Uop Lcc

Yoga R Ayar

Peter Kokayeff

Soumendra Mohan Banerjee

John Anthony Petri

David A Lindsay

Richard K Hoehn

Donald A Eizenga

Kiran Ladkat

Priyesh Jayendrakumar Jani

Vikrant Vilasrao Dalal

Massimo Sangalli

Rajesh Sivadasan

Magaly Estremera

Ashwin Singh Tensingh

Pallavi Luharuka

A hydrocracking process for maximization of naphtha while producing base oil is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking unit in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream, a diesel stream and a first unconverted oil stream. A recycle stream comprising a portion of the kerosene stream, a portion of the diesel stream, and a portion of the first unconverted oil stream is recycled to the hydrocracking unit to provide a second unconverted oil stream. A remaining portion of the first unconverted oil stream is withdrawn for base oil production.

Hydrocracking process for maximization of naphtha

The process and apparatus of the disclosure utilize a heater between a hydroprocessing reactor and a hydroisomerization reactor. A hydroprocessing feed exchanger cools hydroprocessed effluent to effect turndown of heated hydroprocessed effluent so as to not feed the hydroprocessed effluent to the hydroisomerization reactor at a higher temperature than necessary.

Apparatus and process for heating hydroisomerization feed

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204&#xb0; C. (399&#xb0; F.) to about 238&#xb0; C. (460&#xb0; F.), a diesel stream having a T90 temperature of about 360&#xb0; C. (680&#xb0; F.) to about 383&#xb0; C. (721&#xb0; F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

Process for hydrocracking a hydrocarbon feed stream

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 is presented for the production of high quality kerosene from lower quality feedstocks, including kerosene produced from coker units, or kerosene from cracking units. The process includes hydrotreating the feedstock to remove contaminants in the feedstock. The hydrotreated process stream is then treated in a trim reactor at higher pressure to reduce the bromine index of the kerosene.

Kerosene hydrotreating with a separate high pressure trim reactor

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Buffalo Grove, IL, United States of America

Yoga R Ayar