Exxon Research and Engineering Company

Exxon Chemical Patents, Inc.

Other

Fmc Corporation

Exxonmobil Chemicals Patents, Inc.

Robert C Michaelson

Richard G Austin

Richard S Myers

Ramzi Yanni Saleh

Gustavo Cerri

Elena N Suciu

Donald A White

Barbara Kuhlmann

Richard Henry Schlosberg

Christopher Lynn Becker

Jeffrey S Plotkin

Ji-Yong Ryu

George A Knudsen

Dan E Hendriksen

Daniel D Rosenfeld

Di-Yi (John) Ou

John J Cikut

Daniel R Mills

Terry A Fons

Alkyl aromatic compounds are converted to alkyl aromatic aldehydes by a carbonylation reaction. The carbonylation catalyst can be a high boiling point carbonylation catalyst which allows for the separation of the aldehyde product by selective volatilization. Alternatively, the carbonylation catalyst can be selected from perfluoroalkyl sulfonic acids having 2 to 18 carbon atoms, perfluoroether sulfonic acids having 2 to 18 carbon atoms, BF,(ROH),wherein R represents CH,or H and X is a number within the range of from 0.2 to 2, GaBr,, GaCl,, TaF,, NbF,, and NbBr,, with the proviso that when the catalyst is TaF,, NbF,, or NbBr,, then the reaction takes place in the absence of added HF. Preferably, all of the carbonylation reactions take place in the absence of added HF. The alkyl aromatic aldehydes can be oxidized to form an aromatic acid. A mixed xylene feed stock can be converted to a mixture of dimethylbenzaldehydes and then oxidized to form trimellitic acid without the need to separate the xylene or dimethylbenzaldehyde isomers.

Process for making aromatic aldehydes

A process for making a dialkyl carbonate which comprises reacting urea with a first alcohol in a carbamate reactor at a temperature and pressure sufficient to convert said urea to an alkyl carbamate; and reacting the alkyl carbamate with a second alcohol in the presence of a dialkyl isocyanato alkoxy tin catalyst or derivatives in a carbonate reactor at a temperature and pressure sufficient to convert the alkyl carbamate to a dialkyl carbonate, wherein the molar ratio of alkyl carbamate to second alcohol is in the range between about 2:1 to about 10:1 and wherein dialkyl carbonate is present within the carbonate reactor in an amount between about 1 to about 3 weight %, based on total alkyl carbamate and second alcohol content, and wherein the second alcohol is either the same as or different from the first alcohol or a mixture of alcohols.

Process for manufacturing dialkyl carbonate from urea and alcohol

Dialkyl isocyanato tin alcoholate catalysts and dimers thereof

A process for making a catalyst product which comprises reacting dialkyltin oxide with an alcohol and the corresponding dialkyl carbonate at a temperature in the range between about 50.degree. to 200.degree. C. and at a pressure in the range between about 75 to 600 psi (0.52 to 4.14 MPa), wherein the catalyst product comprises dialkyltin dialkoxide in the range between about 90 to 100 mole % based on the tin species of the catalyst product. This process also forms effective catalyst product when the methanol is replaced with either a primary or secondary alcohol.

Process for the preparation of dialkyltin dialkoxide

A process for regenerating a catalyst which involves washing a catalyst with a liquid at a temperature within the range of about 50.degree. C. to about 70.degree. C. for a time sufficient to remove foulants thereby recovering catalyst activity. The wash liquid is preferably a member selected from the group consisting of ethers, alcohols and mixtures of ethers and alcohols wherein the ether is a tertiary alkyl ether, preferably selected from the group consisting of tertiary amyl methyl ether and methyl tertiary butyl ether, and wherein the alcohol is preferably selected from the group consisting of tertiary butyl alcohol and methanol. The catalyst is preferably a clay treated with an acid selected from the group consisting of hydrofluoric acid, hydrochloric acid and mixtures of hydrofluoric and hydrochloric acid, wherein the clay is preferably selected from the group consisting of montmorillonite, kaolinite, attapulgite, bentoninte and natural clay.

Process for regenerating a catalyst used in production of olefins by

The present invention is directed to a process for producing dienes which involves reacting a reaction mixture of tertiary alkyl ether and a source of oxygen over two functionally distinct catalysts under reaction conditions sufficient to produce high yields of the dienes with minimal recycle of the ether. The two functionally different catalysts are selected from a group of bifunctional catalysts having both oxidation sites and acidic sites and monofunctional acidic catalysts, such as bifunctional catalysts containing components selected from a group of oxides of vanadium, tungsten, molybdenum, copper, iron, chromium, and uranium and mixtures thereof; and monofuctional acid catalysts such as acid treated montmorillonite clays, and acid catalysts comprising an inorganic amorphous or substantially amorphous oxide material comprising the following components reacted therein:

Isoprene process

A method for producing alkyl tertiary alkyl ether involves supplying a feed including isoolefins, alcohols, and dialkyl sulfides into a feed zone of a reactor; contacting the feed with a catalyst material in the reaction zone; and catalytically reacting the isooolefins and alcohols under conditions which favor forming resultant ether and inhibiting reaction of dialkyl sulfides with the catalyst material.

Minimizing deactivation of ether synthesis catalyst

A catalyst system for codimerization of alpha-monoolefins and conjugated diolefins to yield 1,4-dienes. The catalyst system includes at least one ruthenium salt and at least one aluminum halide. Suitable aluminum halides include both alkyl aluminum halides and nonalkylated aluminum halides, as well as mixtures thereof.

Ruthenium salt and aluminum halide catalyst system for codimerization of

A method for increasing the ratio of 2-methyl-2-butene (2MB2) to 2-methyl-1-butene (2MB1) in isoamylenes involves fractionating a feedstream containing tertiary amyl methyl ether (TAME) and isoamylenes including 2MB2 and 2MB1 in a ratio of about 2:1 to effect a separation between an overhead hydrocarbon fraction of isoamylenes including 2MB2 and 2MB1 in a ratio of about 1:1, a bottoms fraction including TAME, and a sidestream hydrocarbon fraction consisting essentially of isoamylenes including 2MB2 and 2MB1 in a ratio of about 6 to 12:1, recovering the sidestream hydrocarbon fraction, and recycling the overhead hydrocarbon fraction of isoamylenes to form a mixture which is subsequently reacted to form the feedstream. Prior to fractionation, the feedstream is formed by passing isoamylene, and optionally TAME, in a vapor phase over an ether cracking catalyst which isomerizes isoamylene and converts 2MB1 to 2MB2, i.e., the feedstream for fractionating, which contains 2MB2 and 2MB1 in a ratio of 2 to 5:1. A method for converting 2-methyl-1-butene to 2-methyl-2-butene which may be used to form the feedstream for fractionating involves providing a hydrocarbon stream comprising isoamylenes including 2MB1 and 2MB2 in a ratio of within the range of 1:1 to 5, adding about TAME to the isoamylenes to form a mixture which is passed in the liquid phase at a temperature and a LHSV which favors isomerization over an acidic ion exchange resin catalyst to produce a reaction product including 2MB1, 2MB2 in a ratio of 1:6 to 12, and TAME.

Increasing the level of 2-methyl-2-butene in isoamylene

A process for regenerating a catalyst which involves washing a catalyst with a liquid at a temperature within the range of about 50.degree. C. to about 70.degree. C. for a time sufficient to remove foulants thereby recovering catalyst activity. The wash liquid is preferably a member selected from the group consisting of ethers, alcohols and mixtures of ethers and alcohols wherein the ether is a tertiary alkyl ether, preferably selected from the group consisting of tertiary amyl methyl ether and methyl tertiary butyl ether, and wherein the alcohol is preferably selected from the group consisting of tertiary butyl alcohol and methanol. The catalyst is preferably a clay treated with an acid selected from the group consisting of hydrofluoric acid, hydrochloric acid and mixtures of hydrofluoric and hydrochlorica acid, wherein the clay is preferably selected from the group consisting of montmorillonite, kaolinite, attapulgite, bentonite and natural clay.

Process for regenerating a catalyst and resultant regenerated catalyst

A process for reacting in admixture, an olefin with oxygen, CO, and water, to form a cyclic alkylene carbonate, in the presence of a catalyst composition comprising a catalytically active osmium compound, copper containing co-catalyst I (e.g. CuBr.sub.2) and a co-catalyst II (e.g. pyridine) is disclosed.

Process for preparing cyclic carbonate esters from olefins in a single

In a process for separating C.sup.4 to C.sup.7 tertiary mono-olefins(s) present in a C.sup.4 to C.sup.7 hydrocarbon mixture containing diolefins which comprises selectively reacting said tertiary mono-olefin mixture with a primary alcohol in the presence of an acid catalyst to convert it to tertiary ether(s), separating the tertiary ether(s) from the unreacted hydrocarbon mixture and containing said tertiary ether(s) in the presence of a catalyst to decompose it to tertiary olefin(s) and a primary alcohol, the improvement which comprises hydrogenating the tertiary ether(s) after it has been separated from the unreacted hydrocarbon mixture and prior to decomposition to saturate the unsaturated ether(s) formed from the diolefins present in the hydrocarbon mixture.

Tertiary olefin process

High purity tertiary olefins are obtained in extremely high yields over a sustained period by cracking alkyl tert-alkyl ethers over clay catalysts which have been treated with HF and/or HC1. Preferably temperature are 100.degree.-250.degree. C., the surface area of the catalyst is above 40 M.sup.2 /gm and the cracking step is part of a process for recovering isobutylene or isoamylene from steam cracked streams.

Production of tertiary olefins

The process for hydroxylating olefins with oxygen in the presence of water, an osmium-halide (e.g., OsBr.sub.3) catalyst and transition metal containing co-catalyst (CuBr.sub.2) is disclosed.

Process for directly hydroxylating olefins using an osmium-halide

A process for hydroxylating olefins, such as ethylene or propylene, using an osmium oxide catalyst such as OsO.sub.4, a carboxylate salt co-catalyst, such as sodium acetate, and organic hydroperoxide oxidant is disclosed.

Growing community of inventors

Kinnelon, NJ, United States of America

Robert C Michaelson