Exxonmobil Chemical Patents Inc.

Exxonmobil Research and Engineering Company

Exxonmobil Technology and Engineering Company

Exxon Chemical Patents, Inc.

Exxon Research and Engineering Company

Air Company Holdings, Inc.

Jihad Mohammed Dakka

Edmund John Mozeleski

Stephen Zushma

John Scott Buchanan

Christopher Lynn Becker

Francisco Manuel Benitez

Kun Wang

James Richardson Lattner

Terry Eugene Helton

Tan-Jen Chen

Chuansheng Bai

Keith Holroyd Kuechler

Jon E Stanat

Allen David Godwin

James C Vartuli

Gary David Mohr

Lisa Saunders Baugh

Teng Xu

Jane C Cheng

Charles Morris Smith

Stephen Harold Brown

Larry Lee Iaccino

Guang Cao

Jose G Santiesteban

Doron Levin

Catherine Anne Faler

Scott Jeffrey Weigel

Christine Nicole Elia

Sabato Miseo

Robert G Tinger

Shifang Luke Luo

Patrick Loring Hanks

Karla Schall Colle

Machteld Maria Mertens

Lei Zhang

Bruce R Cook

Mark Paul Hagemeister

Jeevan Sahib Abichandani

Matthew William Holtcamp

Stuart Leon Soled

Michel A Daage

Gabor Kiss

Ivy Dawn Johnson

Ajit Bhaskar Dandekar

Lorenzo C DeCaul

Jason D Davis

Kirk C Nadler

Michael Salciccioli

Georges M K Mathys

Victor DeFlorio

Christine A Costello

Xiaobing Feng

Hans K T Goris

Neeraj Sangar

Preeti Kamakoti

Bryan A Patel

Anita S Lee

Robert A Crane

Anjaneya Sarma Kovvali

Matthew Scott Ide

Didier A Naert

Michael P Lanci

Jörg F W Weber

Wilfried Jozef Mortier

Hari Nair

Brenda Anne Raich

Georges Marie Mathys

Michael W Weber

Roberto Garcia

Jose M Vargas

Seth McConkie Washburn

Lubo Zhou

Nicolas P Coute

Mobae Afeworki

Raphael Frans Caers

Johan Adriaan Martens

Enock Berluche

Enrique Iglesia

Joseph Ernest Baumgartner

Daria N Lissy

Xiaochun Xu

Steven E Silverberg

Alan Anthony Galuska

James Peter Stokes

Sebastian Carmen Reyes

Suzzy C Ho

Christine Esther Kliewer

Himanshu Gupta

Helge Jaensch

John Stephen Godsmark

James Ronald Bielenberg

Sumathy Raman

Arsam Behkish

Brian Michael Weiss

Arun K Sharma

Xinrui Yu

J Scott Buchanan

Thomas Marshall Larson

Ulrich Kortz

Stafford Wheeler Sheehan

Systems and methods are provided for increasing the yield of products generated during co-processing of biomass oil in a fluid catalytic cracking (FCC) system. The systems and methods can allow for increased yield by reducing or minimizing formation of carbon oxides, gas phase products, and/or coke yields during the co-processing. This can be achieved by adding a hydrogen-rich co-feed to the co-processing environment. Examples of hydrogen-rich co-feeds include high hydrogen content vacuum gas oil co-feed, high hydrogen content distillate co-feed, and/or high hydrogen content naphtha co-feed. Additionally or alternately, various types of fractions that contain a sufficient amount of hydrogen donor compounds can be used to reduce or minimize carbon oxide formation.

FCC co-processing of biomass oil with hydrogen rich co-feed

Isomerization of normal paraffins to form branched paraffins may be complicated by significant cracking of Cparaffins under isomerization reaction conditions. This issue may complicate upgrading of hydrocarbon feeds having significant quantities of heavier normal paraffins. Cracking selectivity may be decreased by combining one or more naphthenic compounds with a feed mixture comprising at least one Cnormal paraffin and/or by utilizing tungstated zirconium catalysts having decreased tungsten loading. Further, Cand Cnormal paraffins may undergo isomerization in the presence of Cnormal paraffins. Methods for isomerizing normal paraffins may comprise: providing a feed mixture comprising at least C-Cnormal paraffins and lacking normal paraffins larger than C; and contacting the feed mixture with a bifunctional mixed metal oxide catalyst under isomerization reaction conditions effective to form a product mixture comprising one or more branched paraffins formed from each of the C-Cnormal paraffins.

Isomerization of normal paraffins

Provided herein are systems and methods for converting COand a reduction gas such as Hor a hydrocarbon to mixtures of paraffins and aromatics suitable for use as aviation fuel.

Synthetic fuels, and methods and apparatus for production thereof

A method of producing bifunctional catalysts by extrusion may include mixing an acid catalyst, a metal catalyst, optionally a binder, and a fluid to produce a dough; extruding the dough to form an extrudate; producing a powder from the extrudate; and calcining the powder to produce an acid/metal bifunctional catalyst. Such acid/metal bifunctional catalysts may be useful in, among other things, converting syngas to dimethyl ether in a single reactor.

Acid/metal bifunctional catalyst produced by extrusion

Hydroxycarboxylic acids may be biosynthesized from a carbonaceous feedstock and then isolated through forming and subsequently hydrolyzing an intermediate sophorolipid. After biosynthesizing a hydroxycarboxylic acid in a cell culture medium or otherwise providing a hydroxycarboxylic acid in a first aqueous medium, the hydroxycarboxylic acid and glucose may be converted into at least one sophorolipid by a suitable microorganism or an enzyme cocktail. The at least one sophorolipid may be then be separated from the cell culture medium or first aqueous medium and then hydrolyzed in a second aqueous medium to form the hydroxycarboxylic acid and glucose as free components separate from the cell culture medium or first aqueous medium. The hydroxycarboxylic acid is present as a phase separate from the second aqueous medium and the glucose remains in the second aqueous medium.

Formation and isolation of hydroxycarboxylic acids via a sophorolipid intermediate

Tungstated zirconium catalysts for paraffin isomerization may comprise: a mixed metal oxide that is at least partially crystalline and comprises tungsten, zirconium, and a variable oxidation state metal selected from Fe, Mn, Co, Cu, Ce, Ni, and any combination thereof. The mixed metal oxide comprises about 5 wt. % to about 25 wt. % tungsten, about 40 wt. % to about 70 wt. % zirconium, and about 0.01 wt. % to about 5 wt. % variable oxidation state metal, each based on a total mass of the mixed metal oxide. The mixed metal oxide has a total surface area of about 50 m/g or greater as measured according to ISO 9277, and at least one of the following: an ammonia uptake of about 0.05 to about 0.3 mmol/g as measured by temperature programmed adsorption/desorption, or a collidine uptake of about 100 &#x3bc;mol/g or greater as measured gravimetrically.

Bifunctional metal oxides and paraffin isomerization therewith

A method of producing bifunctional catalyst systems that include a carbon-coated metal catalyst may comprise: coating a metal catalyst particle with a carbon-containing small molecule to produce a coated metal catalyst particle; carbonizing the carbon-containing small molecule on the coated metal catalyst particle to produce a carbon-coated metal catalyst particle; and mixing the carbon-coated metal catalyst particle with an acid catalyst particle to produce an acid/metal bifunctional catalyst system. Further, a method of producing bifunctional catalyst systems that include a carbon-coated acid catalyst may be similarly performed by coating a metal catalyst particle with a carbon-containing small molecule to produce a coated metal catalyst particle; carbonizing the carbon-containing small molecule on the coated metal catalyst particle to produce a carbon-coated metal catalyst particle; and mixing the carbon-coated metal catalyst particle with an acid catalyst particle to produce an acid/metal bifunctional catalyst system.

Acid/metal bifunctional catalyst systems produced with carbon coatings

Methods of producing metal catalysts can include mixing two or more metal salts and an aluminum salt in water to produce a metal catalyst precursor solution; mixing the metal catalyst precursor solution and an alkali metal buffer solution to produce a precipitate; ion exchanging the alkali metal in the precipitate for a non-alkali cation to produce a low-alkali metal precipitate comprising 3 wt % or less alkali metal by weight of the precipitate on a dry basis; producing a powder from the low-alkali metal precipitate; and calcining the powder to produce a metal catalyst. Such metal catalysts may be useful in producing bifunctional catalyst systems that are useful in, among other things, converting syngas to dimethyl ether in a single reactor.

Metal catalysts with low-alkali metal content and acid/metal bifunctional catalyst systems thereof

A method of producing a acid/metal bifunctional catalyst may include: mixing an acid catalyst, a metal catalyst, and a fluid to produce a slurry, wherein the acid catalyst is present at 50 wt % or less relative to a total catalyst weight in the slurry; heating the slurry; producing a powder from the slurry; and calcining the powder to produce the acid/metal bifunctional catalyst. Such acid/metal bifunctional catalyst would be useful in the direct conversion of syngas to dimethyl ether as well as other reactions.

Acid/metal bifunctional catalysts produced by slurry methods

Provided herein are methods for hydroisomerization of a hydrocarbon feedstock comprising contacting the hydrocarbon feedstock with hydrogen and a catalyst to yield a hydrocarbon product having an increase in branched hydrocarbons relative to the hydrocarbon feedstock. The present catalysts comprise a heteroatom-doped Beta zeolite having a trivalent cation as a framework metal oxide, an extra-framework species comprised of cerium and/or cobalt, and from 0.01 to 1.5 wt. % of a group VIII or VIB metal, or a combination thereof.

Heteroatom-doped zeolites for bifunctional catalytic applications

Isobutanol may be converted into predominantly Colefin oligomers under specified conditions. Such methods may comprise: contacting a feed comprising isobutanol with a zeolite solid acid catalyst having a MWW framework under conditions effective to convert the isobutanol into a product comprising Colefin oligomers, wherein n is an integer having a value of two or greater and about 80 wt. % or greater of the Colefin oligomers are larger than C.

Oligomerization of isobutanol in the presence of MWW zeolite solid acid catalysts

The application relates to processes and systems that use a furfural compound for producing five-membered carbocyclic rings that are unsaturated, such as cyclopentene and cyclopentadiene. Examples methods for conversion of furfural compounds may include converting a furfural compound to at least a five-membered, saturated carbocyclic ring, and converting the five-membered, saturated carbocyclic ring in a presence of a catalyst to at least a five-membered, unsaturated carbocyclic ring.

Production of cyclopentadiene from furfural

In a process for producing a methyl-substituted biphenyl compound, at least one methyl-substituted cyclohexylbenzene compound of the formula: wherein each of m and n is independently 1, 2, or 3, is contacted with hydrogen in the presence of a hydrogenation catalyst to produce a hydrogenation reaction product comprising at least one methyl-substituted bicyclohexane compound, and the methyl-substituted bicyclohexane compound is then contacted with a dehydrogenation catalyst to produce a dehydrogenation reaction product comprising at least one methyl-substituted biphenyl compound.

Production of methyl-substituted biphenyl compounds

A method for producing a metal nitride and/or a metal carbide, a metal nitride and/or metal carbide optionally produced according to the method, and the use of the metal nitride and/or carbide in catalysis optionally catalytic hydroprocessing. Optionally, the method comprises: i) contacting at least one metal oxide comprising at least one first metal Mwith a cyanometallate comprising at least one second metal Mto form a reaction mixture; and, ii) subjecting the reaction mixture to a temperature of at least 300&#xb0; C. for a reaction period. Optionally, the metal nitride and/or metal carbide is a metal nitride comprising tungsten nitride.

Method for producing metal nitrides and metal carbides

Systems and methods are provided for conversion of gas phase reactants including CO and Hto Cproducts using multiple catalysts in a single reactor while reducing or minimizing deactivation of the catalysts. Separate catalysts can be used that correspond to a first catalyst, such as a catalyst for synthesis of methanol from synthesis gas, and a second catalyst, such as a catalyst for conversion of methanol to a desired Cproduct. The separate catalysts can be loaded into the reactor in distinct layers that are separated by spacer layers. The spacer layers can correspond to relatively inert particles, such as silica particles. Optionally, the spacer layer can include an adsorbent, such as boron supported on alumina or boron carbide particles. The adsorbent can be suitable for selective adsorption of the one or more reaction products (such as one or more reaction by-products), to allow for further reduction or minimization of the deactivation of the conversion catalysts.

Layered catalyst loading for synthesis gas conversion

Growing community of inventors

Whitehouse Station, NJ, United States of America

Jihad Mohammed Dakka