Processes and apparatuses for isomerizing hydrocarbons are provided. In an embodiment, a process for isomerizing hydrocarbons includes providing a first hydrocarbon feed that includes hydrocarbons having from 5 to 7 carbon atoms. The first hydrocarbon feed is fractionated to produce a first separated stream that includes hydrocarbons having from 5 to 6 carbon atoms and a second separated stream that includes hydrocarbons having 7 carbon atoms. The first separated stream is contacted with a benzene saturation catalyst at benzene saturation conditions to produce an intermediate stream and subsequently isomerized in the presence of a first isomerization catalyst and hydrogen under first isomerization conditions to produce a first isomerized stream. The second separated stream is isomerized in the presence of a second isomerization catalyst and hydrogen under second isomerization conditions that are different from the first isomerization conditions to produce a second isomerized stream.

Processes and apparatuses for isomerizing hydrocarbons are provided. In an embodiment, a process for isomerizing hydrocarbons includes providing a first hydrocarbon feed that includes hydrocarbons having from 5 to 7 carbon atoms. The first hydrocarbon feed is fractionated to produce a first separated stream that includes hydrocarbons having from 5 to 6 carbon atoms and a second separated stream that includes hydrocarbons having 7 carbon atoms. The first separated stream is contacted with a benzene saturation catalyst at benzene saturation conditions to produce an intermediate stream and subsequently isomerized in the presence of a first isomerization catalyst and hydrogen under first isomerization conditions to produce a first isomerized stream. The second separated stream is isomerized in the presence of a second isomerization catalyst and hydrogen under second isomerization conditions that are different from the first isomerization conditions to produce a second isomerized stream.

Processes and apparatuses for isomerizing hydrocarbons are provided. In an embodiment, a process for isomerizing hydrocarbons includes providing a first hydrocarbon feed that includes hydrocarbons having from 5 to 7 carbon atoms. The first hydrocarbon feed is fractionated to produce a first separated stream that includes hydrocarbons having from 5 to 6 carbon atoms and a second separated stream that includes hydrocarbons having 7 carbon atoms. The first separated stream is contacted with a benzene saturation catalyst at benzene saturation conditions to produce an intermediate stream and subsequently isomerized in the presence of a first isomerization catalyst and hydrogen under first isomerization conditions to produce a first isomerized stream. The second separated stream is isomerized in the presence of a second isomerization catalyst and hydrogen under second isomerization conditions that are different from the first isomerization conditions to produce a second isomerized stream.

Bimetallic catalysts for the hydrodeoxygenation (HDO) conversion of lignin into useful hydrocarbons are provided. The catalysts are bifunctional bimetallic ruthenium catalysts Ru-M/X.sup.+Y comprising a metal M such as iron (Fe), nickel (Ni), copper (Cu) or zinc (Zn), zeolite Y and cation X.sup.+ (e.g. H.sup.+) associated with zeolite Y.

Bimetallic catalysts for the hydrodeoxygenation (HDO) conversion of lignin into useful hydrocarbons are provided. The catalysts are bifunctional bimetallic ruthenium catalysts Ru-M/X.sup.+Y comprising a metal M such as iron (Fe), nickel (Ni), copper (Cu) or zinc (Zn), zeolite Y and cation X.sup.+ (e.g. H.sup.+) associated with zeolite Y.

A mononuclear iron bivalent complex having iron-silicon bonds, which is represented by formula (1), can exhibit an excellent catalytic activity in at least one reaction selected from three reactions, i.e., a hydrosilylation reaction, a hydrogenation reaction and a reaction for reducing a carbonyl compound. ##STR00001## (In the formula, R.sup.1 to R.sup.6 independently represent a hydrogen atom, an alkyl group which may be substituted by X, or the like; X represents a halogen atom, or the like; L.sup.1 represents at least one two-electron ligand selected from an isonitrile ligand, an amine ligand, an imine ligand, a nitrogenated heterocyclic ring, a phosphine ligand, a phosphite ligand and a sulfide ligand, wherein, when multiple L.sup.1's are present, two L.sup.1's may be bonded to each other; L.sup.2 represents a two-electron ligand that is different from a CO ligand or the above-mentioned L.sup.1, wherein, when multiple L.sup.2's are present, two L.sup.2's may be bonded to each other; and m.sup.1 represents an integer of 1 to 4 and m.sup.2 represents an integer of 0 to 3, wherein the sum total of m.sup.1 and m.sup.2 (i.e., m.sup.1+m.sup.2) satisfies 3 or 4.)

A mononuclear iron bivalent complex having iron-silicon bonds, which is represented by formula (1), can exhibit an excellent catalytic activity in at least one reaction selected from three reactions, i.e., a hydrosilylation reaction, a hydrogenation reaction and a reaction for reducing a carbonyl compound. ##STR00001## (In the formula, R.sup.1 to R.sup.6 independently represent a hydrogen atom, an alkyl group which may be substituted by X, or the like; X represents a halogen atom, or the like; L.sup.1 represents at least one two-electron ligand selected from an isonitrile ligand, an amine ligand, an imine ligand, a nitrogenated heterocyclic ring, a phosphine ligand, a phosphite ligand and a sulfide ligand, wherein, when multiple L.sup.1's are present, two L.sup.1's may be bonded to each other; L.sup.2 represents a two-electron ligand that is different from a CO ligand or the above-mentioned L.sup.1, wherein, when multiple L.sup.2's are present, two L.sup.2's may be bonded to each other; and m.sup.1 represents an integer of 1 to 4 and m.sup.2 represents an integer of 0 to 3, wherein the sum total of m.sup.1 and m.sup.2 (i.e., m.sup.1+m.sup.2) satisfies 3 or 4.)

A mononuclear iron bivalent complex having iron-silicon bonds, which is represented by formula (1), can exhibit an excellent catalytic activity in at least one reaction selected from three reactions, i.e., a hydrosilylation reaction, a hydrogenation reaction and a reaction for reducing a carbonyl compound. ##STR00001## (In the formula, R.sup.1 to R.sup.6 independently represent a hydrogen atom, an alkyl group which may be substituted by X, or the like; X represents a halogen atom, or the like; L.sup.1 represents at least one two-electron ligand selected from an isonitrile ligand, an amine ligand, an imine ligand, a nitrogenated heterocyclic ring, a phosphine ligand, a phosphite ligand and a sulfide ligand, wherein, when multiple L.sup.1's are present, two L.sup.1's may be bonded to each other; L.sup.2 represents a two-electron ligand that is different from a CO ligand or the above-mentioned L.sup.1, wherein, when multiple L.sup.2's are present, two L.sup.2's may be bonded to each other; and m.sup.1 represents an integer of 1 to 4 and m.sup.2 represents an integer of 0 to 3, wherein the sum total of m.sup.1 and m.sup.2 (i.e., m.sup.1+m.sup.2) satisfies 3 or 4.)

A catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina, the nickel content being in the range 5% to 65% by weight of said element with respect to the total mass of catalyst, said active phase not comprising any metal from group VIB, the nickel particles having a diameter of less than 15 nm, said catalyst having a median mesopore diameter in the range 12 nm to 25 nm, a median macropore diameter in the range 50 to 300 nm, a mesopore volume, measured by mercury porosimetry, of 0.40 mL/g or more and a total pore volume, measured by mercury porosimetry, of 0.45 mL/g or more. The process for the preparation of said catalyst, and its use in a hydrogenation process.

A catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina, the nickel content being in the range 5% to 65% by weight of said element with respect to the total mass of catalyst, said active phase not comprising any metal from group VIB, the nickel particles having a diameter of less than 15 nm, said catalyst having a median mesopore diameter in the range 12 nm to 25 nm, a median macropore diameter in the range 50 to 300 nm, a mesopore volume, measured by mercury porosimetry, of 0.40 mL/g or more and a total pore volume, measured by mercury porosimetry, of 0.45 mL/g or more. The process for the preparation of said catalyst, and its use in a hydrogenation process.