Desulfurization of hydrocarbons

• US 4,336,130 A
• Filed: 11/28/1980
• Issued: 06/22/1982
• Est. Priority Date: 11/28/1980
• Status: Expired due to Term

• Current Assignee: UOP Llc (Honeywell International Inc.)
• Original Assignee: Union Oil Company of California (Chevron Corp.)
• Inventors: Ward, John W., Miller, J. Wayne
• Primary Examiner(s): Gantz, Delbert E.
• Assistant Examiner(s): Chaudhuri, Olik
• Application Number:
  US06/211,376
• Time in Patent Office: 571 Days
• Field of Search: 208/244, 208/243, 585/850
• US Class Current: 208/243
• CPC Class Codes: C10G 25/003 Specific sorbent material, not covered by C10G25/02 or C10G25/03
• CPC Class Codes: C10G 29/04 Metals, or metals deposited on a carrier
• CPC Class Codes: C10G 29/06 Metal salts, or metal salts deposited on a carrier
• CPC Class Codes: C10G 61/06 the refining step being a sorption process

Abstract

A hydrocarbon feedstock containing organo-sulfur compounds, such as a naphtha containing mercaptans, is desulfurized by contact, under non-hydrogenative conditions, with a reduced catalytic absorbent comprising one or more nickel components and one or more platinum group metal promoters composited with a porous refractory oxide.

Claims

1. A process comprising (a) contacting a hydrocarbon feedstock containing organo-sulfur compounds with a reduced catalytic absorbent comprising one or more nickel components a molybdenum or tungsten component and one or more platinum group metal promoters composited with a porous refractory oxide, said contacting being under substantially non-hydrogenative conditions including an elevated temperature such that a substantial proportion of said organo-sulfur compounds is removed from said feedstock and said catalytic absorbent increases in sulfur content;

and (b) recovering a hydrocarbon product stream containing less organo-sulfur compounds than are contained in said feedstock.

2. The process as defined in claim 1 wherein said feedstock is a reformer feed containing more than about 0.1 ppmw sulfur and said product stream contains less than 0.1 ppmw sulfur.

3. The process as defined in claim 1 wherein said catalytic absorbent comprises between about 5 and 50 wt.% nickel components, calculated as NiO.

4. The process as defined in claim 3 wherein said catalytic absorbent comprises nickel and one or more platinum group metals in an atomic ratio between 1:

1 to 5000;

1, nickel to platinum group metals.

5. The process as defined in claim 4 wherein said contacting is accomplished in the absence of hydrogen.

6. The process as defined in claim 5 wherein said organo-sulfur compounds comprise a substantial proportion of mercaptans.

7. The process as defined in claim 1 or 3 wherein said catalytic absorbent is reduced with hydrogen.

8. A process comprising (a) contacting a reformer feedstock containing mercaptans with a catalytic absorbent comprising between about 5 and 50% by weight of nickel components, calculated as NiO, a molybdenum or tungsten component and one or more platinum group metal promoters composited with a porous refractory oxide, said catalytic absorbent having been reduced by hydrogen at an elevated temperature, said contacting being under substantially non-hydrogenative conditions including a temperature between 100°

F. and 600°

F. such that a substantial proportion of said mercaptans is removed from said feedstock; and

(b) recovering a product stream containing less mercaptans than are contained in said feedstock.

9. The process as defined in claim 8 wherein said feedstock contains more than about 0.1 ppmw sulfur and said product stream contains less than 0.1 ppmw sulfur.

10. The process as defined in claim 9 wherein said catalytic absorbent comprises nickel and one or more platinum group metals in an atomic ratio between 1:

1 to 5000;

1, nickel to platinum group metal.

11. The process as defined in claim 10 wherein said contacting is accomplished in the absence of hydrogen.

12. A process comprising (a) contacting, in the absence of hydrogen and at a temperature in the range of about 200°

F. to 400°

F., a reformer feedstock containing more than 0.1 ppmw sulfur comprising a substantial proportion of mercaptans with a catalytic absorbent comprising between about 5 and 50 wt.% of nickel components, calculated as NiO, a molybdenum or tungsten component and one or more platinum group metal promoters in an atomic ratio between about 1;

1 to 5000;

1, nickel to platinum group metal, composited with a porous refractory oxide consisting essentially of alumina, said catalytic absorbent having been reduced with hydrogen at a temperature between 500°

F. and 900°

F., such that a substantial proportion of said mercaptans is removed from said feedstock while said catalytic absorbent increases in sulfur content; and

(b) recovering a product stream containing less than about 0.1 ppmw sulfur.

13. A process comprising (a) contacting a hydrocarbon feedstock containing organo-sulfur compounds with a reduced catalytic absorbent comprising one or more nickel components a molybdenum or tungsten component and one or more platinum or palladium metal promoters, composited with a porous refractory oxide, said contacting being under substantially non-hydrogenative conditions including an elevated temperature such that a substantial proportion of said organo-sulfur compounds is removed from said feedstock and said catalytic absorbent increases in sulfur content;

and (b) recovering a hydrocarbon product stream containing less organo-sulfur compounds than are contained in said feedstock.

14. The process as defined in claim 13 wherein said feedstock is a reformer feed containing more than about 0.1 ppmw sulfur and said product stream contains less than 0.1 ppmw sulfur.

15. The process as defined in claim 14 wherein said catalytic absorbent comprises between about 5 and 50 wt.% nickel components, calculated as NiO.

16. The process as defined in claim 15 wherein said catalytic absorbent comprises nickel and platinum or palladium in an atomic ratio between 1:

1 to 5000;

1, nickel to platinum or palladium metal.

17. The process as defined in claim 16 wherein said contacting is accomplished in the absence of hydrogen.

18. The process as defined in claim 17 wherein said organo-sulfur compounds comprise a substantial proportion of mercaptans.

19. The process as defined in claim 18 wherein said catalytic absorbent is reduced with hydrogen.

20. A process comprising (a) contacting a reformer feedstock containing mercaptans with a catalytic absorbent comprising between about 5 and 50% by weight of nickel components calculated as NiO, a molybdenum or tungsten component and one or more platinum metal promoters composited with a porous refractory oxide, said catalytic absorbent having been reduced by hydrogen at an elevated temperature, said contacting being under substantially non-hydrogenative conditions including a temperature between 100°

F. and 600°

F., such that a substantial proportion of said mercaptans is removed from said feedstock; and

(b) recovering a product stream containing less mercaptans than are contained in said feedstock.

21. The process as defined in claim 20 wherein said feedstock contains more than about 0.1 ppmw sulfur and said product stream contains less than 0.1 ppmw sulfur.

22. The process as defined in claim 21 wherein said catalytic absorbent comprises nickel and platinum metal in an atomic ratio between 1:

1 to 5000;

1, nickel to platinum metal.

23. The process as defined in claim 22 wherein said contacting is accomplished in the absence of hydrogen.

24. A process comprising (a) contacting, in the absence of hydrogen and at a temperature in the range of about 200°

F. to 400°

F., a reformer feedstock containing more than 0.1 ppmw sulfur comprising a substantial proportion of mercaptans with a catalytic absorbent comprising between about 5 and 50 wt.% of nickel components calculated as NiO, a molybdenum or tungsten component and one or more platinum metal promoters in an atomic ratio between 1;

1 to 5000;

1, nickel to platinum metal, composited with a porous refractory oxide consisting essentially of alumina, said catalytic absorbent having been reduced with hydrogen at a temperature between 500°

F. and 900°

F., such that a substantial proportion of said mercaptans is removed from said feedstock while said catalytic absorbent increases in sulfur content; and

(b) recovering a product stream containing less than about 0.1 ppmw sulfur.