Uop Lcc

Honeywell International Inc.

Priyesh Jayendrakumar Jani

Soumendra Mohan Banerjee

Deepak Bisht

Gautam Pandey

Krishna Mani

Ram Ganesh Rokkam

Vikrant Vilasrao Dalal

Stephen W Sohn

Amit Sharma

Nishesh Garg

Bryan K Glover

Peter Kokayeff

Keith Allen Couch

Mark Paul Lapinski

Rajeswar R Gattupalli

David W Ablin

Steven F Zink

Avnish Kumar

Mohamed S Shakur

Shuguang Zhang

David A Lindsay

Yoga R Ayar

Michael W Penninger

Pijus Kanti Roy

Sarbotrika Sengupta

Tuhin Suvra Khan

This disclosure provides an apparatus and method for harnessing machine learning and data analytics for a real-time predictive model for a FCC pre-treatment unit. The method includes collecting operating parameters of a pre-treatment unit and fluid catalytic cracking (FCC) unit; evaluating an independent variable of the operating parameters; and adjusting an input to the pre-treatment unit to control the independent variable within specifications in an output of the FCC unit.

Harnessing machine learning and data analytics for a real time predictive model for a FCC pre-treatment unit

An integrated process for maximizing recovery of aromatics is provided. The process comprises passing at least a portion of a xylene column bottoms stream to a heavy aromatics column to provide a heavy aromatics column bottoms stream comprising Caromatics and a heavy aromatics column overhead stream. The heavy aromatics column bottoms stream is passed to a second stage hydrocracking reactor of a two-stage hydrocracking reactor. In the second stage hydrocracking reactor, the heavy aromatics column bottoms stream is hydrocracked in the presence of a hydrocracking catalyst and hydrogen to provide a hydrocracked effluent stream.

Integrated process for maximizing recovery of aromatics

An integrated process for maximizing recovery of hydrogen is provided. The process comprises: providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone, wherein the hydrogen stream is obtained from at least one of a hydrocracking zone, a transalkylation zone, and an isomerization zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream is passed to a debutanizer column of the reforming zone to provide a net hydrogen stream and a fraction comprising liquid petroleum gas (LPG). At least a portion of the net hydrogen stream is recycled to the reforming zone as the hydrogen stream.

Integrated process for maximizing recovery of hydrogen

An integrated process for maximizing recovery of LPG is provided. The process comprises providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream and at least one stream comprising Chydrocarbons from one or more of a hydrocracking zone, an isomerization zone, and a transalkylation zone is passed to a debutanizer column of the reforming zone to provide a fraction comprising liquid petroleum gas (LPG) and a debutanizer column bottoms stream.

Integrated process for maximizing recovery of liquid petroleum gas

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

A process and apparatus for reducing the sulfur content of naphtha. The process includes introducing at least a portion of a naphtha feed stream to a selective hydrodesulfurization zone under selective hydrodesulfurization conditions in the presence of a selective hydrodesulfurization catalyst to form a low sulfur stream which contains mercaptan and thiophene compounds. At least a portion of the low sulfur stream is separated into at least two streams, a mercaptan rich stream containing mercaptan and thiophene compounds and an overhead stream containing hydrogen sulfide and liquid petroleum gas. The mercaptan rich stream is treated in an adsorbent zone to remove at least a portion of the mercaptan and thiophene compounds to form a mercaptan lean stream.

Removal of sulfur from naphtha

Processes for transalkylation of aromatic hydrocarbons is disclosed. The process includes introducing a feed stream comprising aromatic hydrocarbon compounds to a transalkylation zone. A water source is introduced to the transalkylation zone, the water source being in an amount to provide about 80 to about 120 wppm of water based upon the mass of the feed stream. The feed stream is contacted with a transalkylation catalyst in the transalkylation zone under transalkylation conditions comprising a transalkylation temperature of about 130&#xb0; C. to about 230&#xb0; C. in the presence of the water to provide a transalkylation reaction effluent.

Processes for transalkylating aromatic hydrocarbons

A process for hydrotreating coker kerosene is described. Instead of a post treat reactor, a smaller trim reactor zone which operates at a lower pressure than the post treat reactor is used downstream of the product stripper. The trim reactor uses a noble metal catalyst to reduce the BI of the stripped product to less than about 150, and desirably in the range of about 50 to about 100.

Hydrotreating coker kerosene with a separate trim reactor

A process for producing alkylaromatic compounds is described. The process involves utilizing at least a portion of the aromatic compound used to regenerate the alkylation catalyst in a spent alkylation reaction zone as a reactant in the active alkylation reaction zone. The process further includes utilizing a portion of the process stream leaving the alkylation zone as a recycle stream to the alkylation zone.

Combined reactor effluent and regenerant recirculation for detergent alkylation process

Methods and apparatuses for selective hydrogenation of olefins are provided. The method for selective hydrogenation of olefins comprises reacting a hydrocarbonaceous feedstock comprising olefins and aromatic compounds with hydrogen in a reaction zone. The reaction contains a catalyst producing a reaction zone product stream comprising aromatic compounds. The reaction zone product stream is passed to a flash vessel, recovering a first product stream and a second product stream from the flash vessel. The first product stream is passed to a liquid jet eductor, whereas the second product stream comprising aromatic compounds having a reduced concentration of olefins is subsequently recovered.

Methods and apparatuses for selective hydrogenation of olefins

A process for producing alkylaromatic compounds is described. The process involves utilizing at least a portion of the aromatic compound used to regenerate the alkylation catalyst in a spent alkylation reaction zone as a reactant in the active alkylation reaction zone.

Method of producing alkylaromatic compounds using aromatic compound from catalyst regeneration

A process for separating benzene from a reactor effluent in which the reactor effluent is passed to a first separation zone to separate the effluent into a bottom benzene lean stream and an overhead stream. The bottom benzene lean stream does not need to be processed further to remove benzene. The overhead stream may be cooled and is passed to a second separation zone in which it is separated into a bottom benzene rich stream and a second overhead stream. The bottom benzene rich stream contains at least 80% of the benzene from the reactor effluent. The operating temperature of the first separation zone is greater than the operating temperature of the second separation zone.

Growing community of inventors

Gurgaon, India

Priyesh Jayendrakumar Jani