Exxonmobil Research and Engineering Company

Exxonmobil Technology and Engineering Company

Exxonmobil Chemical Patents Inc.

Randolph John Smiley

Shifang Luke Luo

Stephen Harold Brown

Rustom Merwan Billimoria

Samia Ilias

Brian A Cunningham

Thomas Francis Degnan, Jr

Ramanathan Sundararaman

William Ernest Lewis

Xiaochun Xu

Brenda Anne Raich

Xinrui Yu

Natalie Ann Fassbender

Ivy Dawn Johnson

Jean Willem Beeckman

Patrick Loring Hanks

Michele Sue Touvelle

Peter I Ravikovitch

Anjaneya Sarma Kovvali

Tilman W Beutel

Garland B Brignac

Nadya A Hrycenko

Keith Wilson

Tien V Le

Shifang Luo

Harry William Deckman

Roby Bearden, Jr

Kenneth L Riley

Lei Zhang

Chuansheng Bai

Jack Wayne Johnson

Ajit Bhaskar Dandekar

Alan Roy Katritzky

David T Ferrughelli

Bruce R Cook

Sheryl B Rubin-Pitel

Kenneth C H Kar

Bryan A Patel

Gary Paul Schleicher

Keith K Aldous

Kendall S Fruchey

Richard A Demmin

John P Greeley

Joseph E Gatt

Hyung Suk Woo

William J Tracy, Iii

Anthony Go

Manuel Anthony Francisco

Ian J Laurenzi

Mike T Noorman

Lisa M Guay

David G Hammond

Steven S Lowenthal

Sara K Green

Gregory K Lilik

Robert Allen Bradway

Daniel E Kadlecek

Jacob Johannes Thiart

Jesse R McManus

Saurabh S Maduskar

Sundararajan Uppili

Lawrence R Gros

Melissa D Foster

Stacey E Siporin

Philippe Laurent

Poturovic Jasmina

Grace Shi Qian Yeo

Aldrin G Cuevas

Robert A Bradway

William J Tracy

Kenneth Ch Kar

Thomas Francis Degnan

Jasmina Poturovic

Systems and methods are provided for integration of a reactor for polyolefin pyrolysis with the effluent processing train for a steam cracker. The polyolefins can correspond to, for example, polyolefins in plastic waste. Integrating a process for polyolefin pyrolysis with a steam cracker processing train can allow a mixture of polymers to be converted to monomer units while reducing or minimizing costs and/or equipment footprint. This can allow for direct conversion of polyolefins to the light olefin monomers in high yield while significantly lowering capital and energy usage due to integration with a steam cracking process train. The integration can be enabled in part by selecting feeds with appropriate mixtures of various polymer types and/or by limiting the volume of the plastic waste pyrolysis product relative to the volume from the steam cracker(s) in the steam cracking process train. By selecting plastic waste and/or other polyolefin sources with an appropriate mixture of polyolefins as the feedstock, the resulting polyolefin pyrolysis product can be separated in a steam cracking process train to produce separate fractions for various polymer grade small olefin products.

Light olefin recovery from plastic waste pyrolysis

Methods of refining a whole crude oil stream. The methods involve first processing the crude either through a hydrotreating reactor comprising a dewaxing reactor bed or a flash evaporation separator. The treated streams are then further processed through a demetalization reactor bed, a hydroprocessing reactor bed, or both. The stream can then be still further processed via additional hydrotreating, distillation, or both.

Methods of whole crude and whole crude wide cut hydrotreating and dewaxing low hetroatom content petroleum

Method of refining whole crude oil or a wide cut crude oil, the methods comprising a combination of a hydrotreating reactor, a distillation tower, and an optional flash evaporation separator. The methods can also include light ends processing, fluid catalytic cracking, reforming, hydrocracking, and demetalization. In some methods a whole crude oil is first processed through a flash evaporation separator to create a wide cut crude oil and in other methods, the flash evaporation separator is not used as the whole crude oil is first treated in a hydrotreater.

Methods of whole crude and whole crude wide cut hydrotreating low hetroatom content petroleum

This disclosure relates to new processes to produce high paraffinic diesel from crude oil, such as tight oil from the Permian basin. This disclosure also relates to high paraffinic diesel compositions and high paraffinic diesel blends.

Process to produce high paraffinic diesel

Kerosene boiling range or jet fuel boiling range compositions are provided that are formed from crude oils with unexpected combinations of high naphthenes to aromatics weight and/or volume ratio and a low sulfur content. The resulting kerosene boiling range fractions can have an unexpected combination of a high naphthenes to aromatics weight ratio, a low but substantial aromatics content, and a low sulfur content. Such fractions can potentially be used as fuel after a reduced or minimized amount of additional refinery processing. By reducing, minimizing, or avoiding the amount of refinery processing needed to meet fuel and/or fuel blending product specifications, the fractions derived from the high naphthenes to aromatics ratio and low sulfur crudes can provide fuels and/or fuel blending products having a reduced or minimized carbon intensity.

High napthenic content kerosene compositions

Hydroprocessed residual fuel and/or fuel blending components are provided that have a sulfur and nitrogen level comparable to liquefied natural gas (LNG). Because of the low starting level of sulfur and/or nitrogen, the severity of the hydroprocessing that is needed for the crude oil or bottoms fraction in order to remove sulfur to a level that is comparable to LNG is reduced or minimized. This can allow the resulting marine residual fuels to have low carbon intensity, low SOx and NOx emission and high energy density. Since the hydroprocessed fractions correspond to a fuel oil product, the resulting marine fuel can be used in existing fleets, and can be distributed in existing bunkering systems.

Ultra low sulfur marine fuel compositions

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 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

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

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 slurry hydroconversion of a heavy oil feed, such as an atmospheric or vacuum resid. The systems and methods allow for slurry hydroconversion using catalysts with enhanced activity and/or catalysts that can be recycled as a side product from a complementary refinery process.

Slurry hydroconversion using enhanced slurry catalysts

Systems and methods are provided for use of coking and slurry hydroconversion for conversion of heavy oil feeds. The combination of coking and slurry hydroconversion allows for improved yield of liquid products while reducing or minimizing the consumption of hydrogen in slurry hydroconversion reaction stages. Coking and slurry hydroconversion can be combined by segregating feeds based on Conradson carbon residue. Alternatively, slurry hydroconversion can be used to process unconverted bottoms from a coking process.

Slurry hydroconversion and coking of heavy oils

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

Systems and methods are provided for sequential slurry hydroconversion of heavy oil feedstocks. One or more low pressure slurry hydroconversion stages can be used to perform a majority of the conversion of a heavy oil feedstock. The bottoms from the low pressure stages can then be slurry hydroconverted in one or more high pressure stages to further convert the feedstock.

Sequential slurry hydroconversion of heavy oils

Growing community of inventors

Hellertown, PA, United States of America

Randolph John Smiley