Process for the production of petrochemical feedstock and high octane gasoline from middle distillates

Patent metadata

Field	Value
Publication number	US-11001771-B2
Application number	US-202016850822-A
Country	US
Kind code	B2
Filing date	Apr 16, 2020
Priority date	May 27, 2019
Publication date	May 11, 2021
Grant date	May 11, 2021

Abstract

A process for upgrading light cycle oil (LCO) to a high octane gasoline and a high aromatic feedstock for aromatic complex, by utilizing fluid catalytic cracking (FCC) is disclosed. FCC cracks unconverted diesel range stream from a hydrocracker to a high octane gasoline. This process further improves the quality (e.g., research octane number (RON), and Sulfur) of gasoline by utilizing FCC and hydrocracking process.

First claim

The invention claimed is:

1. A process for production of high octane gasoline and high aromatic feedstock, the process comprising:
(a) subjecting a light cycle oil (LCO) feed having a boiling point in a range of 180 to 410° C. to hydro-treatment in a first reactor to obtain a hydrotreated stream, wherein in the hydrotreated stream heteroatoms are removed and one or two rings of multi-ring aromatic molecules are selectively saturated, leaving at least one ring of the multi-ring aromatic molecules present in the feed unsaturated, wherein the multi-ring aromatic molecules comprise di-aromatics and tri-aromatics;
(b) subjecting the hydrotreated stream to hydrocracking in a second reactor filled with a catalyst for selectively opening a naphthenic ring attached to an aromatic ring present in the hydrotreated stream to obtain a hydrocracked stream;
(c) fractionating the hydrocracked stream into three cuts, wherein:
(i) a first cut is a light naphtha having a boiling point in a range of initial boiling point (IBP) to 95° C.,
(ii) a second cut is a high aromatic feedstock having an aromatic content in a range of 50 and 80 wt. % and a boiling point in a range of 95 to 210° C., wherein the second cut is rich in alkyl benzene, and
(iii) a third cut is an unconverted oil (UCO) having an IBP initial boiling point more than 210° C.; wherein the UCO is rich in tetra-hydro-naphthalene or substituted tetra-hydro-naphthalene;

(d) cracking the third cut comprising the UCO in a fluid catalytic cracking (FCC) unit, wherein a temperature in a range of 500 to 600° C. is maintained in a FCC riser of the FCC unit, and wherein the UCO is blended with fresh feed and fed into the FCC unit to produce products comprising ethylene, propylene, light cracked naphtha (LCN), heavy cracked naphtha (HCN), LCO distillates, and clarified oil (CLO) distillates; and
(e) feeding back the LCO distillates generated in the FCC unit to the step (a).

2. The process as claimed in claim 1 , wherein the LCO generated in the FCC unit has 10 wt % higher aromatic content compared to the light cycle oil generated from fresh feed.

3. The process as claimed in claim 1 , wherein LCO generated in the FCC unit has 10 wt % higher aromatic content than the light cycle oil generated from the fresh feed, and wherein the LCO has a di-aromatic concentration of at least 80 wt %.

4. The process as claimed in claim 3 , wherein LCO generated in the FCC unit increases alkyl-benzene concentration in the second cut by 5 wt %.

5. The process as claimed in claim 1 , wherein the UCO comprises 15-20 wt % of cyclo-paraffin, 15-20 wt % of alkyl benzene and 25-30 wt % of benzo-cyclo-paraffin.

6. The process as claimed in claim 1 , wherein the hydro-treatment is carried out at a temperature in a range of 310 to 420° C.

7. The process as claimed in claim 1 , wherein the hydro-treatment is carried out at a pressure in a range of 25 to 100 bar g.

8. The process as claimed in claim 1 , wherein a Linear Hourly Space Velocity (LHSV) while hydrotreatment is maintained in a range of 0.5 to 1.5.

9. The process as claimed in claim 1 , wherein the second reactor is maintained at a temperature in a range of 350 to 450° C.

10. The process as claimed in claim 1 , wherein the second reactor is maintained at a Linear Hourly Space Velocity (LHSV) in a range of 0.2 to 2.0.

11. The process as claimed in claim 1 , wherein the second reactor is maintained at a pressure in a range of 25 to 100 bar g.

12. The process as claimed in claim 1 , wherein the riser of the FCC reactor is maintained at a residence time in a range of 0.5 to 5.0 seconds.

13. The process as claimed in claim 1 , wherein the LCO stream has an aromatic content in a range of 60 to 90 wt % and out of the total aromatic content, the concentration of mono-aromatic is in a range of 20-30 wt %, di-aromatic is in a range of 60-70 wt % and polycyclic aromatic is in a range of 10-20 wt %.

Assignees

• Indian Oil Corp Ltd

Inventors

• Sarkar Mainak
• Das Nayan
• Butley Ganesh Vitthalrao
• Kumar Sandeep
• Thakur Ram Mohan
• Karumanchi Ramesh
• Kumar Sarvesh
• Sau Madhusudan
• Mazumdar Sanjiv Kumar
• RAMAKUMAR Sankara Sri Venkata

Classifications

• C10G2300/1048

  Middle distillates · CPC title

• C10G2300/305

  Octane number, e.g. motor octane number [MON], research octane number [RON] · CPC title

• C10G2300/4025

  Yield · CPC title

• C10G11/18

  according to the "fluidised-bed" technique · CPC title

• C10G2400/02

  Gasoline · CPC title