Uop Lcc

Upo LLC

Zhihao Fei

Robert L Mehlberg

Charles P Luebke

Brian W Hedrick

Paolo Palmas

Keith Allen Couch

Christopher P Nicholas

Kurt M Vanden Bussche

Lev Davydov

Michael S Sandacz

Matthew Lippmann

Lisa M Wolschlag

Hosoo Lim

Kirk Liu

David A Wegerer

Laura Elise Leonard

Daniel N Myers

Steven Lee Krupa

Trung S Pham

Sathit Kulprathipanja

Mohammad-Reza Mostofi-Ashtiani

Ping Sun

Carl John Stevens

Todd M Kruse

Grant H Yokomizo

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

A counter-current catalyst regenerator with at least two stages of counter-current contact is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst.

Process for combustion coke from coked catalyst

A counter-current catalyst regenerator with at least two stages of counter-current contact along with a regenerator riser is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst. The regenerator riser may provide a passage to transport the catalyst and may serve as a secondary stage for coke combustion to provide the regenerated catalyst.

FCC counter-current regenerator with a regenerator riser

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

Processes for regenerating adsorbent in a nitrile removal zone. The regenerant comprises a stream of hot liquid that may comprise a portion of the oligomerized effluent or a portion of a hydrotreated effluent. A spent regenerant comprising the desorbed nitriles may be processed along with the oligomerized effluent with existing separation equipment.

Processes for removing nitriles from a feed to an oligomerization zone

The present invention discloses a process optimizing the yield of propylene from a fluid catalytic cracking unit. The method combines a first catalytic reactor, a fractionation zone, a separation unit and a second catalytic reactor. The separation unit produces a first separation unit stream and a second separation unit stream, the first separation unit stream comprising Cparaffins, and the second separation unit stream comprising Colefins, wherein the second separation unit stream is passed to a second catalytic reactor and the first separation unit stream is removed from the process.

Process and apparatus for improving propylene yield from a fluid catalytic cracking process

An integrated process and apparatus for conversion of gas oil and heavy oil is described. The process includes passing a gas oil feed to a fluid catalytic cracking (FCC) zone to obtain a FCC effluent; separating the FCC effluent in a separation zone into at least two fractions comprising a clarified slurry oil fraction and an overhead fraction; passing the clarified slurry oil fraction to a slurry hydrocracking zone forming at least a naphtha stream; and recycling at least a portion of the slurry hydrocracking naphtha stream to the FCC zone.

Integrated process for conversion of vacuum gas oil and heavy oil

The present invention discloses a process optimizing the yield of ethylene and propylene from a fluid catalytic cracking unit. The method combines a first catalytic reactor, a fractionation zone, a separation unit and a second catalytic reactor. The separation unit produces a first separate stream comprising Colefins and a second separate stream comprising Colefins. The separate streams may be combined and are passed to a second catalytic reactor for additional conversion to ethylene and propylene.

Process and apparatus for improving light olefin yield from a fluid catalytic cracking process

One exemplary embodiment can be a fluid catalytic cracking process. The process can include a reaction zone operating at conditions to facilitate olefin production and including at least one riser. The at least one riser can receive a first feed having a boiling point of about 180&#xb0; to about 800&#xb0; C., and a second feed having more than about 70%, by weight, of one or more Colefins.

Fluid catalytic cracking process

A process for improving the yield of ethylene and propylene from a light naphtha feedstock includes obtaining light naphtha feedstock from a primary cracking zone having a cracking catalyst. The light naphtha feedstock is contacted with an olefin catalyst in an olefin producing zone to produce an ethylene- and propylene-rich stream. After reacting with the olefin catalyst, the ethylene- and propylene-rich stream is separated from the olefin catalyst from in a separator zone. At least a portion of the olefin catalyst is regenerated by combusting coke deposited on a surface of the olefin catalyst in an oxygen-containing environment, and at least a portion of the olefin catalyst is heated. These portions could be the same one or they could be different. In some embodiments, at least a portion of the olefin catalyst could be neither regenerated nor heated. The olefin catalyst is returned to the olefin producing zone.

Dual riser catalytic cracker for increased light olefin yield

One exemplary embodiment can be a fluid catalytic cracking system. The system can include a reaction zone operating at conditions to facilitate olefin production and including at least one riser. The at least one riser can receive a first feed having a boiling point of about 180-about 800&#xb0; C., and a second feed having more than about 70%, by weight, of one or more C4olefins.

Fluid catalytic cracking system

An FCC process producing lower NOx emissions during regeneration by using excess oxygen levels at less than or equal to about 0.5 mol-% and a plenum temperature above about 730&#xb0; C. (about 1350&#xb0; F.). The process may further include limiting the Pt content in the catalyst to less than or equal to about 0.5 ppm. NOemissions, NO to NO, produced through this process may be equal to or less than 25 ppmv. The process may also include adjusting the metal content of the feedstock for such metals as antimony, nickel, or vanadium. Additional variables for reducing NOemissions that may be used in conjunction with this process may include increasing the flue gas residence time, injecting NHinto the flue gas, adding or using NO-reducing catalysts, increasing stripping of the catalyst, and increasing the catalyst zeolite to matrix ratio.

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Naperville, IL, United States of America

Zhihao Fei