Abstract: This invention provides a resid cracking apparatus comprising a riser, reactor, stripper cum separator with adjustable outlets in flow communication with adsorbent and catalyst regenerators for converting hydrocarbon residues containing higher concentration of conradson carbon content, poisonous metals such as nickel & vanadium and basic nitrogen etc., into lighter and valuable products and a process thereof.

Abstract: The present invention relates to a stabilized dual zeolite catalyst for cracking heavier hydrocarbons into lighter useful products said catalyst comprising two types of zeolites viz., low silica molecular sieve and stabilized high silica zeolite, silica-alumina based binder and kaolin clay and a process for the preparation of the stabilized dual zeolite catalyst.

Abstract: A process for preparing bi-functional catalyst for Fluid Catalytic Cracking (FCC), that comprises molecular sieves, modified clay and semi-basic alumina and the catalyst for highly effective cracking of high boiling petroleum feedstock to provide simultaneously, enhanced yields of Liquefied Petroleum Gas (LPG) and reduction of undesirable bottoms.

Abstract: A process for preparing bi-functional catalyst for Fluid Catalytic Cracking (FCC), that comprises molecular sieves, modified clay and semi-basic alumina and the catalyst for highly effective cracking of high boiling petroleum feedstock to provide simultaneously, enhanced yields of Liquefied Petroleum Gas (LPG) and reduction of undesirable bottoms.

Abstract: The present invention provides a process for the upgradation of petroleum residue into useful fractions by subjecting petroleum residue in the presence of a solvent and ferrous sulphate catalyst to a pressure in the range of 10 atm. to 120 atm., temperature in the range of 380-420° C., for a period in the range of 0-120 minutes, in a reactor vessel, in an inert atmosphere. The charge is then cooled to room temperature and the product gas released through scrubbers. The residue is re-heated, if required, for free flow of liquid product. The resulting liquid product is distilled to obtain useful fractions.

Abstract: A process for preparing a hydrocarbon conversion catalyst for use in a Fluid Catalyst Cracking (FCC) unit includes the steps of preparing a modified alumina-silica composite by reacting alumina with an acid to obtain an acidified alumina, aging the acidified alumina for from 0.25 to 60 hours, adding a silica source to the acidified alumina to obtain the composite; preparing a dispersed precursor slurry of the modified alumina-silica composite, and a rare earth exchanged USY zeolite (REUSY) containing at least one rare earth oxide present in an amount ranging from 3.8 to 4.0 wt %, and optionally kaolin clay; spray-drying the slurry to obtain spherical particles; and subjecting the spherical particles to calcination.

Abstract: A fluid catalytic cracking additive composition to obtain enhanced yield of Liquified Petroleum Gas in catalytic cracking of high boiling petroleum feed stocks comprising 4 to 20 wt. % aluminum phosphate composite, 1-40 wt. % crystalline molecular sieve Zeolites from the group selected from mordenite ZSM-5, Beta and mixtures thereof and 40-90 wt. % clay.

Abstract: 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, Na2O nd nucleation centers, wherein the reaction mixture has molar ratios of constituents including Na2O/SiO2, 0.4-0.9; SiO2/Al2O3, 7-13; and H2O/Na2O, 30-45, and wherein the nucleation centers have molar ratios of constituents including Na2O/SiO2, 0.5-2.0; SiO2/Al203, 10-20; and H2O/Na2O, 10-40; and heating the reaction mixture to a temperature ranging from 90 to 110° 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 Å, a particle size ranging from 4000 to 8000 Å, 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° C. for 3 hours and with 100% steam.

Abstract: 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.

Abstract: A fluidized catalytic cracking apparatus includes a riser containing a regenerated catalyst and adsorbant, and has a first inlet for introduction of high velocity steam, a second inlet for introduction of a feed stream containing heavy residual fractions with high concentrations of conradson coke, metals including vanadium and nickel, and additional poisons including nitrogen, a third inlet for introduction of an adsorbent, and a fourth inlet disposed above the third inlet means for introduction of a regenerated catalyst, the adsorbent having a particle size which is larger than that of the regenerated catalyst.

Abstract: 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.

Abstract: 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.