Mobil Oil Corporation

Robert L Smith

Robert L Gorring

Eric J Scott

Clarence D Chang

David S Shihabi

William H Lang

Anthony J Silvestri

Rene B La Pierre

A process which comprises a two-stage method for the preparation, from heavy residual oils, of a feedstock suitable for subsequent catalytic processing, such as for employment in FCC reactors. The firt process step comprises pentane deasphalting which results in substantial reduction of the refractory heavy metals present in the resid. The second step comprises removing any remaining metals by subjecting the treated heavy oil to a mild hydrocracking in the presence of a ZSM-5-type catalyst.

Deasphalting and hydrocracking

The present invention provides a process for low pressure catalytic hydrocracking of refractory hydrocarbon charge stocks, such as coker gas oil or shale oil to products of reduced pour points by catalytic hydrotreating and cascading the hydrotreater effluent through a hydrocracking zone, containing a catalyst which is characterized by an alkali metal substantilly non-acidic crystalline zeolite having an alpha activity of less than about 10, a silica/alumina ratio of at least about 12 and a constraint index of approximately 1 to 12.

Low pressure hydrocracking of refractory feed

The present invention provides a process for catalytic upgrading of refractory hydrocarbon charge stocks, such as coker gas oil, to premium products including gasoline, kerosene, diesel fuel and low sulfur cracking stock initially by catalytic hydrotreating and cascading the hydrotreater effluent, through a hydrocracking zone, without change in the pressure of the system, containing a catalyst which is characterized by a crystalline zeolite having a silica/alumina ratio greater than 12 and a constraint index of 1 to 12.

Catalytic upgrading of refractory hydrocarbon stocks

Liquid products from retorting oil shale are upgraded to a total liquid suited to pipeline transport and containing increased amounts of the premium products gasoline through distillate fuel by hydrotreating to convert sulfur, oxygen, nitrogen and metal constituents and cascading the hydrotreater effluent through a hydrocracking reactor containing a catalyst which is characterized by a crystalline zeolite having a silica/alumina ratio greater than 12 and a constraint index of 1 to 12, for example zeolite ZSM-5.

Upgrading shale oil

Synthesis gas is contacted with an intimate mixture of a carbon monoxide hydrogen reduction catalyst, comprising a methanol synthesis catalyst in combination with a selective class of acidic crystalline aluminosilicate having a silica/alumina ratio greater than 12, a pore dimension greater than about 5 Angstroms to produce hydrocarbon mixtures useful in the manufacture of heating fuels, gasoline, aromatic hydrocarbons, and chemicals intermediates.

Conversion of synthesis gas to hydrocarbon mixtures

A stabilized lubricating oil resistant to oxidation and sludge formation upon exposure to an oxidative environment is prepared without forming undesirable color bodies therein by the steps (1) contacting the lubricating oil stock with a small amount of added elemental sulfur of from about 0.05 to about 1.0 percent by weight at a contact temperature of from about 25.degree. C. to about 130.degree. C. and (2) contacting the product of step (1) with hydrogen in the presence of alumina impregnated with at least about 10 weight percent MoO.sub.3 and at least about 2.5 weight percent CoO to remove any unreacted added elemental sulfur therefrom. The impregnated alumina catalyst of step (2) must have at least 50 percent of the pores with a pore diameter of 50 Angstrom Units or more.

Process for manufacture of stabilized lubricating oil with elemental

A stabilized lubricating oil resistant to oxidation and sludge formation upon exposure to an oxidative environment is prepared without forming undesirable color bodies therein by contacting the lubricating oil stock with a small amount of elemental sulfur of from about 0.1 to about 0.5 percent by weight at a contact temperature of from about 25.degree.C to about 70.degree.C and, thereafter, removing any unreacted sulfur therefrom.

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Hopewell, NJ, United States of America

Robert L Smith