Mobil Oil Corporation

Chevron U.s.a. Inc.

University of South Alabama

Other

Uop Lcc

Chevron Phillips Chemical Company LP

W.r. Grace & Co. -conn.

Hye Kyung Timken

Michael Sean Driver

Robert A Ware

Daniel Chinn

Kathleen M Keville

James Hillard Davis, Jr

Zunqing He

Kevin N West

David O Marler

Russell Evan Cooper

Donald Henry Mohr

Robert Fletcher Cleverdon

Christine Marie Phillips

Thomas F Degnan

Wieslaw J Roth

Charles T Kresge

David S Shihabi

Albin Huss, Jr

Jane C Cheng

Huping Luo

Dominick N Mazzone

Ai-Fu Chang

Lei Ji

Brenda H Rose

Mohsen N Harandi

James C Vartuli

Stuart Damon Hellring

Arthur W Chester

John Scott Buchanan

Stuart S Shih

Philip Jay Angevine

Werner O Haag

Mae K Rubin

John P McWilliams

Catherine S Chen

Krishniah Parimi

Jeffrey C Trewella

Roger A Morrison

Rajeswar R Gattupalli

Richard F Socha

Daria N Lissy

Michael E Landis

Michael S Sarli

Guenter H Kuehl

Michael Scott Ziebarth

Donald J Klocke

John V Heyse

Wu-Cheng Cheng

Bong-Kyu Chang

Weldon K Bell

Douglas A Nafis

Terry G Roberie

Thomas R Forbus, Jr

Xinjin Zhao

James H Beech, Jr

Gerald J Teitman

Sanjay B Sharma

Rahul Shankar Bhaduri

Charles M Sorensen

Gregory A Jablonski

Viorel Duma

Michael John Girgis

Shawn Shlomo Winter

Altaf Husain

Elizabeth Carter

Jeff Johns

Bong Kyu Chang

Matthew C Cole

Steven E Wentzek

Rebecca Mudrock

Birbal Chawla

Paul P Durand

Clifford Michael Lowe

Paul A Howley

Annie T Pathiparampil

Scott Kevin Purnell

Norman J Rouleau

Kenneth G Simons, Deceased

Dominik N Mazzone

W Thomas Mo

Samual A Tabak

L Deane Rollmann

Sherri L Riedinger

David G Freyman

Dominic P Weber

Rusell Evan Cooper

Frank Thomas Diguiseppi

Michael Tung-Hai Cheng

Douglas Robert Cyr

Izadyar Dalvand

Processes for the direct alkylation of ethylene with isobutane or isopentane using a highly active ionic liquid alkylation catalyst are described. Ethylene is sent to a high-temperature alkylation reactor loop, and C, C, and Colefins are routed to a low temperature alkylation reactor loop. In each reactor, the olefins are contacted with an excess of isobutane or isopentane in the presence of a highly active ionic liquid catalyst. Portions of the reactor effluent streams are fed to a common downstream catalyst separation and product fractionation sections. The remainder of the reactor effluent is recycled back to the respective alkylation reactor.

Combined process for alkylation of light olefins using ionic liquid catalysts

Processes for regenerating ionic liquid catalyst by contacting the ionic liquid catalyst with hydrogen gas in a regeneration reactor. The amount of hydrogen is less than 550 SCF/BBL (97.96 m/m) of spent ionic liquid catalyst, or less than 500 SCF/BBL (89.05 m/m) of spent ionic liquid catalyst, or between 550 and 45 SCF/BBL (97.96 and 8.015 m/m) of spent ionic liquid catalyst, or between 500 and 50 SCF/BBL (89.05 and 8.905 m/m) of spent ionic liquid catalyst. Alkylation processes are also disclosed.

Ionic liquid catalyst regeneration with reduced hydrogen amounts

Disclosed are systems and methods which provide a process stream comprising a gaseous component, capture the gaseous component from the process stream by an ionic liquid solvent of a separator, and recover a captured gaseous component from the ionic liquid solvent in a regenerator. A second gaseous component from the process stream may be captured by the ionic liquid solvent of the separator, and the second gaseous component may be recovered from the ionic liquid solvent in the regenerator. Alternatively, the second gaseous component from the process stream may be uncaptured by the ionic liquid solvent, and the uncaptured second gaseous component may be recovered from a membrane unit.

Separations with ionic liquid solvents

A process and system for separating COfrom a flue gas stream is disclosed. The process involves (a) contacting a flue gas stream containing water vapor and COwith an ionic absorbent under absorption conditions to absorb at least a portion of the COfrom the flue gas stream and form a CO-absorbent complex; wherein the ionic absorbent comprises a cation and an anion comprising an amine moiety; and (b) recovering a gaseous product having a reduced COcontent.

Process for the separation of carbon dioxide from flue gas

An aqueous ionic absorbent solution is disclosed containing (a) about 15 wt. % to about 80 wt. % of one or more diluents, based on the total weight of the aqueous ionic absorbent solution; and (b) an ionic absorbent containing a cation and an anion comprising an amine moiety.

Aqueous solutions of amine functionalized ionic compounds for carbon capture processes

A process for determining ionic liquid catalyst deactivation including (a) collecting at least one sample of an ionic liquid catalyst; (b) hydrolyzing the at least one sample to provide at least one hydrolyzed sample; (c) titrating the at least one hydrolyzed sample with a basic reagent to determine a volume of the basic reagent necessary to neutralize a Lewis acid species of the ionic liquid catalyst; and (d) calculating the acid content of the at least one sample from the volume of basic reagent determined in step (c) is described. Processes incorporating such a process for determining ionic liquid catalyst deactivation are also described. These processes are an alkylation process, a process for controlling ionic liquid catalyst activity in a reaction producing by-product conjunct polymers, and a continuous process for maintaining the acid content of an ionic liquid catalyst at a target acid content in a reaction producing by-product conjunct polymers.

Process for controlling ionic liquid catalyst activity by titration

This invention provides a method of producing an aromatics alkylation catalyst comprising the steps of:

Method of producing an aromatics alkylation catalyst

Large crystal ZSM-5, its synthesis and use

This is a process for upgrading a petroleum naphtha fraction. The naphtha is subjected to reforming and the reformate is cascaded to a benzene and toluene synthesis zone over a benzene and toluene synthesis catalyst comprising a molecular sieve of low acid activity. The preferred molecular sieve is steamed ZSM-5. The benzene and toluene synthesis zone is operated under conditions compatible with the conditions of the reformer such as pressures of above about 50 psig (446 kPa) and temperatures above about 800.degree. F. (427.degree. C). In one aspect of the invention, the benzene and toluene synthesis catalyst includes a metal hydrogenation component such as cobalt, nickel, platinum or palladium. In one mode of operation, the benzene and toluene synthesis catalyst replaces at least a portion of the catalyst of the reformer. The process produces a product containing an increased proportion of benzene and toluene, and a reduced proportion of C8 aromatics, particularly ethylbenzenes, as compared to the reformate.

Hydrocarbon conversion

Cracked naphtha feeds such as FCC naphtha and coker naphtha are upgraded to produce chemical grade BTX (benzene, toluene, xylene with ethylbenzene) while co-producing a low sulfur gasoline of relatively high octane number. The cracked, sulfur-containing naphtha is processed by hydrodesulfurization followed by treatment over an acidic catalyst, preferably a zeolite such as ZSM-5 or zeolite beta with a hydrogenation component, preferably molybdenum. The treatment over the acidic catalyst in the second step restores the octane loss which takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product to permit a low sulfur gasoline of blending quality to be obtained with the BTX. The BTX can be extracted from the second stage effluent, preferably from a C.sub.6 -C.sub.8 fraction of this effluent.

Production of benzene, toluene, and xylene (BTX) from FCC naphtha

Low sulfur gasoline of relatively high octane number is produced from a thermally cracked sulfur-containing naphtha such as coker naphtha, by hydrodesulfurization followed by treatment over an acidic catalyst, preferably a zeolite such as ZSM-5 or zeolite beta with a hydrogenation component, preferably molybdenum. The treatment over the acidic catalyst in the second step restores the octane loss which takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product

Naphtha upgrading process

At least one olefin and at least one isoparaffin are converted to a diesel fuel blending component by contacting the olefin and the isoparaffin with a catalyst selected from MCM-22, MCM-36, MCM-49, and MCM-56 to provide a product containing a diesel fuel.

Process for producing low aromatic diesel fuel with high cetane index

Growing community of inventors

Woodbury, NJ, United States of America

Hye Kyung Timken