Uop Lcc

Upo LLC

Robert L Mehlberg

Paolo Palmas

Laura Elise Leonard

Zhanping Xu

John Joseph Senetar

Christopher P Nicholas

Kurt M Vanden Bussche

Charles P Luebke

David A Wegerer

Lev Davydov

Keith Allen Couch

Daniel Robert Johnson

Mohammad-Reza Mostofi-Ashtiani

Michael S Sandacz

Brian W Hedrick

Zhihao Fei

Lisa M Wolschlag

Michael A Stine

Thomas W Lorsbach

Chad R Huovie

Peter J Van Opdorp

Karthikeyan Paramanandam

Sathit Kulprathipanja

Jibreel A Qafisheh

Kurt A Detrick

Dale James Shields

Sean G Mueller

David S Lafyatis

Matthew R Wojtowicz

Mohammad Reza Mostofi-Ashtiani

Paul S Nishimura

Kelly D Seibert

Mohammad Reza Mostofi Ashtiani

Antoine Negiz

Peter Kokayeff

Steven Lee Krupa

Trung S Pham

Avram Michael Buchbinder

Douglas A Nafis

Carl John Stevens

Michael R Smith

Todd M Kruse

Lawrence L Upson

Steven F Zink

Christian D Freet

Patrick D Walker

James P Glavin

Eric Leeton

Gregory J Schrad

Hosoo Lim

Sakthivelan Maadasamy Durai

Robert Jason Lee Noe

Reza Mohammad Mostofi Ashtiani

Frank Rosser, Jr

An apparatus comprising a feed distributor comprising a side cluster of orifices instead of or in combination with an end cluster of orifices for distributing hydrocarbon feed into a catalyst stream. A side cluster of orifices in conjunction with an end cluster of orifices on a feed distributor can distribute hydrocarbon feed into a riser over a greater cross-sectional extent enabling emission of smaller droplet sizes which provide better conversion with less coke production.

Apparatus for distributing feed with a cluster of orifices on a side of the distributor

In an apparatus for fluid catalytic cracking a riser having a top and a bottom for fluidizing and cracking a hydrocarbon feed stream by contact with catalyst exits an outlet at the top of the riser. A downer in communication with the outlet of the riser receives cracked hydrocarbon product and catalyst. A swirl duct in communication with the downer has a discharge opening below the outlet for discharging said cracked hydrocarbon product and catalyst. A stream of hydrocarbon feed and a catalyst is passed upwardly in a riser. A stream of gaseous hydrocarbon products and catalyst is directedly downwardly and then the stream of gaseous hydrocarbon products and catalyst are directed to flow in an angular direction to separate gaseous hydrocarbon products from the catalyst.

Riser extension apparatus and process

In an FCC apparatus and process gas and catalyst exit from a riser, are disengaged from each other and the catalyst is stripped. Product gases are evacuated from catalyst that can over crack the product gases to other undesired products. A baffle in or above the stripping section can direct product gases into a passage that evacuates the product gases to product recovery in isolation from the catalyst.

Apparatus and process for capturing product gases from catalyst stripper

In an FCC apparatus in which swirl arms are used to discharge gas and catalyst from a riser, the swirling movement of the catalyst particles is inhibited while impeding the catalyst particles and gaseous products from exiting the disengaging chamber and entering a reactor annulus. The catalyst particles and gaseous products pass through a tunnel comprising a vertical wall to enter the reactor annulus. The vertical wall presents a face that is opposed to the angular direction in which the catalyst particles and gaseous products swirl. A baffle may be located at the intersection between the reactor annulus and the disengaging chamber to deflect catalyst laterally in a stripping section after exiting the reactor annulus. The baffle may be equipped with openings to fluidize the large proportion of catalyst passing over this region to effectively pre-strip this catalyst before it enters a stripping section.

Apparatus and process for separating gases from catalyst

A fluid catalytic cracking (FCC) process for cracking multiple feedstocks in a FCC apparatus comprising a first set of feed distributors having first distributor tips and a second set of feed distributors having second distributor tips is provided. A first feed is injected into the riser from first distributor tips. A second feed is injected into the riser from second distributor tips. The first distributor tips and the second distributor tips are positioned at different radii in the riser. The first feed and the second feed are cracked in the riser in the presence of an FCC catalyst to provide a cracked effluent stream. The first distributor tips and the second distributor tips are located into a region of lower catalyst density and a region of higher catalyst density respectively in the riser.

Fluid catalytic cracking process for cracking multiple feedstocks

Reactor systems for use with ionic liquid catalyst. The reactor systems include one or more stages, which include a reactor and a heat exchanger, and a separation zone. The reactor and the heat exchanger may have a vertical orientation. Additionally, a separation vessel may also include a vertical orientation. The heat exchanger may allow for linear flow of process fluid to control residence time.

Reactor system for use with an ionic liquid catalyst

Processes and apparatuses are disclosed for catalytically cracking hydrocarbons comprising hydrotreating a residual feed stream and a recycle cracked stream comprising an oil to provide a hydrotreated effluent stream. The hydrotreated effluent stream is separated to provide a FCC feed stream and a distillate stream. The FCC feed stream is fed to a first riser reactor to provide a first cracked stream. The distillate stream is fed to a second riser reactor to provide a second cracked stream. The first cracked stream and the second cracked stream are fed to a main fractionation column. The first cracked stream and the second cracked stream are fractionated in the main fractionation column. The recycle cracked stream is taken from the main fractionation column.

Process and apparatus for recycling cracked hydrocarbons

Processes for oligomerizing olefins to produce diesel. The oligomerization zone temperature is controlled to counteract catalyst deactivation caused by coking, by contaminants such as cyclo C5 and/or cyclo C6 hydrocarbons, or both. The temperature is increased in increments to ensure that that the oligomerization zone is producing product at a target product yield with a target product quality, which may be measured by a product cetane number. The target product yield is at least 50 wt % and a target product cetane number may be at least 35.

Process for producing a diesel fuel by oligomerization

One exemplary embodiment can be a process for cooling a vent stream from a receiver. Generally, the process may include providing a refrigerant including at least one compound contained in the receiver so the refrigerant leaking into the receiver can be compatible with the process.

Alkylation system and a process for cooling a vent stream

A process and apparatus for combusting coke from catalyst two stages is disclosed. Catalyst and flue gas from a lower chamber ascends to an upper chamber to be roughly separated by swirl ducts extending from a combustion conduit. The swirl ducts may discharge into a container in the upper chamber.

Compact two-stage regenerator and process for using

Process for using a compact two-stage regenerator

A process is presented for the control of the exotherm from an oligomerization process. The oligomerization process is for the conversion of C3 and C4 olefins to distillate. The process includes controlling the extent of the reaction to limit temperature rise, and recycle of a portion of the reactor effluent stream for dilution of the C3 and C4 olefins passed to the oligomerization reactors, and for separating out the product distillate.

Exotherm, conversion and selectivity management for oligomerization process

A method of controlling a hydrocarbon conversion process is described. The method involves introducing a reactant into a reaction zone containing an ionic liquid catalyst. The reaction zone has at least two zones. The mass transfer resistance in the second zone is greater than the mass transfer resistance in the first zone.

Selectivity of ionic liquid alkylation

A process and apparatus for heating catalyst is presented. Cooler catalyst is removed from a reactor and heated with a hot gas in a riser, heated in a heating tube or heated in a heating chamber. Heated catalyst is disengaged from the hot gas if necessary and returned to the reactor. The process and apparatus can be used for producing light olefins. The hot gas may be a flue gas from an FCC regenerator or a combustion gas from a heater.

Apparatus and process for heating catalyst from a reactor

A process is presented for the production of light olefins. The process provides for the separation of the effluent stream from a catalytic cracking process into a stream having light olefins and a stream having heavier hydrocarbons. The heavier stream is oligomerized to generate an oligomer stream having heavier hydrocarbons, and then separated into a stream to be passed to the catalytic cracking process, and a stream to be passed to a reforming unit.

FCC process with a dehydrogenation zone for max propylene production

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Des Plaines, IL, United States of America

Robert L Mehlberg