Process for the selective hydrogenation and hydrodesulferization of a pyrolysis gasoline feedstock

Patent metadata

Field	Value
Publication number	US-9260670-B2
Application number	US-201013376531-A
Country	US
Kind code	B2
Filing date	Jun 9, 2010
Priority date	Jun 11, 2009
Publication date	Feb 16, 2016
Grant date	Feb 16, 2016

Abstract

Disclosed is a process for the selective hydrogenation of diolefins and sulfur compounds that are contained in a pyrolysis gasoline feedstream. The process includes utilizing a single hydrotreating reaction stage by introducing the pyrolysis gasoline feedstock that includes a diolefin concentration and an organic sulfur concentration into a reactor that is loaded with a high activity hydrotreating catalyst and which is operated under selective hydrogenation conditions. A reactor effluent having a reduced diolefin concentration and a reduced organic sulfur concentration is yielded from the reactor and is separated into a portion that is recycled as a reactor feed. The remaining portion of the reactor effluent is passed downstream for further processing or handling.

First claim

What is claimed is:

1. A process for the selective hydrogenation of diolefins and sulphur compounds contained in a pyrolysis gasoline feedstock, comprising a diolefin concentration exceeding 3 wt % and an organic sulfur concentration exceeding 50 ppmw, wherein said process comprises:
introducing a hydrocarbon stream that comprises said pyrolysis gasoline feedstock into a reactor that contains a single hydrotreating reaction stage comprising hydrotreating catalyst and operated at selective hydrogenation conditions, wherein said hydrocarbon stream is contacted with said hydrotreating catalyst;
yielding from said reactor a reactor effluent comprising a reduced diolefin concentration of less than 10 ppmw, a reduced organic sulfur concentration of less than 3 ppmw, and an aromatics content of at least 90 wt % of a reactor inlet aromatics content;
separating said reactor effluent into a portion of said reactor effluent and a remaining portion of said reactor effluent;
and introducing as a recycle said portion of said reactor effluent into said reactor wherein the weight ratio of said recycle to said hydrocarbon stream is greater than 1:1.

2. A process as recited in claim 1 , wherein said selective hydrogenation conditions include a feed inlet temperature to said reactor that is in the range of from 100° C. to 250° C., a reactor operating pressure in the range of from 10 bara to 100 bara, and a weight hourly space velocity in the range of from 0.2 to 40 hr −1 .

3. A process as recited in claim 2 , wherein said pyrolysis gasoline feedstock further comprises monoolefins at a concentration in the range of from 1 to 20 wt % and aromatics at a concentration in the range of from 10 wt % to 80 wt %, and wherein said reactor effluent has a reduced monoolefin concentration as measured by a bromine number of less than 1 and aromatics content of at least 95 wt % of said hydrocarbon stream.

4. A process as recited in claim 2 , wherein said hydrotreating catalyst comprises molybdenum and either nickel or cobalt supported on alumina.

5. A process as recited in claim 4 , wherein said step of separating said reactor effluent includes:
separating said reactor effluent into a total reactor effluent portion of said reactor effluent and a total reactor effluent remaining portion of said reactor effluent; and
using said total reactor effluent portion as a total recycle stream of said recycle.

6. A process as recited in claim 4 , wherein said step of separating said reactor effluent includes:
passing said reactor effluent to a separator for separating said reactor effluent into a liquid fraction and a vapor fraction;
passing said liquid fraction to a fractionator for separating said liquid fraction into a light cut and a heavy cut;
separating said heavy cut into a heavy cut portion of said heavy cut and a heavy cut remaining portion of said heavy cut; and
using said heavy cut portion of said heavy cut as a heavy cut recycle stream of said recycle.

7. A process as recited in claim 4 , wherein said step of separating said reactor effluent includes:
passing said reactor effluent to a separator for separating said reactor effluent into a liquid fraction and a vapor fraction;
separating said liquid fraction into a liquid fraction portion of said liquid fraction and a liquid fraction remaining portion of said liquid fraction; and
using said liquid fraction portion of said liquid fraction as a first recycle stream of said recycle.

8. A process as recited in claim 7 , wherein said step of separating said reactor effluent further includes:
passing said liquid fraction remaining portion of said liquid fraction to a fractionater for separating said liquid fraction remaining portion of said liquid fraction into a light cut and a heavy cut;
separating said heavy cut into a heavy cut portion of said heavy cut and a heavy cut remaining portion of said heavy cut; and
using said heavy cut portion of said heavy cut as a second recycle stream of said recycle.

9. A process as recited in claim 6 , further comprising:
introducing said vapor fraction into said reactor along with said hydrocarbon stream and said recycle.

10. A process for the selective hydrogenation of monoolefins, diolefins, and sulfur compounds contained in a pyrolysis gasoline feedstock, wherein said pyrolysis gasoline feedstock having a monoolefins concentration, a diolefins concentration, an aromatics concentration, and an organic sulfur concentration, and wherein said process comprises:
introducing a hydrocarbon stream that comprises said pyrolysis gasoline feedstock into a reactor that contains a single hydrotreating reaction stage comprising hydrotreating catalyst and operated under selective hydrogenation conditions, wherein said hydrocarbon stream is contacted with said hydrotreating catalyst;
yielding from a reactor outlet of said reactor a reactor effluent having a reduced monoolefin concentration, a reduced diolefin concentration, a reduced organic sulfur concentration, and an aromatics content of at least 90 wt % of a reactor inlet aromatics content; and
introducing as a recycle a portion of said reactor effluent into said reactor wherein the weight ratio of said recycle to said hydrocarbon stream is greater than 1:1.

11. A process as recited in claim 10 , wherein said monoolefins concentration is in the range of from 1 to 20 wt %, said diolefins concentration exceeds 3 wt %, said aromatics concentration is in the range of from 10 wt % to 80 wt %, and said organic sulphur concentration exceeds 50 ppmw, and wherein said reduced monoolefin concentration is measured by a bromine number of less than 1, said reduced diolefin concentration is less than 10 ppmw, and said reduced organic sulfur concentration is less than 3 ppmw.

12. A process as recited in claim 11 , further comprising:
introducing into said reactor with said hydrocarbon stream a portion of said reactor effluent as a recycle at a rate so as to provide a weight ratio recycle-to-hydrocarbon stream that is greater than 1:1.

13. A process as recited in claim 12 , wherein said selective hydrogenation conditions include a feed inlet temperature to said reactor that is in the range of from 100° C. to 250° C., a reactor operating pressure in the range of from 10 bara to 100 bara, and a weight hourly space velocity in the range of from 0.2 to 40 hr −1 .

14. A process as recited in claim 13 , wherein said hydrotreating catalyst comprises molybdenum and either nickel or cobalt supported on alumina.

Assignees

• Grenoble Dane Clark
• Himelfarb Paul Benjerman
• Treybig Michael Norris
• Vanderwilp Brian Scott
• Shell Oil Co

Inventors

• Grenoble Dane Clark
• Himelfarb Paul Benjerman
• Treybig Michael Norris
• Vanderwilp Brian Scott

Classifications

• C10G69/06

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

• C10G2300/4018

  Spatial velocity, e.g. LHSV, WHSV · CPC title

• C10G2300/202

  Heteroatoms content, i.e. S, N, O, P · CPC title

• C10G2400/30

  Aromatics · CPC title

• C10G2300/104

  Light gasoline having a boiling range of about 20 - 100 °C · CPC title