Removal of sulfur compounds from hydrocarbon feedstreams using cobalt containing adsorbents in the substantial absence of hydrogen

• US 6,579,444 B2
• Filed: 12/17/2001
• Issued: 06/17/2003
• Est. Priority Date: 12/28/2000
• Status: Expired due to Fees

• Current Assignee: ExxonMobil Research & Engineering Company (Exxon Mobil Corporation)
• Original Assignee: ExxonMobil Research & Engineering Company (Exxon Mobil Corporation)
• Inventors: Kaul, Bal K., Feimer, Joseph L., Baker, Myles W., OʼBara, Joseph T., Zinkie, David N., Stuntz, Gordon F.
• Primary Examiner(s): NORTON, NADINE GEORGIANNA
• Application Number:
  US10/022,948
• Publication Number:
  US 20020157990A1
• Time in Patent Office: 547 Days
• Field of Search: 208/208.R, 208/243, 208/244, 585/820
• US Class Current: 208/243
• CPC Class Codes: C10G 25/003 Specific sorbent material, not covered by C10G25/02 or C10G25/03

Abstract

A process for removing sulfur compounds from hydrocarbon feedstreams, particularly those boiling in the naphtha range, by contacting the feedstream with an adsorbent comprised of cobalt and one or more Group VI metals selected from molybdenum and tungsten on a refractory support. This invention also relates to a process wherein a naphtha feedstream is first subjected to selective hydrodesulfurization to remove sulfur but not appreciably saturate olefins. A product stream is produced containing mercaptans that are removed by use of the cobalt-containing adsorbents of the present invention.

Claims

1. A process for removing sulfur compounds from sulfur compound-containing hydrocarbon streams boiling in the range of about 10°

C. to about 600°

C., which process comprises contacting the sulfur compound-containing hydrocarbon stream, in the substantial absence of added hydrogen, with an adsorbent comprised of Co and at least one Group VI metal selected from Mo and W on an inorganic refractory support under conditions that include temperatures up to about 150°

C.

2. The process of claim 1 wherein the hydrocarbon stream is a naphtha stream boiling in the range of about 10°

C. to about 230°

C.

3. The process of claim 1 wherein the hydrocarbon stream is a distillate stream boiling in the range of about 150°

C. to about 600°

C.

4. The process of claim 1 wherein the Co content of the adsorbent is from about 0.5 wt. % to about 20 wt. %, in terms of CoO.

5. The process of claim 4 wherein the Group VI metal content of the adsorbent is from about 1 wt. % to about 40 wt. %.

6. The process of claim 5 wherein the Co content is from about 2 wt. % to about 20 wt. % and the Group VI metal content from about 5 wt. % to about 30 wt. % on support.

7. The process of claim 6 wherein the Co content is from about 4 wt. % to about 15 wt. % and the content of the Group VI metal is from about 20 wt. % to about 30 wt. % on support.

8. The process of claim 1 wherein said support is selected from the group consisting of alumina, silica, silica-alumina, clay, titania, calcium oxide, strontium oxide, barium oxide, carbons, zirconia, diatomaceous earth, lanthanide oxides including cerium oxide, lanthanum oxide, neodynium oxide, yttrium oxide, and praesodynium oxide;

chromia, thorium oxide, urania, niobia, tantala, tin oxide, zinc oxide, and large pore zeolites.

9. The process of claim 8 wherein said support is selected from alumina, silica, alumina-silica, and large pore zeolites.

10. The process of claim 1 wherein said hydrocarbon stream is contacted with said adsorbent at a temperature from about −

30°

C. to about 150°

C.

11. The process of claim 10 wherein said hydrocarbon stream is contacted with said adsorbent at a temperature from about 10°

C. to about 100°

C.

12. The process of claim 1 wherein the adsorbent is in a fixed-bed arrangement when contacted with the hydrocarbon stream.

13. The process of claim 6 wherein said support is selected from alumina, silica, alumina-silica, and large pore zeolites.

14. The process of claim 1 wherein said adsorbent is preconditioned with hydrogen.

15. The process of claim 13 wherein said adsorbent is preconditioned with hydrogen.

16. The process of claim 1 wherein said adsorbent is preconditioned with a mixture of hydrogen and hydrogen sulfide.

17. The process of claim 13 wherein said adsorbent is preconditioned with a mixture of hydrogen and hydrogen sulfide.

18. A process for removing sulfur compounds from sulfur compound-containing naphtha streams boiling in the range of about 10°

C. to about 230°

C., which process comprises contacting the sulfur compound-containing naphtha stream, in the substantial absence of added hydrogen, with an adsorbent comprised of Co and at least one Group VI metal selected from Mo and W on an inorganic refractory support under conditions that include temperatures from about 10°

C. to about 150°

C.

19. The process of claim 18 wherein the Co content of said adsorbent is from about 2 wt. % to about 20 wt. % and the Group VI metal content from about 5 wt. % to about 30 wt. % on support.

20. The process of claim 19 wherein said support is selected from alumina, silica, alumina-silica, and large pore zeolites.

21. The process of claim 20 wherein said adsorbent is preconditioned with hydrogen.

22. The process of claim 20 wherein said adsorbent is preconditioned with a mixture of hydrogen and hydrogen sulfide.

23. A process for removing sulfur compounds from sulfur compound-containing naphtha streams boiling in the range of about 10°

C. to about 230°

C., which process comprises contacting the sulfur compound-containing naphtha stream, in the substantial absence of added hydrogen, with an adsorbent comprised of Co and at least one Group VI metal selected from Mo and W on an inorganic refractory support under conditions that include temperatures from about 10°

C. to about 150°

C., wherein said adsorbent was preconditioned with hydrogen.

24. The process of claim 23 wherein the Co content of said adsorbent is from about 2 wt. % to about 20 wt. % and the Group VI metal content from about 5 wt. % to about 30 wt. % on support.

25. The process of claim 24 wherein said support is selected from alumina, silica, alumina-silica, and large pore zeolites.

26. The process of claim 23 wherein hydrogen sulfide is used in combination with hydrogen to precondition said adsorbent.

27. The process of claim 25 wherein hydrogen sulfide is used in combination with hydrogen to precondition said adsorbent.

28. A process for removing sulfur from sulfur compound-containing naphtha streams boiling in the range of about 10°

C. to about 230°

C., which process comprises;

a) hydrodesulfurizing said naphtha stream, which contains olefins and sulfur in the form of organic sulfur compounds, to form a hydrodesulfurization effluent at an initial temperature, the hydrodesulfurization effluent comprising a hot mixture of sulfur reduced naphtha at an initial pressure, H₂S and mercaptans, and then

b) contacting said mixture with an adsorbent comprised of Co and at least one Group VI metal selected from Mo and W on an inorganic support under conditions that include temperatures up to about 150°

C., in the substantial absence of added hydrogen.

29. The process of claim 28 wherein there is provided, between step (a) and step (b) a step wherein the system is rapidly depressurized for a depressurization time at least a portion of the hydrodesulfurization effluent to destroy at least a portion of the mercaptans to form more H₂S and a depressurized naphtha further reduced in sulfur.