# US 10,870,806 B2 · Hydroprocessing of catalytic slurry oil and coker bottoms > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 10,870,806 B2 - Document ID: US10870806B2 - Status: Granted - Kind: B2 - Application number: 15/928,436 - Filed: 2018-03-22 - Published: 2018-10-11 - Granted: 2020-12-22 - Earliest claimed: 2017-04-07 - Assignees: ExxonMobil Research and Engineering Company - Applicants: ExxonMobil Research and Engineering Company - Inventors: Stephen H. Brown; Brian A. Cunningham; Randolph J. Smiley; Samia Ilias; Brenda A. Raich; Tien V. Le - Web page: https://patentgrep.com/patent/US10870806B2 ## CPC - C10G 69/04: including at least one step of catalytic cracking in the absence of hydrogen - C10B 49/22: according to the "fluidised bed" technique - C10B 57/045: {containing mineral oils, bitumen, tar or the like or mixtures thereof} - C10G 45/00: Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds - C10G 45/04: characterised by the catalyst used - C10G 47/00: Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06) - C10G 47/02: characterised by the catalyst used - C10G 67/0454: {Solvent desasphalting} - C10G 69/06: including at least one step of thermal cracking in the absence of hydrogen - C10G 69/14: plural parallel stages only - C10G 2300/205: Metal content - C10G 2300/206: Asphaltenes - C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES - C10B: DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS (cracking oils C10G; underground gasification of minerals E21B43/295) ## Abstract Systems and methods are provided for upgrading a mixture of catalytic slurry oil and coker bottoms by hydroprocessing. Optionally, the upgrading can further include deasphalting the mixture of catalytic slurry oil and coker bottoms to form a deasphalted oil and a deasphalter residue or rock fraction. The mixture of catalytic slurry oil and coker bottoms and/or the deasphalted oil can then be hydroprocessed to form an upgraded effluent that includes fuels boiling range products. Optionally, in some aspects where the feed mixture is deasphalted prior to hydroprocessing, the feed mixture can further include a portion of a (sour) vacuum resid. ## Claims ### Claim 1 A method for processing product fractions from a fluid catalytic cracking process and a coking process, comprising: performing solvent deasphalting on a feed comprising at least 10 wt % of a catalytic slurry oil and at least 10-50 wt % of a coker bottoms, the coker bottoms having an aromatic carbon content of 20 wt % to 50 wt % relative to a weight of the coker bottoms, to form a deasphalted oil and a deasphalter residue, a yield of the deasphalted oil being about 50 wt % or more relative to a weight of the feed having less than about 10 wppm of catalyst fines, and the deasphalter residue containing more than 100 wppm of catalyst fines; and exposing the deasphalted oil to a hydroprocessing catalyst under effective fixed bed hydroprocessing conditions to form a hydroprocessed effluent, wherein the hydroprocessed effluent comprises about 0.1 wt % or less of sulfur. ### Claim 2 (depends on 1) The method of claim 1, wherein a weight of catalytic slurry oil in the feed is equal to or greater than a weight of coker bottoms in the feed; or wherein the feed comprises 40 wt % or more of the catalytic slurry oil; or a combination thereof. ### Claim 3 (depends on 1) The method of claim 1, further comprising settling at least one of the catalytic slurry oil and the feed prior to exposing the deasphalted oil to the hydroprocessing catalyst, the at least one of the catalytic slurry oil and the deasphalted oil having a catalyst fines content of 1 wppm or less after settling. ### Claim 4 (depends on 1) The method of claim 1, wherein the effective hydroprocessing conditions are effective for 55 wt % or more conversion of the deasphalted oil relative to 566° C. ### Claim 5 (depends on 1) The method of claim 1, further comprising coking a first feedstock comprising a 566° C.+ portion in a coker to form at least a coker naphtha fraction, a coker gas oil fraction, and at least a portion of the coker bottoms. ### Claim 6 (depends on 1) The method of claim 1, further comprising exposing a second feedstock having a T90 distillation point of 566° C. or less to a catalyst under fluid catalytic cracking conditions to form at least an FCC naphtha fraction, a cycle oil, and at least a portion of the catalytic slurry oil. ### Claim 7 (depends on 1) The method of claim 1, wherein the coker bottoms has a T10 distillation point of at least 300° C.; or wherein the coker bottoms has a T90 distillation point of 566° C. or less; or a combination thereof. ### Claim 8 (depends on 1) The method of claim 1, wherein the coker bottoms comprises 4.0 wt % or more of micro carbon residue; or wherein the hydroprocessed effluent comprises 4.0 wt % or less of micro carbon residue; or wherein the catalytic slurry oil comprises 5.0 wt % or more of micro carbon residue; or a combination thereof. ### Claim 9 (depends on 1) The method of claim 1, wherein the feed comprises at least 1.0 wt % of organic sulfur, the hydroprocessed effluent comprising about 0.5 wt % or less of organic sulfur. ### Claim 10 (depends on 1) The method of claim 1, wherein the catalytic slurry oil comprises a 343° C.+ bottoms fraction from a fluid catalytic cracking process.