Uop Lcc

Honeywell International Inc.

Rajeswar R Gattupalli

Quan Yuan

Alakananda A Bhattacharyya

Christopher P Nicholas

Beckay J Mezza

Bryan James Egolf

Laura Elise Leonard

Michael Jerome Vetter

Haiyan Wang

Brenna E Huovie

Jason T Corradi

Matthew Martin

Mark Paul Lapinski

Gregory R Werba

Aziz A Sattar

Peter H Shafe

Clayton Colin Sadler

Soumendra Mohan Banerjee

Mohamed S Shakur

Mohammad Reza Mostofi-Ashtiani

Michael W Penninger

Charles Brabson

Stanley Joseph Frey

Bryan K Glover

Andrea G Bozzano

Timothy A Brandvold

Huping Luo

Gregory A Funk

Keith Allen Couch

Hye Kyung Timken

Jonathan Andrew Tertel

Joseph Edward Zimmermann

Patrick C Whitchurch

Jan De Ren

Christopher D DiGiulio

Carl John Stevens

Ka Leung Lok

Grant H Yokomizo

Gautam Pandey

William M Hartman

Priyesh Jayendrakumar Jani

William J Whyman

Joao Jorge Da Silva Ferreira Alves

Louis A Lattanzio

Deepak Bisht

Bong Kyu Chang

Vinayender Kuchana

J W Adriaan Sachtler

Bart Dziabala

Matthew C Cole

Rebecca Mudrock

Mohamed S M Shakur

Massimo Sangalli

Naiyl A Rashid

David A Roman

Amit Sharma

Nishesh Garg

Krishna M

Vighneswara R Kollati

Mohamad R Mostofi-Ashtiani

Alakananda Bhatacharyya

Dominic P Weber

Rajaraman Panchapakesan

A process for maximizing production of heavy naphtha from a hydrocarbon stream is disclosed. The process comprises providing a hydrocarbon feed stream comprising diesel to a separation column to provide a light diesel stream and a heavy diesel stream. The heavy diesel stream is hydrocracked in the presence of a hydrogen stream and a first hydrocracking catalyst in a first hydrocracking reactor at a first hydrocracking pressure of 13790 kPa to 17237 kPa to provide a first hydrocracked effluent stream. The light diesel stream is hydrocracked in the presence of a hydrogen stream and a second hydrocracking catalyst in a second hydrocracking reactor at a second hydrocracking pressure of 3450 kPa to 6205 kPa to provide a second hydrocracked effluent stream. At least a portion of the first hydrocracked effluent stream and at least a portion of the second hydrocracked effluent stream are fractioned to produce heavy naphtha.

Process for maximizing production of heavy naphtha from a hydrocarbon stream

Processes for the direct alkylation of ethylene with isobutane or isopentane using a highly active ionic liquid alkylation catalyst are described. Ethylene is sent to a high-temperature alkylation reactor loop, and C, C, and Colefins are routed to a low temperature alkylation reactor loop. In each reactor, the olefins are contacted with an excess of isobutane or isopentane in the presence of a highly active ionic liquid catalyst. Portions of the reactor effluent streams are fed to a common downstream catalyst separation and product fractionation sections. The remainder of the reactor effluent is recycled back to the respective alkylation reactor.

Combined process for alkylation of light olefins using ionic liquid catalysts

Processes for treating effluent streams in alkylation processes are described. One or more process streams rom HF alkylation processes, HSOalkylation processes, or ionic liquid alkylation processes can be thermally oxidized in a thermal oxidation system. The thermal oxidation system can replace at least one of the caustic wash unit, the neutralization unit, and the acid gas treatment unit.

Alkylation process with thermal oxidation system

A fired heater with a film temperature optimizer is presented. The fired heater is for heating a process fluid in process coils within the fired heater. The process coils experience high temperatures at the outlets. The film temperature optimizer includes baffles or means for changing the flow of the fired heating gas around the process coils near the coil outlets. The baffles are positioned near the process coil outlets.

Film temperature optimizer for fired process heaters

Processes for producing a gasoline blend in which Chydrocarbons are separated from a naphtha feed. The Chydrocarbons are isomerized and dehydrogenated to increase the octane value of the components therein. In order to avoid conversion of methylcyclohexane to toluene in the dehydrogenation reactor, the various processes provide flow schemes in which the methylcyclohexane bypasses the Cdehydrogenation reaction zone.

Processes for increasing an octane value of a gasoline component

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.

A process for production of gasoline comprising separating a naphtha feed in a naphtha splitter into a stream comprising i-C, a stream comprising Cand lighter boiling hydrocarbons, a Cstream comprising Chydrocarbons, and a heavy stream comprising Cand heavier hydrocarbons; isomerizing at least a portion of the stream comprising Cand lighter boiling hydrocarbons in a C-Cisomerization zone at isomerization conditions to form a C-Cisomerization effluent; dehydrogenating at least a portion of the stream comprising Chydrocarbons to form a Cdehydrogenation effluent comprising Colefins; reforming the heavy stream in a reforming zone under reforming conditions forming a reformate stream; and blending one or more of the stream comprising i-C, the C-Cisomerization effluent, the Cdehydrogenation effluent and the reformate stream to form a gasoline blend.

Dehydrogenation process for gasoline production

An apparatus for heating a process fluid is presented. The apparatus is for improving the foot-print of a fired heater and to reduce the fired heater volume. The apparatus includes a W-shaped process coil to provide for a smaller single-cell fired heater, and a fired heater with a lower profile, providing flexibility in positioning relative to downstream reactors.

Reactor and heater configuration synergies in paraffin dehydrogenation process

An apparatus for a fired heater is presented. The fired heater is designed with process coils inside a shell, and with a positioning of the burners for reducing the size of the fired heater. The shell has a general rectangular prismatic shape with combustion inlets for admitting combustion gases from the burners, and the process coils include at least two inlet ports and at least one outlet port.

Process fired heater configuration

An apparatus for a fired heater is presented. The fired heater is designed with a plurality of process coils inside a shell, and with a positioning of the burners for reducing the size of the fired heater. The shell has a general rectangular prismatic shape with combustion inlets for admitting combustion gases from the burners, and the process coils include at least two inlet ports and at least one outlet port.

Alternative coil for fired process heater

Methods and apparatus to produce alkynes are described. The method includes combusting fuel and an oxidizer in a combustion zone to create a carrier gas stream, which is accelerated to supersonic speed in an expansion zone. A feedstock material is injected into a feedstock injection zone using two or more pluralities of injection nozzles. The injection nozzles are arranged annularly. The carrier gas stream is transitioned from supersonic speed to subsonic speed to create a shockwave in a reaction zone. The reaction zone is directly connected to the feedstock injection zone, and the shockwave is created adjacent to the feedstock injection zone. The carrier gas stream and the feedstock material are simultaneously mixed and reacted.

Pyrolytic reactor and method of using

A method of making light olefins is described. The method involves producing an alkyne in a pyrolysis process. The alkyne is catalytically hydrogenated in a hydrogenation zone to produce a product stream containing a light olefin. A byproduct stream from the pyrolysis process comprises carbon oxide and hydrogen. The byproduct stream is treated to convert the carbon oxide and the hydrogen to an oxygenated product in a carbon oxide conversion zone, which can then be converted to an olefin in an oxygenate to olefin process.

Integrated pyrolysis and oxygenate to olefin process

A process is presented for the dehydrogenation of paraffins. The process utilizes heated air for the combustion of a fuel within the dehydrogenation reactor to provide the heat of reaction for oxidative dehydrogenation. The nitrogen in the air is utilized as a diluent. A paraffin feedstream is mixed with a fuel, and the fuel/paraffin feedstream is mixed with an oxidant air stream at the inlet of dehydrogenation reactor.

Use of membrane for oxidative-dehydrogenation process

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Buffalo Grove, IL, United States of America

Rajeswar R Gattupalli