Exxon Research and Engineering Company

Paul E Eberly

William C Baird, Jr

William E Winter, Jr

Charles H Mauldin

David E Vaughan

Edward William Corcoran, Jr

Tan-Jen Chen

Geoffrey R Say

William A Wachter

Neville L Cull

Francis X Mayer

Todd R Steffens

Willibald Serrand

Jose M Vargas

William L Schuette

Patrick H Terry

George J Balinsky

Duane A Goetsch

Philip Holmes

Judeth H Brannon

Killian D Efird

A catalytic cracking process and apparatus wherein particles of cracking catalyst circulate continuously between a reaction zone and a regeneration zone and hot regenerated catalyst from the regeneration zone contacts hydrocarbon feed in the reaction zone to produce cracked hydrocarbon products and spent catalyst. The spent catalyst is recovered and subjected to stripping in a stripping zone to remove strippable material therefrom. The stripped spent catalyst is circulated to the regeneration zone for oxidative exothermic regeneration. Some hot regenerated catalyst is passed directly from the regenerator to the stripping zone via a conduit provided for this purpose. Another hydrocarbon stream is passed into contact with the hot regenerated catalyst in this conduit. The said other hydrocarbon stream is converted to products of enhanced value (e.g., olefins) during contact with catalyst in the conduit, and the said products are recovered. The heat for the conversion is abstracted from the catalyst particles passing via the pipe to the stripping zone. The hot catalyst particles entering the stripping zone from the pipe increase the temperature in the stripping zone, thereby improving the stripping in the stripping zone.

Catalytic cracking process with circulation of hot, regenerated catalyst

A fluid catalytic cracking process for producing relatively low emissions fuels. The feedstock is relatively low in nitrogen and aromatics and high in hydrogen content and the catalyst is a mixture of zeolite-Y and ZSM-5, or an amorphous acid catalytic material with ZSM-5, or a combination of all three. The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.

FCC for producing low emission fuels from high hydrogen and low nitrogen

A fluid catalytic cracking process for producing relatively low emissions fuels. The feedstock is exceptionally low in nitrogen and aromatics and relatively high in hydrogen. The catalyst is an amorphous silica-alumina or a zeolitic material having a relatively small unit cell size. The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.

Fluid cracking process for producing low emissions fuels

Disclosed is a fluid catalytic cracking process for producing low emissions fuels. The feedstock is exceptionally low in nitrogen and aromatics and relatively high in hydrogen. The catalyst is a mixture of zeolite Y and zeolite beta (.beta.). The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.

Fluid catalytic cracking process for producing low emissions fuels

A fluid coking-gasification process for converting heavy hydrocarbonaceous chargestocks to lower boiling products in which an inorganic metal composition is used to mitigate slagging in the gasifier, wherein the metal is selected from the alkaline-earths, the rare earths, and zirconium. The inorganic metal composition is added either directly into the gasifier or it is mixed with the coke passing from the heating zone to the gasification zone.

Improved integrated coking-gasification process with mitigation of

Natural gas containing hydrogen sulfide is treated at well-head pressures by contact with a crystalline substituted or unsubstituted stannosilicate for removal of hydrogen sulfide.

Substituted stannosilicates, their preparation and use as natural gas

Highly crystalline stannosilicates are formed by reacting a tin salt with a source of silica and a hydroxide of a Group IA or Group IIA metal or an amine.

Stannosilicates and preparation thereof

Stannosilicates and preparation thereof (C-2417)

A catalyst is provided which comprises a crystalline zeolite, discrete particles of phosphorus containing alumina, particularly an alkaline earth metal phosphate containing alumina, dispersed in a non-zeolitic inorganic oxide matrix. A catalytic cracking process utilizing the catalyst is also provided. Such phosphate treated catalysts exhibit increased attrition resistance.

Cracking catalyst

A catalytic cracking process is provided wherein a phosphorous containing alumina or an alkaline earth phosphorous containing alumina is added to a catalytic cracking zone for admixture with a zeolite containing cracking catalyst.

Cracking process

Synthesis gas is produced by the reaction of light hydrocarbons, primarily methane, in a fluid bed reaction zone of attrition resistant nickel on alpha-alumina catalyst, with steam and oxygen and the conversion level is preserved by limiting the loss of nickel from the reaction and thereby limiting the back reaction of the synthesis gas to form methane in the presence of entrained catalyst in a cooling zone.

Synthesis gas preparation and catalyst therefor

A process for the use of such sorbent, or catalyst, to effectively remove sulfur from naphthas at temperatures above about 350.degree. F. without the significant production, if any, of PNA's. The invention embodies a particulate mass of a sorbent, or catalyst, comprised of nickel in concentration ranging from about 10 percent to about 70 percent, preferably from about 20 percent to about 50 percent, calculated as metallic nickel based on the total weight of the sorbent, iron in concentration ranging from about 1 percent to about 15 percent, preferably from about 2 percent to about 10 percent, calculated as metallic iron based on the total weight of the sorbent, or catalyst composition and a porous, refractory inorganic oxide such as silica, alumina, clays, or mixture thereof; preferably alumina, with which the nickel and iron are composited.

Desulfurization of hydrocarbons

A catalyst is provided which comprises a crystalline silica zeolite, a hydrogenation component and a support. The catalyst may be a physical mixture of the zeolite and the supported hydrogenation component or a composite catalyst. Hydrocarbon hydroprocessing processes such as hydroconversion and hydrodesulfurization utilizing the catalyst are also provided. The catalyst is particularly suited for the simultaneous pour point reduction and hydrodesulfurization of hydrocarbonaceous oils.

Crystalline silica zeolite-containing catalyst

A hydrodesulfurization process is provided in which a heavy hydrocarbonaceous feed comprising materials boiling above 1020.degree. F. is desulfurized at conditions to convert at least a portion of the 1020.degree. F..sup.+ materials, in the presence of hydrogen and a non-zeolitic hydrodesulfurization catalyst comprising a Group IIA metal component such as magnesia.

Hydrodesulfurization process with conversion of heavy hydrocarbons

A process wherein a regenerated, spent sulfided vanadium-containing Group VIII metal, Group VI-B metal, or Group VI-B/Group VIII metals containing catalyst is contacted with a stream of an oxygen-containing gas and the coke burned therefrom to regenerate the catalyst. The regenerated catalyst as such, or after reduction of the catalytic metals by contact with hydrogen, can be used as an adsorbent to remove essentially all of the sulfur from a naphtha feed which contains as much as 50 weight ppm sulfur, and greater.

Growing community of inventors

Baton Rouge, LA, United States of America

Paul E Eberly