Abstract: Provided is a system for the hydroconversion of heavy oils essentially consisting of a solid accumulation reactor and a stripping section of the products of hydroconversion outside or inside the reactor itself.

Abstract: System and relative process for the complete and high-productivity hydroconversion of heavy oils essentially consisting of a solid accumulation reactor and a stripping section of the conversion products outside or inside the reactor itself. In particular, the system proposed consists of a solid accumulation hydroconversion reactor in which the solids deriving from and generated by the feedstock treated (metals in the form of sulphides and coke) are accumulated, up to very high levels, and a hot gas stripping section of the reaction liquid, designed in relation to the type of reactor adopted, for the direct and continuous removal of the conversion products, including high-boiling products.

Abstract: Process for the hydroconversion of heavy oils, selected from crude oils, heavy crude oils, bitumens from tar sands, distillation residues, distillation heavy cuts, distillation deasphalted residues, vegetable oils, oils from coal and oil shale, oils from the thermodecomposition of waste material, polymers, biomasses, comprising sending the heavy oil to a hydroconversion area, effected in one or more ebullated bed reactors, wherein hydrogen is introduced, in the presence of a suitable heterogeneous, supported, hydroconversion catalyst, in addition to a suitable hydrogenation catalyst, nano-dispersed in said heavy oil, and sending the stream coming from the hydroconversion area to a separation area, in which the separated liquid fraction, containing the nano-dispersed catalyst, is recycled to the ebullated bed reactor(s).

Abstract: Process for the hydroconversion of heavy oils, selected from crude oils, heavy crude oils, bitumens from tar sands, distillation residues, distillation heavy cuts, distillation deasphalted residues, vegetable oils, oils from coal and oil shale, oils from the thermodecomposition of waste material, polymers, biomasses, comprising sending the heavy oil to a hydroconversion area, effected in one or more ebullated bed reactors, wherein hydrogen is introduced, in the presence of a suitable heterogeneous, supported, hydroconversion catalyst, in addition to a suitable hydrogenation catalyst, nano-dispersed in said heavy oil, and sending the stream coming from the hydroconversion area to a separation area, in which the separated liquid fraction, containing the nano-dispersed catalyst, is recycled to the ebullated bed reactor(s).

Abstract: System and relative process for the complete and high productivity hydroconversion of heavy oils essentially consisting of a solid accumulation reactor and a stripping section of the conversion products outside or inside the reactor itself. In particular, the system proposed consists of a solid accumulation hydroconversion reactor in which the solids deriving from and generated by the feedstock treated (metals in the form of sulphides and coke) are accumulated, up to very high levels, and a hot gas stripping section of the reaction liquid, designed in relation to the type of reactor adopted, for the direct and continuous removal of the conversion products, including high-boiling products.

Abstract: A process is described for the production of hydrocarbons with a high octane number starting from hydrocarbon cuts containing isobutene by means of selective dimerization with acid catalysts, characterized in that the dimerization reaction is carried out in a tubular reactor using a feeding containing isobutene in quantities of less than 20% by weight and with a molar ratio linear olefins/isobutene greater than 3, preferably operating at a reaction temperature ranging from 30 to 120° C., at a pressure of less than 5 MPa and at feeding space velocities of less than 60 h−1.

Abstract: A process is described for the production of hydrocarbons with a high octane number starting from hydrocarbon cuts containing isobutene by selective dimerization with acid catalysts, characterized in that the dimerization reaction is carried out in the presence of tertiary alcohols, alkyl ethers and primary alcohols in such a quantity as to have, in the feeding, a molar ratio tertiary alcohols+alkyl ethers+primary alcohols/isobutene higher than 0.1, a molar ratio tertiary alcohols/isobutene lower than 0.2 and a molar ratio primary alcohols/isobutene lower than 0.2, preferably operating at a reaction temperature ranging from 30 to 120° C., at a pressure lower than 5 MPa and feeding space velocities of less than 30 h−1.

Abstract: A process is described for the production of hydrocarbons with a high octane number starting from hydrocarbon cuts containing isobutene by means of selective dimerization with acid catalysts, characterized in that the dimerization reaction is carried out in a tubular reactor using a feeding containing isobutene in quantities of less than 20% by weight and with a molar ratio linear olefins/isobutene greater than 3, preferably operating at a reaction temperature ranging from 30 to 120° C., at a pressure of less than 5 MPa and at feeding space velocities of less than 60 h−1.

Abstract: Process for the production of styrene which comprises:a) feeding to an alkylation unit a stream of benzene and a stream of recycled product containing ethylene;b) mixing the stream at the outlet of the alkylation unit, containing ethylbenzene, with a stream consisting of ethane;c) feeding the mixture thus obtained to a dehydrogenation unit containing a catalyst capable of contemporaneously dehydrogenating ethane and ethylbenzene;d) feeding the product leaving the dehydrogenation unit to a separation section to produce a stream essentially consisting of styrene and a stream containing ethylene;e) recycling the stream containing ethylene to the alkylation unit.

Abstract: A process is described for the production of hydrocarbons with a high octane number starting from hydrocarbon cuts containing isobutene by selective dimerization with acid catalysts characterized in that the dimerization reaction is carried out in the presence of primary alcohols and alkyl others in such a quantity as to have in the feeding a molar ratio primary alcohols+alkyl ethers/isobutene of more than 0.1 and a molar ratio primary alcohols/isobutene of less than 0.2, operating, preferably, at a reaction temperature of between 30 and 120.degree. C., at a pressure of less than 5 MPa and feeding space velocities of less than 30 h.sup.-1.