Mobil Oil Corporation

Mobile Oil Corporation

Sadi Mizrahi

Philip Jay Angevine

Samuel A Tabak

Stuart S Shih

Pochen Chu

Joseph A Herbst

Garry W Kirker

Charles M Sorensen

Gunter H Kuhl

Robert G Bundens

James C Vartuli

Stuart Damon Hellring

Ralph M Dessau

Arthur W Chester

John Scott Buchanan

Terry Eugene Helton

Albin Huss, Jr

Mae K Rubin

David H Olson

Robert A Ware

Stephen M Oleck

Daria N Lissy

Michael E Landis

Michael S Sarli

Guenter H Kuehl

Robert P Absil

Robert C Wilson, Jr

James H Beech, Jr

Anthony S Fung

Daniel J Neuman

Kenneth R Albinson

Timothy F Kinn

Norman J Rouleau

Timothy Frederick Kinn

A process for converting a heavy aromatics feed to lighter aromatic products, such as benzene and xylene, by reacting C.sub.9+ aromatic hydrocarbons and toluene or benzene under transalkylation reaction conditions, over a first catalyst composition including a zeolite having a constraint index ranging from 0.5 to 3 and a hydrogenation component and a second catalyst composition including an intermediate pore size zeolite having a constraint index ranging from 3 to 12 and a silica to alumina ratio of at least about 5, to produce a transalkylation reaction product containing benzene or toluene and xylene. The benzene or toluene from the reaction product can then be distilled to obtain a benzene or toluene product.

Process for converting C.sub.9 + aromatic hydrocarbons to lighter

Para-xylene is produced by toluene methylation by charging toluene and a methylating agent to a fluidized bed of catalyst at a rate sufficient to maintain the fluidized bed in a turbulent sub-transport flow regime, reacting the toluene with the methylating agent, and recovering para-xylene from the fluidized bed. The fluidizable catalyst is a microporous material having a Constraint Index of about 1 to about 12. The relative concentration of the catalyst particles having a major dimension of less than 40 microns is controlled at between about 5 and 35 weight percent. The catalyst particles have an apparent particle density of about 0.9 to 1.6 grams per cubic centimeter, a size range of about 1 to 150 microns, and average particle size of about 20 to 100 microns.

Fluid bed process for para-xylene production

A heavy aromatics feed is converted to lighter aromatics products, such as benzene, toluene and xylenes by contacting a C.sub.9 + aromatics fraction and benzene and/or toluene over a catalyst comprising a zeolite, such as ZSM-12, and a hydrogenation component, preferably platinum. The catalyst, complete with hydrogenation component, is treated to reduce aromatics loss. Treatment includes exposure to steam and/or sulfur after incorporation of the hydrogenation component. For additional stability and aromatics retention the steamed and/or sulfur treated catalyst is sulfided by cofeeding a source of sulfur. In a further embodiment of the invention a low hydrogen partial pressure is employed to retain aromatics.

Transalkylation process for producing aromatic product using a treated

A moderate pressure hydrocracking process in which a highly aromatic, substantially dealkylated feedstock is processed to high octane gasoline and low sulfur distillate by hydrocracking over a catalyst, preferably comprising ultrastable Y and a Group VIII metal and a Group VI metal, in which the amount of the Group VIII metal content is incorporated at specified proportion into the framework aluminum content of the ultrastable Y 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 400-1000 psig at moderate to high conversion levels to maximize the production of monocyclic aromatics which provide the requisite octane value to the product gasoline. The distillate products from the hydrocracker are reduced in their sulfur content.

Catalyst for light cycle oil upgrading

Light olefins are converted to gasoline with a high enough content of ethers to provide a significant octane improvement over a base (or `cracking`) gasoline (clear RON=90-92; clear MON=79-80). One portion of the olefins is hydrated to produce alcohols, and the other is used to synthesize an olefin-rich gasoline. The alcohols are used to etherify the gasoline. The combination of unit operations minimizes the energy needed to run the process for which no external solvent is needed. The process capitalizes on the higher solubility in gasoline of ethanol, propanol and butanol, compared to methanol. Besides having very low solubility in gasoline, etherification with methanol or ethanol produces an inadequately rewarding increase in octane number, compared to propanol or isopropanol. Taking advantage of the inherent chemical and physical properties of C.sub.3 -C.sub.4 alcohol/gasoline mixtures results both in an unexpectedly high octane number for the ether-rich gasoline as well as an effective and economical process for producing it. The improvement in octane is particularly noteworthy because the weight percent of oxygen in olefinic gasoline etherified with C.sub.3 -C.sub.4 alcohols is less than one-half that of gasoline etherified with either C.sub.1 or C.sub.2 alcohol.

Process for the conversion of light olefins to ether-rich gasoline

A process is disclosed for upgrading C.sub.5 -C.sub.8 olefin-containing gasoline to a high octane motor gasoline blending component. C.sub.3 -C.sub.4 olefins are hydrated to alcohols and then selectively removed from the aqueous hydration reactor effluent stream via liquid extraction with the gasoline feedstream. The alcohol enriched gasoline extract stream is then etherified and unreacted alcohols are extracted to yield a high octane gasoline blending component free of metal-bearing additives.

Process for upgrading olefinic gasoline by etherification wherein

A novel catalyst composition is provided for catalytic cracking of a hydrocarbon oil to provide a product of increased octane number and increased C.sub.5 + gasoline content. The catalyst composition contains a large pore crystalline molecular sieve component and an MCM-22 zeolite component.

Catalyst composition for octane improvement in catalytic cracking

A two-stage hydrocracking process for producing high density jet fuel from an aromatic feedstock using a synthetic zeolite catalyst. The feedstock is hydrotreated in the first stage to convert heteroatoms. After removal of sulfur and nitrogen compounds, the feed is directed to a hydrocracker where it contacted with MCM-22 zeolite.

Hydrocracking process for producing a high density jet fuel

A process for increasing the volume of feed throughput to the catalytic cracker by decreasing hydrogen and total gas volume production, under catalytic cracking conditions temperature of 950.degree. F. to about 1150.degree. F., a catalyst to feed ratio of 3:1 to 10:1 and a catalyst contact time of from about 1 to about 20 in the presence of catalyst comprising ZSM-20 and a matrix.

Increasing feed volume throughput in FCC process

The use of a catalyst containing Mn, a large pore crystalline molecular sieve, and optionally rare earths in catalytic cracking is disclosed. This catalyst gives high gasoline selectivity with low coke yields and is suitable for either gas oil or resid cracking applications.

Catalytic cracking

The present invention is directed to a cascade catalytic hydrotreating/dewaxing process, wherein a hydrocarbon feedstock containing waxy components is treated. The hydrotreating phase precedes the dewaxing phase in order to remove contaminants, such as nitrogen and sulfur, from the feedstock to prolong the life of the catalyst used in the subsequent dewaxing step. A conventional hydrotreating catalyst is used. The dewaxing catalyst is a Zeolite Beta catalyst. The cascade process is conducted with or without interstage gas separation. The treatment occurs in the same or in separate reactors. The ratio of hydrotreating catalyst to dewaxing catalyst is greater than 1:2. This sequence of treatments enhances distillate yields and lowers processing and capital costs.

Catalyst hydrotreating and dewaxing process

A catalytic cracking process is disclosed in which octane improvement is attained by the addition to conventional cracking catalysts of small amounts of additive catalyst comprising a class of zeolites characterized by a silica to alumina mole ratio greater than about 12 and a Constraint Index of about 1 to 12 bound in a matrix chosen such that the matrix component forms a thermodynamically favored compound with selected cations. Sustained catalytic activity is achieved by pre-exchanging the catalyst to a high level of selected cation loading. By extending the active life of the additive catalyst, markedly lower makeup catalyst addition rates are required.

Catalytic cracking process using high equilibrium activity additive

Octane and improvement in catalytic cracking processes can be attained by the addition to conventional cracking catalysts of small amounts of additive catalyst comprising a class of zeolites characterized by a silica to alumina mole ratio greater than about 12 and a Constraint Index of about 1 to 12 bound in a matrix chosen such that the matrix component forms a thermodynamically favored compound with selected cations. Sustained catalytic activity is achieved by pre-exchanging the catalyst to a high level of selected cation loading. By extending the active life of the additive catalyst, markedly lower makeup catalyst addition rates are required.

High equilibrium activity additive catalyst for catalytic cracking

The invention provides a process of converting shale oil fractions with the catalyst made by beginning the synthesis in the usual way and adding additional trivalent metal ion after crystallization is 20 to 90 percent complete and continuing the crystallization, whereby a zeolite having the same crystal structure throughout, but having different silica-to-alumina molar ratios in the inner core and outer shell is obtained.

Catalytic conversion of shale oil

There is provided a zeolite containing catalyst support for denitrogenation of oil feedstocks such as shale oil. The denitrogenation catalyst contains an active hydrogenation catalyst component such as a nickel/molybdenum catalyst.

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Cherry Hill, NJ, United States of America

Sadi Mizrahi