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 C.sub.4 -C.sub.6 feed to an isomerization zone containing substantial amounts of cyclic hydrocarbons is contacted with a high chloride, platinum alumina catalyst to simultaneously open cyclic hydrocarbon rings and isomerize paraffins to more highly branched paraffins. The process can operate at relatively low severity conditions that provide favorable equilibrium conditions for isoparaffin conversion. The ring opening is also obtained without excessive generation of light hydrocarbons. Multiple stage reaction zones may be used to operate the first stage at slightly higher severity than the second stage to maximize ring opening and obtain favorable equilibrium of iso to normal paraffins.

Abstract: A method for the in situ conversion and recovery of heavy hydrocarbonaceous crude oil containing indigenous trace metal from two adjacent non-communicating hydrocarbon reservoirs which are alternately pressured and recovered which method comprises: (a) heating the heavy hydrocarbonaceous crude oil in a first reservoir to a hydrocarbon conversion temperature; (b) contacting the first reservoir with elemental essentially-anhydrous hydrogen at a pressure from about 200 to about 10,000 psig; (c) heating the heavy hydrocarbonaceous crude oil in a second reservoir to a hydrocarbon conversion temperature; (d) depressuring the first reservoir to yield an effluent comprising hydrocarbonaceous crude oil and unreacted elemental hydrogen; (e) separating the effluent from the first reservoir to recover a hydrocarbonaceous crude oil and a gaseous component comprising elemental hydrogen; (f) contacting the second reservoir with elemental essentially-anhydrous hydrogen, a portion of which is recovered in step (e), at a press

Abstract: A process for the in situ conversion of heavy hydrocarbonaceous crude oil containing indigenous trace metal which comprises heating said heavy hydrocarbonaceous oil in situ to a hydrocarbon conversion temperature, contacting the hot hydrocarbonaceous oil with hydrogen at a pressure from about 200 to about 5000 psig, and recovering the resulting converted hydrocarbonaceous oil.

Abstract: A process for the direct catalytic conversion of hydrocarbon oil is disclosed wherein the hydrocarbon feedstock, hydrogen and hot solid catalyst particles are contacted at a temperature from about 600.degree. F. to about 995.degree. F. to form a suspension in a riser reactor thereby producing lower boiling hydrocarbon components.

Abstract: A contaminating metal on a cracking catalyst used for the cracking of hydrocarbons is passivated by contacting the catalyst at reduction conditions with a reducing gas such as hydrogen that has been saturated with water at ambient conditions.

Abstract: A method for regenerating a coke-contaminated cracking catalyst with the simultaneous carefully controlled combustion of CO to CO.sub.2 within a regeneration zone to produce regenerated catalyst and flue gas. Novel features of the method include adding to the regeneration zone, independently of the cracking catalyst, a CO oxidation promoter and combusting CO to CO.sub.2 in the presence of the promoter and regenerated catalyst. The oxidation promoter may be added to the regeneration zone in amounts to control the CO concentration in the flue gas, a regeneration zone temperature, or the residual carbon concentration on regenerated catalyst.

Abstract: A method for regenerating a coke-contaminated cracking catalyst with the simultaneous carefully controlled catalyzed combustion of CO to CO.sub.2 within a regeneration zone to produce regenerated catalyst and flue gas. Novel features of the method include adding to the regeneration zone, independently of the cracking catalyst, a supported CO oxidation promoter and combusting CO to CO.sub.2 in the presence of the promoter and regenerated catalyst. A supported oxidation promoter may be added to the regeneration zone in amounts to control the CO concentration in the flue gas, a regeneration zone temperature, or the residual carbon concentration on regenerated catalyst.

Abstract: A method for regenerating a coke-contaminated cracking catalyst with the simultaneous carefully controlled combustion of CO to CO.sub.2 within a regeneration zone to produce regenerated catalyst and flue gas. Novel features of the method include adding to the regeneration zone, independently of the cracking catalyst, a liquid comprising a soluble CO oxidation promoter selected from the group consisting of the noble metals and compounds thereof and combusting CO to CO.sub.2 in the presence of the promoter and regenerated catalyst. The liquid may be added to the regeneration zone in amounts to control the CO concentration in the flue gas, a regeneration zone temperature, or the residual carbon concentration on regenerated catalyst.

Abstract: A continuous catalytic reaction and catalyst reactivation process is performed using a simulated moving catalyst bed to effect simultaneously in different zones of a multi-zone fixed catalyst bed an alkylation reaction of olefinic and aromatic reactants and a reactivation of catalyst.

Abstract: A continuous catalytic reaction and catalyst reactivation process is carried out using a simulated moving catalyst bed to effect simultaneously in different zones of a multi-zone fixed catalyst bed an alkylation reaction of olefin and isoparaffin reactants and a reactivation of catalyst.