Uop Lcc

Honeywell International Inc.

Robert J Schmidt

Deng-Yang Jan

James A Johnson

Paula L Bogdan

Terry L Marker

Robert S Haizmann

Tamotsu Imai

Laurence O Stine

R Joe Lawson

Steven P Lankton

Richard E Marinangeli

J W Sachtler

Russell C Schulz

Paul J Kuchar

Stanley Joseph Frey

Andrew S Zarchy

Constante P Tagamolila

Beth McCulloch

Paul Alvin Sechrist

Gregory J Gajda

Srikantiah Raghuram

Mathias P Koljack

Raelynn M Miller

Mark M Davis

Patrick Jerome Bullen

William Bachop Dolan

Lynn H Rice

Michael B Russ

Carl John Stevens

Debarshi Majumder

Guy B Woodle

Thomas M Reynolds

Frank H Adams

Michael E Fettis

John J Jeanneret

Mark R Ford

Christopher J Garrett

Elena Z Maurukas

Gary A Peterson

C David Low

Paul T Barger

Xin X Zhu

David A Wegerer

Jennifer S Holmgren

Timothy A Brandvold

Christopher D Gosling

Leonid B Galperin

Susie C Martins

Trung S Pham

Avram Michael Buchbinder

Kurt A Detrick

Michael R Smith

Randy J Lawson

Robert E Tsai

Scott R Keenan

Pelin Cox

Chad A Williams

Praneeth Dayanthe Edirisinghe

Charlotte Y Fang

Heather D Tsihlis

Jose L Miramontes

Allyn T Gilbert

Norman L Gilsdorf

Richard E Marinageli

Russell C Schultz

One or more processes for recovering entrained ionic liquid from a hydrocarbon phase containing droplets of ionic liquid are described. The processes includes contacting the hydrocarbon phase containing the droplets of ionic liquid with a retaining material in a separation zone. The droplets of ionic liquid are retained by the retaining material. The ionic liquid may be recovered from the retaining material with a solvent or desorbent. The retaining material may be regenerated and the ionic liquid may be reactivated. The retaining material may be used in a wash vessel to retain or remove contaminant solids within the reactor or other vessels.

Processes for removing entrained ionic liquid from a hydrocarbon phase

This present disclosure relates to processes and apparatuses for use of a single dividing wall distillation column for phenol fractionation. More specifically, the present disclosure relates to processes and apparatuses for phenol fractionation by combining crude acetone column and cumene-AMS column into a single dividing wall distillation column. The proper allocation of steam or water injection, chemical treatment reactor and internal liquid phase separator, the positioning of the side draw enables high yield of acetone and phenol.

Methods and apparatuses for phenol fractionation in a single dividing wall column

Byproduct formation in aromatic alkylation processes is reduced when different polyalkylated aromatic compounds are first fractionated into separate streams enriched in these respective polyalkylated aromatic compounds, and the separate streams are sent to different transalkylation reaction zones, which may or may not be in the same reactor. The different transalkylation reaction zones allow for greater control of the transalkylation of the respective polyalkylated aromatic compounds, such as diisopropylbenzene (DIPB) and triisopropylbenzene (TIPB) that accompany the alkylation of benzene with propylene in a process for cumene production.

Aromatic alkylation process with reduced byproduct formation

A method for alkylation of a feedstock is described. The method includes contacting the feedstock comprising at least one alkylatable aromatic compound and an alkylating agent with a first alkylating catalyst composition under alkylating conditions, the first alkylating catalyst composition comprising UZM-8 zeolite and a binder, the first alkylating catalyst composition having less than 50 wt% UZM-8 zeolite; wherein a total alkylated selectivity at a temperature and a molar ratio of alkylatable aromatic compound to alkylating agent is greater than 99.0%.

Highly selective alkylation process with low zeolite catalyst composition

A aromatic alkylation catalyst, processes for producing the catalyst, and aromatic alkylation processes employing the catalysts are disclosed. The catalyst comprises a UZM-8 zeolite and nitrogen, and the catalyst has a nitrogen to zeolite aluminum molar ratio of at least about 0.015. In an exemplary alkylation process, the catalyst provides improved product yield.

Aromatic alkylation catalyst

Processes for preparing alkylation aromatic compounds are provided herein. In an embodiment, a process for preparing alkylated aromatic compounds includes reacting an aromatic compound and an olefin in a first alkylation reaction in the presence of a first alkylation catalyst to produce a first effluent that includes an alkylated aromatic compound and unreacted aromatic compound. Unreacted aromatic compound from the first effluent and additional olefin are reacted in at least one downstream alkylation reaction in the presence of a second alkylation catalyst to produce a second effluent including the alkylated aromatic compound. A recycle stream including the alkylated aromatic compound is recycled from the second effluent to the at least one downstream alkylation reaction and, optionally, the first alkylation reaction. A ratio of the recycle stream to a total mass flow is greater in the at least one downstream alkylation reaction than in the first alkylation reaction.

Processes for preparing alkylated aromatic compounds

Processes for preparing alkylation aromatic compounds are provided. One process for preparing alkylated aromatic compounds includes reacting an aromatic compound and an olefin in at least one primary alkylation reaction in the presence of a first alkylation catalyst to produce a first effluent. The first effluent is split into a first product-rich stream and a first recycle stream, and the first recycle stream is recycled to the at least one primary alkylation reaction. Unreacted aromatic compound from the first product-rich stream and an additional olefin are reacted in at least one downstream alkylation reaction in the presence of a second alkylation catalyst to produce a second effluent. The second effluent is split into a second product-rich stream and a second recycle stream, and the second recycle stream is recycled to the at least one primary alkylation reaction and, optionally, to the at least one downstream alkylation reaction.

Cumene production methods are disclosed, based on the alkylation of benzene with propylene, in which byproducts of the alkylation reaction are advantageously reduced to achieve a high cumene selectivity. This may be attained by (i) reducing the portion of the total alkylation effluent that is recycled, after cooling, to the alkylation reaction zone for quenching or direct heat exchange and/or (ii) reducing the benzene:propylene molar ratio of the alkylation feedstock. To manage the temperature differential across catalyst bed(s) in the alkylation reaction zone, indirect heat exchange may be used to remove heat.

Cumene production with high selectivity

The present invention provides a process for decomposing a cumene hydroperoxide to produce phenol and acetone. The process utilizes a solid catalyst that can be non-layered or layered. The process includes: (1) introducing a process stream containing cumene hydroperoxide into a reaction vessel; (2) contacting the process stream with catalyst particles to form a process stream; and (3) withdrawing a portion of the product stream from the reactor and recovering phenol and acetone products.

Solid acid catalyst and process for decomposition of cumene hydroperoxide

Disclosed is a process and apparatus for removing nitrogen compounds from an alkylation substrate such as benzene. A conventional adsorbent bed can be used to adsorb basic organic nitrogen compounds and a hot adsorbent bed of acidic molecular sieve can adsorb the weakly basic nitrogen compounds such as nitrites. Water facilitates the adsorption of the weakly basic nitrogen compounds. Running an alkylation substrate stream from a fractionation column of elevated temperature and suitable water concentration to the hot adsorbent bed may be advantageous.

Process and apparatus for the removal of nitrogen compounds from a fluid stream

A process for converting polyalkylaromatics to monoalkylaromatics, particularly cumene, in the presence of a modified LZ-210 zeolite catalyst is disclosed. The process attains greater selectivity, reduced formation of undesired byproducts, and increased activity.

Aromatic transalkylation using a modified LZ-210 zeolite

An improved alkylation reactor design is disclosed. The design uses reactor effluent recycle to reduce the difference in temperature across the reaction zone improving selectivity and insuring the maintenance of a liquid phase in the reactor.

Alkylation reactor design with effluent recycle and impure benzene regeneration

Disclosed is a process and apparatus for alkylating light olefin with benzene at near but less than full conversion of the olefin. We have found that stopping below full conversion of the olefin maximizes yield of monoalkylbenzene.

Process for the high yield production of monoalkylaromatics

A process for converting polyalkylaromatics to monoalkylaromatics, particularly cumene, in the presence of a modified LZ-210 zeolite is disclosed. The process attains greater selectivity, reduced formation of undesired byproducts, and increased activity.

Aromatic transalkylation using a LZ-210 zeolite

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Barrington, IL, United States of America

Robert J Schmidt