Coking with solvent separation of recycle oil using coker naphtha

Claim 2

A coking process comprising the steps of: (a) coking a carbonaceous chargestock in a coking stock at coking conditions to produce coke and a vapor phase product, including heavy and light normally liquid hydrocarbons; (b) separating at least a portion of said heavy hydrocarbons from said vapor phase product, said separated hydrocarbons having a Conradson carbon content ranging from about 5 to about 50 weight percent; (c) subsequently contacting at least a portion of said separated heavy hydrocarbons with coker naphtha in a solvent separation zone at solvent separation conditions, including a volumetric ratio of said solvent to said portion of separated heavy hydrocarbon ranging from about 0.5:1 to 10:1, to separate said heavy hydrocarbons into a high Conradson carbon hydrocarbonaceous product comprising a minor portion of said coker naphtha and a low Conradson carbon hydrocarbonaceous product comprising a major portion of said coker naphtha; (d) recycling at least a portion of said high Conradson carbon hydrocarbonaceous product comprising said minor portion of coker naphtha to said coking zone; and (e) recovering said low Conradson carbn hydrocarbonaceous product of step (c).

Claim 3

The process of claim 1 wherein a naphtha fraction is separated from said vapor phase product of step (a) and wherein at least a portion of said separated naphtha fraction is passed to said solvent separation zone of step (c).

Claim 4

The process of claim 1 wherein said coking process is a fluid coking process wherein said carbonaceous chargestock is contacted with hot fluidized solids in a fluidized bed contained in said coking zone.

Claim 5

The process of claim 3 wherein the initial atmospheric pressure boiling point of said heavy hydrocarbons separated from said vapor phase product ranges from about 650° to about 1100° F.

Claim 6

The process of claim 3 wherein said vapor phase product of step (a) is passed to a scrubbing zone, and wherein said heavy hydrocarbons of step (b) are separated in said scrubbing zone and said separated heavy hydrocarbons are withdrawn from said scrubbing zone and passed to said solvent separation zone.

Claim 7

The process of claim 1 wherein said carbonaceous chargestock comprises a hydrocarbonaceous oil having a Conradson carbon content of at least about 5 weight percent.

Claim 8

The process of claim 3 wherein said coking conditions include a temperature ranging from about 850° to about 1800° F. and a pressure ranging from about 0 to about 150 psig.

Claim 9

The process of claim 3 wherein said coking conditions include a temperature ranging from about 900° to about 1200° F.

Claim 10

The process of claim 1 wherein said coking process is delayed coking.

Claim 11

The process of claim 1 wherein said solvent separation conditions include a temperature ranging from about 170° F. to about 700° F.

Claim 12

The process of claim 1, wherein said solvent separation conditions include a pressure ranging from about 50 to 1500 psig.

Claim 13

A fluid coking process comprising the steps of: (a) contacting a carbonaceous chargestock with hot fluidized solids in a fluidized bed contained in a coking zone at coking conditions to produce coke which deposits on said fluidized solids and a vapor phase product, including heavy and light normally liquid hydrocarbons; (b) passing said vapor phase product of step (a) to a scrubbing zone and separating at least a portion of said heavy hydrocarbons from said vapor phase product in said scrubbing zone, said separated hydrocarbons having a Conradson carbon content ranging from 5 to 50 weight percent; (c) subsequently contacting at least a portion of said separated heavy hydrocarbons with coker naphtha in a solvent separation zone at solvent separation conditions, including a volumetric ratio of said solvent to said portion of separated heavy hydrocarbons ranging from about 0.5:1 to 10:1, to separate said heavy hydrocarbons into a high Conradson carbon hydrocarbonaceous product comprising a minor portion of said coker naphtha and a low Conradson carbon hydrocarbonaceous product comprising a major portion of said coker naphtha; (d) recycling at least a portion of said high Conradson carbon hydrocarbonaceous product comprising said minor portion of coker naphtha to said coking zone, and (e) recovering said low Conradson carbon hydrocarbonaceous product.

Claim 14

A fluid coking process comprising the steps of: (a) contacting a carbonaceous chargestock with hot fluidized solids in a fluidized bed contained in a coking zone at coking conditions to produce coke which deposits on said fluidized solids and a vapor phase product, including heavy and light normally liquid hydrocarbons; (b) passing said vapor phase product of step (a) to a scrubbing zone and separating at least a portion of said heavy hydrocarbons from said vapor phase product in said scrubbing zone, said separated hydrocarbons having a Conradson carbon content ranging from 5 to 50 weight percent; (c) subsequently contacting at least a portion of said separated heavy hydrocarbons with coker naphtha in a solvent separation zone at solvent separation conditions, including a volumetric ratio of said solvent to said portion of separated heavy hydrocarbons ranging from about 0.5:1 to 10:1, to separate said heavy hydrocarbons into a high Conradson carbon hydrocarbonaceous product comprising a minor portion of said coker naphtha and a low Conradson carbon hydrocarbonaceous product comprising a major portion of said coker naphtha; (d) recycling at least a portion of said high Conradson carbon hydrocarbonaceous product comprising said minor portion of coker naphtha to said coking zone, and (e) recovering said low Conradson carbon hydrocarbonaceous product.

Claim 15

The process of claim 12 wherein said coker naphtha has a boiling point ranging from about C5° to about 350° F.