Exxonmobil Research and Engineering Company

Exxonmobil Chemical Patents Inc.

Exxonmobil Oil Corporation

Exxonmobil Technology and Engineering Company

Exxonmobile Research and Engineering Company

Exxonmobil Research and Engineering

Exxon Mobil Chemical, Inc.

Ajit Bhaskar Dandekar

John P McWilliams

Michel A Daage

Bradley R Fingland

Thomas F Degnan

David Lawrence Stern

Wenyih Frank Lai

Stephen John McCarthy

Michael C Clark

Richard F Socha

Michael B Carroll

Rohit Vijay

Wieslaw J Roth

Christine Nicole Elia

Timothy Lee Hilbert

Donald J Klocke

Kendall S Fruchey

Brandon J O'Neill

Jeffrey S Beck

Lei Zhang

Charles Lambert Baker, Jr

Anjaneya Sarma Kovvali

Chaya R Venkat

Benjamin S Umansky

Keith K Aldous

Mohsen N Harandi

James Richardson Lattner

Jihad Mohammed Dakka

Stephen Harold Brown

Scott Jeffrey Weigel

Jane C Cheng

Jose G Santiesteban

Doron Levin

Ivy Dawn Johnson

Charles Morris Smith

William Ernest Lewis

Krista Marie Prentice

Richard L Eckes

S Beau Waldrup

Tracie L Owens

Eric B Senzer

Sara L Yohe

Sara K Green

Lisa I-Ching Yeh

Eric D Joseck

Ronald M Gould

William G Borghard

Jason Wu

Charles L Baker

Michael Hryniszak

Christopher Gordon Oliveri

April D Ross

Mark A Deimund

Jason M McMullan

Steven Pyl

Michael Alan Steckel

Michael Alan Better

Thomas Francis Degnan, Jr

Hye Kyung Cho Timken

Patrick Loring Hanks

Randall David Partridge

William Alois Weber

Kathleen M Keville

Mohan Kalyanaraman

Gary Paul Schleicher

Randolph John Smiley

William Joseph Novak

Benjamin A McCool

Himanshu Gupta

Frank C Wang

Robert Ellis Kay

Darryl Donald Lacy

Rustom Merwan Billimoria

Jane Chi-Ya Cheng

C Morris Smith

Bryan E Hagee

Eugenio Sanchez

Gregory J DeMartin

John Stephen Szobota

Glenn C Wood

Tahmid I Mizan

Ramanathan Sundararaman

Shamel Merchant

Rugved P Pathare

Teck-Mui Hoo

David Mentzer

Jianxin Jason Wu

Madhav Acharya

Camden N Henderson

Matthew S Mettler

Jocelyn A Kowalski

Joshua W Allen

Darden Sinclair

Cynthia F Omilian

Herbert W Barry

Wei-Ping Tai

Jon M McConnachie

Cathleen Yung

José Guadalupe Santiesteban

Systems and methods are provided for conversion of a combined feed of oxygenates (such as methanol or dimethyl ether) and olefins to a high octane naphtha boiling range product with a reduced or minimized aromatics content. The oxygenate conversion can be performed under conditions that reduce or minimize hydrogen transfer. Optionally, a catalyst that further facilitates formation of branched paraffins can be used, such as a catalyst that has some type of 12-member ring site available on the catalyst surface.

Olefin methylation for production of low aromatic gasoline

Systems and methods are provided for conversion of oxygenate feeds to lubricant and/or distillate boiling range compounds with desirable properties by first selectively converting oxygenates to light olefins and then converting the light olefins to distillate and lubricant boiling range compounds with beneficial properties. The distillate boiling range products can have an unexpectedly high cetane, while the lubricant boiling range products can have an unexpectedly high viscosity index. The ability to form the distillate boiling range products and lubricant boiling range products is facilitated by using a Ni-enhanced oligomerization catalyst.

Oligomerization of olefins derived from oxygenates

Systems and methods are provided for integration of use deasphalted resid as a feed for fuels and/or lubricant base stock production with use of the corresponding deasphalter rock for gasification to generate hydrogen and/or fuel for the fuels and/or lubricant production process. The integration can include using hydrogen generated during gasification as a fuel to provide heat for solvent processing and/or using the hydrogen for hydroprocessing of deasphalted oil.

Integrated resid deasphalting and gasification

Systems and methods are provided for performing selective catalytic reduction on engine exhaust using ethanol from the engine fuel as the reducing agent. Fuel from a fuel tank or other fuel source can be passed through a separation module to produce a fuel stream with a reduced ethanol content and an ethanol-enriched fraction. After combustion of fuel under lean conditions, the combustion exhaust can be exposed to a catalyst system in the presence of the ethanol-enriched fraction.

Treatment of combustion exhaust

Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510&#xb0; C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks that are resistant to haze formation.

Bright stock production from low severity resid deasphalting

Methods are provided for producing lubricant base stocks from deasphalted oils formed by sequential deasphalting. The deasphalted oil can be exposed a first deasphalting process using a first solvent that can provide a lower severity of deasphalting and a second deasphalting process using a second solvent that can provide a higher severity of deasphalting. This can result in formation of at least a deasphalted oil and a resin fraction. The resin fraction can represent a fraction that traditionally would have been included as part of a deasphalter rock fraction.

Sequential deasphalting for base stock production

Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor.

Lubricant basestock production with enhanced aromatic saturation

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

Improved yields of fuels and/or lubricants from a resid or other heavy oil feed can be achieved using slurry hydroconversion to convert at least about 90 wt % of the feed. The converted portion of the feed can then be passed into one or more hydroprocessing stages. An initial processing stage can be a hydrotreatment stage for additional removal of contaminants and for passivation of high activity functional groups that may be created during slurry hydroconversion. The hydrotreatment effluent can then be fractionated to separate naphtha boiling range fractions from distillate fuel boiling range fractions and lubricant boiling range fractions. At least the lubricant boiling range fraction can then be hydrocracked to improve the viscosity properties. The hydrocracking effluent can also be dewaxed to improve the cold flow properties. The hydrocracked and/or dewaxed product can then be optionally hydrofinished.

Integrated hydrocracking and slurry hydroconversion of heavy oils

An integrated process for producing naphtha fuel, diesel fuel and/or lubricant base oils from feedstocks under sour conditions is provided. The ability to process feedstocks under higher sulfur and/or nitrogen conditions allows for reduced cost processing and increases the flexibility in selecting a suitable feedstock. The sour feed can be delivered to a catalytic dewaxing step without any separation of sulfur and nitrogen contaminants. The integrated process includes an initial dewaxing of a feed under sour conditions, optional hydrocracking of the dewaxed feed, and a separation to form a first diesel product and a bottoms fraction. The bottoms fraction is then exposed to additional hydrocracking and dewaxing to form a second diesel product and optionally a lubricant base oil product. Alternatively, a feedstock can be hydrotreated, fractionated, dewaxed, and then hydrocracked to form a diesel fuel and a dewaxed, hydrocracked bottoms fraction that is optionally suitable for use as a lubricant base oil.

Integrated hydrocracking and dewaxing of hydrocarbons

Provided are high viscosity high quality Group II lube base stocks with improved properties produced by an integrated hydrocracking and dewaxing process. In one form, the Group II lube base stock includes greater than or equal to 90 wt. % saturates, and less than 10 wt. % aromatics, and has an aromatic performance ratio between 1.0 and 5.0. Also provided are lubricant formulations including the high viscosity high quality Group II lube base stock.

High viscosity high quality group II lube base stocks

Methods are provided for producing multiple lubricating oil basestocks from a feedstock. Prior to dewaxing, various fractions of the feedstock are exposed to hydrocracking conditions of different severity to produce a higher overall yield of basestocks. The hydrocracking conditions of different severity can represent exposing fractions of a feedstock to different processing conditions, exposing fractions of a feedstock to different amounts of hydrocracking catalyst, or a combination thereof.

Production of lubricating oil basestocks

Systems and methods are provided for using field enhanced separations to produce multiple fractions from a petroleum input. A liquid thermal diffusion and/or electric field separation is used to produce the fractions. The fractions can then be used to form multiple outputs that share a first feature while being different with regard to a second feature. For example, a first fraction from the plurality of fractions can have a desired value for a first property such as viscosity index. Two or more additional fractions from the plurality of fractions can then be blended together to make a blended fraction or output. The blended fraction can have a value for the first property that is substantially similar to the value for the first fraction. However, for a second property, the first fraction and the blended fraction can have distinct values. As a result, multiple output fractions can be formed that share a first feature but differ in a second feature.

Field enhanced separation of hydrocarbon fractions

Methods are provided for improving the yield of distillate products from hydroprocessing of gas oil feedstocks, such as vacuum gas oils. It has been unexpectedly found that stripping of gases or fractionation to separate out a distillate fraction during initial hydrotreatment of a feed can provide a substantial increase in distillate yield at a desired amount of feedstock conversion. The improvement in yield of distillate products can allow a desired level of conversion to be performed on a feedstock for generating lubricating base oil products while reducing or minimizing the amount of naphtha (or lower) boiling range products. Alternatively, the improvement in yield of distillate products can correspond to an improved yield during a single pass through a reaction system, so that distillate yield is increased even though a lubricant boiling range product is not generated.

Hydrocracking of gas oils with increased distillate yield

Growing community of inventors

Bridgewater, NJ, United States of America

Ajit Bhaskar Dandekar