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Bryan K Glover

Andrea G Bozzano

Tom N Kalnes

Stephen W Sohn

Daniel H Wei

Xin X Zhu

Mark G Riley

William Yanez

Robert E Tsai

Bipin Virpal Vora

Dean E Rende

Gavin Paul Towler

Paul T Barger

John Joseph Senetar

Antoine Negiz

Peter R Pujado

Robert S Haizmann

Joseph Edward Zimmermann

Timur V Voskoboynikov

Mohamed S Shakur

Tokhanh Ngo

Santi Kulprathipanja

Paul Alvin Sechrist

Michael A Schultz

Christopher D Gosling

Robert B James

James W Priegnitz

Michael Jerome Vetter

Norman H Scott

Wei Pan

Mary Jo Wier

Ka Leung Lok

Guy B Woodle

Feng Xu

Eleftherios Adamopoulos

Alexander V Sabitov

Stephen M Casey

Julie A Zarraga

Alakananda A Bhattacharyya

Paolo Palmas

Terry L Marker

Jeffery C Bricker

John Qianjun Chen

Daniel N Myers

Keith Allen Couch

Mark Paul Lapinski

Soumendra Mohan Banerjee

Rajeswar R Gattupalli

John Anthony Petri

Susie C Martins

Robert B Larson

Douglas A Nafis

Stuart Smith

Debarshi Majumder

Gautam Pandey

Priyesh Jayendrakumar Jani

Jeffrey R Grott

Deepak Bisht

David S Lafyatis

Brian S Muldoon

Rebecca Mudrock

Mohamed S M Shakur

Wim Frans Elseviers

Jennifer J Ozmen

Hosoo Lim

Lester F Smith, Jr

Aronson L Huebner

Michael W Penninger

Joel S Paustian

Michael A Moore

Amit Sharma

Nishesh Garg

Jalesh Kalra

Marina Minin

Gary A Marr

Stephen Wayne Sohn

A regenerator vessel for adsorbing halogen-containing material from a regenerator vent gas stream has a plurality of catalyst nozzles disposed at a top portion of the regenerator vessel. A first gas outlet is associated with a chlorination zone, and a second gas outlet associated with a combustion zone. A drying zone is in fluid communication with an air heater and the drying zone located in a bottom portion of the regenerator vessel. The first gas outlet is configured to withdraw a first gas stream from the chlorination zone and the second gas outlet is configured to withdraw a second gas stream from the combustion zone. The top portion of the regenerator vessel has an adsorption zone having a vent gas inlet port, a vent gas outlet port, and a portion of an annular catalyst bed.

Regeneration vessel adsorption zone and process for adsorbing halogen-containing material and sampling catalyst

This present disclosure relates to processes and apparatuses for removing contaminants from hydrogen streams. More specifically, the present disclosure relates to processes and apparatuses wherein hydrogen is used in units that utilize catalysts that are sensitive to oxygenates. The contaminants like carbon oxides and water are removed simultaneously from the hydrogen stream to provide a rich hydrogen stream with high purity to units that utilizes catalysts that are sensitive to oxygenates.

Processes and apparatuses for removing contaminants from hydrogen streams

Processes for the production of a gasoline blend. A Cportion of a naphtha stream is first isomerized to increase the branched, iso-paraffins, and then, the isomerized effluent is passed to a dehydrogenation reaction zone. In the dehydrogenation zone, the Csaturated hydrocarbons are convert to Colefins. The Colefins have a higher octane number than the Csaturated hydrocarbons, and the branched olefins have a higher octane number than the normal olefins. The Colefins can be blended in a gasoline pool. Cand Chydrocarbons can be isomerized and dehydrogenated as well, separately or with the Ccomponents.

Processes for increasing an octane value of a gasoline component

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

Process for producing a naphtha stream

A reforming reactor and process of using same in which residence time of feed within a chamber of a reactor is shortened. Feed is injected into the reactor into a non-reactive zone. The non-reactive zone has two portions, a first portion receiving the feed, and a second portion receiving a purge gas. The purge gas will flow from the second portion to the first portion to prevent flow of the feed from the first portion to the second portion. The combined gas may be passed to a reaction zone for catalytic reforming. The first portion and the second portion may be separated by a baffle.

Process for increasing hydrocarbon yield from catalytic reformer

An integrated process for gasoline production is described. The process includes introducing a feed comprising n-Chydrocarbons into a disproportionation reaction zone in the presence of a disproportionation catalyst to form a disproportionation mixture comprising iso-Cand Cdisproportionation products and unreacted n-Chydrocarbons. An iso-Chydrocarbon stream and an olefin feed are introduced into an alkylation reaction zone in the presence of an alkylation catalyst to produce an alkylation mixture comprising alkylate and unreacted iso-Cparaffins. The disproportionation mixture and the alkylation mixture are combined, and the combined mixture is separated into at least a stream comprising the alkylate product, an iso-Cstream, and an unreacted n-Chydrocarbon stream. The iso-Cstream is recycled to the alkylation reaction zone, and the unreacted n-Chydrocarbon stream is recycled to the disproportionation reaction zone. The stream comprising the alkylate product is recovered.

Integrated process for gasoline production

The present disclosure generally relates to methods and systems for reforming and isomerizing hydrocarbons. More particularly, the present disclosure relates to a novel combination of two traditionally separate reforming and isomerization reaction zones. A first hydrocarbon stream comprising C-Chydrocarbons is isomerized in a first isomerization zone. A second hydrocarbon stream comprising Chydrocarbons is reformed thus producing a Chydrocarbon stream and a Chydrocarbon stream. The reformed Cstream is then isomerized in a second isomerization zone.

Methods and apparatuses for an integrated isomerization and platforming process

A process for regenerating catalyst particles is disclosed. The process includes the steps: (a) withdrawing a regeneration zone effluent comprising halogen from a regeneration zone, wherein the regeneration zone contains catalyst particles comprising halogen; (b) contacting a first portion of the regeneration zone effluent with adsorbent in a first adsorption zone, removing halogen from the first portion of the regeneration zone effluent, and withdrawing from the first adsorption zone a first adsorption zone effluent; (c) contacting the first adsorption zone effluent with a water removing material to create a first water-depleted stream; and (d) passing the first water-depleted stream to the regeneration zone. Other embodiments include different orders of the steps.

Process for regenerating catalyst particles

Embodiments of apparatuses and methods for reforming of hydrocarbons including recovery of products are provided. In one example, a method comprises separating a reforming-zone effluent to form a net gas phase stream and a liquid phase hydrocarbon stream. The net gas phase stream is compressed, partially condensed and cooled to form a partially condensed, compressed net gas phase stream. The partially condensed, compressed net gas phase stream is separated to form an intermediate gas phase stream. The intermediate gas phase stream is cooled to form a cooled intermediate gas phase stream. The liquid phase hydrocarbon stream is cooled to form a cooled liquid phase hydrocarbon stream. The cooled intermediate gas phase stream is contacted with the cooled liquid phase hydrocarbon stream to form an H-rich stream and a cooled second intermediate liquid phase hydrocarbon stream that is enriched with C/Chydrocarbons.

Methods and apparatuses for reforming of hydrocarbons including recovery of products using an absorption zone

Embodiments of apparatuses and methods for reforming of hydrocarbons including recovery of products are provided. In one example, a method comprises separating a reforming-zone effluent to form a net gas phase stream and a liquid phase hydrocarbon stream. The net gas phase stream is compressed, partially condensed and cooled, and separated to form an intermediate gas phase stream. The intermediate gas phase stream is cooled to form a cooled intermediate gas phase stream. The liquid phase hydrocarbon stream is cooled to form a cooled liquid phase hydrocarbon stream. The cooled intermediate gas phase stream is contacted with the cooled liquid phase hydrocarbon stream to form an H-rich stream and a cooled second intermediate liquid phase hydrocarbon stream that is enriched with C/Chydrocarbons. The H-rich stream is contacted with an adsorbent to form an H-ultra rich stream.

Methods and apparatuses for reforming of hydrocarbons including recovery of products using an absorption zone and a pressure swing adsorption zone

One exemplary embodiment can be a process for catalytic reforming. The process can include catalytically reforming a hydrocarbon feed in a reaction zone, obtaining an effluent stream having hydrogen and hydrocarbons from the reaction zone, obtaining from at least a portion of the effluent stream a waste hydrocarbon stream from an adsorption zone, passing at least a portion of the waste hydrocarbon stream as a feed stream across a feed side of a membrane having the feed side and a permeate side, and being selective for hydrogen over one or more C1-C6 hydrocarbons, and withdrawing from the permeate side a permeate stream enriched in hydrogen compared with a residue stream withdrawn from the feed side.

Process for catalytic reforming

Embodiments of apparatuses and methods for reforming of hydrocarbons including recovery of products are provided. In one example, a method comprises separating a reforming-zone effluent into a net gas phase stream and a liquid phase hydrocarbon stream. The net gas phase stream is separated for forming an H-rich stream and a first intermediate liquid phase hydrocarbon stream. The H-rich stream is contacted with an adsorbent to form an H-ultra rich stream and a PSA tail gas stream. The PSA tail gas stream is contacted with an H/hydrocarbon separation membrane to separate the PSA tail gas stream and form an H-ultra rich permeate stream and a PSA tail gas hydrocarbon-containing non-permeate residue stream.

Methods and apparatuses for reforming of hydrocarbons including recovery of products using a recovery zone, a pressure swing adsorption zone, and a membrane separation zone

Processes for making Cto Colefins are provided. The processes include reacting a feedstock comprising Cand Colefins under dimerization or oligomerization conditions to provide a dimerization or oligomerization product. The product is separated into a stream comprising unreacted Cand Cparaffins, a stream comprising Cto Colefins, and a stream comprising Cto Colefins, wherein X is at least 14 and Y is greater than X and less than or equal to 36.

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Methods and systems for reforming and transalkylating hydrocarbons are disclosed. A method for processing a hydrocarbon stream includes the steps of separating para-xylene from a first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream and isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene. The method further includes transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream, separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream, and isomerizing the second non-equilibrium xylene and ethylbenzene stream using an ethylbenzene dealkylation type xylene isomerization process to produce additional para-xylene.

Methods and systems for reforming and transalkylating hydrocarbons

Growing community of inventors

Algonquin, IL, United States of America

Bryan K Glover