Saudi Basic Industries Corporation

Sabic Global Technologies B.v.

Mobil Oil Corporation

Exxonmobil Oil Corporation

Sabic Basic Industries Corporation

Scott A Stevenson

Alla Konstantin Khanmamedova

Wugeng Liang

Scott F Mitchell

Dustin Farmer

Joseph R Linzer

Clarence D Chang

David S Shihabi

Ashim Kumar Ghosh

James Kauffman

Gopalakrishnan G Juttu

Michael Edward Huckman

Angie McGuffey

James C Vartuli

Luis Aramburo

Jim Vartuli

Michael Mier

Joseph William Schroer

Jose G Santiesteban

Andrew Mark Ward

John S Ledford

Paul E Ellis

Zhun Zhao

David L Sullivan

Lixia Cai

Kenneth Francis Lawson

Tim Abbott

Arno Oprins

Mohsen N Harandi

Terry Eugene Helton

Paul H Schipper

Jane C Cheng

Richard F Socha

Neeta Kulkarni

Dustin Fickel

Jaap Willem Van Hal

Michael Alan Steckel

Emiel Van Kimmenade

Sanjeev Deshpande

Travis Conant

Robin J Bates

Mike Mier

Sheetal Bafna

Jose Armando Salazar-Guillen

Jim Allman

David Sullivan

Scott S Han

Stuart Damon Hellring

Costandi A Audeh

David O Marler

Charles T Kresge

David L Johnson

John P McWilliams

Amos A Avidan

Ajit V Sapre

Mark F Mathias

Gerald J Teitman

Sanjay B Sharma

Pooja Bajaj

Maikel Van Iersel

Raghu K Menon

Maria D Farnos

Joseph F Sodomin, Iii

Heng Shou

Allen R Hansen

Dimitri Daniëls

Balamurali Krishna Nair

Meghann Simmons

MyatNoeZin Myint

Corina Mihut

Cong Nguyen

Gopalakrishnam G Juttu

Meghan Simmons

Dustin B Farmer

Japp W Van Hal

A chemical synthesis plant comprising: one or more reactors configured for producing, from one or more reactants, a process stream comprising at least one chemical product; a feed preparation system configured to prepare one or more feed streams comprising one or more of the one or more reactants for introduction into the one or more reactors; and/or a product purification system configured to separate the at least one chemical product from reaction byproducts, unreacted reactants, or a combination thereof within the process stream, wherein the chemical synthesis plant is configured such that a majority of the net energy needed for heating, cooling, compressing, or a combination thereof utilized via the one or more reactors, the feed preparation system, the product purification system, or a combination thereof is provided from a noncarbon based energy source, from a renewable energy source, and/or from electricity.

Use of renewable energy in the production of chemicals

An olefin synthesis plant comprising: a feed pretreatment section configured to pretreat a feed stream; a pyrolysis section comprising one or more pyrolysis reactors configured to crack hydrocarbons in the feed stream in the presence of a diluent to produce a cracked gas stream; a primary fractionation and compression section configured to provide heat recovery from and quenching of the cracked gas stream; remove a component from the cracked gas stream; and compress the cracked gas stream, thus providing a compressed cracked gas stream; and/or a product separation section configured to separate a product olefin stream from the compressed cracked gas stream, wherein the olefin synthesis plant is configured such that, relative to a conventional olefin synthesis plant, more of the energy and/or the net energy required by the olefin synthesis plant and/or one or more sections thereof, is provided by a non-carbon based and/or renewable energy source and/or electricity.

Use of renewable energy in olefin synthesis

A methanol synthesis plant comprising: a feed pretreating section operable to pretreat a feed stream; a synthesis gas (syngas) generation section comprising one or more reactors operable to produce a syngas synthesis product stream comprising synthesis gas from the feed stream; a methanol synthesis section comprising one or more methanol synthesis reactors operable to produce a synthesis product comprising methanol; and/or a methanol purification section operable to remove at least one component from the synthesis product to provide a purified methanol product; wherein the methanol synthesis plant is configured such that, relative to a conventional methanol synthesis plant, more of the net energy required by the methanol synthesis plant, the feed pretreating section, the syngas generation section, the methanol synthesis section, the methanol purification section, or a combination thereof, is provided by a non-carbon based energy source, a renewable energy source, and/or electricity.

Use of renewable energy in methanol synthesis

A process for producing methyl tert-butyl ether (MTBE) comprising introducing a butane feed stream (n-butane, i-butane) and hydrogen to a hydrogenolysis reactor comprising a hydrogenolysis catalyst to produce a hydrogenolysis product stream comprising hydrogen, methane, ethane, propane, i-butane, and optionally n-butane; separating the hydrogenolysis product stream into a first hydrogen-containing stream, an optional methane stream, a Cto Cgas stream (ethane, propane), and a butane stream (i-butane, optionally n-butane); feeding the butane stream to a dehydrogenation reactor to produce a dehydrogenation product stream, wherein the dehydrogenation reactor comprises a dehydrogenation catalyst, and wherein the dehydrogenation product stream comprises hydrogen, i-butane, and isobutylene; and feeding the dehydrogenation product stream and methanol to an etherification unit to produce an unreacted methanol stream, an unreacted isobutylene stream, and an MTBE stream.

Selective hydrogenolysis integrated with MTBE production

A method for preparing a hydrocracking catalyst comprising: (i) providing a shaped body comprising a zeolite and a binder, wherein the shaped body has been obtained by shaping, calcination and cooling, wherein the zeolite is ZSM-5 having a silica (SiO) to alumina (AlO) molar ratio of 25-75; (ii) optionally drying the shaped body at a temperature of 100-300&#xb0; C. for a period of at least 1 hour; (iii) depositing a hydrogenation metal on the shaped body by an impregnation for a period of at most 2 hours such that the amount of the hydrogenation metal is 0.010-0.30 wt % with respect to the total catalyst; (iv) optionally rinsing the metal deposited shaped body with water; and (v) heat-treating the metal deposited shaped body in air at a temperature of 250-300&#xb0; C. for a period of 1-5 hours; wherein the catalyst comprises a total of less than 0.05 wt % sodium and cesium.

Process for producing BTX from a C&#x2014;Chydrocarbon mixture

A process for increasing olefin production from refinery that processes hydrocarbon streams that are rich in aromatic compounds and includes steam cracking and hydrotreating an aromatically rich feedstock to produce a hydrotreated pyrolysis gasoline stream and light pyrolysis oil byproduct, saturating at least one additional naphtha/hydrocarbon stream together with the hydrotreated pyrolysis gasoline stream or together with the light pyrolysis oil byproducts to form a first naphthene stream, and steam cracking the first naphthene stream to produce olefins.

Process for producing olefins using aromatic saturation

A process for hydrocracking 2,4-dimethylpentane and/or 2,2,3-trimethylbutane can comprise: contacting a hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst, wherein the hydrocracking feed stream comprises at least 0.5 wt % of 2,4-dimethylpentane and/or 2,2,3-trimethylbutane, based upon a total weight of the hydrocracking feed stream; and wherein the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75; preferably the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75 and a large pore zeolite having a pore size of 6-8 A and a silica to alumina molar ratio of 10-80, wherein the hydrogenation metal is deposited on the medium pore zeolite and the large pore zeolite.

Hydrocracking process

The invention relates to a process for preparing a hydrocracking catalyst, comprising (i) contacting a shaped body comprising a zeolite and a binder with an aqueous solution of a hydrogenation metal compound which is a complex or a salt of a hydrogenation metal to deposit the hydrogenation metal onto the shaped body, wherein the aqueous solution comprises an ammonium salt and (ii) calcining the shaped body obtained by step (i).

Process for preparing hydrocracking catalyst

The present invention relates to a process for producing monoaromatic hydrocarbons from a hydrocarbon feed comprising polyaromatics, the process comprising contacting said feed in the presence of hydrogen with a M/zeolite catalyst under hydrocracking process conditions.

Process for producing aromatics from a heavy hydrocarbon feed

The present invention relates to a process for producing monoaromatic hydrocarbons from a hydrocarbon feed comprising polyaromatics, the process comprising contacting said feed in the presence of hydrogen with a M/A/zeolite catalyst under hydrocracking process conditions.

The present invention relates to a process for producing benzene from a mixed hydrocarbon feedstream comprising subjecting C6 cut separated from said mixed hydrocarbon feedstream to aromatization to provide a benzene-rich aromatic stream and recovering the benzene from the benzene-rich aromatic stream.

Process for producing purified aromatic hydrocarbons from a mixed hydrocarbon feedstream

An integrated process for forming a combined feedstock stream comprising catalytically cracking a first hydrocarbon feedstock to form a full range cracked full naphtha stream and a first light olefins stream, steam cracking a second hydrocarbon feedstock to form a pyrolysis gasoline stream and a second light olefins stream mixing at least a portion of each of the full range cracked naphtha stream and the pyrolysis gasoline stream to form a combined stream, hydro-processing the combined stream to form a hydro-processed combined stream splitting the hydro-processed combined stream into a C/Cstream, and a first aromatic rich stream, splitting the first aromatic rich stream into a second aromatic rich stream and a heavy oil stream.

Method of co-processing fluidized catalytic cracking naphtha and pyrolysis gasoline

A process comprising contacting said feed in the presence of hydrogen with a M/zeolite catalyst under hydrocracking process conditions.

Process for producing LPG from a heavy hydrocarbon feed

In an aspect, a method for the aromatization of hydrocarbons comprises contacting a hydrocarbon feedstream with a catalyst; wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide.

Catalyst with improved activity/selectivity for light naphtha aromatization

An integrated process for increasing olefin production is described through which heavy cracker residues of fluid catalytic cracking unit and steam cracking unit are completely mixed, and mixed stream is properly recycled and further combined with atmospheric tower bottoms. Combined stream is deasphalted and hydrotreated to produce a proper feedstock for steam cracking unit for manufacturing light olefin compounds. The integrated process produces higher amount of light olefins than a substantially similar process without processing the heavy cracker residues.

Integrated process for increasing olefin production by recycling and processing heavy cracker residue

Growing community of inventors

Sugar Land, TX, United States of America

Scott A Stevenson