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

Patent metadata

Field	Value
Publication number	US-10407630-B2
Application number	US-201715817140-A
Country	US
Kind code	B2
Filing date	Nov 17, 2017
Priority date	Nov 21, 2016
Publication date	Sep 10, 2019
Grant date	Sep 10, 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 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 the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a solvent deasphalting unit to produce deasphalted oil as additional feed to the gas oil hydroprocessing 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;

solvent deasphalting at least a portion of the vacuum residue in a solvent deasphalting zone, recovering a deasphalted oil phase and an asphalt phase,
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;
hydroprocessing in a gas oil hydroprocessing (GOHP) zone vacuum gas oil from the first VDU fraction and deasphalted oil from the solvent deasphalting step, 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;
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, heavy 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 an 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 integrated process of claim 1 , wherein the solvent deasphalting step comprises
mixing the vacuum residue with make-up solvent and optionally fresh solvent;
transferring the mixture to a primary settler in which a primary deasphalted and demetalized oil phase and a primary asphalt phase are formed;
transferring the primary deasphalted and demetalized oil phase to a secondary settler in which a secondary deasphalted and demetalized oil phase and a secondary asphalt phase are formed;
recycling the secondary asphalt phase to the primary settler to recover additional deasphalted and demetalized oil;
conveying the secondary deasphalted and demetalized oil phase to a deasphalted and demetalized oil separation zone to obtain a recycle solvent stream and a substantially solvent-free deasphalted and demetalized oil stream;
conveying the primary asphalt phase to a separator vessel for flash separation of an additional recycle solvent stream and a bottom asphalt phase; and
wherein at least a portion of the substantially solvent-free deasphalted and demetalized oil stream is the deasphalted oil processed in the vacuum gas oil hydroprocessing zone.

3. The integrated process of claim 1 , further wherein at least a portion of pyrolysis oil from steam cracking is processed in the solvent deasphalting step.

4. The integrated process of claim 1 , further wherein pyrolysis oil comprises light pyrolysis oil and heavy pyrolysis oil, and wherein at least a portion of light pyrolysis oil is blended with deasphalted oil and wherein at least a portion of heavy pyrolysis oil is processed in the solvent deasphalting step.

5. 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 GOHP zone.

6. 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.

7. 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.

8. The process as in claim 7 , further wherein the middle distillates in the second ADU fraction comprise heavy atmospheric gas oil that is processed in the GOHP zone or the GOSC zone.

9. 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.

10. The process as in claim 1 , wherein at least a significant portion of naphtha from the first GOHP fraction is routed to the MFSC zone or to the ADU.

11. The process as in claim 1 , wherein at least a significant portion of the first GOHP fraction is routed to the DHP zone.

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

13. 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.

14. The process as in claim 13 , 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.

15. The process as in claim 13 , 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.

16. The process as in claim 15 wherein the recovered C5s are passed to the mixed feed stream cracking zone.

17. The process as in claim 15 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.

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

19. The process as in claim 13 , wherein the separate processing zone converts mixture of butenes into mixed butanols.

20. 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; and
at least a significant portion of naphtha from the first GOHP fraction is routed to the MFSC zone, the ADU or the DHP zone.

21. The process as in claim 20 , further wherein the middle distillates in the second ADU fraction comprise
k

Assignees

• Saudi Arabian Oil Co

Inventors

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

Classifications

• C10G69/08

  including at least one step of reforming naphtha · CPC title

• C10G69/06

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

• C10G67/0454

  Solvent desasphalting · 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

• C10G21/003 Primary

  Solvent de-asphalting · CPC title