Mobil Oil Corporation

Ronald H Fischer

Rene B LaPierre

Philip Varghese

Donald Milstein

Peter J Owens

Stephen M Oleck

Howard S Sherry

Yun-Yang Huang

Stuart S Shih

David Lawrence Stern

Jeffrey S Beck

Ivy Dawn Johnson

Edward J Rosinski

Thomas R Stein

Jeevan S Abichandani

Julius Ciric

Thaddeus E Whyte, Jr

There is provided a continuous toluene disproportionation process to selectively produce para-xylene. The process includes a steady-state of operation, wherein the conversion of toluene and selectivity to para-xylene is maintained at essentially constant target levels. Prior to such a steady-state of operation, the reaction is conducted under a relatively high temperature.

Continuous toluene disproportionation process

A moderate pressure hydrocracking process in which a highly aromatic, substantially dealkylated feedstock having a boiling point in the range between 300.degree. and 650.degree. F. is processed directly to high octane gasoline by hydrocracking over a catalyst, preferably comprising a large pore size, crystalline alumino-silicate zeolite hydrocracking catalyst such as zeolite Y together with a hydrogenation-dehydrogenation component. The feedstock which is preferably a light cut light cycle oil has an aromatic content of at least 50, usually at least 60 percent and an API gravity not more than 25. The hydrocracking typically operates at 600-1000 psig at moderate to high conversion levels to maximize the production of monocyclic aromatics which provide the requisite octane value to the product gasoline.

Production of high octane gasoline

A moderate pressure hydrocracking process in which a highly aromatic, substantially dealkylated feedstock is processed directly to high octane gasoline by hydrocracking over a monofunctional acidic cracking catalyst, preferably comprising a large pore size, crystalline alumino-silicate zeolite hydrocracking catalyst such as zeolite Y. The feedstock which is preferably a light cycle oil obtained from catalytic cracking with an aromatic content of at least 50, usually at least 60 percent and an API gravity not more than 25. The hydrocracking typically operates at 600-1000 psig at moderate to high conversion levels to mazimize the production of monocyclic aromatics which provide the requiste octane value to the product gasoline.

A moderate pressure hydrocracking process in which a highly aromatic, substantially dealkylated feedstock is processed directly to high octane gasoline by hydrocracking over a catalyst, preferably comprising a large pore size, crystalline alumino-silicate zeolite hydrocracking catalyst such as zeolite Y together with a hydrogenation-dehydrogenation component. The feedstock which is preferably a light cycle oil has an aromatic content of at least 50, usually at least 60 percent and an API gravity not more than 25. The hydrocracking typically operates at 600-1000 psig at moderate to high conversion leavels to maximize the production of monocyclic aromatics which provide the requisite octane value to the product gasoline. The unconverted products from the hydrocracker are recyclied to the catalytic cracking unit to obtain further improvements in gasoline yield and octane.

Production of high octane gasoline by hydrocracking catalytic cracking

A moderate pressure hydrocracking process is disclosed in which substantially dealkylated heavy distillate feedstocks are processed directly to high octane gasoline over a catalyst, preferably comprising a crystalline silicate zeolite hydrocracking component having a Constraint Index less than 2. The bottoms fraction produced from the contacting may be passed to an FCC unit for further processing. In another embodiment, the substantially dealkylated heavy distillate feedstock may be fractionated into a lighter boiling stream and a heavier boiling stream for better ease of processing.

This invention is concerned with removing metal and sulfur contaminants from residual oil fractions by catalytic contact with an improved catalyst comprising the oxides or sulfides of a Group VIB metal and an iron group metal supported on an alumina that contains dispersed Delta and/or Theta phase alumina, the catalyst having at least 45% of its pore volume in pores 30 to 150A diameter, at least 10% of its pore volume in pores less than 30A diameter, and at least 15% of its pore volume in pores greater than 300A diameter. The process can be used to prepare feedstock for catalytic cracking.

Process for demetalation and desulfurization of petroleum oils

The disclosure concerns the demetalation and desulfurization of metal and sulfur containing petroleum oils, preferably those containing residua hydrocarbon components, through the use of a catalyst comprising a hydrogenating component composited on a refractory base, preferably an alumina, whose pores are substantially distributed over a narrow 100A to 200A diameter range, but also having at least about 5% of its pores of a diameter greater than 500A.

Catalyst for residua demetalation and desulfurization

A catalyst composition is provided which comprises a magnesium aluminate spinel having a surface area of greater than about 50 m.sup.2 /g, a total pore volume of greater than about 0.475 cc/g from about 50 to about 70 percent of the total pore volume in pores of diameter of from about 50 Angstroms to about 150 Angstroms, greater than about 30 percent of the total pore volume in pores of diameter of from about 80 Angstroms to about 150 Angstroms and from about 5 to about 20 percent of the total pore volume in pores of diameter of greater than 300 Angstroms, said magnesium aluminate spinel having deposited thereon from about 1 to about 5 weight percent cobalt oxide and from about 8 to about 20 weight percent molybdenum oxide.

Catalyst composition

This invention is concerned with removing metal and sulfur contaminants from residual oil fractions by catalytic contact with two different catalysts in the presence of hydrogen. In this process, the oil is first contacted with the major fraction of a catalyst comprising a Group VIB metal and an iron group metal oxide, such as a mixture of cobalt and molybdenum oxides, composited with an alumina support, the catalyst having at least 60% of its pore volume in pores of 100A to 200A diameter and at least about 5% of its pore volume in pores having a diameter greater than 500A. The oil is then contacted with a secondcatalyst of the high surface-area, cobalt-molybdenum on alumina type having a major fraction of its pores in the 30 to 100A diameter range. Finally, the oil is contacted with the remainder of the large-pore catalyst.

Demetalation and desulfurization of residual oil utilizing hydrogen and

This invention is concerned with removing metal and sulfur contaminants from residual oil fractions by catalytic contact in a novel dual bed system. In this process the oil is first contacted with a catalyst comprising a Group VIB metal and an iron group metal oxide, such as a mixture of cobalt and molybdenum oxides, composited with an alumina support that contains delta or theta phase alumina, the catalyst having at least 60% of its pore volume in pores of 100A to 200A diameter, at least about 5% of its pore volume in pores having a diameter greater than 500A, and a surface area up to about 110m.sup.2 /g. The oil is then contacted with a second catalyst of the high surface-area, cobalt-molybdenum on alumina type. The second catalyst has a major fraction of its pores in the 30 to 100A diameter range.

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Cherry Hill, NJ, United States of America

Ronald H Fischer