Indian Oil Corporation Limited

Ganga Shanker Mishra

Debasis Bhattacharyya

Satyen Kumar Das

Ram Mohan Thakur

Satish Makhija

Jagdev Kumar Dixit

Manoranjan Santra

Latoor Lal Saroya

Asit Kumar Das

Sukumar Mandal

Santanam Rajagopal

Mohan Prabhu Kuvettu

Sobhan Ghosh

Arumugam Velayutham Karthikeyani

Pankaj Kumar Kasliwal

Shankar Sharma

Brijesh Kumar

Ravinder Kumar Malhotra

Gadari Saidulu

Sanjay Kumar Ray

Venkatachalam Krishnan

Marri Rama Rao

Sanjeev Singh

Arvind Pratap Singh

Brijesh Kumar Verma

Bandaru Venkata Hari Prasad Gupta

Sudipta Roy

Vutukuru Lakshmi Murthy

Christopher J

Soban Ghosh

Ashok Kumar Tewari

Suresh Kumarshah

Disclosed herein is an improved fluidized catalytic cracking process for converting normally liquid hydrocarbon feedstock with simultaneous reduction of sulfur content in the liquid products obtained therefrom which comprises carrying out the cracking process in the presence of carbon monoxide gas as a reducing agent. The process optionally includes a step of premixing the hydrocarbon feedstock with carbon monoxide gas causing major sulfur reduction before effecting the cracking. The premixing is done in a specified nozzle assembly linked to the FCC unit.

Process for reduction of sulfur in FCC liquid products through the use of carbon monoxide as a reducing agent

An apparatus for catalytic cracking of feedstock includes a first channel in which a feedstock is treated with an adsorbent to obtain a treated intermediate. The apparatus further comprises a separator-reactor vessel. The separator-reactor vessel includes an adsorbent separating region to remove the adsorbent from the treated intermediate. The separator-reactor vessel further includes a second channel connected to the adsorbent separating region. The treated intermediate is contacted with a catalyst in the second channel to produce a cracking yield. The second channel terminates in a catalyst separating region of the separator-reactor vessel. The catalyst is removed from the cracking yield in the catalyst separating region. The separator-reactor vessel further includes a physical partition disposed between the adsorbent separating region and the catalyst separating region to separate the two regions.

Method and apparatus for catalytic cracking

A synthetic faujasite zeolite and a process for preparing the same which includes forming a reaction mixture consisting essentially of water, a source of silica, a source of alumina, Na,O nd nucleation centers, wherein the reaction mixture has molar ratios of constituents including Na,O/SiO,, 0.4-0.9; SiO,/Al,O,, 7-13; and H,O/Na,O, 30-45, and wherein the nucleation centers have molar ratios of constituents including Na,O/SiO,, 0.5-2.0; SiO,/Al,0,, 10-20; and H,O/Na,O, 10-40; and heating the reaction mixture to a temperature ranging from 90 to 110&deg; C. for a time period ranging from 23 to 29 hours to obtain the synthetic faujasite zeolite, wherein the synthetic faujasite zeolite has a crystallite size ranging from 1500 to 2000 &angst;, a particle size ranging from 4000 to 8000 &angst;, and a retention of surface of more than 70% of that of a parent zeolite, when exchanged with ammonia and subjected to hydrothermal treatment at 650&deg; C. for 3 hours and with 100% steam.

Process for preparing an hydrothermally stable, large crystallite sized, highly crystallite sized, highly crystalline synthetic faujasite zeolite

A process for converting undesirable olefinic hydrocarbon streams to hydrogen and petrochemical feedstock e.g. light olefins in C.sub.2 -C.sub.4 range and aromatics especially toluene and xylenes, which comprises simultaneous cracking and reforming at olefin rich hydrocarbons using a catalyst consisting of dehydrogenating metal components, shape selective zeolite components and large pore acidic components in different proportions in a circulating fluidized bed reactor-regenerator system having reactor temperature within 450-750.degree. C. and WHSV of 0.1-60 hour.sup.-1.

Upgradation of undesirable olefinic liquid hydrocarbon streams

A process for selective catalytic cracking of a petroleum-based feedstock to produce a product having a high yield of liquified petroleum gas (LPG) and light olefins having 3 to 4 carbons includes providing a fluidized bed reactor which is a high velocity riser, continuously circulating fluidized bed reactor; providing a solid acidic catalyst comprised of: from 1 to 6% by wt. of ultra stable Y-zeolite; from 8-25% by wt. of Pentasil zeolite which is shape selective; from 0-8% by wt. of an active material which is bottom selective; from 0-1% by wt. of rare earth constituents; and from 91 to 60% by wt. of nonacidic constituents and binder; charging the fluidized bed reactor with the solid acidic catalyst and the petroleum-based feedstock; and cracking the petroleum-based feedstock in the presence of the solid acidic catalyst in the fluidized bed reactor. The reactor is operated at a Weight Hourly Space Velocity (WHSV) ranging from 40 to 120 hr.sup.-1, a ratio of solid acidic catalyst to petroleum-based feedstock ranging from 15 to 25, a temperature at the top of the high velocity riser ranging from 530.degree. C. to 600.degree. C., recycled riser products ranging from 0 to 40%, a pressure in the fluidized bed reactor ranging from 1.0 to 4.0 kg/cm.sup.2 g, and an amount of steam for dilution and quenching of hydrocarbons ranging from 3 to 50 wt. % of the petroleum-based feedstock. The Pentasil zeolite has a pore size ranging from 5 to 6 .ANG. so that the catalyst is highly selective for LPG and C.sub.4 light olefins with minimum dry gas and coke make, and so that the vanadium tolerance of the catalyst is increased and ranges up to 21,000 PPM. The process produces a LPG yield ranging up to 40 to 65 wt. % of the fresh petroleum-based feedstock, a selectivity for the light olefins of at least 40 wt. %, and a selectivity for the LPG of at least 45 wt.

Process for catalytic cracking of petroleum based feed stocks

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Faridabad, India

Ganga Shanker Mishra