Mobil Oil Corporation

Donald Milstein

Ronald H Fischer

Stephen M Oleck

Thomas R Stein

Howard S Sherry

Stuart S Shih

Grant G Karsner

Byung C Choi

Alan W Peters

Madhava Malladi

Chang-Kuei Lee

Frederick Banta

A solvent extract obtained from a conventional hydrocarbon oil solvent extraction process, e.g., one employing furfural as the extraction solvent, is cooled to a temperature providing, following a secondary decantation of the cooled extract, a pseudo raffinate containing most of the non-aromatics and a pseudo extract possessing a hydro-aromatic content of H.sub.alpha hydrogen of at least 20 percent of the total hydrogen content. The pseudo extract is ideally suited as a hydrogen-donor for a variety of refinery operations such as visbreaking. The pseudo raffinate is suitable as a co-feed for such catalytic cracking operations as fluidized catalytic cracking (FCC) and thermofor catalytic cracking (TCC) and can be recycled to the extraction unit to produce more lube oil.

Upgrading solvent extracts by double decantation and use of pseudo

Resids are hydrocracked at low pressure (600 psig and 825.degree. F.) in a solvent, while being demetalated, desulfurized, and decarbonized, by passing the solution through a dual-bed catalytic system having a large-pore catalyst as the first bed and a small-pore as the second bed. The solvent is preferably process generated and recycled, boiling at about 400.degree.-700.degree. F.

Low pressure cyclic hydrocracking process using multi-catalyst bed

Cyclic hydrotreating of resids with low pressure, short term on-stream periods yields desirable products.

Low pressure hydrotreating of residual fractions

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

Upgrading a Fischer-Tropsch synthesis product by separating a 350.degree. to 850.degree. F product fraction thereof into a 650.degree. F minus fraction and a 650.degree. F plus fraction; separating the 650.degree. F minus fraction to provide a more narrow 350.degree. to 650.degree. F fraction; combining the 650.degree. F plus fraction with a portion of the 350.degree. to 650.degree. F fraction to form a wide boiling range feed material; contacting this formed wide boiling range feed material, together with hydrogen, with a special catalyst comprising a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least 12 and a constraint index of 1 to 12, at a temperature of about 500.degree. to 800.degree. F, a hydrogen partial pressure of about 100 to 800 psia and a space velocity of about 0.5 to 5 LHSV to produce a converted product thereof separating the zeolite conversion product to recover a 350.degree. F minus fraction from a 350.degree. F plus fractions; and separating the 350.degree. F plus fraction to recover a 350.degree. to 450.degree. F jet fuel fraction having a freeze point of less than about -58.degree. F.

Conversion of Fischer-Tropsch heavy product to high quality jet fuel

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

Upgrading a fraction of a heavy Fischer-Tropsch oil to jet fuel by hydropretreating a 350.degree. to 850.degree. F boiling fraction; separating the hydrotreated product into a 650.degree. F minus and a 650.degree. F plus fraction, separating the650.degree. F minus fraction to provide a 350.degree. F minus naphtha boiling range fraction and a 350.degree. to 650.degree. F light distillate fraction; distilling the 350.degree. to 650.degree. F hydrotreated fraction to provide a fraction boiling in the range of 350.degree. F to 550.degree. F separate from a 550.degree. to 650.degree. F fraction processing either of the 650.degree. F plus fraction above separated or the 350.degree. to 550.degree. F boiling fraction above obtained over a catalyst comprising a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least 12 and a constraint index of 1 to 12 with hydrogen, at a temperature of about 500.degree. to 800.degree. F, a hydrogen partial pressure of about 100 to 800 psig and a space velocity in the range of about 0.5 to 5 LHSV to produce a converted product comprising lower boiling hydrocarbons than the feed charged and recovering as a product of the process a reduced pour point diesel oil fraction, a 350.degree. to 550.degree. F jet fuel fraction, and a 350.degree. F minus naphtha product fraction.

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.

An improved process for desulfurization of metals and sulfur containing petroleum oils, preferably those containing residua hydrocarbon components, comprising passing the sulfur containing petroleum oils through a bed of substantially aged desulfurization catalyst at a temperature not less than 770.degree.F preceeding conventional hydrodesulfurization treatment.

Demetalation and desulfurization of oil in separate catalytic zones

This 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 180A to 300A diameter range.

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Cherry Hill, NJ, United States of America

Donald Milstein