Process for the production of light olefins and aromatics from a hydrocarbon feedstock

Patent metadata

Field	Value
Publication number	US-2016369189-A1
Application number	US-201414901736-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 the production of light olefins and aromatics from a hydrocarbon feedstock, comprising the following steps of: (a) feeding a hydrocarbon feedstock into a FCC unit (b) separating reaction products, which are generated from the FCC reaction, into a bottom stream, and middle stream and a top stream; (c) feeding the middle stream from (b) to a gasoline hydrocracker (GHC) unit, (d) separating reaction products of said GHC of step (c) into an overhead gas stream comprising hydrogen, methane and C2-C4 paraffins, and a bottom stream comprising aromatic hydrocarbon compounds, (e) feeding the overhead stream from the gasoline hydrocracker (GHC) unit into a steam cracker unit.

First claim

1 . A process for the production of light olefins and aromatics from a hydrocarbon feedstock, comprising
(a) feeding a hydrocarbon feedstock into a fluid catalytic cracker (FCC) unit (b) separating reaction products, which are generated from the FCC reaction, into a bottom stream, and middle stream and a top stream; (c) feeding the middle stream from (b) to a gasoline hydrocracker (GHC) unit, (d) separating reaction products of said GHC of step (c) into an overhead gas stream comprising hydrogen, methane and C2-C4 paraffins, and a bottom stream comprising aromatic hydrocarbon compounds, and (e) feeding the overhead stream from the gasoline hydrocracker (GHC) unit directly to the furnace section of a steam cracker unit.

2 . The process as set forth in claim 1 , further comprising pretreating the hydrocarbon feedstock in a distillation unit, from which distillation unit its bottom stream is fed into said FCC unit and its overhead stream is fed into said steam cracker unit.

3 . The process as set forth in claim 1 , further comprising separating C2-C4 paraffins from said overhead gas stream coming from the gasoline hydrocracker (GHC) unit, and
feeding only said C2-C4 paraffins thus separated from the overhead gas stream directly to the furnace section of a steam cracker unit.

4 . The process according to claim 3 , further comprising separating C2-C4 paraffins in individual streams, each stream predominantly comprising C2 paraffins, C3 paraffins and C4 paraffins, respectively, and feeding each individual stream to a specific furnace section of said steam cracker unit.

5 . The process as set forth in claim 1 , further comprising separating reaction products of said steam cracking unit into an overhead stream, comprising C2-C6 alkanes, a middle stream, comprising C2=, C3= and C4=, and a first bottom stream, comprising C9+ hydrocarbons, and a second bottom stream comprising aromatic hydrocarbon compounds and non-aromatic hydrocarbon compounds.

6 . The process as set forth in claim 5 , further comprising returning said overhead stream to said steam cracking unit.

7 . The process as set forth in claim 5 , further comprising feeding said second bottom stream into said gasoline hydrocracker (GHC) unit.

8 . The process as set forth in claim 5 , further comprising feeding said first bottom stream into said FCC unit, preferably by first combining said first bottom stream with a hydrogen donor type feedstock and then feeding the thus combined materials to said FCC unit.

9 . The process as set forth in claim 8 , wherein the hydrogen donor type feedstock is hydrogen or a light feedstock, such as naphtha, or a combination thereof.

10 . The process as set forth in claim 1 , further comprising feeding said overhead stream from the gasoline hydrocracker (GHC) unit to a dehydrogenation unit, preferably feeding the C3-C4 fraction of said overhead stream from the gasoline hydrocracker (GHC) unit.

11 . The process as set forth in claim 1 , further comprising combing said top stream from said FCC unit with said stream of reaction products coming from said steam cracking unit.

12 . The process as set forth in claim 1 , wherein said hydrocarbon feedstock into said FCC unit is chosen from the group of naphtha, kerosene, diesel, atmospheric gas oil (AGO), gas condensates, waxes, crude contaminated naphtha, vacuum gas oil (VGO), vacuum residue, atmospheric residue, pretreated naphtha, or a combination thereof.

13 . The process as set forth in claim 1 , wherein the process conditions prevailing in said FCC unit include a temperature of 425-570° C. and a pressure of 10-800 kPa gauge (low-severity) or a temperature of 540-700° C. and a pressure of 10-800 kPa gauge (high severity).

14 . The process as set forth in claim 1 , wherein the process conditions prevailing in said gasoline hydrocracker (GHC) unit are a temperature of 300-450° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-10 h−1, preferably a temperature of 300-400° C., a pressure of 600-3000 kPa gauge and a Weight Hourly Space Velocity of 0.2-2 h−1.

15 . The process as set forth in claim 1 , wherein the process conditions prevailing in said steam cracking unit include a reaction temperature of 750-900° C., a residence time of 50-1000 milliseconds and a pressure of atmospheric up to 175 kPa gauge.

16 . The process as set forth in claim 1 , further comprising not feeding a substantial part of the overhead stream from the gasoline hydrocracker (GHC) unit directly to the separation section of a steam cracker unit.

17 . The process as set forth in claim 1 , further comprising using a gaseous light fraction of a multi stage FCC and hydrocracked hydrocarbon feedstock as a feedstock for a steam cracking unit.

Assignees

• Saudi Basic Ind Corp
• Sabic Global Technologies Bv

Inventors

• Ward Andrew Mark
• Oprins Arno Johannes Maria
• Housmans Thomas Hubertus Maria

Classifications

• C10G2300/107

  Atmospheric residues having a boiling point of at least about 538 °C · CPC title

• C10G69/00

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

• C10G2400/20

  C2-C4 olefins · CPC title

• C10G2300/1051

  Kerosene having a boiling range of about 180 - 230 °C · CPC title

• C10G2300/1055

  Diesel having a boiling range of about 230 - 330 °C · CPC title