Method for converting a high-boiling hydrocarbon feedstock into lighter boiling hydrocarbon products

Patent metadata

Field	Value
Publication number	US-2016369185-A1
Application number	US-201414902135-A
Country	US
Kind code	A1
Filing date	Jun 30, 2014
Priority date	Jul 2, 2013
Publication date	Dec 22, 2016
Grant date	—

Abstract

The present invention relates to a process for converting a high-boiling hydrocarbon feedstock into lighter boiling hydrocarbon products, said lighter boiling hydrocarbon products being suitable as a feedstock for petrochemicals processes, said converting process comprising the following steps of: feeding a hydrocarbon feedstock having a boiling point of >350 deg Celsius to a cascade of hydrocracking unit(s), feeding the bottom stream of a hydrocracking unit as a feedstock for a subsequent hydrocracking unit, wherein the process conditions in each hydrocracking unit(s) are different from each other, in which the hydrocracking conditions from the first to the subsequent hydrocracking unit(s) increase from least severe to most severe, and processing the lighter boiling hydrocarbon products from each hydrocracking unit(s) as a feedstock for one or more petrochemicals processes.

First claim

1 . A process for converting a high-boiling hydrocarbon feedstock into lighter boiling hydrocarbon products, said lighter boiling hydrocarbon products being suitable as a feedstock for petrochemicals processes, said converting process comprising:
feeding a hydrocarbon feedstock having a boiling point of greater than 350 deg Celsius to a cascade of hydrocracking unit(s), feeding the bottom stream of a hydrocracking unit as a feedstock for a subsequent hydrocracking unit such that said feedstock for a subsequent hydrocracking unit is heavier than the feedstock of a previous hydrocracking unit in the cascade of hydrocracking unit(s) wherein the process conditions in each hydrocracking unit(s) are different from each other, in which the hydrocracking conditions from the first to the subsequent hydrocracking unit(s) increase from least severe to most severe, and processing the lighter boiling hydrocarbon products from each hydrocracking unit(s) as a feedstock for one or more petrochemicals processes.

2 . The process according to claim 1 , in which said hydrocarbon feedstock having a boiling point of greater than 350 deg Celsius is a member chosen from the group of a bottom stream from a crude oil distillation, tar sand oil, shale oil and bio based materials, or a combination thereof.

3 . The process according to claim 1 , wherein the petrochemicals processes comprise (Fluid Catalytic) Cracking, Steam Cracking, dehydrogenation units, alkylation units, isomerization units and reforming units, or combinations thereof.

4 . The process according to claim 1 , wherein the lighter boiling hydrocarbon products from all hydrocracking units are combined and processed as a feedstock for one or more petrochemicals processes.

5 . The process according to claim 4 , wherein the lighter boiling hydrocarbon products thus collected are separated into individual streams by a distillation process, wherein the individual streams thus separated are each sent to individual petrochemicals processes.

6 . The process according to claim 1 , further comprising separating the lighter boiling hydrocarbon products into (i) a first stream containing the unused hydrogen, possible H 2 S NH 3 , H 2 O, and methane and (ii) a second stream comprising C 2 and C 2 + products with boiling points below 350° C.

7 . The process according to claim 6 , wherein the first stream is returned to a hydrocracking unit.

8 . The process according to claim 1 , wherein the cascade of hydrocracking units comprises at least two hydrocracking units.

9 . The process according claim 8 , wherein the temperature in the first hydrocracking unit is lower than the temperature in the second hydrocracking unit.

10 . The process according to claim 1 , wherein the particle size of the catalyst present in the cascade of hydrocracking units decreases from the first hydrocracking unit to the subsequent hydrocracking unit(s).

11 . The process according to claim 1 , wherein the cascade of hydrocracking units comprises at least three hydrocracking units, wherein the three hydrocracking units are preceded by a hydrotreating unit, wherein the bottom stream of said hydrotreating unit is used as a feedstock for said first hydrocracking unit, wherein the pressure for the first hydrocracking stage is 150 to 200 Barg operating pressure, the pressure for the second hydrocracking stage is 100 to 200 Barg operating pressure and the pressure for the third hydrocracking stage is 100 to 300 Barg operating pressure, respectively.

12 . The process according claim 11 , wherein the temperature prevailing in said hydrotreating unit is higher than in said first hydrocracking unit,

13 . The process according to claim 11 , wherein the temperature in the cascade of hydrocracking units increases, wherein the temperature prevailing in said third hydrocracking unit is higher than in said hydrotreating unit.

14 . The process according to claim 11 , wherein the reactor type design of the hydrocracking unit(s) is chosen from the group of the fixed bed type, ebullated bed reactor type and the slurry phase type.

15 . The process according to claim 11 , wherein the reactor type design of said hydrotreating unit is of the fixed bed type.

16 . The process according to claim 11 , wherein the reactor type design of said first hydrocracking unit is of the ebullated bed reactor type.

17 . The process according to claim 11 , wherein the reactor type design of said second hydrocracking unit is of the slurry phase type.

18 . The process according to claim 1 , wherein the bottom stream of the final hydrocracking unit is recycled to the inlet of said final hydrocracking unit.

19 . The process according to claim 1 , wherein the hydrocarbon feedstock to one or more of the hydrocracking unit(s) of the cascade of hydrocracking unit(s) comprises a heavy stream originating from steam cracker unit and/or refinery.

20 . (canceled)

Assignees

• Saudi Basic Ind Corp
• Sabic Global Technologies Bv

Inventors

• Ward Andrew Mark
• Narayanaswamy Ravichander
• Rajagopalan Vijayanand
• Powale Lakshmikant Suryakant
• Housmans Thomas Hubertus Maria
• Oprins Amo Johannes Maria
• Tumer William Jay

Classifications

• C10G65/10

  including only cracking steps · CPC title

• C10G2400/30

  Aromatics · CPC title

• C10G69/00 Primary

  Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process (C10G67/00 takes precedence) · CPC title

• C10G2300/1011

  Biomass · CPC title

• C10G2400/20

  C2-C4 olefins · CPC title