Uop Lcc

Michael J Humbach

John G Hale

Anthony G Vickers

A process for the conversion of an aromatic-rich, distillable gas oil charge stock which is essentially free from asphaltenic hydrocarbons and possesses an aromatic hydrocarbon concentration greater than about 20 volume percent to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption which process comprises the steps of: (a) reacting the charge stock with hydrogen, in a catalytic hydrocracking reaction zone, at hydrocracking conditions including a maximum catalyst bed temperature in the range of about 600.degree. F. (315.degree. C.) to about 850.degree. F. (454.degree. C.) selected to convert at least a portion of the charge stock to lower-boiling hydrocarbon products including middle distillate and to convert at least about 10 volume percent of the aromatic hydrocarbon compounds contained in the charge stock to provide an increased concentration of paraffin hydrocarbon compounds in the resulting hydrocracking reaction zone effluent; (b) separating the resulting hydrocracking reaction zone effluent to provide a middle distillate product stream and a paraffin-rich hydrocarbonaceous stream boiling at a temperature greater than about 700.degree. F. (371.degree. C.); (c) recovering the middle distillate product stream; (d) reacting the paraffin-rich hydrocarbonaceous stream recovered in step (b) in a non-catalytic thermal reaction zone at mild thermal cracking conditions including an elevated temperature from about 700.degree. F. (371.degree. C.) to about 980.degree. F. (526.degree. C.), a pressure from about 30 psig (207 kPa gauge) to about 1000 psig (6895 kPa gauge) and an equivalent residence time at 900.degree. F. (482.degree. C.) from about 1 to about 60 seconds to provide a non-catalytic thermal reaction zone effluent; and (e) separating the non-catalytic thermal reaction zone effluent to provide a fraction boiling in the range from about 300.degree. F. (149.degree. C.) to about 700.degree. F. (371.degree. C.).

Combination process for the conversion of a distillate hydrocarbon to

A process for the conversion of an aromatic-rich, distillable gas oil charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption which process comprises the steps of reacting the charge stock with hydrogen, in a catalytic hydrocracking reaction zone, at hydrocracking conditions including a maximum catalyst bed temperature in the range of about 600.degree. F. (315.degree. C.) to about 850.degree. F. (454.degree. C.) selected to convert at least a portion of the charge stock to lower-boiling hydrocarbon products including middle distillate and to convert at least about 10 volume percent of the aromatic hydrocarbon compounds contained in the charge stock to provide an increased concentration of paraffin hydrocarbon compounds in the resulting hydrocracking reaction zone effluent; separating the resulting hydrocracking reaction zone effluent to provide a middle distillate product stream and a paraffin-rich hydrocarbonaceous stream boiling at a temperature greater than about 700.degree. F. (371.degree. C.); recovering the middle distillate product stream; reacting the paraffin-rich hydrocarbonaceous stream recovered above in a non-catalytic thermal reaction zone at mild thermal cracking conditions including an elevated temperature from about 700.degree. F. (371.degree. C.) to about 980.degree. F. (526.degree. C.), a pressure from about 30 psig (207 k Pa gage) to about 1000 psig (6895 k Pa gage) and an equivalent residence time at 900.degree. F. (482.degree. C.) from about 1 to about 60 seconds to provide a non-catalytic thermal reaction zone effluent; and separating the non-catalytic thermal reaction zone effluent to provide a fraction boiling in the range from about 300.degree. F. (149.degree. C.) to about 700.degree. F. (371.degree. C.).

A catalyst regeneration process and apparatus for the oxidative removal of coke from a coke-contaminated fluid catalyst. The process utilizes a high temperature coke combustion zone and a catalyst disengagement zone. A mixture of coke-contaminated catalyst, and oxygen-containing gas are contacted in the combustion zone and from there, the regenerated catalyst and flue gas mixture passes to the catalyst disengagement zone. There are one or more diplegs through which regenerated catalyst flows from the disengagement zone to the combustion zone. The diplegs are sized so as to ensure a low maximum accumulation of catalyst in the disengagement zone. The temperature at a lower locus of the combustion zone may be controlled by control of the catalyst inventory in the reactor-regenerator system.

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Wilmette, IL, United States of America

Michael J Humbach