Mobil Oil Corporation

Exxonmobil Research and Engineering Company

Exxonmobil Technology and Engineering Company

Other

Exxonmobil Chemical Patents Inc.

Phillips Petroleum Company

Exxonmobil Engineering & Technology Company

Mobil Oil Coproration

Mohsen N Harandi

Hartley Owen

Suriyanarayanan Rajagopalan

Werner O Haag

Nick Allen Collins

Paul H Schipper

Mitch L Hindman

Samuel A Tabak

Robert A Ware

Paul F Keusenkothen

Roger A Morrison

Weldon K Bell

Stephen Harold Brown

Stuart S Shih

Stephen John McCarthy

David L Johnson

Michael S Sarli

Arthur A Chin

Robert T Thomson

David L Fletcher

Bing Du

Sean C Smyth

John Scott Buchanan

Terry Eugene Helton

Scott A Stevenson

Albin Huss, Jr

Jane C Cheng

Michael F Raterman

Jeffrey C Trewella

Timothy Lee Hilbert

Himanshu Gupta

Rohit Vijay

Lu Han

Eric B Shen

Clay R Sutton

David W Staubs

Zhongcheng Wang

Edward F Kondis

James Richardson Lattner

Stuart Leon Soled

Ralph M Dessau

Doron Levin

David S Shihabi

Joseph A Herbst

Lei Zhang

Chuansheng Bai

Ajit Bhaskar Dandekar

James H Haddad

Dominick N Mazzone

Klaus W Schatz

Frederick J Krambeck

Kenneth J Del Rossi

Hye Kyung Timken

Bal K Kaul

Sergei Yurchak

David C Dankworth

Stephen J McGovern

Brenda Anne Raich

Benjamin S Umansky

Michael B Carroll

Keith K Aldous

Robert J Falkiner

Richard Charles Dougherty

Mayank Shekhar

James H Beech, Jr

Gerald J Teitman

Brett Thomas Loveless

Juan D Henao

David A Pappal

Christopher Gordon Smalley

Francis P Ragonese

Tracie L Owens

J Scott Buchanan

Timothy L Hilbert

Charles M Sorensen

Samia Ilias

April D Ross

James A Stoos

Altaf Husain

Glenn C Wood

Thomas Francis Degnan, Jr

John D Kushnerick

Steven Webster Levine

Eric B Senzer

Paul P Durand

Sara L Yohe

Randall J Meyer

Payman Esmaeili

Steven Pyl

James A Dunn

Allen R Hansen

Michael T Siuta

Todd P Marut

Tien V Le

Jasmina Poturovic

Frederick Earl Daugherty

Stuart S Goldstein

Frank P Ragonese

Norman J Rouleau

Paul J Oswald

Disclosed are process and system for making an asphalt product and an olefin product from an asphaltenes-rich feed without using a vacuum distillation column. The feed is first deep stripped in a first stripping column using a stripping vapor such as steam and/or a C2-C3 paraffins-rich stream to obtain a bottoms liquid effluent having a high cutpoint and an overheads effluent comprising gas oil, lighter hydrocarbons, and the stripping vapor. The high-boiling point bottoms liquids effluent, with optional additional separation and/or treatment, can be used as asphalt products. The overheads effluent, with optional additional separation, can be fed into a pyrolysis furnace cracker, where it is converted into a cracker product mixture comprising olefins, lighter hydrocarbons, hydrogen, and the like, which can be recovered in a products recovery subsystem.

Process and system for processing asphaltenes-rich feed

Systems and methods are provided for performing steam cracking on a feed while using direct heating of the reaction environment. The heating of the reaction environment can be achieved in part by transporting heat transfer particles from a heating zone to cracking zone. This can be performed in a fluidized bed reactor, a moving bed reactor, a riser reactor, or another type of reactor that can allow for catalyst movement and regeneration during operation.

Fluid bed steam cracking using direct heating

Methanol-to-gasoline conversion may be performed using a heavy gasoline treatment, followed by a separation operation. Methanol may be converted into a first product mixture comprising dimethyl ether (DME) under DME formation conditions. In a methanol-to-gasoline (MTG) reactor, the first product mixture may be converted under MTG conversion conditions to produce a second product mixture comprising light gasoline hydrocarbons and untreated heavy gasoline hydrocarbons. The untreated heavy gasoline hydrocarbons may be separated from the light gasoline hydrocarbons and transferred to a heavy gasoline treatment (HGT) reactor. The untreated heavy gasoline hydrocarbons may be catalytically reacted in the HGT reactor to form a third product mixture. A heavy hydrocarbon fraction may be separated from the third product mixture. The heavy hydrocarbon fraction includes heavy gasoline hydrocarbons having a lower boiling endpoint than does the untreated heavy gasoline hydrocarbons.

Methods for methanol-to-gasoline conversion with post-processing of heavy gasoline hydrocarbons

Provided are novel process for upgrading naphtha and increasing the yield of reformate. Olefinic naphtha and light paraffins are combined and fed to a catalytic fluidized bed reactor maintained at a temperature about 775&#xb0; F. and about 1250&#xb0; F. and an operating pressure between about 10 psig and about 500 psig to produce a product comprising at least 1 wt. % higher Chydrocarbon than the combined feed and at least 55 wt. % aromatics.

Processes for producing high octane reformate having high Cyield

A method may include: contacting a light paraffin feed comprising ethane, propane, butane, naphtha or combinations thereof with a restrained catalyst in a reactor; converting at least a portion of the light paraffin feed to ethylene, propylene, or combinations thereof with an olefin selectivity of at least 70 wt. % and methane selectivity of less than 15 wt. %; and withdrawing a product stream from the reactor.

Selective olefins production from light paraffins

A method for identifying sensor drift can include: setting an autocorrelation threshold for a sensor in a long-short term memory (LSTM) model developed based on historical process measurements from an analogous sensor to a sensor; collecting measured data from the sensor; applying the LSTM model to the measured data from the sensor, wherein applying the LSTM model comprises: applying the LSTM model to the measured data from the sensor to yield LSTM predicted data; calculating key performance indicators (KPIs) of the LSTM data based on an accumulated slow drift error (ASDE) model, wherein the KPIs comprise an error, an accumulated prediction error, an accumulated slow-drift error, and an estimated autocorrelation; and identifying sensor drift when the estimated autocorrelation violates the autocorrelation threshold.

Intelligent system for identifying sensor drift

Systems and methods are provided for conversion of methanol to gasoline in an integrated system that can also upgrade light paraffins generated by the methanol conversion process to aromatics. In some aspects, the integrated configuration can include integration of the stage for upgrading of light paraffins to aromatics into the product separation sequence for processing of the methanol conversion effluent. In other aspects, the integrated configuration can further include sharing a common catalyst between the methanol conversion stage and the stage for upgrading light paraffins to aromatics.

Conversion of methanol to gasoline with integrated paraffin conversion

Processes for converting an organic-material-containing feed comprising contacting the feed with a plurality of fluidized hot particles in a pyrolysis zone to product a first pyrolysis effluent, optionally contacting the first pyrolysis effluent with a quenching stream to impart additional pyrolysis of organic materials contained in the quenching stream, separating at least a portion of the particles and feeding them to a combustion zone where the particles are heated to an elevated temperature, optionally contacting the combustion zone effluent with a second organic-material-containing stream to produce, e.g., syngas, and feeding at least a portion of the heated particles to the pyrolysis zone.

Processes for converting organic material-containing feeds via pyrolysis

Methanol-to-gasoline (MTG) conversion may be performed with forward methanol processing. Methanol may be fed to a first reactor where it may be catalytically converted under dimethyl ether formation conditions in the presence of a first catalyst to form a product mixture comprising dimethyl ether (DME), methanol, and water. The DME may be separated from the methanol and the water and delivered to a second reactor. In the second reactor, the DME may be catalytically converted under MTG conversion conditions in the presence of a second catalyst to form a second product mixture comprising gasoline hydrocarbons and light hydrocarbon gas. The methanol and the water from the first reactor may be separated further to obtain substantially water-free methanol, which may be delivered to the second reactor. The separation of methanol from the water may be performed using the light hydrocarbon gas to effect stripping of the methanol.

Methods for methanol-to-gasoline conversion with forwarding methanol processing

Methanol-to-gasoline (MTG) conversion may be performed with a methanol recycling. Methanol may be fed to a first reactor where it may be catalytically converted under dimethyl ether formation conditions in the presence of a first catalyst to form a product mixture comprising dimethyl ether (DME), methanol, and water. The DME may be separated from the methanol and the water and delivered to a second reactor. In the second reactor, the DME may be catalytically converted under MTG conversion conditions in the presence of a second catalyst to form a second product mixture comprising gasoline hydrocarbons and light hydrocarbon gas. The methanol and the water from the first reactor may be separated further to obtain substantially water-free methanol, which may be returned to the first reactor. The separation of methanol from the water may be performed using the light hydrocarbon gas to effect stripping of the methanol.

Methods for methanol-to-gasoline conversion with methanol recycling

A process and system that use the heat produced in the generation of Syngas to provide heat to an endothermic reaction zone are disclosed. A method for providing heat to an endothermic reaction may comprise producing Syngas in a reforming reactor. The method may further comprise recovering heat from the producing the Syngas to heat an endothermic reaction stream in a heat transfer zone. The method may further comprise allowing reactants in the endothermic reaction stream to react to form an endothermic reaction product stream. The method may further comprise withdrawing the endothermic reaction product stream from the heat transfer zone.

Advanced steam cracking

A novel process/system for flexibly producing chemicals and fuels from a petroleum feed such as crude comprise a flashing drum, a first cracker (e.g., a fluidized bed pyrolysis cracker or an oxidative cracker), and an olefin-to-gasoline reaction zone. The process/system can also include a steam cracker and a hydrotreater. The process/system can convert crude oil into hydrogen, C2-C4 olefins, gas oil and distillates with various amounts by adjusting the cut point of the bottoms effluent exiting the flashing drum.

Process and system for processing petroleum feed

Systems and methods are provided for integrating a fluidized coking operation, a reverse osmosis operation, a coke gasification operation and/or processes for production of compounds from the synthesis gas generated during the coke gasification. Conventional FLEXICOKING&#x2122; processes may produce carbon dioxide emissions and low Joule Flexigas, as well as waste water containing metals and poor quality coke containing metals, which may be expensive to process, or may require sending to other facilities for further processing. The systems and methods described herein address these issues in an advantageous and economical manner, with improved carbon capture, waste upgrade and chemicals production, while providing high value ash (e.g., for recovery of metals such as vanadium, nickel, sodium, iron, and mixtures thereof) and upgraded coke streams.

Carbon capture, waste upgrade, and chemicals production using improved flexicoking

Systems and methods are provided for using an oxygen-containing gas as at least part of the stripping gas for the stripping zone or section in a fluidized coker. By using an oxygen-containing gas as the stripping gas, heat can be added to the stripping zone selectively based on combustion of coke and/or hydrocarbons with the oxygen in the stripping gas. This can allow the temperature of the stripping zone to be increased relative to the temperature of the coking zone of a fluidized coking system. The flow of oxygen can be controlled to achieve a desirable temperature in the stripper while the reactor temperature is independently set by preheating of the feed and/or hot coke circulation to the reaction zone.

Fluidized coking with oxygen-containing stripping gas

Systems and methods are provided for catalyst regeneration using a stoichiometric amount or less air for coke combustion.

Upgrading fuel gas using stoichiometric air for catalyst regeneration

Growing community of inventors

Lawrenceville, NJ, United States of America

Mohsen N Harandi