Process and system for conversion of crude oil to petrochemicals and fuel products integrating vacuum residue hydroprocessing

Patent metadata

Field	Value
Publication number	US-10487276-B2
Application number	US-201715817133-A
Country	US
Kind code	B2
Filing date	Nov 17, 2017
Priority date	Nov 21, 2016
Publication date	Nov 26, 2019
Grant date	Nov 26, 2019

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 one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, 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 gas oil range intermediates from the vacuum gas oil hydroprocessing zone and the vacuum residue hydrocracking zone.

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, and
a second VDU fraction comprising vacuum residue;

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;
steam cracking, in a mixed feed steam cracking (MFSC) zone, naphtha from the first ADU fraction and raffinate derived from an aromatics extraction zone, wherein steam cracking in the MFSC zone is under conditions effective to recover a mixed product stream comprising 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;
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; and
hydrocracking at least a portion of the vacuum residue from the second VDU fraction in a vacuum residue hydrocracking zone (VRHCK), recovering VRHCK products boiling at or below an atmospheric residue end boiling point and including LPG, naphtha and middle distillate range components, and recovering VRHCK hydrocracked gas oil.

2. The process as in claim 1 , wherein at least a portion of the VRHCK hydrocracked gas oil is passed to a gas oil steam cracking (GOSC) zone operating under conditions effective to recover at least a mixed product stream comprising H2, methane, ethane, ethylene, mixed C3s and mixed C4s; additional pyrolysis gas to be subjected to aromatics extraction; and additional pyrolysis oil.

3. The process as claim 1 , further comprising hydroprocessing in a gas oil hydroprocessing (GOHP) zone vacuum gas oil from the first VDU fraction, and recovering a first GOHP fraction containing components boiling at or below an atmospheric residue end boiling point and including LPG, naphtha and middle distillate range components, and a second GOHP fraction containing heavy oil, which is hydrotreated gas oil or unconverted oil in the vacuum gas oil range.

4. The process as in claim 3 , further comprising hydroprocessing at least a portion of the VRHCK hydrocracked gas oil in the GOHP zone.

5. The process as in claim 3 , wherein the GOHP zone operates under hydrocracking conditions and in the presence of hydrocracking catalyst to convert 27-99 wt % of feed to the GOHP zone into the first GOHP fraction.

6. The process as in claim 3 , wherein the GOHP zone operates under hydrotreating conditions and in the presence of hydrotreating catalyst to convert 2-30 wt % of feed to the GOHP zone into the first GOHP fraction.

7. The process as in claim 3 , further wherein the middle distillates in the second ADU fraction comprise heavy atmospheric gas oil that is routed to the GOHP zone.

8. The process as in claim 2 , 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 DHP zone.

10. The process as in claim 2 , 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,
a straight run diesel fraction that is the portion of the second ADU fraction that is processed in the DHP zone, and
heavy atmospheric gas oil that is processed in the GOSC zone.

11. The process as in claim 1 , wherein at least a significant portion of the first DHP fraction is passed to the MFSC zone or to the ADU.

12. The process as in claim 3 , wherein at least a significant portion of naphtha from the first GOHP fraction is routed to the MFSC zone or to the ADU.

13. The process as in claim 12 , wherein at least a significant portion of the first GOHP 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 mixed feed stream cracking zone.

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

16. 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.

17. The process as in claim 1 , 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.

18. The process as in claim 17 wherein the recovered C5s are passed to the mixed feed stream cracking zone.

19. The process as in claim 17 wherein the recovered C5s are passed to the separate processing zone for production of additional petrochemicals, wherein the separate processing zone converts mixture of butenes into mixed butanols.

20. The process as in claim 1 , wherein a crude to chemicals conversion ratio of at least about 39 wt % is achieved.

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

22. The process as in claim 1 , wherein a minor portion of the atmospheric residue from the third ADU fraction is routed to the VRHCK zone without separation in the VDU.

23. The process as in claim 1 , wherein at least a significant portion of the vacuum residue from the second VDU fraction is passed to the VRHCK zone.

24. The process as in claim 1 , further comprising separating at least a portion of pyrolysis oil from the MFSC into light pyrolysis oil and heavy pyrolysis oil, and passing at least a portion of light pyrolysis oil to the VRHCK zone.

25. The process as in claim 2 , further comprising separating at least a portion of pyrolysis oil from the MFSC

Assignees

• Saudi Arabian Oil Co

Inventors

• Al-Ghamdi Mohammed Saeed
• Bahammam Bader
• Al Osaimi Naif
• Barnawi Sami

Classifications

• 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

• 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

• C10G69/06 Primary

  including at least one step of thermal cracking in the absence of hydrogen · CPC title

• C10G2300/1077

  Vacuum residues · CPC title