Process for upgrading refinery heavy residues to petrochemicals

Patent metadata

Field	Value
Publication number	US-2016369188-A1
Application number	US-201414901947-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 upgrading refinery heavy residues to petrochemicals, comprising the following steps of: (a) separating a hydrocarbon feedstock in a distillation unit into a to overhead stream and a bottom stream (b) feeding said bottom stream to a hydrocracking reaction area (c) separating reaction products, which are generated from said reaction area of step (b) into a stream rich in mono-aromatics and in a stream rich in poly-aromatics (d) feeding said stream rich in mono-aromatics to a gasoline hydrocracker (GHC) unit, (e) feeding said stream rich in poly-aromatics to a ring opening reaction area.

First claim

1 . A process for upgrading refinery heavy residues to petrochemicals, comprising:
(a) separating a hydrocarbon feedstock in a distillation unit into a to overhead stream and a bottom stream (b) feeding said bottom stream to a hydrocracking reaction area (c) separating reaction products, which are generated from said reaction area of step (b) into a stream rich in mono-aromatics and in a stream rich in poly-aromatics (d) feeding said stream rich in mono-aromatics to a gasoline hydrocracker (GHC) unit, and (e) feeding said stream rich in poly-aromatics to a ring opening reaction area, wherein said gasoline hydrocracker (GHC) unit is operated at a temperature higher than said ring opening reaction area, and wherein said gasoline hydrocracker (GHC) unit is operated at a pressure lower than said ring opening reaction area.

2 . The process as set forth in claim 1 , further comprising separating reaction products of said GHC of step (c) into an overhead gas stream, comprising C2-C4 paraffins, hydrogen and methane and a bottom stream comprising aromatic hydrocarbon compounds and non-aromatic hydrocarbon compounds.

3 . (canceled)

4 . The process as set forth in claim 1 , further comprising pretreating said stream rich in poly-aromatics of step (b) in an aromatics extraction unit, from which aromatics extraction unit its bottom stream is fed into said reaction area for ring opening and its overhead stream is fed into said steam cracker unit.

5 . The process as set forth in claim 1 , further comprising feeding the heavy fraction of reaction products formed in the reaction area for ring opening into the gasoline hydrocracker (GHC) unit or further comprising feeding the light fraction of reaction products formed in the reaction area for ring opening into said steam cracker unit.

6 .- 7 . (canceled)

8 . The process as set forth in claim 4 , wherein said aromatics extraction unit is of the type of a solvent extraction unit, wherein in said solvent extraction unit, its overhead stream is washed for removal of solvent, wherein the thus recovered solvent is returned into said solvent extraction unit and the overhead stream thus washed is fed into said steam cracker unit.

9 .- 11 . (canceled)

12 . The process as set forth in claim 1 , further comprising feeding said overhead stream of said distillation unit of step (a) to a separation section, in which separation section said overhead stream separated in a stream rich in aromatics and a stream rich in paraffins.

13 . The process as set forth in claim 12 , further comprising feeding said stream rich in paraffins to said steam cracker unit and further comprising feeding said stream rich in aromatic to said gasoline hydrocracker (GHC) unit of step (c).

14 . (canceled)

15 . The process as set forth in claim 1 , further comprising feeding the overhead stream from the aromatics extraction unit into an isomerization unit and feeding the thus isomerized stream to said steam cracking unit.

16 . The process as set forth in claim 1 , further comprising feeding said stream rich in paraffins coming from the separation section into an isomerization unit and feeding the thus isomerized stream to said steam cracking unit.

17 . The process as set forth in claim 1 , further separating C2-C4 paraffins from the gaseous stream sent to the steam cracker unit and,
feeding said C2-C4 paraffins thus separated from the gaseous stream to the furnace section of a steam cracker unit.

18 . The process according to claim 17 , 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.

19 . (canceled)

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

21 . (canceled)

22 . The process as set forth in claim 20 , further comprising separating said bottom stream into a stream comprising aromatic hydrocarbon compounds and non-aromatic hydrocarbon compounds and a stream comprising C9+, carbon black oil (CBO) and cracked distillates (CD) and further comprising feeding said C9+, carbon black oil (CBO) and cracked distillates (CD) containing bottom stream into said reaction area for ring opening.

23 . The process as set forth in claim 22 , further comprising feeding said C9+, carbon black oil (CBO) and cracked distillates (CD) containing bottom stream into said hydrocracking reaction area and further comprising feeding, said bottom stream comprising aromatic hydrocarbon compounds and non-aromatic hydrocarbon compounds into said gasoline hydrocraker (GHC) unit.

24 .- 26 . (canceled)

27 . The process as set forth in claim 1 , wherein the process conditions prevailing in said reaction area for ring opening are a temperature from 100° C. to 500° C. and a pressure from 2 to 10 MPa together with from 50 to 300 kg of hydrogen per 1,000 kg of feedstock over an aromatic hydrogenation catalyst and passing the resulting stream to a ring cleavage unit at a temperature from 200° C. to 600° C. and a pressure from 1 to 12 MPa together with from 50 to 200 kg of hydrogen per 1,000 kg of said resulting stream over a ring cleavage catalyst.

28 .- 29 . (canceled)

30 . The process as set forth in claim 1 , wherein the process conditions prevailing in said gasoline hydrocracker (GHC) unit are a reaction temperature of 300-580° C., a pressure of 0.3-5 MPa gauge, a Weight Hourly Space Velocity (WHSV) of 0.1-10 h-1.

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

32 . The process as set forth in claim 1 , wherein the process conditions prevailing in said hydrocracking area of step (b) are a temperature of 300-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-10 h-1.

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

34 .- 36 . (canceled)

37 . The process as set forth in claim 1 , wherein the separation in step (c) is carried out such that said stream rich in mono-aromatics comprising mono-aromatics having a boiling range of from 70° C. to 217° C. is fed to said gasoline hydrocracker (GHC) unit and said stream rich in poly-aromatics comprising poly-aromatics having a boiling range of from 217° C. and higher is fed to said ring opening reaction area.

38 . (canceled)

Assignees

• Housmans Thomas Hubertus Maria
• Oprins Arno Johannes Maria
• Saudi Basic Ind Corp
• Sabic Global Technologies Bv

Inventors

• Housmans Thomas Hubertus Maria
• Oprins Arno Johannes Maria

Classifications

• C10G2300/1077

  Vacuum residues · CPC title

• C10G2300/1055

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

• C10G2300/1051

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

• C10G2300/1059

  Gasoil having a boiling range of about 330 - 427 °C · CPC title

• C10G69/02 Primary

  plural serial stages only · CPC title