Exxonmobil Research and Engineering Company

Exxonmobil Chemical Patents Inc.

International Business Machines Corporation

Exxonmobil Technology and Engineering Company

Exxonmobile Research and Engineering Company

Stephen John McCarthy

Wenyih Frank Lai

Michel A Daage

Sylvain S Hantzer

Jean Willem Beeckman

Timothy Lee Hilbert

Paul Podsiadlo

Chuansheng Bai

Ajit Bhaskar Dandekar

Stuart S Shih

Lei Zhang

Mohsen N Harandi

Stephen Harold Brown

James C Vartuli

Doron Levin

Christine Nicole Elia

Shifang Luke Luo

Preeti Kamakoti

John Scott Buchanan

Samuel A Tabak

David Lawrence Stern

Ian A Cody

Simon Christopher Weston

Ivy Dawn Johnson

David L Johnson

William Ernest Lewis

David Charles Calabro

Mobae Afeworki

Jeevan Sahib Abichandani

Quanchang Li

Michael F Raterman

Xiaochun Xu

Matu J Shah

Stuart Leon Soled

Frank Hershkowitz

Paul F Keusenkothen

Thomas F Degnan

Machteld Maria Mertens

Terry Eugene Helton

Scott Jeffrey Weigel

Jeffrey S Beck

Jane C Cheng

Teh Chung Ho

Daniel Mark Giaquinta

Dominick N Mazzone

Valery Sokolovskii

Daria N Lissy

William A Wachter

David M Lowe

Alfred Hagemeyer

Rohit Vijay

Gary Paul Schleicher

Brett Thomas Loveless

William Joseph Novak

William G Borghard

Christopher Gordon Oliveri

Krista Marie Prentice

Matthew Scott Ide

Robert Ellis Kay

Bradley R Fingland

Mayank Shekhar

Samia Ilias

Kiara M Benitez

Mohan Kalyanaraman

Lorenzo C DeCaul

Richard Charles Dougherty

Brandon J O'Neill

Lu Han

Eric B Shen

Bing Du

Clay R Sutton

Glenn R Sweeten

Mitch L Hindman

David A Griffin

Steven E Silverberg

John Slocum Coleman

Tilman W Beutel

Benjamin S Umansky

Anthony F Volpe

Michael B Carroll

Vijay Swarup

Helge Jaensch

Kuangnan Qian

Darryl Donald Lacy

Robert Andrew Migliorini

John D Ou

Marc H Anthonis

Nikolaos Soultanidis

Eric D Joseck

Tracie L Owens

Suriyanarayanan Rajagopalan

Jason Wu

Jeffrey T Elks

Hyung Suk Woo

Mark A Deimund

El-Mekki El-Malki

William J Tracy, Iii

Carlos N Lopez

Sina Sartipi

Martine Dictus

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 forming noble metal catalysts comprising both platinum and a second Group VIII metal, such as palladium, with improved aromatic saturation activity. Instead of impregnating a catalyst with both platinum and another Group VIII metal at the same time, a sequential impregnation can be used, with the Group VIII metal being impregnated prior to platinum. It has been discovered that by forming a Group VIII metal-impregnated catalyst first, and then impregnating with platinum, the distribution of platinum throughout the catalyst can be improved. The improved distribution of platinum can result in a catalyst with enhanced aromatic saturation activity relative to a catalyst with a similar composition formed by simultaneous impregnation.

Sequential impregnation for noble metal alloy formation

Methods, catalysts, and corresponding catalyst precursors are provided for performing dewaxing of diesel or distillate boiling range fractions. The dewaxing methods, catalysts, and/or catalyst precursors can allow for production of diesel boiling range fuels with improved cold flow properties at desirable yields. The catalysts and/or catalyst precursors can correspond to supported metal catalysts and/or catalyst precursors that include at least one noble metal, such as Pt, at least one Group 8-10 base metal, preferably a non-noble Group 8-10 base metal, such as Ni and/or Co along with a Group 6 metal, such as Mo and/or W as supported metals along. The support can include a zeolitic framework structure. The catalyst precursors can be formed, for example, by impregnating a support including a zeolitic framework structure with impregnation solution(s) that also includes a dispersion agent.

Noble metal and base metal dewaxing catalyst

Methods are provided for making base metal catalysts with improved activity. After forming catalyst particles based on a support comprising a zeolitic molecular sieve, the catalyst particles can be impregnated with a solution comprising a) metal salts (or other precursors) for a plurality of base metals and b) an organic dispersion agent comprising 2 to 10 carbons. The impregnated support particles can be dried to form a base metal catalyst, and then optionally sulfided to form a sulfided base metal catalyst. The resulting (sulfided) base metal catalyst can have improved activity for cloud point reduction and/or for improved activity for heteroatom removal, relative to a base metal dewaxing catalyst prepared without the use of a dispersion agent.

Base metal dewaxing catalyst

Methods for regenerating and/or rejuvenating catalysts, particularly dewaxing catalysts, as well as methods for performing dewaxing of diesel or distillate boiling range feeds with the regenerated and/or rejuvenated catalyst are provided herein. The regeneration and/or rejuvenation methods can include calcining spent catalyst followed by contacting the calcined catalyst with a solution comprising a complexing agent, which can restore hydrotreatment (HDT) activity and dewaxing activity of the spent catalyst such that it may be reused during hydroprocessing.

Methods for regenerating and rejuvenating catalysts

Hydrogenation catalysts for aromatic hydrogenation including an organosilica material support, which is a polymer comprising independent units of a monomer of Formula [ZOZOSiCH](I), wherein each Zand Zindependently represent a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer; and at least one catalyst metal are provided herein. Methods of making the hydrogenation catalysts and processes of using, e.g., aromatic hydrogenation, the hydrogenation catalyst are also provided herein.

Aromatic hydrogenation catalysts and uses thereof

Methods, catalysts, and corresponding catalyst precursors are provided for performing dewaxing of diesel or distillate boiling range fractions. The dewaxing methods, catalysts, and/or catalyst precursors can allow for production of diesel boiling range fuels with improved cold flow properties at desirable yields. The catalysts and/or catalyst precursors can correspond to supported base metal catalysts and/or catalyst precursors that include at least two Group 8-10 base metals supported on the catalyst, such as a catalyst/catalyst precursor including both Ni and Co as supported metals along with a Group 6 metal (i.e., Mo and/or W). The support can correspond to a support including a zeolitic framework structure. The catalyst precursors can be formed, for example, by impregnating a support including a zeolitic framework structure with an impregnation solution that also includes a dispersion agent.

Trimetallic base metal dewaxing catalyst

Systems and methods are provided for integration of an oxygenate conversion process with an olefin oligomerization process. The integrated process can produce gasoline of a desired octane and/or distillate fuel of a desired cetane.

Integrated oxygenate conversion and olefin oligomerization

Systems and methods are provided for activation of noble metal catalysts that are supported on siliceous supports. The activation method can include limiting the amount of water vapor pressure and/or the time of exposure to the water vapor pressure during heating of the catalyst at temperatures of 50&#xb0; C. or less. This can be achieved by introducing heated gas into multiple reactors of a multi-reactor system at the same time. A suitable system for introducing heated gas into multiple reactors can correspond to a system with multiple heated hydrogen lines for delivery of heated hydrogen to a plurality of reactors within a multi-reactor system.

Activation of noble metal catalysts on siliceous supports

Systems and methods are provided for modifying the composition of the conversion catalyst in a reactor for oxygenate conversion during conversion of an oxygenate feed to allow for adjustment of the slate of conversion products. The modification of the conversion catalyst can be performed by introducing a substantial portion (relative to the amount of catalyst inventory in the reaction system) of make-up catalyst having a distinct composition relative to the conversion catalyst in the reaction system. Introducing the distinct composition of make-up catalyst can modify the composition of the conversion catalyst in the reactor to allow for changes in the resulting product slate. By introducing the distinct catalyst composition, the conversion catalyst in the reactor can correspond to a different composition of catalyst than the overall average catalyst composition within the catalyst inventory in the reaction system.

Conversion of oxygenates to hydrocarbons with variable catalyst composition

Apparatuses and processes for converting an oxygenate feedstock, such as methanol and/or dimethyl ether, in a fluidized bed containing a catalyst to hydrocarbons, such as gasoline boiling components, olefins and aromatics are provided herein.

Apparatus and process for producing gasoline, olefins and aromatics from oxygenates

Catalyst compositions including a zeolite having a molar ratio of silicon to aluminum of about 10.0 to about 300.0; a Group 10-12 element and combinations thereof; a Group 15 element and combinations thereof; and optionally, a binder, wherein the catalyst composition has a molar ratio of Group 15 element to Group 10-12 element of about 0.01 to about 10.0 are disclosed. Methods of converting organic compounds to aromatics using such catalyst compositions are also disclosed.

Catalyst for conversion of oxygenates to aromatics

A catalyst composition includes a zeolite, a binder, and a Group 12 transition metal selected from the group consisting of Zn, Cd, or a combination thereof, the zeolite having a silicon to aluminum ratio of at least about 10, the catalyst composition comprising about 50 wt % or less of the binder based on a total weight of the catalyst composition, the catalyst composition having a micropore surface area of at least about 340 m/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of (a) a mesoporosity of greater than about 20 m/g; (b) a diffusivity for 2,2-dimethylbutane of greater than about 1&#xd7;10secwhen measured at a temperature of about 120&#xb0; C. and a 2,2-dimethylbutane pressure of about 60 torr (about 8 kPa).

Bound catalyst for selective conversion of oxygenates to aromatics

A catalyst composition comprising a zeolite, an alumina binder, and a Group 12 transition metal selected from Zn and/or Cd, the zeolite having a Si/Al ratio of at least about 10 and a micropore surface area of at least about 340 m/g, the catalyst composition comprising about 50 wt % or less of the binder, based on a total weight of the catalyst composition, and having a micropore surface area of at least about 290 m/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: a mesoporosity of about 20 m/g to about 120 m/g; a diffusivity for 2,2-dimethylbutane of greater than about 1&#xd7;10secwhen measured at a temperature of about 120&#xb0; C. and a 2,2-dimethylbutane pressure of about 60 torr (8 kPa); and a combined micropore surface area and mesoporosity of at least about 380 m/g.

Alumina bound catalyst for selective conversion of oxygenates to aromatics

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Center Valley, PA, United States of America

Stephen John McCarthy