Process and system for conversion of crude oil to petrochemicals and fuel products integrating vacuum gas oil hydrotreating and steam cracking

Patent metadata

Field	Value
Publication number	US-10619112-B2
Application number	US-201715817127-A
Country	US
Kind code	B2
Filing date	Nov 17, 2017
Priority date	Nov 21, 2016
Publication date	Apr 14, 2020
Grant date	Apr 14, 2020

Abstract

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from vacuum gas oil hydrotreating.

First claim

The invention claimed is:

1. An integrated process for producing petrochemicals and fuel products from a crude oil feed comprising:
separating from the crude oil feed, in an atmospheric distillation unit (ADU), at least
a first ADU fraction comprising straight run naphtha,
a second ADU fraction comprising at least a portion of middle distillates from the crude oil feed, and
a third ADU fraction comprising atmospheric residue;

separating from the third ADU fraction, in a vacuum distillation unit (VDU), at least
a first VDU fraction comprising vacuum gas oil;

hydroprocessing in a distillate hydroprocessing (DHP) zone middle distillates from the second ADU fraction, and recovering at least a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;
hydrotreating in a gas oil hydrotreating (GOHT) zone vacuum gas oil from the first VDU fraction, and recovering a first GOHT fraction containing components boiling at or below an atmospheric residue end boiling point and including LPG, naphtha and middle distillate range components, and hydrotreated gas oil;
steam cracking, in a mixed feed steam cracking (MFSC) zone, naphtha from the first ADU fraction and raffinate derived from an aromatics extraction zone, and, in a gas oil steam cracking (GOSC) zone, hydrotreated gas oil, wherein steam cracking operates under conditions effective to recover at least a mixed product stream H2, methane, ethane, ethylene, mixed C3s and mixed C4s; pyrolysis gas; and pyrolysis oil;
recovering, from the mixed product stream, H2, methane, non-olefinic C2-C4s, and petrochemicals ethylene, propylene and butylenes,
hydroprocessing pyrolysis gas from steam cracking in a naphtha hydroprocessing zone, and recovering hydrotreated pyrolysis gas; and
separating aromatics from hydrotreated pyrolysis gas in the aromatics extraction zone for recovery of petrochemical aromatic products, and aromatics extraction zone raffinate, wherein the raffinate derived from aromatics extraction is all or a portion of the aromatics extraction zone raffinate.

2. The process as in claim 1 , wherein the GOHT zone operates in the presence of hydrotreating catalyst to convert 2-30 wt % of feed to the GOHT zone into the first GOHT fraction.

3. The process as in claim 2 , wherein the GOHT zone operating conditions include:
a reactor inlet temperature (° C.) in the range of from about 324-496;
a reactor outlet temperature (° C.) in the range of from about 338-516;
a start of run (SOR) reaction temperature (° C.), as a weighted average bed temperature (WABT), in the range of from about 302-462;
an end of run (EOR) reaction temperature (° C.), as a WABT, in the range of from about 333-509;
a reaction inlet pressure (barg) in the range of from about 91-137;
a reaction outlet pressure (barg) in the range of from about 85-127;
a hydrogen partial pressure (barg) (outlet) in the range of from about 63-95;
a hydrogen treat gas feed rate (SLt/Lt) up to about 525;
a hydrogen quench gas feed rate (SLt/Lt) up to about 450;
a make-up hydrogen feed rate (SLt/Lt) up to about 220; and
a liquid hourly space velocity (h −1 ), on a fresh feed basis relative to the hydrotreating catalysts, in the range of from about 0.1-10.0.

4. The process as in claim 1 , wherein the GOHT zone operates under conditions effective for feed conditioning and to maximize targeted conversion to petrochemicals.

5. The process as in claim 1 , wherein the GOHT zone operates in the presence of hydrotreating catalyst to convert 20-30 wt % of feed to the GOHT zone into the first GOHT fraction.

6. The process as in claim 5 , wherein the GOHT zone operating conditions include:
a reactor inlet temperature (° C.) in the range of from about 461-496;
a reactor outlet temperature (° C.) in the range of from about 480-516;
a start of run (SOR) reaction temperature (° C.), as a weighted average bed temperature (WABT), in the range of from about 430-462;
an end of run (EOR) reaction temperature (° C.), as a WABT, in the range of from about 473-509;
a reaction inlet pressure (barg) in the range of from about 110-137;
a reaction outlet pressure (barg) in the range of from about 104-118;
a hydrogen partial pressure (barg) (outlet) in the range of from about 76-95;
a hydrogen treat gas feed rate (SLt/Lt) up to about 525;
a hydrogen quench gas feed rate (SLt/Lt) up to about 450;
a make-up hydrogen feed rate (SLt/Lt) up to about 220; and
a liquid hourly space velocity (h −1 ), on a fresh feed basis relative to the hydrotreating catalysts, in the range of from about 0.5-0.7.

7. The process as in claim 1 , further wherein the middle distillates in the second ADU fraction comprise heavy atmospheric gas oil that is routed to the GOHT zone.

8. The process as in claim 1 , further wherein the middle distillates in the second ADU fraction comprise heavy atmospheric gas oil that is processed in the GOSC zone without hydroprocessing.

9. The process as in claim 1 , wherein the middle distillates in the second ADU fraction comprise kerosene that is processed in a kerosene sweetening process to recover a kerosene fuel product, and a straight run diesel fraction that is the portion of the second ADU fraction that is processed in the distillate hydroprocessing zone.

10. The process as in claim 9 , further wherein the middle distillates in the second ADU fraction comprise heavy atmospheric gas oil that is processed in the GOHT zone or the GOSC zone.

11. The process as in claim 1 , wherein at least about 75 weight percent of the first DHP fraction is passed to the MFSC zone or to the ADU.

12. The process as in claim 1 , wherein at least about 75 weight percent of naphtha from the first GOHT fraction is routed to the mixed feed stream cracking zone or to the atmospheric distillation zone.

13. The process as in claim 1 , wherein at least about 75 weight percent of the first GOHT fraction is routed to the DHP zone.

14. The process as in claim 1 , wherein non-olefinic C4s recovered from the mixed product stream are recycled to the MFSC zone.

15. The process as in claim 1 , wherein non-olefinic C4s recovered from the mixed product stream are recycled to a separate processing zone for production of additional petrochemicals.

16. The process as in claim 15 , wherein the separate processing zone converts mixture of butenes into mixed butanols.

17. The process as in claim 15 , further comprising
recovering C5s from the hydrotreated pyrolysis gas;
passing the recovered C5s to the separate processing zone for production of additional petrochemicals;
passing a portion of the recovered ethylene to the separate processing zone;
wherein the separate processing zone is a metathesis reaction zone which produces petrochemical propylene and a C4/C5 raffinate stream that is recycled to the mixed feed stream cracking zone.

18. The process as in claim 15 , further comprising recovering C5s from the hydrotreated pyrolysis gas and passing the recovered C5s to the MFSC zone, the separate processing zone for production of additional petrochemicals, or both to the mixed feed stream cracking zone and the separate processing zone for production of additional petrochemicals.

19. The process as in claim 18 wherein the recovered C5s are passed to the mixed feed stream cracking zone.

20. The process as in claim 18 wherein the recovered C5s are passed to the separate processing zone for production of additional petrochemicals, wherein the

Assignees

• Saudi Arabian Oil Co

Inventors

• Al-Ghamdi Mohammed Saeed

Classifications

• C10G47/00

  Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06) · CPC title

• C10G2400/02

  Gasoline · CPC title

• C10G9/36

  with heated gases or vapours · CPC title

• C10G21/00

  Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents (C10G17/00, C10G19/00 take precedence) · CPC title

• C10G2300/1037

  Hydrocarbon fractions · CPC title