Claims
- 1. A slurry hydrotreating process for hydrotreating a heavy fossil fuel to hydrogenate heavy aromatics and remove sulfur, the process comprising:
- reacting the heavy fossil fuel in a hydrotreating zone with hydrogen in the presence of a non-noble metal containing hydrotreating catalyst;
- separating the catalyst from the product of the hydrotreating zone;
- reactivating the catalyst in a reactivating zone, separate from the hydrotreating zone, by hydrogen stripping; and
- recycling the reactivated catalyst to the hydrotreating zone.
- 2. The process of claim 1 wherein the hydrotreating zone contains the hydrotreating catalyst in the form of a slurry at a solids weight percent in the range of about 10 to 70 percent.
- 3. The process of claim 2, wherein the reactivating zone is at a temperature of about 650 to 780.degree. F. and a pressure of about 800 to 4000 psig.
- 4. The process of claim 3, wherein the hydrotreating zone is at a temperature of about 650.degree. to 780.degree. F. and a pressure of about 800 to 4000 psig.
- 5. The process of claim 4 wherein the hydrotreating catalyst slurry contains 40 to 60 weight percent solids.
- 6. The process of claim 2, wherein the heavy fossil fuel is a product of a petroleum, coal, shale oil, bitumen, tar sand, or synfuel conversion process.
- 7. The process of claim 6, wherein the heavy fossil fuel is a heavy catalytic cracking cycle oil, coker gas oil, or vacuum gas oil.
- 8. The process of claim 7 wherein the heavy fossil fuel is a vacuum gas oil containing at least 0.1 wt% sulfur.
- 9. The process of claim 8 wherein the vacuum gas oil contains at least 1.0 wt.% sulfur.
- 10. The process of claim 7, wherein the heavy fossil fuel is distilled in the range of 500 to 1200.degree. F.
- 11. The process of claim 1, comprising a plurality of staged hydrotreating zones.
- 12. The process of claim wherein the catalyst is comprised of molybdenum sulfide.
- 13. The process of claim 12, wherein the catalyst further comprises nickel and/or cobalt.
- 14. The process of claim 13, wherein the catalyst is supported on an inorganic oxide material.
- 15. The process of claim 14, wherein the inorganic oxide material is selected from group consisting of alumina, silica, titania, silica alumina, silica magnesis, and mixtures thereof.
- 16. The process of claim 2, wherein the catalyst is 10 .mu. to 1/8 inch in average diameter.
- 17. The process of claim 16, wherein the catalyst is 10 .mu. to 400 .mu. in average diameter.
- 18. The process of claim 17, wherein the surface area of the catalyst is 80 to 400 m.sup.2 /g.
- 19. The process of claim 2, wherein the pressure in the reactivating zone is 1500 to 2500 psig.
- 20. The process of claim 19, wherein the stripping rate is 0.15 to 7 SCF/lb cat-hr.
- 21. The process of claim 20, wherein catalyst is circulated at a rate of 0.1 to 0.3 lbs of reactivated catalyst per pound of feed.
- 22. A slurry hydrotreating process for hydrotreating a heavy fossil fuel to hydrogenate heavy aromatics and remove sulfur, the process comprising:
- reacting the heavy fossil fuel in a hydrotreating zone with hydrogen in the presence of a non-noble metal containing hydrotreating catalyst wherein the catalyst is in the form of a slurry at a solids weight percent in the range of about 10 to 70 weight percent;
- separating the catalyst from the product of the hydrotreating zone;
- reactivating the catalyst in a reactivating zone, separate from the hydrotreating zone, at a temperature of between about 650.degree. to 780.degree. F. and a pressure of between about 800 to 4000 psig with hydrogen at a stripping rate of 0.15 to 7 SCF/lb cat-hr; and
- recycling the reactivated catalyst at a rate of 0.1 to 0.3 lbs of reactivated catalyst per pound of feed to the hydrotreating zone.
CROSS REFERENCE TO RELATED APPLICATIONS
This application is a continuation-in-part application of application Ser. No. 414,166, filed Sept. 28, 1989 now abandoned.
US Referenced Citations (19)
Continuation in Parts (1)
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Number |
Date |
Country |
Parent |
414166 |
Sep 1989 |
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