A method for producing ketones includes a) providing a feedstock of biological origin having fatty acids and/or fatty acid derivatives having an average chain length of 24 C-atoms or less; b) subjecting the feedstock to a catalytic ketonization reaction in the presence of aK.sub.2O/TiO.sub.2-catalyst; and c) obtaining from the ketonization reaction a product stream having ketones, which ketones have a longer average hydrocarbon chain length than the average hydrocarbon chain length in the feedstock, wherein step b) is carried out directly on the feedstock and in the presence of the K.sub.2O/TiO.sub.2-catalyst as the sole catalyst applied in the ketonization reaction.

A process for producing xylenes, in particular para-xylene that is less energy intensive than conventional processes is provided. In an embodiment the process comprises contacting a feed mixture in an isomerization zone with a catalyst at isomerization conditions and producing an isomerized product comprising a higher proportion of p-xylene than in the feed mixture, wherein the catalyst comprises an acidic sulfonated catalytic membrane. Xylene isomerization can also be coupled with a p-xylene extraction process, where the raffinate (p-xylene deprived stream) from the extraction process is fed to an isomerization reactor to produce p-xylene. In an embodiment, the process can comprise: a) providing a feed stream comprising a mixture of xylene isomers including p-xylene; b) extracting p-xylene from the feed stream using a separator to separate the feed stream into a p-xylene rich stream and a p-xylene deprived stream; and c) delivering the p-xylene deprived stream to an isomerization unit, the isomerization unit including an acidic sulfonated catalytic membrane, and using the isomerization unit to produce an isomerized product comprising a higher proportion of p-xylene than in the p-xylene deprived stream delivered to the isomerization unit. In any one or more aspects, the isomerization unit can be operated at a temperature in the range of less than 350°, for example about 20° C. to about 200° C.

The invention relates to a method for revamping a conventional refinery of mineral oils into a biorefinery, characterized by a production scheme which allows the treatment of raw materials of a biological origin (vegetable oils, animal fats, exhausted cooking oils) for the production of biofuels, prevalently high-quality biodiesel. This method allows the re-use of existing plants, allowing, in particular, the revamping of a refinery containing a system comprising two hydrodesulfurization units, U1 and U2, into a biorefinery containing a production unit of hydrocarbon fractions from mixtures of a biological origin containing fatty acid esters by means of their hydrodeoxygenation and isomerization, wherein each of the hydrodesulfurization units U1 and U2 comprises: a hydrodesulfurization reactor, (A1) for the unit U1 and (A2) for the unit U2, wherein said reactor contains a hydrodesulfurization catalyst; one or more heat exchangers between the feedstock and effluent of the reactor; a heating system of the feedstock upstream of the reactor; an acid gas treatment unit downstream of the reactor, containing an absorbent (B) for H2S, said unit being called T1 in the unit U1 and T2 in the unit U2, and wherein said method comprises: installing a line L between the units U1 and U2 which connects them in series; installing a recycling line of the product for the unit U1 and possibly for the unit U2, substituting the hydrodesulfurization catalyst in the reactor A1 with a hydrodeoxygenation catalyst; substituting the hydrodesulfurization catalyst in the reactor A2 with an isomerization catalyst; installing a y-pass line X of the acid gas treatment unit T2 of the unit U2; substituting the absorbent (B) in the acid gas treatment unit T1 with a specific absorbent for C02 and H2S. The operative configuration obtained with the method, object of the present invention, also leads to a substantial reduction in emissions of pollutants into the atmosphere, with respect to the original operative mode. The invention also relates to the transformation unit of mixtures of a biological origin obtained with said conversion method and particularly hydrodeoxygenation and isomerization processes.

The invention relates to a method for revamping a conventional refinery of mineral oils into a biorefinery, characterized by a production scheme which allows the treatment of raw materials of a biological origin (vegetable oils, animal fats, exhausted cooking oils) for the production of biofuels, prevalently high-quality biodiesel. This method allows the re-use of existing plants, allowing, in particular, the revamping of a refinery containing a system comprising two hydrodesulfurization units, U1 and U2, into a biorefinery containing a production unit of hydrocarbon fractions from mixtures of a biological origin containing fatty acid esters by means of their hydrodeoxygenation and isomerization, wherein each of the hydrodesulfurization units U1 and U2 comprises: a hydrodesulfurization reactor, (A1) for the unit U1 and (A2) for the unit U2, wherein said reactor contains a hydrodesulfurization catalyst; one or more heat exchangers between the feedstock and effluent of the reactor; a heating system of the feedstock upstream of the reactor; an acid gas treatment unit downstream of the reactor, containing an absorbent (B) for H2S, said unit being called T1 in the unit U1 and T2 in the unit U2, and wherein said method comprises: installing a line L between the units U1 and U2 which connects them in series; installing a recycling line of the product for the unit U1 and possibly for the unit U2, substituting the hydrodesulfurization catalyst in the reactor A1 with a hydrodeoxygenation catalyst; substituting the hydrodesulfurization catalyst in the reactor A2 with an isomerization catalyst; installing a y-pass line X of the acid gas treatment unit T2 of the unit U2; substituting the absorbent (B) in the acid gas treatment unit T1 with a specific absorbent for C02 and H2S. The operative configuration obtained with the method, object of the present invention, also leads to a substantial reduction in emissions of pollutants into the atmosphere, with respect to the original operative mode. The invention also relates to the transformation unit of mixtures of a biological origin obtained with said conversion method and particularly hydrodeoxygenation and isomerization processes.

Provided is a hydrotreating step (A) containing a hydroisomerization step (A1) that obtains a hydroisomerized oil (a1) by bringing a FT synthesis oil into contact with a hydroisomerization catalyst and/or a hydrocracking step (A2) that obtains a hydrocracked oil (a2) by bringing it into contact with a hydrocracking catalyst, and a fractionation step (B) that transfers at least a portion of the hydrotreated oil (a) composed of the hydroisomerized oil (a1) and/or the hydrocracked oil (a2) to a fractionator and, at the very least, obtains a middle distillate (b1) with a 5% distillation point of 130 to 170° C. and a 95% distillation point of 240 to 300° C., and a heavy oil (b2) that is heavier than the middle distillate (b1).

Provided is a hydrotreating step (A) containing a hydroisomerization step (A1) that obtains a hydroisomerized oil (a1) by bringing a FT synthesis oil into contact with a hydroisomerization catalyst and/or a hydrocracking step (A2) that obtains a hydrocracked oil (a2) by bringing it into contact with a hydrocracking catalyst, and a fractionation step (B) that transfers at least a portion of the hydrotreated oil (a) composed of the hydroisomerized oil (a1) and/or the hydrocracked oil (a2) to a fractionator and, at the very least, obtains a middle distillate (b1) with a 5% distillation point of 130 to 170° C. and a 95% distillation point of 240 to 300° C., and a heavy oil (b2) that is heavier than the middle distillate (b1).

A new catalyst hydroisomerizes C18 paraffins from fatty acids to a high degree to produce a composition with acceptable freeze point which retains 18 carbon atoms in the hydrocarbon molecule for jet fuel. We have discovered a fuel composition comprising at least 14 wt % hydrocarbon molecules having at least 18 carbon atoms and a freeze point not higher than −40° C. The composition also may exhibit a exhibiting a final boiling point of no more than 300° C. The hydroisomerization process can be once through or a portion of the product diesel stream may be selectively hydrocracked or recycled to hydroisomerization to obtain a fuel composition that meets jet fuel specifications.

The present disclosure relates to a method that includes a first treating of a first mixture that includes a carboxylic acid having between 2 and 12 carbon atoms, inclusively, to form a second mixture that includes a ketone having between 2 and 25 carbon atoms, inclusively, and a second treating of at least a first portion of the second mixture to form a first product that includes a paraffin having 8 or more carbon atoms.

A feed stream of cyclic paraffins may be separated to obtain an overhead of methylcyclopentane or cyclohexane and a bottoms stream cyclohexane or methylcyclohexane. The overhead stream may be subjected to separation of normal paraffins from non-normal paraffins with the former being isomerized or the entire overhead stream may be isomerized. In a further embodiment, the bottoms stream may be subjected to steam cracking. In an additional embodiment, the feed stream of cyclic paraffins may be formerly subjected to aromatic saturation.

Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).