Abstract: A process for treating a hydrocarbonaceous stream containing a non-distillable component to produce a hydrogenated distillable hydrocarbonaceous product while minimizing thermal degradation of the hydrocarbonaceous stream which process comprises the steps of: (a) contacting the hydrocarbonaceous stream with a hot first hydrogen-rich gaseous stream having a temperture greater than the hydrocarbonaceous stream in a flash zone at flash conditions thereby increasing the temperature of the hydrocarbonaceous stream without indirect heat exchange and vaporizing at least a portion thereof to provide a hydrocarbonaceous vapor stream comprising hydrogen and a heavy stream comprising the non-distillable component; (b) contacting the hydrocarbonaceous vapor stream comprising hydrogen with a hydrogenation catalyst in a hydrogenation reaction zone at hydrogenation conditions to increase the hydrogen content of the hydrocarbonaceous compounds contained in the hydrocarbonaceous vapor stream; (c) condensing at least a portion

Abstract: The rate at which an oxygen-containing gas stream is admixed with hydrocarbons and hydrogen upstream of a catalytic hydrogen oxidation zone is controlled on the basis of temperature differentials across the oxidation zone and an upstream catalytic dehydrogenation zone. This control overrides the normal control mode based upon the outlet temperature of the oxidation zone effluent stream, which is the inlet temperature to a subsequent bed of hydrocarbon conversion catalyst. The control method can be used to apply oxidative reheat technology to a variety of processes.

Abstract: A process for treating a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component to produce a hydrogenated distillable hydrocarbonaceous product while minimizing thermal degradation of the hydrocarbonaceous stream which process comprises the steps of: (a) contacting the hydrocarbonaceous stream with a first hydrogen-rich gaseous stream having a temperature greater than the hydrocarbonaceous stream in a flash zone at flash conditions thereby increasing the temperature of the hydrocarbonaceous stream and vaporizing at least a portion thereof to provide a hydrocarbonaceous vapor stream comprising hydrogen and a heavy stream comprising the non-distillable component; (b) contacting the hydrocarbonaceous vapor stream comprising hydrogen with a hydrogenation catalyst in a hydrogenation reaction zone at hydrogenation conditions to increase the hydrogen content of the hydrocarbonaceous compounds contained in the hydrocarbonaceous vapor stream; (c) condensing at least a portion of the resu

Abstract: A process for the conversion of an aromatic-rich, residual hydrocarbonaceous charge stock which 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 at least a portion of the residual hydrocarbonaceous charge stock and a hereinafter-described paraffin-rich, distillable hydrocarbonaceous stream boiling at a temperature greater than about 700.degree. F. (371.degree. C.) in a thermal coking zone at mild thermal coking conditions selected to provide thermal coking zone effluent rich in middle distillate; (b) separating the thermal coking zone effluent to provide a middle distillate fraction boiling in the range from about 300.degree. F. (149.degree. C.) to about 700.degree. F. (371.degree. C.) and a distillate hydrocarbonaceous stream boiling at a temperature greater than about 700.degree. F. (371.degree. C.

Abstract: 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.

Abstract: A process for the conversion of residual asphaltene-containing hydrocarbonaceous charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption.

Abstract: A process for the conversion of residual asphaltene-containing hydrocarbonaceous charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption.