Catalytica, Inc.

Amoco Corporation

Standard Oil Company (indiana)

Peter H Kilner

Jere D Fellmann

Wayne P Schammel

Paul R Wentrcek

Stephen G Ceisel

Joseph P Egan, Jr

Stanley F Newman

Selective sorption of dialkylated multinuclear aromatic compounds

A process for enriching the fraction of 2,6-diisopropylnaphthalene contained in a quantity of mixed dialkylated naphthalenes. The mixed dialkylated naphthalenes are contacted with an adsorbant bed containing one or more molecular sieves which demonstrate shape selective preference for the 2,6-diisopropylnaphthalene isomer over other dialkylated naphthalenes. The adsorbant bed is then contacted with a desorbant capable of desorbing the 2,6-diisopropylnaphthalene from the pores of the adsorbant.

Selective sorption of 2,6-diisopropylnaphthalene

A process for the selective manufacture of 2,6-diisopropylnaphthalene from naphthalene advantageously combines an equilibration reactor to enhance the amount of monoisopropylnaphthalene fed to the alkylation reactor, and the use of a shape selective catalyst in the alkylation reactor, to obtain an alkylation reaction product in which the 2,6-diisopropylnaphthalene isomer comprises greater than 39 mole percent of the total diisopropylnaphthalene obtained. Further, this combination of reaction steps and conditions produces a reaction product in which the ratio of 2,6-diisopropylnaphthalene to 2,7-diisopropylnaphthalene is greater than 1.0, preferably greater than 1.2. Recycled process components are fed to the equilibration reactor where they are combined with fresh naphthalene feed to provide a monoisopropylnaphthalene enriched feed to the alkylation reactor.

Process for selective manufacture of 2,6-diisopropylnaphthalenes with

A process for the oxidation of pseudocumene to trimellitic acid anhydride is disclosed which comprises catalytic oxidation of pseudocumene with air in the presence of acetic acid in an oxidation zone in the liquid phase wherein the weight ratio of acetic acid to pseudocumene is in the range of about 0.5-4.0:1.0 and the catalyst comprises one or more heavy metal oxidation catalysts comprising zirconium, cobalt, and manganese to provide about 0.1 to about 0.4 weight percent total metals based on pseudocumene and a source of bromine. The addition of the bromine component is controlled to provide a total of about 0.10 to about 0.30 weight percent total bromine based on pseudocumene. The total weight ratio of bromine ions to total metals ions is about 0.5 to about 2.0. The zirconium content is about 1 to about 5% and the manganese content is about 14 to about 60% each by weight of the total metals. The reaction temperature is about 100.degree. C. to about 250.degree. C. The acetic acid and water of reaction are withdrawn during the last 5 to about 20% of the reaction.

Process for the production of trimellitic anhydride

A process for the oxidation of pseudocumene to trimellitic acid anhydride which comprises catalytic oxidation of pseudocumene with air in the presence of acetic acid in an oxidation zone in the liquid phase and wherein the weight ratio of acetic acid to pseudocumene is in the range of about 1.0-2.5:1.0 and the catalyst comprises one or more heavy metal oxidation catalysts comprising zirconium, cobalt and manganese to provide about 0.2 to about 0.4 weight percent total metals based on pseudocumene and a source of bromine. The addition of the bromine component is controlled to provide a total of about 0.10 to about 0.30 weight percent total bromine based on pseudocumene. The total weight ratio of bromide ions to total metals ions is about 0.7 to about 2.0. The zirconium content is about 1 to about 5% and manganese content is about 14 to about 24% each by weight of the total metals. The reaction temperature is about 100.degree. C. to about 250.degree. C. The acetic acid and water of reaction are withdrawn during the last 5 to about 20% of the reaction.

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Sunnyvale, CA, United States of America

Peter H Kilner