초록 ▼

The recovery of solids, and particularly solid particulates used as catalysts in slurry hydroprocessing, from asphaltene containing hydrocarbons is improved by controlling asphaltene precipitation. The formation of agglomerates of the solid particulates, having an increased diameter, results in the

The recovery of solids, and particularly solid particulates used as catalysts in slurry hydroprocessing, from asphaltene containing hydrocarbons is improved by controlling asphaltene precipitation. The formation of agglomerates of the solid particulates, having an increased diameter, results in the presence of precipitated asphaltenes, possibly due to flocculation. Asphaltene precipitation is controlled by varying process parameters or introducing additional diluent or flush streams that change the polarity of an asphaltene containing liquid product recovered from an effluent of a slurry hydroprocessing reaction zone.

대표청구항 ▼

1. A slurry hydroprocessing method comprising: (a) passing a slurry comprising a heavy hydrocarbon feedstock containing asphaltenes and a solid particulate through a reaction zone to provide a slurry effluent;(b) filtering a liquid product through a filter, recovered from the slurry effluent in comb

1. A slurry hydroprocessing method comprising: (a) passing a slurry comprising a heavy hydrocarbon feedstock containing asphaltenes and a solid particulate through a reaction zone to provide a slurry effluent;(b) filtering a liquid product through a filter, recovered from the slurry effluent in combination with the solid particulate, to provide a filtration retentate comprising precipitated asphaltenes and further comprising a retained portion of the solid particulate;(c) recycling the filtration retentate to the reaction zone;(d) the liquid product has a solubility blending number : insolubility number ratio that is less than about 1.4; andwherein the filter has a pore size exceeding the average particle size of the solid particulate. 2. The method of claim 1, wherein both the liquid product and at least one gaseous product are recovered from the slurry effluent by flash separation. 3. The method of claim 1, wherein step (b) provides a filtered liquid product having a solids content of less than about 4% by weight. 4. The method of claim 1, wherein the solid particulate comprises a compound of a metal of Group IVB, Group VB, Group VIB, Group VIIB, or Group VIII. 5. The method of claim 4, wherein the solid particulate comprises an iron-containing catalyst precursor. 6. The method of claim 1, wherein the solid particulate has an average particle size from about 1 micron to about 100 microns. 7. The method of claim 1, wherein the heavy hydrocarbon feedstock comprises a component selected from the group consisting of (i) an atmospheric column residue or a vacuum column residue obtained from the distillation of crude oil; (ii) a heavy hydrocarbon product obtained from thermally or catalytically cracking of (i); (ii) bitumen; (iii) Canadian oil sands; (iv) a biomass derived oil, (v) a waste-derived synthetic oil, (vi) a coal-derived oil; and (vii) blends thereof. 8. The method of claim 7, wherein the heavy hydrocarbon feedstock has an initial boiling point of greater than about 343° C. (650° F.). 9. The method of claim 1 further comprising (c) flushing a filter, for filtering the liquid product, with a flush liquid to provide a flush effluent slurry comprising the solid particulate. 10. The method of claim 9, wherein the flush effluent slurry has a solubility blending number : insolubility number ratio of at least about 1.4. 11. The method of claim 9, wherein the flush liquid is added to the filter or to the liquid product, downstream of a separator used to recover the liquid product from the slurry effluent. 12. The method of claim 9, wherein the flush liquid comprises at least about 40% by weight of aromatics. 13. The method of claim 12, wherein the flush liquid is derived from fluid catalytic cracking. 14. The method of claim 9, further comprising recycling at least a portion of the flush effluent slurry to the reaction zone. 15. The method of claim 1, wherein the reaction zone is maintained at a temperature from about 343° C. (650° F.) to about 593° C. (1100° F.), a hydrogen partial pressure from about 3.5 MPa (500 psig) to about 21 MPa (3000 psig), and a space velocity from about 0.1 to about 30 volumes of heavy hydrocarbon feedstock per hour per volume of the reaction zone. 16. A method for upgrading a hydrocarbon distillation residue, the method comprising: (a) passing a slurry comprising the hydrocarbon distillation residue and a solid particulate through hydroprocessing reaction zone in the presence of hydrogen to provide a slurry effluent, wherein the hydrocarbon distillation residue contains asphaltenes,(b) subjecting the slurry effluent to one or more flash separation or distillation stages to recover a liquid product in combination with the solid particulate,(c) filtering the liquid product through a filter to provide (i) a filtered liquid product having a reduced content of both the solid particulate and asphaltenes and (ii) a retentate comprising a retained fraction of the solid particulate and asphaltenes;(d) continuously or periodically flushing the filter with a flush liquid to provide a flush effluent slurry comprising the retained fraction of the solid particulate and the asphaltenes;(e) recycling the retentate to the reaction zone;wherein the liquid product has a solubility blending number: insolubility number ratio that is less than about 1.4; andwherein the filter has a pore size exceeding the average particle size of the solid particulate. 17. The method of claim 16, further comprising: (f) recycling at least a portion of the flush effluent slurry to the hydroprocessing reaction zone. 18. The method of claim 1 wherein the liquid product has a solubility blending number : insolubility number ratio that is less than about 1.4 obtained by adding a diluent to the liquid product.