Indian Oil Corporation Limited

Other

Manoranjan Santra

Satish Makhija

Sobhan Ghosh

Jagdev Kumar Dixit

Debasis Bhattacharyya

Asit Kumar Das

Satyen Kumar Das

Ram Mohan Thakur

Latoor Lal Saroya

Ganga Shanker Mishra

Sukumar Mandal

Mohan Prabhu Kuvettu

Alex Cheru Pulikottil

Ram Prakash Verma

Sanjay Kumar Ray

Shankar Sharma

Arumugam Velayutham Karthikeyani

Sarvesh Kumar

Alok Sharma

Pankaj Kumar Kasliwal

Venkatachalam Krishnan

Marri Rama Rao

Sanjeev Singh

Arvind Pratap Singh

Mani Karthikeyan

Vutukuru Lakshmi Murthy

Ujjwal Manna

Ventachalam Krishnan

Suresh Kumarshah

Jai Prakash Singh

Hillol Biswas

Dharmendra Kumar Yadav

Ganga Sanker Mishra

Christopher J

Soban Ghosh

Ashok Kumar Tewari

The present invention relates to a adsorbent composition for removing refractory sulphur compounds from refinery streams comprising of base component in the range of 10 to 50 wt %, spinel oxide in the range of 20 to 60 wt % as a reactive metal oxide component and bimetallic alloy in the range of 10 to 40 wt % acting as an adsorption enhancer component, wherein the adsorption enhancer component acts in synergy with base component. The invention also relates to a process for the preparation of said composition by mixing in solid state fine particles of base component, spinel oxide and bimetallic alloy, homogenizing the mixture thus obtained with solvent, peptizing the wet solid with dilute mineral acid, extruding the peptized material with extrusion aiding agents, drying the extrudates, further calcining the dried extrudates and reducing the calcined material under hydrogen flow.

Adsorbent composition for removal of refractory sulphur compounds from refinery streams and process thereof

According to this invention, there is provided a process and apparatus for catalytic cracking of various petroleum based heavy feed stocks in the presence of solid zeolite catalyst and high pore size acidic components for selective bottom cracking and mixtures thereof, in multiple riser type continuously circulating fluidized bed reactors operated at different severities to produce high yield of middle distillates, in the range of 50&#x2013;65 wt % of fresh feed.

Multi stage selective catalytic cracking process and a system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks

A process for the preparation of hydrotreating catalyst which comprises of a Group VIB metal and Group VIII metal on an active composite carrier for the removal of sulfur from gas oil feed stocks, wherein the said carrier comprises of a phosphated alumina and an ultra stable Y zeolite and the metal components mostly reside on the alumina, said process comprising the steps of impregnation of chelated metal complex preferentially on to the alumina component of the composite support and subjecting the composite catalyst to a high-speed ball milling. The catalyst obtained by the process of the present invention consists of the active metals in the nanoparticle range (less than 50 &#x212b;) while also retaining the zeolite properties of the composite carrier and the catalyst produces less than 50 ppm sulfur from gas oil feed stocks containing greater than 1 wt % sulfur under typical commercial operating conditions.

Process for preparing hydro-desulfurization catalyst

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 preparation of fluidized catalytic cracking (FCC) catalyst, comprising silicon stabilized large crystallite sized synthetic faujasite zeolite, aluminum depleted and normal kaolin clay, alumina and silica. The cracking catalyst is highly active and selective for bottom upgradation, it produces less coke and higher gasoline and total cycle oil (TCO) and possesses improved metal tolerance properties when evaluated and compared with a commercial catalyst under conditions of a typical FCC unit in a petroleum refinery.

Process for the preparation of fluidized catalytic cracking (FCC)

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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Haryana, India

Manoranjan Santra