Snamprogetti

Eniricerche S.p.a.

Enitecnologie S.p.a.

Other

Saipem Limited

Andrea Bartolini

Rodolfo Iezzi

Franco Buonomo

Luca Eugenio Basini

Paolo Pollesel

Emilio Sentimenti

Giancarlo Lupi

Domenico Sanfilippo

Edward C Luckenbach

Frederick A Zenz

Ugo Cornaro

Alessandra Guarinoni

Gabriele Carlo Ettore Clerici

Gabriele Carlo Clerici

Michele Checchin

Giovanni Papa

Paul Dominique Oudenne

Antonio Bennardo

Nicola Onorati

Gueorgui Kotelnikov

Vladimir Bespalov

Luca Basini

The present invention relates to a process for the treatment of refinery purge streams, containing a hydrocarbon component in slurry phase having a boiling point higher than or equal to 140&#xb0; C., characterized by the presence of quantities of asphaltenes higher than or equal to 5% by weight and characterized by the presence of a solid content higher than or equal to 5% by weight. The process provides that said purge be mixed with a suitable fluxing agent according to appropriate ratios and under certain conditions, forming a suspension with a content higher than or equal to 10% by weight of compounds having a boiling point TbP lower than or equal to 350&#xb0; C. After mixing, the suspension is sent to a liquid/solid separation step which operates under suitable conditions, separating a solid phase containing a residual organic component and a solid component, called cake, and a liquid phase containing residual solids. The solid phase obtained is cooled to below 60&#xb0; C., including the upper extreme, forming a granular solid which is stored and maintained at a temperature lower than or equal to 60&#xb0; C.

Process for the treatment of refinery purge streams

A process for recovering metals from a stream containing hydrocarbons and carbonaceous residues comprising sending the stream for extraction by mixing the stream with a hydrophilizing agent to remove the hydrophobic components of the stream, sending the mixture of the stream and hydrophilizing agent for separation, separating a liquid phase containing most of the hydrophilizing agent and hydrocarbons dissolved from a solid phase, sending the separated solid phase for leaching with an alkaline solution in the presence of air and/or oxygen, sending the leached mixture for separation, and separating the solid residue from the liquor.

Process for recovering metals from a stream rich in hydrocarbons and carbonaceous residues

The present invention relates to a process for selectively removing molybdenum from a solution which contains molybdenum, said process comprising the following steps: bringing the solution to an acid pH lower than or equal to 3, preferably lower than or equal to 2, even more preferably lower than or equal to 0.5, by the addition of an inorganic acid; adding at least one organic solvent, preferably toluene or xylene, to the solution and stirring continuously so as to create a water-organic emulsion; adding to the water-organic emulsion at least one alkaline metal xanthate having the general formula MeRX, wherein R is a linear or branched alkyl group having a number of carbon atoms higher than or equal to 2, Me is an alkaline metal selected from Li, Na, K, Rb, Cs and Fr, and X is the xanthate group, so as to form a complex with molybdenum wherein the molar ratio molybdenum/alkaline metal xanthate ranges from 1/6 to 1/2, keeping the emulsion at an acid pH by the addition of an inorganic acid, and interrupting the stirring so as to allow the separation of the aqueous phase from the organic phase. The linear or branched alkyl group R preferably has a number of carbon atoms higher than or equal to 2 and lower than or equal to 12. A reductant is optionally added to the starting solution which comprises Mo and V.

Process for the selective removal of molybdenum from a solution containing it

A process for recovering metals from a stream rich in hydrocarbons and carbonaceous residues by means of a treatment section, characterized in that it comprises the following steps: sending said stream to a primary treatment, effected in one or more steps, wherein said stream is treated in the presence of a fluxant agent in a suitable apparatus, at a temperature ranging from 80 to 180&#xb0; C., preferably from 100 to 160&#xb0; C., and subjected to liquid/solid separation in order to obtain a clarified product essentially consisting of liquids and a cake (oilcake); possibly subjecting the separated cake to drying, in order to remove the hydrocarbon component having a boiling point lower than a temperature ranging from 300 to 350&#xb0; C. from the cake; sending the cake, possibly dried, to a secondary thermal treatment comprising: a flameless pyrolysis of the cake effected between 400 and 800&#xb0; C., preferably between 500 and 670&#xb0; C.; an oxidation of the pyrolysis residue effected in an oxidizing environment and at temperatures ranging from 400 to 800&#xb0; C., preferably from 500 to 700&#xb0; C.

Equipment for the atomization of a liquid stream by means of a dispersing gaseous stream and for mixing the atomised product with a further suitable gaseous stream, characterized in that it comprises: a feeding zone (A) equipped with means suitable for feeding the liquid stream, the gaseous dispersing stream and further gaseous stream; one or more two-stage atomization zones (N) of the liquid stream by means of the gaseous dispersing stream; a distribution zone (D) of the further gaseous stream.

Equipment for the atomisation of a liquid stream by means of a dispersing gaseous stream and for mixing the atomised product with a further suitable gaseous stream in equipment for effecting catalytic partial oxidations and relative catalytic partial oxidation process

A device, system and method of mixing two fluids are described herein. A gaseous first fluid is distributed through a distribution zone to a mixing zone by a bundle of pipes parallel to an axis inside which the first fluid is uniformly distributed. A second fluid is uniformly distributed outside the pipes in the distribution zone. The mixing zone is separated from the distribution zone by a pipe-plate supporting the pipes. The pipe-plate has slits or openings to uniformly discharge the second fluid in an axial flow direction into the mixing zone. The pipes extend beyond the pipe-plate into the mixing zone to partialize an outlet flow of the first fluid. In one aspect, the pipes have different lengths to partialize the outlet flow. In another aspect, a terminal portion of the pipes partializes the outlet flow axially, radially, transversally or a combination thereof in the mixing zone.

Fluid mixing device inserted in or combined with a reactor

Process for the catalytic dehydrogenation of alkylaromatic hydrocarbons optionally mixed with ethane which comprises: A) dehydrogenating the hydrocarbon stream, optionally mixed with an inert gas, in a fluid bed reactor in the presence of a catalytic composition based on gallium and manganese supported on alumina modified with silica, at a temperature ranging from 400 to 700&#xb0; C., at a total pressure ranging from 0.1 to 3 ata and with a GHSV (Gas Hourly Space Velocity) ranging from 50 to 10,000 h; and B) regenerating and heating the catalyst, by means of the catalytic oxidation of a fuel, in a fluid bed regenerator at a temperature higher than 400&#xb0; C.

Catalytic composition for the dehydrogenation of alkylaromatic hydrocarbons

Partial oxidation process of liquid fuels, selected from hydrocarbon and/or oxygenated compounds, together with gaseous fuels, selected from hydrocarbon compounds, natural gas and LPG, by means of a suitable catalytic system comprising the following steps: premixing the reagents and possibly heating them to temperatures ranging from 25 to 400&#xb0; C., said reagents consisting of said liquid fuels, said gaseous fuels and oxygen or air or oxygen enriched air, optionally in the presence of vapor and/or CO; reacting the mixture of reagents in the catalytic zone, at inlet temperatures ranging from 50 to 500&#xb0; C. and space velocities ranging from 1,000 to 1,000,000 Nl reagents/L cat&#xd7;h, reaching temperatures ranging from 450 to 1350&#xb0; C.

Catalytic partial oxidation process for producing synthesis gas

A process for preparing light olefins from corresponding paraffins consists of reacting said paraffins in a reactor, operating at a temperature of between 450 and 800&#xb0; C., a pressure of between 0.1 and 3 atm absolute and a GHSV of between 100 and 10000 h, with a catalytic system containing gallium, platinum, possibly one or more alkaline or alkaline-earth metals, and a support consisting of alumina in delta or theta phase or in delta+theta or theta+alpha or delta+theta+alpha mixed phase, modified with silica, the gallium, expressed as GaO, being in a quantity of between 0.1 and 33.6 wt %, the platinum being in a quantity of between 1 and 99 ppm, the alkaline or alkaline-earth metals, expressed as oxide, being in a quantity of between 0 and 5 wt %, and the silica being in a quantity of between 0.08 and 3 wt %, the rest to 100% being alumina, and regenerating said catalytic system in a regenerator by burning off the coke which has deposited on its surface, without subsequently reducing it.

Process for preparing light olefins by dehydrogenation of the corresponding paraffins

A process for obtaining light olefins by the dehydrogenation of corresponding paraffins, by reacting the paraffins with a catalytic system containing chromium oxide, tin oxide, at least one alkali metal oxide, and an alumina-silica carrier, and then regenerating the catalytic system in a regenerator by burning coke deposited on its surface at a temperature higher than the average temperature of the reactor.

Process for obtaining light olefins by the dehydrogenation of the corresponding paraffins

A fluidized bed reactor operating under countercurrent gas-solid flow conditions wherein the reactor is supplied with horizontal baffles having separate passages through which the gas and the solid flow, such that the ascending gas leaves the baffle in a point higher than the point in which the descending solid leaves the same baffle, and the use of the reactor to perform reactions under countercurrent flow conditions while maintaining gas and solids flows of at least 70% of flooding conditions.

Fluidized bed reactor and process for performing reactions therein

A process for dehydrogenating light paraffins, in particular C.sub.2 -C.sub.5, to obtain the corresponding light olefins, comprising reacting said paraffins with a catalytic system containing platinum, tin and an alumina support and possibly an element of the lanthanide group in a fluidized bed reactor, where the heat required for the reaction is provided by said catalytic system as sensible heat, operating at a temperature of between 500.degree. and 700.degree. C. and at a pressure of between 1 and 2 kg/cm.sup.2, and regenerating said catalytic system by burning the coke which has deposited on the surface of the catalytic system, said regeneration being conducted in air and/or oxygen, if necessary by increasing the temperature of the catalytic system to a suitable level, followed by reduction of said catalytic system with a reducing agent.

Process for dehydrogenating light paraffins in a fluidized bed reactor

The process for activating a catalytic composition for paraffin dehydrogenation containing gallium, alumina, possibly silica and/or one or more alkaline or alkaline-earth metals, comprises thermal activation in air followed by post-activation effected by the following stages:

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San Giuliano Milanese, Italy

Andrea Bartolini