Exxonmobil Research and Engineering Company

Air Products and Chemicals, Inc.

Exxonmobil Chemical Patents Inc.

Exxonmobil Technology and Engineering Company

Applied Materials, Inc.

Other

Georgia Tech Research Corporation

Exxonmobil Upstream Research Company

Exxonmobile Research and Engineering Company

Exxonmobil Engineering & Technology Company

Exxonmobil Research and Engineering

Toyota Central Research and Development Labs, Inc.

Versum Materials US, LLC

Scott Jeffrey Weigel

James Edward MacDougall

Darryl Donald Lacy

Karl Gottlieb Strohmaier

Doron Levin

Paul Podsiadlo

John F Kirner

Brian Michael Weiss

Allen Wayne Burton

Alexandros T Demos

Timothy Weidman

Robert Parkash Mandal

Martin Devenney

Michael Salciccioli

Nikolaos Bekiaris

Brian Keith Peterson

Konstantinos Chondroudis

Michael P Nault

Jihad Mohammed Dakka

Wenyih Frank Lai

Simon Christopher Weston

Lei Zhang

David Charles Calabro

Walter Weissman

Quanchang Li

Xiaochun Xu

Michel Molinier

Preeti Kamakoti

John Frances Brody

Tilman W Beutel

Helge Jaensch

Marc H Anthonis

Brett Thomas Loveless

Joseph E Gatt

Mark Leonard O'Neill

Ivy Dawn Johnson

Chuansheng Bai

Christine Nicole Elia

Ajit Bhaskar Dandekar

Charles G Coe

Randall David Partridge

Hari Nair

Matthew Scott Ide

Himanshu Gupta

Eugine Choi

Brandon J O'Neill

Brita Engels

Thomas Albert Braymer

Terry Eugene Helton

Raymond Nicholas Vrtis

Ramesh Gupta

Narasimhan Sundaram

Mobae Afeworki

Neeraj Sangar

Hans Thomann

Franklin F Mittricker

Bal K Kaul

Loren K Starcher

Lorenzo C DeCaul

Bradley R Fingland

Yunfeng Lu

Machteld M W Mertens

James William Gleeson

Christopher Gordon Oliveri

Jeffrey Richard Brzozowski

Harry William Deckman

Manchao Xiao

Kun Wang

Michel A Daage

Daniel Paul Leta

Stephen John McCarthy

Guang Cao

Shifang Luke Luo

Jean Willem Beeckman

Johan Adriaan Martens

Bing Han

Thomas R Gaffney

Peter I Ravikovitch

Jean Louise Vincent

Joseph M Falkowski

Steven Gerard Mayorga

Aiping Wu

Kendall S Fruchey

Sumathy Raman

Robert Ellis Kay

Mayank Shekhar

Rohit Vijay

Hansong Cheng

Xinrui Yu

Michael P Lanci

Javier Guzman

Nikolaos Soultanidis

John Giles Langan

Laura M Matz

Samia Ilias

Jason Wu

Todd E Detjen

Pierre A Jacobs

Changyub Paek

Barbara Carstensen

An isomerization catalyst is provided, along with corresponding systems and methods, which provides improved isomerization for bio-derived feeds in reaction environments where by-products from deoxygenation are present. The catalyst provides unexpectedly increased activity and/or selectivity in situations where, for example, a deoxygenation effluent is cascaded to the isomerization catalyst. Additionally, the isomerization catalyst can assist with reducing or minimizing hydrogen consumption during isomerization. The increased activity, stability, and/or reduced hydrogen consumption is achieved in part based on using a dispersion agent when adding base metals to the catalyst. In addition to the base metals, the catalyst includes a zeolitic framework structure suitable for isomerization.

Isomerization of biofeeds over base metal catalysts

Systems and methods are provided for reducing hydrogen consumption during deoxygenation of bio-derived (or at least partially bio-derived) feedstocks. The reduced hydrogen consumption is achieved by performing the deoxygenation in the presence of a bulk multimetallic catalyst and/or in the presence of a base metal dewaxing catalyst having reduced metal stack heights. Additionally, due in part to being able to reduce or minimize hydrogen consumption, the heat release during deoxygenation can also be reduced, thus allowing a smaller catalyst volume to perform deoxygenation.

Reduced H2 consumption during deoxygenation

A catalyst may include a metallic function derived from a metal constrained within cages and/or channels of a microporous material, wherein the cages and/or channels of the microporous material are defined by 8 tetrahedral atoms or fewer; and an acidic function derived from an additional zeolite having cages and/or channels defined by 10 or more tetrahedral atoms, wherein the microporous material providing the metallic function and additional zeolite providing the acidic function are coupled by a binder.

Conversion of heavy aromatics to lighter aromatics with low ring saturation and hydrocarbon cracking

The present disclosure provides mesoporous catalyst compounds and compositions having one or more group 13 atoms. The present disclosure further relates to processes for converting hydrocarbon feedstocks to small olefins. In one aspect, a catalyst compound includes a zeolite having a structural type selected from MFI, MSE, MTW, Theta-One (TON), Ferrierite (FER), AFI, AFS, ATO, BEA, BEC, BOG, BPH, CAN, CON, EMT, EON, EZT, FAU, GME, GON, IFR, ISV, ITN, IWR, IWW, LTL, MAZ, MEI, MOR, MOZ, OFF, OKO, OSI, SAF, SAO, SEW, SFE, SFO, SSF, SSY, and USI, or a combination thereof, the zeolite having a silicon to aluminum molar ratio (Si/Al ratio) of from about 5 to about 40. In one aspect, a catalyst composition includes the catalyst compound and one or more group 13 metal.

Mesoporous catalyst compounds and uses thereof

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

Catalyst composition which comprises a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m/g is disclosed. These catalyst compositions are used to remove catalyst poisons from untreated feed streams having one or more impurities which cause deactivation of the downstream catalysts employed in hydrocarbon conversion processes, such as those that produce mono-alkylated aromatic compounds.

Catalyst compositions and their use in aromatic alkylation processes

Provided herein are methods and systems of making a high quality isoparaffinic base stock which include contacting an adsorbent material with a hydrocarbon feedstock and a solvent and separating at least some of the one or more high VI components from the hydrocarbon feedstock to produce a first fraction base stock having a first fraction base stock viscosity index. The adsorbent material is desorbed with a second solvent to produce a second fraction base stock having a second fraction base stock viscosity index. In these methods, the first fraction base stock viscosity index is less than the hydrocarbon feedstock viscosity index and the second fraction base stock viscosity index is greater than the hydrocarbon feedstock viscosity index.

Adsorptive process for separation of isoparaffinic lube base stock from lower quality oils

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 hydrocarbon feed stream, particularly one comprising heavier hydrocarbons, may be converted to valuable products such as motor gasoline and/or lubricating oil by employing one or more MOF catalysts, which may be prepared from a precursor metal-organic framework (MOF). A MOF catalyst may be prepared by exchanging one or more organic linking ligands of the precursor MOF for an organic linking ligand having a different acidity and/or electron-withdrawing properties, which, in turn, may affect catalytic activity.

Metal-organic framework catalysts and their use thereof in catalytic cracking

Methods are provided for formulation of catalysts with improved catalyst exposure lifetimes under oxygenate conversion conditions. In various additional aspects, methods are described for performing oxygenate conversion reactions using such catalysts with improved catalyst exposure lifetimes. The catalyst formulation methods can include formulation of oxygenate conversion catalysts with binders that are selected from binders having a surface area of roughly 250 m/g or less, or 200 m/g or less. In various aspects, during formulation, a weak base can be added to the zeotype crystals, to the binder material, or to the mixture of the zeotype and the binder. It has been unexpectedly discovered that addition of a weak base, so that the weak base is present in at least one component of the binder mixture prior to formulation, can result in longer catalyst exposure lifetimes under methanol conversion conditions.

Catalyst formulation for methanol conversion catalysts

Methods are provided for using a molecular sieve catalyst for dewaxing formed using a synthesis mixture comprising a morphology modifier. The catalyst may be used, for example, for production of a lubricant base stock. For example, ZSM-48 crystals formed using the morphology modifier (and/or formulated catalysts made using such crystals) can have an increased activity and/or can provide an improved yield during catalytic dewaxing of lubricant base stocks.

Dewaxing using a molecular sieve catalyst

Methods are provided for activation of catalysts comprising low amounts of a hydrogenation metal, such as low amounts of a Group 8-10 noble metal. The amount of hydrogenation metal on the catalyst can correspond to 0.5 wt % or less (with respect to the weight of the catalyst), or 0.1 wt % or less, or 0.05 wt % or less. Prior to loading a catalyst into a reactor, the corresponding catalyst precursor can be first activated in a hydrogen-containing atmosphere containing 1.0 vppm of CO or less. The thus first-activated catalyst can be transferred to a reactor with optional exposure to oxygen during the transfer, where it can be further activated using a hydrogen-containing atmosphere containing 3.0 vppm of CO or higher, to yield a twice-activated catalyst with high performance. The catalyst can be advantageously a transalkylation catalyst or an isomerization catalyst useful for converting aromatic hydrocarbons.

Activation of low metal content catalyst

Disclosed are processes and systems for the removal of water from a feed stream utilizing swing adsorption processes including an adsorbent bed comprising an adsorbent material which is a cationic zeolite RHO. The cationic zeolite RHO comprises at least one, preferably two, metal cations selected from Group 1 and 2 elements (new Group 1-18 IUPAC numbering). The swing adsorption processes and systems utilizing the cationic zeolite RHO have an adsorption selectivity for water and are useful in selective dehydration of commercial feed streams. The cationic zeolite RHO additionally has an exceptionally high water adsorption stability for use in feed streams with wet acid gas environments operating under cyclic swing adsorption conditions.

Dehydration processes utilizing cationic zeolite RHO

A process and related system for producing para-xylene (PX). In an embodiment, the process includes (a) separating a feed stream comprising Caromatic hydrocarbons into a toluene containing stream and a Chydrocarbon containing stream and (b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit to convert toluene to xylenes and produce a methylated effluent stream. In addition, the process includes (c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream and (d) transalkylating the PX depleted stream to produce a transalkylation effluent stream. The transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream. Further, the process includes (e) converting at least some ethylbenzene (EB) within the Chydrocarbon containing stream into toluene and (f) flowing the toluene converted in (e) to the contacting in (b).

Xylene production processes and systems

Growing community of inventors

Allentown, PA, United States of America

Scott Jeffrey Weigel