Abstract: 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° 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° 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° C.

Abstract: 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° 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° 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° C.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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° C., preferably from 100 to 160° 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° 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° C., preferably between 500 and 670° C.

Abstract: 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 an extraction by mixing said stream with a suitable hydrophilizing agent, i.e.

Abstract: 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° C., preferably from 100 to 160° 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° 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° C., preferably between 500 and 670° C.

Abstract: 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.

Abstract: 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.

Abstract: 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° 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?1; 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° C.

Abstract: A device is described for mixing two fluids, inserted in or combined with a reactor, which can also be used for catalytic partial oxidation, substantially consisting of the following zones:—a first feeding zone equipped with means for allowing a first fluid, possibly gaseous under the operating conditions, to enter in an axial direction;—an underlying distribution zone containing a bundle of pipes preferably parallel to the axis inside which said fluid is uniformly distributed;—a second feeding zone equipped with means for allowing a second fluid to enter the distribution zone containing the bundle of preferably parallel pipes and to be uniformly distributed outside said parallel pipes;—a mixing zone separated from the distribution zone by a pipe-plate supporting said parallel pipes, said pipe-plate having slits or openings in order to uniformly discharge the second fluid in an axial direction into the mixing area, and said parallel pipes extending beyond said pipe-plate into the mixing zone.

Abstract: 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° 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 CO2; reacting the mixture of reagents in the catalytic zone, at inlet temperatures ranging from 50 to 500° C. and space velocities ranging from 1,000 to 1,000,000 Nl reagents/L cat×h, reaching temperatures ranging from 450 to 1350° C.

Abstract: 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, 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 atomisation zones (N) of the liquid stream by means of the gaseous dispersing stream; a distribution zone (D) of the further gaseous stream; the first stage of the atomisation zone (N1) essentially consisting of a tubular core (2), through which the liquid stream passes, equipped with an appropriate series of nozzles (5), situated at the same height, and an outer jacket (4) coaxial to said core, through which the gaseous dispersing stream passes, wherein said nozzles (5) allow the gaseous dispersing stream to enter the tubular core, perpendicularly to the axis of said tubular core (2), effecting a first atomisation of the liquid stream, the second stage of

Abstract: 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° C., a pressure of between 0.1 and 3 atm absolute and a GHSV of between 100 and 10000 h?1, 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 Ga2O3, 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.

Abstract: 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° C., said reagents consisting of said liquid fuels, said gaseous fuels and oxygen or air or oxygen enriched air, optionally in the presence of vapour and/or CO2; reacting the mixture of reagents in the catalytic zone, at inlet temperatures ranging from 50 to 500° C. and space velocities ranging from 1,000 to 1,000,000 Nl reagents/L cat×h, reaching temperatures ranging from 450 to 1350° C.

Abstract: 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° 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−1; 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° C.

Abstract: 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° C., a pressure of between 0.1 and 3 atm absolute and a GHSV of between 100 and 10000 h−1, 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 Ga2O3, 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.

Abstract: 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.

Abstract: 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.