Exxonmobil Chemical Patents Inc.

Exxonmobil Research and Engineering Company

Mobil Oil Corporation

Exxonmobil Oil Corporation

Exxonmobil Technology and Engineering Company

Yale University

Engelhard Corporation

Exxonmobile Research and Engineering Company

Englehard Corporation

Exxonmobil Chemical Company

Badger Licensing LLC

Exxonmobil Chemicals Patents, Inc.

Stephen Harold Brown

William Alois Weber

John Stephen Godsmark

Paul F Keusenkothen

Georges M K Mathys

Keith Holroyd Kuechler

Anjaneya Sarma Kovvali

Brenda Anne Raich

John Scott Buchanan

David H Olson

Jihad Mohammed Dakka

Raphael Frans Caers

Robert A Ware

Reuel Shinnar

Jeffrey C Trewella

Mark F Mathias

Randolph John Smiley

Teng Xu

Michel A Daage

David Lawrence Stern

Terry Eugene Helton

Jeffrey S Beck

Jane C Cheng

Ajit Bhaskar Dandekar

Steven E Silverberg

Keith K Aldous

An Verberckmoes

Mohsen N Harandi

Doron Levin

Stephen John McCarthy

Robert James Saxton

Teh Chung Ho

Lei Zhang

Charles Morris Smith

David M Stockwell

Timothy Lee Hilbert

Bryan A Patel

Michael B Carroll

Himanshu Gupta

Arun K Sharma

Kendall S Fruchey

Georges Marie Mathys

Rohit Vijay

Larry Lee Iaccino

Jose G Santiesteban

Gary David Mohr

Daniel Paul Leta

Ivy Dawn Johnson

Richard Charles Stell

Luc R M Martens

Stephen M Davis

Michael C Clark

Shifang Luke Luo

Bruce R Cook

James N McCoy

Nick Allen Collins

Richard B Hall

John Richard Shutt

Eric Bart Sirota

Lorenzo C DeCaul

Weldon K Bell

Eddy Theophile Van Driessche

Mayank Shekhar

Richard Charles Dougherty

James Richardson Lattner

Stuart Leon Soled

Frank Hershkowitz

Stephen Neil Vaughn

Karl Gottlieb Strohmaier

Guang Cao

Quang N Le

Chuansheng Bai

Christine Nicole Elia

Sharon B McCullen

Jean Willem Beeckman

Nicolas P Coute

David T Ferrughelli

Patrick Loring Hanks

Randall David Partridge

Daniel Mark Giaquinta

Yun-Feng Chang

Valery Sokolovskii

Sheryl B Rubin-Pitel

Daria N Lissy

David M Lowe

Halou Oumar-Mahamat

David C Dankworth

Kenneth C H Kar

Mohan Kalyanaraman

Robert David Strack

Tilman W Beutel

Benjamin S Umansky

Jeffrey Scott Smith

Anthony F Volpe

Bradley R Fingland

Helge Jaensch

Frank C Wang

John D Y Ou

Robert J Falkiner

Richard A Demmin

Systems and methods are provided for partial upgrading of heavy hydrocarbon feeds to meet transport specifications, such as pipeline transport specifications. The systems and methods can allow for one or more types of improvement in heavy hydrocarbon processing prior to transport. In some aspects, the systems and methods can produce a partially upgraded heavy hydrocarbon product that satisfies one or more transport specifications while incorporating an increased amount of vacuum gas oil and a reduced amount of pitch into the partially upgraded heavy hydrocarbon product. In other aspects, the systems and methods can allow for increased incorporation of hydrocarbons into the fraction upgraded for transport, thereby reducing or minimizing the amount of hydrocarbons requiring an alternative method of disposal or transport. In still other aspects, the systems and methods can allow for reduced incorporation of external streams into the final product for transport while still satisfying one or more target properties.

Apparatus and process for upgrading heavy hydrocarbons

An hydroconverted effluent composition is provided, along with systems and methods for making such a composition. The hydroconverted effluent composition can have an unexpectedly high percentage of vacuum gas oil boiling range components while having a reduce or minimized amount of components boiling above 593° C. (1100° F.). In some aspects, based in part on the hydroprocessing used to form the hydroconverted effluent composition, the composition can include unexpectedly high contents of nitrogen. Still other unexpected features of the composition can include, but are not limited to, an unexpectedly high nitrogen content in the naphtha fraction; and an unexpected vacuum gas oil fraction including an unexpectedly high content of polynuclear aromatics, an unexpectedly high content of waxy, paraffinic compounds, and/or an unexpectedly high content of n-pentane asphaltenes

Hydroconverted compositions

Slurry hydroconversion process for upgrading heavy hydrocarbons

An upgraded crude composition is provided, along with systems and methods for making such a composition. The upgraded crude composition can include an unexpectedly high percentage of vacuum gas oil boiling range components while having a reduce or minimized amount of components boiling above 593&#xb0; C. (1100&#xb0; F.). In some aspects, based in part on the hydroprocessing used to form the upgraded crude composition, the composition can include unexpectedly high contents of nitrogen. Still other unexpected features of the composition can include, but are not limited to, an unexpectedly high nitrogen content in the naphtha fraction; and an unexpected vacuum gas oil fraction including an unexpectedly high content of polynuclear aromatics, an unexpectedly high content of waxy, paraffinic compounds, and/or an unexpectedly high content of n-pentane asphaltenes.

Synthetic crude composition

Methods are provided for processing deasphalted gas oils derived from thermally cracked resid fractions to form Group I, Group II, and/or Group III lubricant base oils. The yield of lubricant base oils (optionally also referred to as base stocks) can be increased by thermally cracking a resid fraction at an intermediate level of single pass severity relative to conventional methods. By performing thermal cracking to a partial level of conversion, compounds within a resid fraction that are beneficial for increasing both the viscosity and the viscosity index of a lubricant base oil can be retained, thus allowing for an improved yield of higher viscosity lubricant base oils from a thermally cracked resid fraction.

Production of lubricant oils from thermally cracked resids

A method of upgrading refining streams with high polynucleararomatic hydrocarbon (PNA) concentrations can include: hydrocracking a PNA feed in the presence of a catalyst and hydrogen at 380&#xb0; C. to 430&#xb0; C., 2500 psig or greater, and 0.1 hrto 5 hrliquid hourly space velocity (LSHV), wherein the weight ratio of PNA feed to hydrogen is 30:1 to 10:1, wherein the PNA feed comprises 25 wt % or less of hydrocarbons having a boiling point of 700&#xb0; F. (371&#xb0; C.) or less and having an aromatic content of 50 wt % or greater to form a product comprising 50 wt % or greater of the hydrocarbons having a boiling point of 700&#xb0; F. (371&#xb0; C.) or less and having an aromatic content of 20 wt % or less.

Upgrading polynucleararomatic hydrocarbon-rich feeds

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 upgrading a mixture of catalytic slurry oil and coker bottoms by hydroprocessing. Optionally, the upgrading can further include deasphalting the mixture of catalytic slurry oil and coker bottoms to form a deasphalted oil and a deasphalter residue or rock fraction. The mixture of catalytic slurry oil and coker bottoms and/or the deasphalted oil can then be hydroprocessed to form an upgraded effluent that includes fuels boiling range products. Optionally, in some aspects where the feed mixture is deasphalted prior to hydroprocessing, the feed mixture can further include a portion of a (sour) vacuum resid.

Hydroprocessing of catalytic slurry oil and coker bottoms

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

Systems and methods are provided for upgrading catalytic slurry oil. The upgrading can be performed by deasphalting the catalytic slurry oil to form a deasphalted oil and a residual or rock fraction. The deasphalted oil can then be hydroprocessed to form an upgraded effluent that includes fuels boiling range products.

Hydroprocessing of deasphalted catalytic slurry oil

Systems and methods are provided for improving the processing of heavy or challenged feeds in a refinery based on integrated use of deasphalting, coking, and hydroprocessing. An optional fluid catalytic cracking unit can be included in the integrated system to allow for further improvements. The improved processing can be facilitated based on a process configuration where the vacuum resid fractions and/or other difficult fractions are deasphalted to generate a deasphalted oil and a deasphalter residue or rock fraction. The deasphalted oil can be passed into a hydroprocessing unit for further processing. The rock fraction can be used as the feed to a coking unit. Although deasphalter residue or rock is typically a feed with a high content of micro carbon residue, a high lift deasphalting process can allow a portion of the micro carbon residue in the initial feed to remain with the deasphalted oil. The portion of micro carbon residue that remains in the deasphalted oil can then be upgraded during hydroprocessing and/or during subsequent processing of the feed. By reducing the amount of micro carbon residue passed into a coker for a given initial feed source, the overall capacity for a reaction system to handle heavy feeds can be increased relative to the rate of coke production from the reaction system.

Resid upgrading with reduced coke formation

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 forming specialty products from hydrotreated FCC fractions. Optionally, the hydrotreated FCC fractions used for forming the specialty products can further include a (hydrotreated) portion of a steam cracker tar fraction. The specialty products that can be formed from hydrotreated FCC fractions include, but are not limited to, carbon blacks, resins, and carbon fibers. A convenient method for forming the hydrotreated FCC fractions can be fixed bed hydrotreatment.

Production of carbon blacks and resins from hydrotreated catalytic slurry oil

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any 'pitch' generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Processing of heavy hydrocarbon feeds

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Bernardsville, NJ, United States of America

Stephen Harold Brown