Granted Patent B2

US 12,325,833 · App. 17/865,751 · Granted Jun 10, 2025

Inventors: Aaron Chi Akah (Dhahran, SA); Qi Xu (Dhahran, SA); Musaed Salem Al-Ghrami (Dammam, SA); Zhonglin Zhang (Dhahran, SA)

Assignee: Saudi Arabian Oil Company

C10G69/14C01B3/24C10B55/00C10G9/36C10G11/20C10G21/003C10G49/22C01B2203/065C01B2203/1241C10G2300/1033C10G2300/301C10G2300/4006C10G2300/4012C10G2300/4018C10G2300/4081C10G2300/42C10G2400/20C10G2400/30

Abstract

Claims (52)

1. An integrated process for upgrading a hydrocarbon oil feed stream utilizing a delayed coker and steam enhanced catalytic cracker, the method comprising:

solvent deasphalting the hydrocarbon oil stream to form at least a deasphalted oil stream and heavy residual hydrocarbons, the heavy residual hydrocarbons comprising atleast asphaltenes;

delayed coking the heavy residual hydrocarbons to form petroleum coke and a delayed coker product stream;

hydrotreating the delayed coker product stream and the deasphalted oil stream to form a light C 5+ hydrocarbon stream, and a heavy C 5+ hydrocarbon stream;

steam enhanced catalytically cracking the light C 5+ hydrocarbon stream in a first steam enhanced catalytic cracker to form a light steam enhanced catalytically cracked product comprising olefins, benzene, toluene, xylene, naphtha, or combinations thereof; and

steam enhanced catalytically cracking the heavy C 5+ hydrocarbon stream in a second steam enhanced catalytic cracker to form a heavy steam enhanced catalytically cracked product comprising olefins, benzene, toluene, xylene, naphtha, or combinations thereof, and wherein,

a first ratio of gas hourly space velocity of steam to gas hourly space velocity of the light C 5+ hydrocarbon stream in the first steam enhanced catalytic cracker is less than a second ratio of gas hourly space velocity of steam to gas hourly space velocity of the heavy C 5+ hydrocarbon stream in the second steam enhanced catalytic cracker,

the first ratio is from 0.2 to 0.8, and

the second ratio is from 0.8 to 1.0.

2. The process of claim 1 , further comprising passing at least a portion of the light steam enhanced catalytically cracked product, the heavy steam enhanced catalytically cracked product, or both to a final product separator to produce one or more product streams and one or more recycle streams.

3. The process of claim 1 , wherein the one or more product streams comprise:

a first product stream comprising ethylene, propylene, butylene, or combinations thereof; and

a second product stream comprising benzene, toluene, xylenes, or combinations thereof.

4. The process of claim 1 , wherein:

the light C 5+ hydrocarbon fraction comprises C 5+ hydrocarbons having a T 95 boiling point of less than 200° C.; and

the heavy C 5+ hydrocarbon fraction comprises C 5+ hydrocarbons having a T 5 boiling point of greater than or equal to 200° C.

5. The process of claim 2 , wherein

hydrotreating the delayed coker product stream and the deasphalted oil stream additionally forms a C 1 hydrocarbon stream and a C 2 -C 4 hydrocarbon stream; and

the C 1 hydrocarbon stream, the C 2 -C 4 hydrocarbon stream, the light C 5+ hydrocarbon stream, and the heavy C 5+ hydrocarbon stream together comprise a hydrotreated product stream.

6. The process of claim 5 , further comprising:

methane cracking the C 1 hydrocarbon stream to form hydrogen;

steam cracking the C 2 -C 4 hydrocarbon stream to form a steam cracked product stream comprising light olefins, naphtha, and BTX; and

passing the steam cracked product stream to the final separator to thereby separate the olefins, the naphtha, and the BTX, and to thereby produce the one or more product streams and the one or more recycle streams, wherein the one or more recycle streams comprise a methane recycle stream, a steam cracker recycle stream, a hydrotreater recycle stream, and a delayed coker recycle stream;

delayed coking the delayed coker recycle stream to form additional delayed coker product stream, wherein the delayed coker recycle stream comprises heavy cycle oil having boiling points of between 426° C. to 650° C.;

hydrotreating the hydrotreater recycle stream to form additional C 1 hydrocarbon stream, C 2 -C 4 hydrocarbon stream, light C 5+ hydrocarbon stream, heavy C 5+ hydrocarbon stream, or combinations thereof, wherein the hydrotreater recycle stream comprises cracked naphtha and light cycle oil having boiling points of between 185° C. to 426° C.;

methane cracking the methane recycle stream to form additional hydrogen;

steam cracking the steam cracker recycle stream to form additional steam cracked product stream, wherein the steam cracker recycle stream comprises C 2 -C 4 hydrocarbons; and

passing the hydrogen to the hydrotreater to be recycled in the hydrotreater.

7. The process of claim 6 , further comprising passing the hydrotreated product stream to a first product separator to separate the C 1 hydrocarbon stream, the C 2 -C 4 hydrocarbon stream, the light C 5+ hydrocarbon stream, and the heavy C 5+ hydrocarbon stream.

8. The process of claim 1 , further comprising

initially passing the hydrocarbon oil stream through a feed separator to separate the hydrocarbon oil stream into a heavy hydrocarbon fraction and a light hydrocarbon fraction;

solvent deasphalting the heavy hydrocarbon fraction to form at least the deasphalted oil stream and the heavy residual hydrocarbons; and

steam enhanced catalytically cracking at least the light hydrocarbon fraction in the first steam enhanced catalytic cracker to form the light steam enhanced catalytically cracked product.

9. The process of claim 1 , wherein the hydrocarbon oil stream comprises whole crude oil or crude oil fractions.

10. The process of claim 6 , wherein:

the solvent deasphalting unit is operated at a temperature of from 60° C. to 90° C. and a pressure of from 0.1 MPa to 0.4 MPa;

the delayed coker is operated at a temperature of from 450° C. to 600° C. and a pressure of from 0.1 MPa to 0.4 MPa;

the hydrotreating zone is operated at a temperature of from 370° C. to 500° C. and a pressure of from 0.1 MPa to 0.2 MPa;

the steam enhanced catalytic cracking system is operated at a temperature of from 525° C. to 750° C. and a pressure of from 0.1 MPa to 0.2 MPa;

the methane cracking zone is operated at a temperature of from 850° C. to 1200° C. and a pressure of from 0.1 MPa to 0.2 MPa; and

the steam cracking zone is operated at a temperature of from 800° C. to 950° C. and a pressure of from 0.1 MPa to 0.2 MPa.

11. The process of claim 1 , wherein:

the deasphalted oil stream comprises C 1 to C 5+ hydrocarbons;

the heavy residual hydrocarbons comprise hydrocarbons C 5+ hydrocarbons having boiling points of between 426° C. to 650° C.;

the delayed coker oil stream comprises C 1 to C 5+ hydrocarbons having boiling points of less than 650° C.; and

the petroleum coke comprises hydrocarbons having boiling points of greater than 650° C.

12. The process of claim 1 , wherein:

steam enhanced catalytically cracking the light C 5+ hydrocarbon stream in the first steam enhanced catalytic cracker forms the olefins and the naphtha in a ratio of from 2:1 to 7:1 olefins to naphtha; and

steam enhanced catalytically cracking the heavy C 5+ hydrocarbon stream in the second steam enhanced catalytic cracker forms the olefins and the naphtha in a ratio of from 1.5:1 to 0.8:1 olefins to naphtha.

13. The process of claim 12 , wherein:

the first steam enhanced catalytic cracker operates with a residence time of from 3 seconds to 10 seconds, a hourly space velocity of from 0.1 h −1 to 1 h −1 , or both; and

the second steam enhanced catalytic cracker operates with a residence time of from 1 second to 3 seconds, a hourly space velocity of from 9 h −1 to 40 h −1 , or both.

Assignments (1)

Continuity (1)

References Cited (45)