초록 ▼

The invention described herein is directed to (a) slurry hydroprocessing (SHP) of a feed under SHP conditions; (b) deasphalting, under deasphalting conditions the product obtained from said step (a) and recovering a solvent deasphalted oil and solvent deasphalted rock; (c) calcining said solvent dea

The invention described herein is directed to (a) slurry hydroprocessing (SHP) of a feed under SHP conditions; (b) deasphalting, under deasphalting conditions the product obtained from said step (a) and recovering a solvent deasphalted oil and solvent deasphalted rock; (c) calcining said solvent deasphalted rock at a temperature of ≤about 1200° F. to produce an ash catalyst precursor; (d) recycling said ash catalyst precursor to said step (a).

대표청구항 ▼

1. A process comprising the steps of: (a) slurry hydroprocessing (SHP) of a feed under SHP conditions; (b) deasphalting, under deasphalting conditions the product obtained from said step (a) and recovering a solvent deasphalted oil and solvent deasphalted rock; (c) calcining said solvent deasph

1. A process comprising the steps of: (a) slurry hydroprocessing (SHP) of a feed under SHP conditions; (b) deasphalting, under deasphalting conditions the product obtained from said step (a) and recovering a solvent deasphalted oil and solvent deasphalted rock; (c) calcining said solvent deasphalted rock at a temperature of ≤about 1200° F. to produce an ash catalyst precursor; (d) recycling said ash catalyst precursor to said step (a). 2. A catalyst precursor composition prepared by calcining, at a temperature≤about 1200° F. a solvent deasphalted rock obtained in the solvent deasphalting of a product from SHP of heavy feed wherein said heavy feed has an API gravity of ≤15 with a viscosity of ≥60 centistokes at 60° C. 3. The method according to claim 1 wherein said feed has an API gravity of ≤15 with a viscosity of ≥60 centistokes at 60° C. 4. The method of claim 1 wherein said solvent deasphalted rock is converted to coke at temperatures of about 800 to about 1200° F. prior to said calcination step (c). 5. The process of claim 1 wherein said ash provides from about 0.1 to about 5.0 wt % metals based on the weight of feed. 6. The process of claim 1 wherein said SHP is conducted at temperatures of about 725° to about 850° F. and pressures from about 800 to about 2500 psig. 7. The process of claim 6 wherein conversion of at least about 30% is obtained. 8. The process of claim 1 wherein said calcination step generates heat and said heat is used to generate steam or to preheat said heavy feed in said step (c). 9. The process of claim 1 wherein said ash catalyst is activated prior to said step (c). 10. The process of claim 1 wherein said ash catalyst contains one or more metals or metal compounds of vanadium, nickel, iron or molybdenum. 11. The process of claim 1 wherein the SHP step (a) is conducted using a slurry hydrotreating catalyst and said slurry hydrotreating catalyst is replaced, reduced, or used in conjunction with said ash catalyst precursor of said step (d) as catalyst for said SHP step (a). 12. The process of claim 1 wherein said ash catalyst precursor is activated in situ in said slurry hydroprocessing step. 13. The process of claim 1 wherein said ash catalyst precursor is activated ex-situ prior to recycling to said step (a). 14. A catalyst composition according to claim 2 wherein said catalyst precursor is activated. 15. A catalyst composition according to claim 14 wherein said activation is achieved by sulfiding said catalyst precursor.