITUTE OF PETROLEUM PROCESSING, SINOPEC, Beijing (CN)
PCT Filed Mar. 17, 2020, PCT No. PCT/CN2020/079666
§ 371(c)(1), (2) Date Sep. 22, 2021,
PCT Pub. No. WO2020/192491, PCT Pub. Date Oct. 1, 2020.
Claims priority of application No. 201910224120.2 (CN), filed on Mar. 22, 2019.
Prior Publication US 2022/0169930 A1, Jun. 2, 2022
Int. Cl. C10G 69/12 (2006.01); C10G 11/05 (2006.01); C10G 11/18 (2006.01); C10G 45/54 (2006.01); C10G 50/00 (2006.01); C10G 57/02 (2006.01)
CPC C10G 69/126 (2013.01) [C10G 11/05 (2013.01); C10G 11/18 (2013.01); C10G 45/54 (2013.01); C10G 50/00 (2013.01); C10G 57/02 (2013.01); C10G 2300/4006 (2013.01); C10G 2300/4012 (2013.01); C10G 2300/4018 (2013.01); C10G 2300/4025 (2013.01); C10G 2300/4081 (2013.01); C10G 2300/70 (2013.01); C10G 2400/02 (2013.01); C10G 2400/20 (2013.01)] 13 Claims
OG exemplary drawing
 
1. A process for producing gasoline and propylene, comprising the steps of:
1) Subjecting a feedstock oil to a first catalytic conversion reaction in a first catalytic conversion reaction device to obtain a first reaction product comprising propylene, C4 olefin and a gasoline component;
2) Separating the first reaction product to obtain a propylene fraction, a gasoline fraction, a first C4 olefin-containing fraction having 40-100 wt % C4 olefin, optionally a light cycle oil fraction and optionally a fluidized catalytic cracking gas oil (FGO) fraction;
3) Subjecting the first C4 olefin-containing fraction obtained in step 2) or a combination of the first C4 olefin-containing fraction obtained in step 2) and a C4 olefin-containing fraction from an external source to olefin oligomerization in an oligomerization reactor to obtain an oligomerization product comprising C12 olefin,
separating the oligomerization product to obtain a second C4 olefin-containing fraction, a C8 olefin-containing fraction, and a C12 olefin-containing fraction, wherein the C12 olefin-containing fraction has a C12 olefin content of no less than 70 wt %, based on the weight of the C12 olefin-containing fraction;
4) Sending the C12 olefin-containing fraction to the first catalytic conversion reaction device, and/or sending the C12 olefin-containing fraction to a second catalytic conversion reaction device for a second catalytic conversion reaction to obtain a second reaction product comprising propylene; and
5) Optionally, subjecting the FGO fraction to a first hydrotreatment in a first hydrotreating reactor to obtain a hydrogenated FGO, and recycling at least a part of the hydrogenated FGO to the first catalytic conversion reaction device and/or sending it to the second catalytic conversion reaction device, and/or recycling the light cycle oil fraction to the first catalytic conversion reaction device and/or sending it to the second catalytic conversion reaction device,
wherein the first catalytic conversion reaction device is a diameter-transformed riser reactor comprising a first reaction zone and a second reaction zone having a diameter greater than the first reaction zone along the direction of the reaction stream,
wherein the second catalytic conversion reaction device, when present, is a fluidized bed reactor that is a riser reactor or a composite reactor comprising a riser in combination with a dense phase bed, wherein the riser reactor is an equal-diameter riser reactor, a constant-linear-velocity riser reactor or a diameter-transformed riser reactor,
wherein the reaction conditions in the first reaction zone include a reaction temperature of about 450-620° C., a reaction time of about 0.5-2.0 seconds, a catalyst-to-feedstock weight ratio of about 3:1 to about 15:1, a steam-to-feedstock weight ratio of about 0.03:1 to about 0.3:1,
wherein the reaction conditions in the second reaction zone include a reaction temperature of about 460-550° C., a reaction time of about 2-30 seconds, a catalyst-to-feedstock weight ratio of about 4:1 to about 18:1, and a steam-to-feedstock weight ratio of about 0.03:1 to about 0.3:1, and
wherein:
the second C4 olefin-containing fraction is sent to the oligomerization reactor,
the C8 olefin-containing fraction is sent to the first reaction zone in the diameter-transformed riser reactor, and
the C12 olefin-containing fraction is sent to the second reaction zone of the diameter-transformed riser reactor.