Saudi Basic Industries Corporation

Fina Technology, Inc.

Sabic Global Technologies B.v.

Other

Ghosh, Ashim Kumar

Harvey, Pamela

Ashim Kumar Ghosh

Pamela Lawyer Harvey

Neeta Kulkarni

James R Butler

Scott A Stevenson

Edwar Shoukri Shamshoum

Alla Konstantin Khanmamedova

Mohammad Shafiei

James T Merrill

Gopalakrishnan G Juttu

Thomas R Schuler

Manuel Castelan

Michael Mier

Mohamed Elbaccouch

Mike Mier

David Sullivan

Roncalli J Twomey

Murali Gopalakrishnan

Corina Mihut

Meghann Simmons

Ravichander Narayanaswamy

Peter Loezos

Krishna Kumar Ramamurthy

Dustin Fickel

Pooja Bajaj

Luis Aramburo

Alexander Stanislaus

Dustin Farmer

Jonathan Banke

Girish Koripelly

David L Sullivan

Santosh Ganji

Frederick Merrill Galloway, Jr

Heng Shou

Abrar A Hakeem

Raul Velasco Pelaez

Katherine Barton

Balamurali Krishna Nair

Mohammad Javeed

MyatNoeZin Myint

Cong Nguyen

Prasanna Dasari

Pamela Lawyer-Harvey

Meghan Simmons

Peter N Loezos

Pamela Sabic Technology Center Harvey

A hydrogenolysis bimetallic supported catalyst comprising a first metal, a second metal, and a zeolitic support; wherein the first metal and the second metal are different; and wherein the first metal and the second metal can each independently be selected from the group consisting of iridium (Ir), platinum (Pt), rhodium (Rh), ruthenium (Ru), palladium (Pd), molybdenum (Mo), tungsten (W), nickel (Ni), and cobalt (Co).

Bimetallic catalysts supported on zeolites for selective conversion of n-butane to ethane

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 method of producing a purified mixed xylene comprising: introducing toluene and methanol to an alkylation reactor; reacting the toluene and the methanol in the alkylation reactor to form a hydrocarbon stream comprising a first mixed xylene, wherein the alkylation reactor comprises an alkylation catalyst; separating the hydrocarbon stream into a toluene stream and a separated Cstream; introducing the toluene stream to a transalkylation reactor with a transalkylation catalyst to produce a transalkylated stream comprising a second mixed xylene; adding the transalkylated stream to the hydrocarbon stream; and separating a Cproduct stream comprising the purified mixed xylene from the separated Cstream.

Toluene methylation with transalkylation of heavy aromatics

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

A process for processing mixed plastics comprising simultaneous pyrolysis and dechlorination of the mixed plastics, the process comprising contacting the mixed plastics with a zeolitic catalyst in a pyrolysis unit to produce a hydrocarbon product comprising a gas phase and a liquid phase; and separating the hydrocarbon product into a hydrocarbon gas stream and a hydrocarbon liquid stream, wherein the hydrocarbon gas stream comprises at least a portion of the gas phase of the hydrocarbon product, wherein the hydrocarbon liquid stream comprises at least a portion of the liquid phase of the hydrocarbon product, wherein the hydrocarbon liquid stream comprises one or more chloride compounds in an amount of less than about 100 ppmw chloride, based on the total weight of the hydrocarbon liquid stream, and wherein the hydrocarbon liquid stream is characterized by a viscosity of less than about 400 cP at a temperature of 300&#xb0; C.

Catalytic process of simultaneous pyrolysis of mixed plastics and dechlorination of the pyrolysis oil

Disclosed herein is a process for preparing a hydrocracking catalyst, comprising (i) combining a zeolite, a binder, water and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal to obtain a mixture, wherein the zeolite has not been treated with a phosphorus-containing compound and the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the mixture into a shaped body; and (iii) calcining the shaped body to form the catalyst.

In one embodiment, a formed catalyst can comprise: a Ge-ZSM-5 zeolite; a binder comprising silica with 1 to less than 5 wt % non-silica oxides; less than or equal to 0.1 wt % residual carbon; 0.4 to 1.5 wt % platinum; and 4.0 to 4.8 wt % Cs; wherein the weight percentages are based upon a total weight of the catalyst. In one embodiment, a method of making a formed catalyst can comprise: mixing an uncalcined Ge-ZSM-5 zeolite and a binder to form a mixture; forming the mixture into a formed zeolite; calcining the formed zeolite to result in the formed zeolite having less than or equal to 0.1 wt % of residual carbon; ion-exchanging the formed zeolite with cesium; depositing platinum on the formed zeolite; and heating the formed zeolite to result in a final catalyst; wherein the final catalyst comprises 4.0 to 4.8 wt % cesium and 0.4 to 1.5 wt % platinum.

Method of preparing hydrocarbon aromatization catalyst, the catalyst, and the use of the catalyst

A method of producing a purified mixed xylene comprising: introducing toluene and methanol to an alkylation reactor (); reacting the toluene and the methanol in the alkylation reactor () to form a hydrocarbon stream () comprising a first mixed xylene, wherein the alkylation reactor () comprises an alkylation catalyst; separating the hydrocarbon stream () into a toluene stream () and a separated Cstream (); introducing the toluene stream () to a transalkylation reactor () with a transalkylation catalyst to produce a transalkylated stream () comprising a second mixed xylene; adding the transalkylated stream () to the hydrocarbon stream (); and separating a Cproduct stream () comprising the purified mixed xylene from the separated Cstream ().

Disclosed is a method for converting an alkyl halide to an olefin. The method includes contacting a silicoaluminophosphate (SAPO) catalyst with a feed that includes an alkyl halide under reaction conditions sufficient to produce an olefin hydrocarbon product that includes Cto Colefins. The SAPO catalyst has bimodal acidity designated as weak acid sites and strong acid sites. The weak acid concentration is less than 0.55 mmol/g-cat and the total acid concentration is less than 1.5 mmol/g-cat.

Stable silicoaluminophosphate catalysts for conversion of alkyl halides to olefins

A method for forming a catalyst can comprise: heating a Ge-ZSM-5 zeolite powder at a temperature of 400 to 600&#xb0; C.; ion-exchanging the heat-treated zeolite powder with an alkali metal and impregnating the heat-treated zeolite powder with noble metal; heating the ion-exchanged, impregnated zeolite powder to a temperature of 250 to 350&#xb0; C.; mixing the second heat-treated zeolite powder with a solid silica binder and a colloidal silica binder to form a mixture, wherein if the solid silica has a purity of less than or equal to 66 wt % of silica oxide based on the total weight of the solid silica, then the mixture is free of an extrusion aide and the colloidal silica has a particle size of less than 20 nm as measured along a major axis; forming the mixture into a shaped body; and heating the shaped body to 100 to 350&#xb0; C. to result in the catalyst.

Hydrocarbon aromatization catalyst composition and method of formation

In an embodiment, a method of forming a catalyst can comprises: treating a detemplated pentasil zeolite material with a phosphorus-containing compound to form a phosphorus treated zeolite; combining a hydrogenating material, the phosphorus treated zeolite, and a binder material to form a mixture; forming the mixture into a shaped body, wherein the mixture is formed into the shaped body without the mixture being heat-treated; and calcining the shaped body to form the catalyst. Combining the hydrogenating material with the phosphorus treated zeolite and the binder material occurs prior to forming of the shaped body.

Method of making a catalyst and catalyst made thereby

A method of modifying a phosphorus-treated zeolite catalyst is carried out by contacting an unbound and calcined phosphorus-treated pentasil zeolite with water in a water treatment wherein at least a portion of the water is in a liquid phase. The water treatment is sufficient to remove at least 80% by weight or more of phosphorus from the phosphorus-treated zeolite and provide an increase in the pore volume of the zeolite by at least 50% prior to the water treatment to form a modified phosphorus-treated zeolite catalyst. A zeolite catalyst is also provided in the form of a phosphorus-containing pentasil zeolite having a phosphorus content of 7.5% or less by weight of zeolite and aAl MAS NMR peak at 50 ppm that is greater than any otherAl MAS NMR and a pore volume of 0.2 ml/g or more.

Method of modifying a phosphorus-containing zeolite catalyst

Methods for preparing bound non-acidic germanium zeolite catalysts are disclosed, where the preparation is reproducible and scalable and where the catalysts have similar or the same activity and selectivities of a standard naphtha aromatization catalyst and methods for aromatizing naphtha.

Catalyst for light naphtha aromatization

A method of forming a zeolite shaped body is carried out by preparing an aqueous mixture containing a zeolite, a silica binder material and an extrusion aid. The extrusion aid is at least one of PVAc-PVA1 (80-89) and polyacrylamide. The mixture is formed into a body having a selected shape. The shaped body is heated to form the zeolite shaped body.

Method of forming zeolite shaped body with silica binder

Growing community of inventors

Houston, TX, United States of America

Ashim Kumar Ghosh