Snamprogetti

Enitecnologie S.p.a.

Other

Eniricerche S.p.a.

Enitechnologie S.p.a.

Eniricerche S.p.a.-and- Snamprogetti S.p.a.

Mario Marchionna

Alberto Delbianco

Nicoletta Panariti

Renata Patrini

Massimo Lami

Domenico Sanfilippo

Francesco Ancillotti

Romolo Montanari

Sergio Rosi

Luca Eugenio Basini

Alberto Paggini

Marco Di Girolamo

Luigi Patron

Lorenzo Tagliabue

Salvatore Meli

Marco Di Gerolamo

Carlo Perego

Cristina Flego

Roberto Trotta

Sebastiano Correra

Roberto Catani

Mario Di Girolamo

Stephano Rossini

A process for converting a heavy charge such as a heavy crude oil, a tar from oil sand and a distillation residue, by combining a hydroconversion with catalysts in slurry phase process, a distillation or flash process, and a deasphalting process, wherein the three processes operate on mixed streams consisting of fresh charge and recycled streams.

Process for the conversion of heavy charges such as heavy crude oils and distillation residues

A process for the conversion of heavy feedstocks selected from heavy crude oils, distillation residues from crude oil or coming from catalytic treatment, visbreaker tars, thermal tars, bitumens from oil sands, liquids from coats of different origins and other high-boiling feedstocks of a hydrocarbon nature known as 'black oils.'

Process for the total conversion of heavy feedstocks to distillates

A process for the conversion of heavy feedstocks using hydrotreatment, distillation or flash, and deasphalting that includes mixing a heavy feedstock with a hydrogenation catalyst and subjecting the thus-formed mixture to a hydrotreatment reactor for reaction with one or more of hydrogen and hydrogen sulfide to form a first product stream; subjecting the first product stream to a distillation or flash to form a plurality of distillate fractions; and recycling heavies from the distillation residue and/or tar by deasphalting in the presence of a solvent; where the hydrotreatment reaction product is pre-separated under high pressure to form light and heavy fractions and sending the heavy fraction to the distillation and/or flash.

Process for the conversion of heavy feedstocks such as heavy crude oils and distillation residues

Process for the conversion of heavy feedstocks selected from heavy crude oils, distillation residues from crude oil or catalytic treatment, 'visbreaker tars', 'thermal tars', bitumens from &#x201c;oil sands&#x201d; liquids from coals of different origins and other high boiling feedstocks of a hydrocarbon origin.

Process for the conversion of heavy feedstocks selected from heavy crude oils, distillation residues, heavy oils coming from catalytic treatment, thermal tars, oil sand bitumens, various kinds of coals and other high-boiling feedstocks of a hydrocarbon origin known as black oils, by the combined use of the following three process units: hydroconversion with catalysts in slurry phase (HT), distillation or flash (D), and deasphalting (SDA).

Heavy hydrocarbon charges are converted in a deasphalting section in the presence of solvents and obtaining two streams, one consisting of deasphalted oil and the other one containing asphaltenes, mixing the deasphalted oil stream with a hydrogenation catalyst and passing the thus obtained mixture to a hydroprocessing section containing hydrogen or hydrogen/HS, mixing the stream consisting of asphaltenes discharged from the deasphalting section with an appropriate hydrogenation catalyst and passing the obtained mixture to a second hydroprocessing section where it is reacted with hydrogen or a mixture of hydrogen and HS, passing both the stream containing the reaction product with dispersed catalyst from the hydroprocessing section and the stream containing the reaction product with dispersed catalyst from the second hydroprocessing section, to one or more distillation or flash stages, whereby the more volatile fractions are separated from the distillation residue (tar) or from the liquid discharged from the flash unit, sending the distillation residue (tar) or the liquid discharged from the flash unit, containing the catalyst in the dispersed phase, with a high content of metal sulphides, produced by demetallization of the charge, to a second deasphalting section thereby obtaining deasphalted oil and asphaltenes.

A process is described for the hydrogenation of olefinic streams containing sulfurated compounds, obtained starting from hydrocarbon cuts containing isobutene (by means of selective dimerization), characterized by fractionating said streams in one or more distillation columns and hydrogenating separately the two fractions obtained. The stream at the head, with a minimum content of sulfurated compounds, is hydrogenated with conventional catalysts based on nickel or noble metals (Platinum and/or Palladium), extremely active but also very sensitive to sulfur, whereas the bottom of the column, rich in sulfurated compounds, is treated with bimetallic catalysts (for example Ni/Co and/or Ni/Mo), less active but not deactivated by sulfur.

Process for the hydrogenation of branched olefins deriving from the dimerization of isobutene

Use of a liquid oxygenated product with a cetane number higher than 50, consisting of one or more compounds selected from dialkyl-polyformals represented by the formulaRO(CHO)Rwherein R is an alkyl chain CH,

Use of an oxygenated product as a substitute of gas oil in diesel engines

Process for obtaining a 'diesel cut' fuel having a CN cetane number equal to or greater than 48 and a content of aromatics lower than 0.4% by weight starting from olefins or their mixtures, characterized in that it comprises oligomerizing said olefins having from 2 to 10 carbon, distilling the stream obtained from the oligomerization, and hydrogenating the separated C-Chydrocarbon stream.

Process for obtaining a 'diesel cut' fuel by the oligomerization of olefins or their mixtures

A process is described for the production of hydrocarbons with a high octane number starting from mixtures essentially consisting of n-butane and isobutane (such as for example field butanes) comprising a skeleton isomerization section, a dehydrogenation section of paraffins, a selective hydrogenation section of butadiene, two conversion sections of olefins, in which the isobutene is firstly selectively transformed by means of dimerization and/or etherification, followed by the linear butenes by means of alkylation, in order to obtain, by joining the products of the two conversion sections, a product having excellent motoristic properties (octane number, volatility and distillation curve).

Process for the production of hydrocarbons with a high octane number starting from mixtures of n-butane/isobutane such as field butanes

Liquid mixture consisting of diesel gas oils and oxygenated compounds

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&deg; C., at a pressure of less than 5 MPa and at feeding space velocities of less than 60 h .

Process for the production of hydrocarbons with a high octane number by means of the selective dimerization of isobutene with acid catalysts

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&plus;alkyl ethers&plus;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&deg; C., at a pressure lower than 5 MPa and feeding space velocities of less than 30 h .

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Milan, Italy

Mario Marchionna