Kenneth L. Riley
Engineering at Rodney Dr, Baton Rouge, LA

6620313, Sep 16, 2003

Aug 22, 2001

09/869986

Richard Alan Demmin - Highland Park NJ
Kenneth Lloyd Riley - Baton Rouge LA
Stuart Leon Soled - Pittstown NJ
Sabato Miseo - Pittstown NJ

ExxonMobil Research and Engineering Company - Annandale NJ

C10G 7306

208112, 208 33, 208 87, 208124, 208121, 208137, 208143, 208213, 208217, 208251 R, 208254 H

Hydroconversion process of petroleum and chemical feedstocks using bulk Group VIII/Group VIB catalysts. Preferred catalysts include those comprised of Ni—Mo—W.

5182248, Jan 26, 1993

May 10, 1991

7/699101

Ian A. Cody - Clearwater, CA
David H. Dumfries - Sarnia-Clearwater, CA
Arthur H. Neal - Baton Rouge LA
Kenneth L. Riley - Baton Rouge LA

Exxon Research and Engineering Company - Florham Park NJ

B01J 2104, B01J 2712, B01J 2713, B01J 27132

502230

A novel, high porosity, high surface area catalyst is disclosed which is useful in wax isomerization processes, especially for the production of high viscosity index, low pour point lubricating oil base stocks or blending stocks. The catalyst contains a catalytically active metal component selected from the group consisting of Group VIB and Group VIII metals, and mixtures thereof, preferably Group VIII metals, and mixtures thereof, more preferably noble Group VIII metals and mixtures thereof, most preferably platinum which catalytically active metal component is present in the range of about 0. 01 to 5. 0 wt. %, and a fluorine content in the range of about 0. 01 to about 10. The catalyst employs a refractory metal oxide support material, one preferably predominantly (i. e. , at least 50 wt. %) alumina, most preferably completely alumina, e. g.

5866739, Feb 2, 1999

Jul 29, 1997

8/902047

Stuart Leon Soled - Pittstown NJ
Jose Augusto da Costa Paes - Sao Paulo, BR
Antonio Gutierrez - Mercerville NJ
Sabato Miseo - Pittstown NJ
William E. Gates - Port Murray NJ
Kenneth L. Riley - Baton Rouge LA

Exxon Research and Engineering Company - Florham Park NJ

C07C 270

585467

The present invention relates to a catalyst composition, its methods of preparation and its use in aromatic alkylation processes. The composition comprises a heteropoly compound selected from the group consisting of heteropoly salts and heteropolyacid salts deposited in the interior of a porous support selected from the group consisting of silica, titania, and zirconia, wherein said salt of said heteropoly salt and said heteropolyacid salt is selected from the group consisting of ammonium, cesium, potassium, and rubidium salts and mixtures thereof, and wherein said heteropoly salt and said heteropolyacid salt are formed with a heteropolyacid selected from the group consisting of 12-tungstophosphoric, 12-tungstosilicic, 12-molybdophosphoric, and 12-molybdosilicic acid.

5258567, Nov 2, 1993

Aug 26, 1992

7/935503

Michael C. Kerby - Baton Rouge LA
Kenneth L. Riley - Baton Rouge LA
Fred M. Long - Baton Rouge LA
Jack W. Johnson - Clinton NJ
John F. Brody - Bound Brook NJ

Exxon Research and Engineering Company - Florham Park NJ

C07C 509, C07C 5333

585654

This invention relates to a process for the dehydrogenation of C. sub. 2 -C. sub. 10 hydrocarbons at dehydrogenation conditions with a pillared mica catalyst which contains an active metal selected from the group consisting of Pt, Cr and mixtures thereof, and a first modifier metal selected from the group consisting of Sn, Ga and mixtures thereof. The micas may also contain a second modifier metal selected from the group consisting of alkali metals, alkaline earth metals, and rare earth metals, and mixtures thereof.

5750819, May 12, 1998

Nov 5, 1996

8/740972

Robert J. Wittenbrink - Baton Rouge LA
Daniel F. Ryan - Baton Rouge LA
William C. Baird - Baton Rouge LA
Kenneth L. Riley - Baton Rouge LA
Jack W. Johnson - Clinton NJ

Exxon Research and Engineering Company - Florham Park NJ

C07C 513, B01J 2300

585734

Hydroconversion of paraffin containing hydrocarbon feeds is effected over a supported Group VIII and Group VI metal containing catalyst also containing a hydrocracking suppressant such as a Group IB metal, wherein the catalyst is preferably prepared by fixing the Group IB metal on to the support prior to incorporating the Group VI metal on to the support.

3974096, Aug 10, 1976

Nov 22, 1974

5/526306

Marnell A. Segura - Baton Rouge LA
Clyde L. Aldridge - Baton Rouge LA
Kenneth L. Riley - Baton Rouge LA
Lloyd A. Pine - Baton Rouge LA

Exxon Research and Engineering Company - Linden NJ

B01J 2704, B01J 2710

252439

Hydrogen is produced by reacting carbon monoxide with steam at a temperature of at least 200. degree. F. in the presence of a supported catalyst containing: (1) at least one alkali metal compound derived from an acid having an ionization constant below 1. times. 10. sup. sup. -3, (2) a metallic hydrogenation-dehydrogenation material, and (3) a halogen moiety. The ratio of metal component to alkali metal compound, each calculated on the basis of the oxide thereof, ranges from 0. 0001 to about 10 parts by weight per part by weight of the alkali metal compound. The halide constituent is present in amounts in excess of about 0. 01 weight %, based on total catalyst. A preferred catalyst composition comprises potassium carbonate, a mixture of cobalt and molybdenum oxides and combined chlorine contained on an alumina support.

7288182, Oct 30, 2007

Jan 14, 2000

09/869984

Stuart Leon Soled - Pittstown NJ, US
Sabato Miseo - Pittstown NJ, US
Roman Krycak - Annandale NJ, US
Hilda B. Vroman - Piscataway NJ, US
Teh Chung Ho - Bridgewater NJ, US
Kenneth Lloyd Riley - Baton Rouge LA, US

ExxonMobil Research and Engineering Company - Annandale NJ

C10G 73/02, C10G 11/00, B01J 29/70, B01J 23/00, B01J 23/70

208112, 208 28, 208 46, 208113, 208133, 208216 R, 208245 R, 502305, 502313, 502315, 502321, 502325, 502326, 502335, 502337

A process for hydroprocessing petroleum and chemical feedstocks by use of a bulk multimetallic catalyst comprised of at least one Group VIII non-noble metal and at least one, preferably two Group VIB metal wherein the ratio of Group VIB metal to Group VIII metal is from about 10:1 to 1:10.

5968465, Oct 19, 1999

Sep 19, 1997

8/929314

Russell J. Koveal - Baton Rouge LA
Kenneth L. Riley - Baton Rouge LA
Keith E. Corkern - Denham Springs LA

Exxon Research and Engineering Co. - Florham Park NJ

B01D 5354

423236

Hydrogen cyanide is removed from an HCN containing gas, e. g. , a gas containing CO+H. sub. 2, by contact with a metal oxide catalyst comprised of the oxides of molybdenum, titanium, and aluminum in the presence of water vapor, and subsequently water washing the resulting gas.

2002017, Dec 5, 2002

Jul 6, 2001

09/900068

Gerald Markley - Baton Rouge LA, US
Kenneth Riley - Baton Rouge LA, US
Ramesh Gupta - Berkeley Heights NJ, US

C10G065/02

208/210000, 208/21600R

A multi-stage process for removing heteroatoms particularly organic sulfur and nitrogen components, from liquid petroleum and chemical streams. The feedstream flows countercurrent to the flow of a hydrogen-containing treat gas and is reacted with a first catalyst which is relatively tolerant to sulfur and nitrogen, such as a CoMo supported catalyst. When the level of organic sulfur in the feedstream is less than about 3,000 wppm and the level of organic nitrogen is less than about 1,000 wppm, the feedstream is reacted with said counter flowing hydrogen-containing treat gas in the presence of a catalyst comprised of Ni and a Group VIA metal selected from Mo, W, or both, on a refractory support. The reaction vessel preferably contains vapor and optionally liquid by-pass means in one or more of the catalyst beds.

5474670, Dec 12, 1995

May 17, 1994

8/245181

Michel Daage - Baton Rouge LA
Teh C. Ho - Bridgewater NJ
Kenneth L. Riley - Baton Rouge LA

Exxon Research and Engineering Company - Florham Park NJ

C10G 4504, C10G 4508

208210

The present invention relates to a method of removing sulfur from a hydrotreating process stream comprising contacting a sulfur containing feedstock with a stacked bed catalyst system comprising a first catalyst bed comprising hydrodesulfurization catalysts followed by a second catalyst bed comprising ruthenium sulfide having a surface area of at least about 30 m. sup. 2 /g and wherein said hydrodesulfurization process is conducted at a temperature of about 150. degree. C. to about 400. degree. C. and a pressure of about 50 psig (344. 74 kPa) to about 2500 psig (17236. 89 kPa).