US20070267324A1

US20070267324A1 - Process and Catalysts for the Production of Linear Alkanes

Info

Publication number: US20070267324A1
Application number: US10/590,313
Authority: US
Inventors: Leonardo Dalloro; Alberto Cesana; Roberto Buzzoni; Franco Rivetti
Original assignee: Polimeri Europa SpA
Current assignee: Versalis SpA
Priority date: 2004-02-23
Filing date: 2005-02-04
Publication date: 2007-11-22
Also published as: WO2005080532A1; CA2556571A1; ITMI20040299A1; CN1934229A; EP1778820A1; EA200601355A1; BRPI0507920A

Abstract

The invention relates to a process for the production of linear alkanes, containing less than 6′ carbon atoms, from a mix comprising one or more hydrocarbons containing at least 6 carbon atoms. The process uses a catalytic composition comprising particular combinations of a Y-type zeolite, at least one element selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals of Group VIII and optionally one or more lanthanides.

Description

The present invention relates to a process for the production of linear alkanes containing less than 6 carbon atoms, which comprises putting a mix including one or more hydrocarbons containing at least 6 carbon atoms, in contact with a suitable catalytic composition containing one or more metals and a Y-type zeolite.
The mixtures which can be used for the process of the present invention are, for example, mixtures comprising one or more C6+ hydrocarbons selected from alkanes, alkenes with one or more unsaturations, aromatic compounds. In particular, these mixtures can be fractions from mineral oil, fractions from catalytic or thermo conversion plants, and fractions deriving therefrom by hydrogenation.
Mixtures of hydrocarbons rich in aromatic components are very common in the petrochemical industry: for example, those deriving from the steam-cracking of virgin naphtha to olefins, or those obtained from the reforming of petroleum fractions, can be mentioned.
Low molecular weight aromatic compounds (<9 carbon atoms) which can be obtained from these mixtures, are widely used as chemical intermediates and as components of motor-vehicle fuels. The use of medium molecular weight (up to 12 carbon atoms) components of these mixtures as chemical intermediates and in fuels is more restrained, but still economically important. The use of higher molecular weight components is less advantageous and their main destination is as a low-price fuel.
The percentage of aromatic compounds which are used as fuel components is inevitably decreasing. The legislation in Europe, as well as in other parts of the world, is in fact tending to progressively decrease the aromatic content in fuel, for environmental reasons, and there will therefore be an excess production of aromatic products with 7 and 8 carbon atoms, which will not easily find alternative uses in the chemical field and a significant loss in the value of these fractions is expected in a reasonably near future.
Higher molecular weight fractions already have a current low market value, in fact, with the rare exceptions of mixtures with a moderate content of asphaltenes, they are at the same price level as fuel oil.
In particular, mixtures containing hydrocarbons with a different chemical structure for which the necessity is presently felt for finding alternative means of exploitation, are those deriving from so-called cracking gasolines and reforming residues. These hydrocarbon fractions derive from cracking gasolines (also called pyrolysis asoline or pygas) or from reforming gasoline after the ore valuable components, such as benzene, toluene and ylenes, have been at least partially separated from hem. Cracking/reforming gasolina residue does not have a fixed composition, also because mixtures of a different origin can be joined in varying proportions. From the point of view of the components, it should be pointed out that benzene, toluene and xylenes are still present in these mixtures, as the previous separation process is never total, the main components present are aliphatic hydrocarbons with varying structures having 7-9 carbon atoms, ethyl benzene and other alkyl benzenes with 9-12 carbon atoms, styrene and methyl styrenes, methyl cyclopentadiene, dicyclopentadiene and various co-dimers of cyclopentadiene and methyl cyclopentadiene starting from 9 carbon atoms (for example in the case of the codimer between cyclopentadiene and butadiene) up to 15 carbon atoms (for example in the case of co-dimers between methyl styrene and methyl cyclopentadiene), indene and methyl indenes, naphthalene and methyl naphthalenes. In mixtures of this type there are therefore carbon-carbon bonds prevalently of the aromatic type, but bonds of the aliphatic, olefinic and dienic type are present, prevalently with cyclic structures.
Fractions containing alkanes and/or alkenes with one or more unsaturations for which the necessity is felt for finding alternative means of exploitation, can directly derive from the fractionation of crude mineral oil, but for the purposes of the present invention, mixtures deriving from other processings and which, being by-products, have a low commercial value, are considered as being preferential. Mixtures of hydrocarbons of particular interest are those which do not require any further preliminary intervention of a chemical or physico-chemical nature, for example residual paraffinic waxes from the dewaxing treatment of lubricants, mixtures, however, obtained with known treatments, which are relatively simple and with a wide application, can also be well used, such as for example naphthene fractions deriving from the hydrogenation of aromatic hydrocarbon mixtures.
With respect to the possible exploitation of various hydrocarbon cuts described above, conversion processes of mineral oil fractions comprising cyclic and aromatic alkanes to non-cyclic branched alkanes, are known in the state of the art.
U.S. Pat. No. 5,831,139, for example, describes a process for the production of aliphatic fuels from naphtha with a high boiling point. The naphtha is subjected to hydrogenation, in a first step, to transform the aromatic compounds into cyclic alkanes. After the hydrogenation, the synthesis of isoparaffins is effected in a second phase. liphatic gasoline components are produced with this process by the opening of the ring and the synthesis of isoparaffins, with as many branchings as possible, without a decrease in the number of carbon atoms with respect to the hydrocarbons charged. The octane number of the product must in fact be high.
U.S. Pat. No. 5,334,792, as in the above patent U.S. Pat. No. 5,831,139, describes a process for the opening of the ring for aromatic and cyclo-aliphatic compounds. This opening step is followed by an isomerization step. Also in this case, iso-alkanes are produced without a reduction in the number of carbon atoms with respect to the starting hydrocarbons.
The conversion, by means of ring opening, of fractions containing naphthenes in diesel fuels, is also known. A process of this type is described, for example, in WO 97/09288. Also in this case, alkanes are produced without a decrease in the number of carbon atoms with respect to the hydrocarbons charged. The cetane number of the product must be as high as possible.
The processes of the known art therefore aim at transforming aromatic or cyclo-aliphatic compounds into iso-alkanes or alkanes with a high number of carbon atoms, suitable for diesel fuels, i.e. the transformations take place without a substantial variation in the number of carbon atoms.
An object of the present invention relates to a process which allows hydrocarbons mixtures deriving from mineral oil, to be transformed by means of a catalyzed hydrocracking reaction, into linear alkanes with a lower molecular weight, in particular linear alkanes containing less than 6 carbon atoms, which are an excellent charge for steam-cracking plants.
WO 01/27223 claims, for this purpose, the use of zeolites with a Spaciousness Index (S.I.) lower than 20, exchanged with hydrogenating metals. The preferred zeolite is ZSM-5 exchanged with palladium.
Using this catalyst, the complete conversion of model charges (toluene, cyclo-hexane or pseudo-cumene) is obtained with a distribution of the reaction products ranging from methane to butanes. Approximately 5% of methane is formed among the alkanes, which is a compound that in the subsequent steam-cracking treatment of the mixture obtained with the process indicated, does not give any yield to olefins. In WO 01/27223, it is demonstrated that large pore zeolites, such as Y-zeolite (S.I.=21) cannot be used in this reaction as their catalytic activity rapidly declines. After only 8 hours of life, using Y-zeolite in acidic form, the conversion, in fact, passes from 1000 to 74%. The life of ZSM-5 zeolite/Pd, on the contrary, is at least 10 hours.
Italian patent application MI2003A000347 describes a process for the conversion of mixtures containing aromatic compounds in linear alkanes which uses a catalytic composition containing at least one lanthanide, at least one metal of group VIII and a Y-type zeolite.
It has now been found that by using catalytic compositions containing a Y-type zeolite in a mixture with suitable elements, it is possible to produce linear alkanes with a low molecular weight, in particular linear alkanes containing less than 6 carbon atoms, from mixtures comprising one or more hydrocarbons whose structure contains at least 6 carbon atoms.
An object of the present invention therefore relates to a process for the production of linear alkanes containing less than 6 carbon atoms which comprises putting a mixture comprising one or more hydrocarbons containing at least 6 carbon atoms, in contact with a catalytic composition comprising:

a) at least an element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals of group VIII Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt,
b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
with the exclusion of a catalytic composition comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B when the mixture treated is a mixture containing aromatic compounds.

The process of the present invention allows n-alkanes to be obtained, with a lower number of carbon atoms than that of the hydrocarbon fed. In particular, prevalently linear alkanes containing from 2 to 5 carbon atoms, are obtained.
Various kinds of hydrocarbon charge can be used and the resulting products form an excellent feed for steam-cracking plants, where they undergo transformation into olefins, mainly ethylene and propylene. With these catalytic compositions optimum results are obtained in terms of activity and catalytic life.
The mixtures which can be subjected to the process of the present invention are mixtures comprising one or more hydrocarbons, whose structure contains at least 6 carbon atoms, selected from aromatic compounds, alkanes or alkenes with one or more unsaturations. The aromatic compounds can contain several condensed benzene rings.
Mixtures containing aromatic compounds or mixtures containing one or more alkanes with open chains or cyclic structures and/or alkenes having one or more unsaturations with open-chains or cyclic structures, optionally mixed with aromatic compounds, are preferably used.
For mixtures containing aromatics, catalytic compositions are used, comprising:

(a) at least an element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals belonging to group VIII,
(b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
with the exclusion of a catalytic composition comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and modified Y-zeolite.

Modified Y-zeolite always refers in this description to a Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B.
In particular, the mixtures containing aromatic compounds can be treated with catalytic compositions which essentially consist of:

(a) at least an element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals belonging to group VIII,
(b) a zeolite selected from Y-zeolite and modified Y-zeolite.

According to an aspect of the invention, catalytic compositions additionally containing one or more lanthanides, can be used.
A further aspect of the present invention therefore relates to a process for the production of linear alkanes containing less than 6 carbon atoms which comprises putting a mixture comprising one or more hydrocarbons containing at least 6 carbon atoms, in contact with a catalytic composition comprising:

a) at least an element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals of group VIII, Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt,
b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
c) one or more lanthanides,
with the exclusion of a catalytic composition comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and modified Y-zeolite when the mixture treated is a mixture containing aromatic compounds.

In the case of mixtures containing aromatic compounds, compositions can be well used, containing:

a) at least an element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti,
b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
c) one or more lanthanides,
with the exclusion of a catalytic composition comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and modified Y-zeolite.

In particular, mixtures containing aromatic compounds can be converted using catalytic compositions essentially consisting of:

a) at least an element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti,
b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
c) one or more lanthanides.

Y-zeolite is described for the first time in U.S. Pat. No. 3,130,007 and has the following formula expressed in terms of moles of oxides
0.9±0.2 Na₂O.Al₂O₃.wSiO₂.xH₂O
wherein w has a value greater than 3 up to about 6 and x can be a value up to about 9. Its preparation is described for example in “Verified Synthesis of Zeolitic materials” H. Robson Editor, Elsevier, second revised edition 2001, whereas the post-synthesis treatment to which the Y-zeolite can be subjected, including dealumination, is described in “Introduction to Zeolite Science and Practice” chapter 5, H. van Bekkum et al. Editors, Studies in Surface Science and Catalysis, vol. 58, Elsevier. In the compositions of the present invention, Y-zeolites can be used with a molar ratio SiO₂/Al₂O₃ranging from 3 to 400.
Modifications of the Y-zeolite obtained by partial or total isomorphous substitution of the aluminum of the zeolite with Fe, Ga or B, and/or partial or total substitution of the Si with Ti or Ge, can also be used in the process of the present invention. These modifications of the Y-zeolite can be prepared, for example, by substituting, in the synthesis process of the Y-zeolite described in U.S. Pat. No. 3,130,007, part of the silicon and/or aluminum sources with sources of Fe, Ga, B, Ti and/or Ge. The Y-zeolite in which Ge has totally substituted the Si is described in R. M. Barrer et al. J. Chem. Soc., 195-208 (1959) and in G. M. Johnson, Microporous and Mesoporous Material, 31, 195-204 (1999); the Y-zeolite in which the Si and Al have been completely substituted by Ge and Ga are described in Barrer, J. Chem. Soc., 195-208 (1959).
The catalytic composition of the present invention preferably contains the zeolite in partially acidic form, that is part of the cationic sites present in the zeolite is occupied by hydrogen ions.
A particularly preferred aspect is to use Y-zeolite. In the Y-zeolite, the molar ratio between silicon oxide and aluminum oxide preferably ranges from 5 to 50.
With respect to the element Me, compositions containing Pt, Pd, Ti, Mo, Zn, Cu or Ni, are preferably used. Among the metals of group VIII, Pd is preferably adopted. The mixtures of elements preferably used are selected from Pd/Ti, Zn/Mo, Cu/Zn and Ni/Mo.
The element Me can be present in the catalytic composition in the form of an oxide, ion, metal, sulfide or a mixture of these forms can be present. In particular, the elements Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, are prevalently present in the form of oxides, the elements of group VIII are prevalently present in the metal form.
When Me is an element selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, the quantity of Me, expressed as an element, can vary from 0.1 to 50% by weight, preferably from 0.5 to 30% by weight, with respect to the total weight of the catalytic composition.
When Me is an element selected from metals of group VIII, the quantity of Me, expressed as an element, can vary from 0.001 to 10% by weight, preferably from 0.1 to 5% by weight with respect to the total weight of the catalytic composition.
When present, the element belonging to the group of lanthanides which is preferably used is lanthanum.
The lanthanide, or lanthanides, present in the catalytic composition can be in the form of an oxide or ion or a mixture of these forms can be present. The quantity of lanthanide, or lanthanides, expressed as an elements can vary from 0.5 to 20% by weight, preferably from 1 to 15% by weight, with respect to the total weight of the catalytic composition.
The catalytic compositions of the present invention are prepared by introducing the element Me by means of the ionic exchange or impregnation techniques.
If the element Me is introduced by ion exchange, the zeolite, preferably in acidic form, is treated with an aqueous solution of a salt of the element Me. For example, in the case of metals of group VIII, an aqueous solution can be used with a concentration of 0.01-0.5 M, preferably 0.01-0.1 M, of a corresponding complex. For palladium, Pd(NH₃)₄(NO₃)₂, can be used, for example.
The sample deriving from the ion exchange, is dried, after suitable washings, and then calcined at a temperature ranging from 400 to 600° C. for 1-10 hours.
If the element Me is introduced by impregnation, the known incipient wetness inbibition technique (wet imbibition) is adopted, wherein the volume of solution containing a salt of the element Me corresponds to the pore volume of the zeolite, it is then dried and calcined as in the case of the ion exchange. Also in this case, an aqueous solution of a salt of the element Me is used, preferably with an anion which does not leave residues in the end-product, for example a nitrate or an acetate decomposable by calcination. When the quantity of the element Me to be introduced is high, the salt to be added is divided and various impregnations are effected, with drying phases in between. The drying is carried out by heating the sample and, in order to facilitate the evaporation of the solvent, vacuum or a stream of gas can be optionally used.
As a result of the calcination, an at least partial transformation of the ion of the element Me into the corresponding oxide, can take place.
Impregnation is the preferred technique for introducing the element Me.
In catalytic compositions in which the introduction f more than one element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti and metals of group VIII on the zeolite, preferably in acidic form, is required, the elements can be introduced separately or contemporaneously. In the former case, the calcination between the introduction step of a first element and the introduction step of a second element is optional; if this calcination is not effected, the partial transformation of the ions into the corresponding oxides, takes place contemporaneously during the calcination effected at the end of the second step.
According to the preferred technique, the introduction of several elements is effected contemporaneously and for this purpose, aqueous solutions containing said elements in the desired atomic ratio, are used.
When the catalytic composition envisages the introduction of a lanthanide, any of the known techniques can be used, such as exchange in the solid state with a lanthanide salt, ion exchange in aqueous solution or impregnation.
Ion exchange or impregnation is preferably used.
In the former case, the zeolite, preferably in acidic or ammonium form, is treated with an aqueous solution of a lanthanum salt having a concentration varying from 0.01 to 1.0 M, preferably from 0.01 to 0.5 M. For example, an aqueous solution can be used, within the concentration limits indicated above of lanthanum nitrate, citrate, acetate, chloride or sulfate, at reflux temperature for 1-24 hours. After suitable washings with distilled water, the sample deriving from the ion exchange is dried and then calcined at a temperature ranging from 400 to 600° C for 1-10 hours.
If the lanthanide is introduced by impregnation, the incipient wetness imbibition technique is used and it is then dried and calcined as in the case of ion exchange.
As a result of the calcination, an at least partial transformation of the lanthanide ion into the corresponding oxide, takes place.
Ion exchange is the preferred technique for introducing the lanthanide.
The catalytic compositions of the present invention containing one or more lanthanides and one or more elements Me can be prepared using a mixture of compounds of these elements and any of the techniques described above.
These catalytic compositions are preferably prepared by introducing first the lanthanide and then the element Me onto the zeolite. The zeolite used in the preparation is preferably in acidic form. When these catalytic compositions contain one or more lanthanide or more than one element Me, a mixture of compounds of these elements is used in their preparation.
According to a particularly preferred aspect, the catalytic compositions of the present invention containing lanthanum are prepared by inserting the lanthanide in the zeolite in acidic form by means of ion exchange, optionally calcining the product thus obtained, and then depositing the element Me by ion exchange and calcining the product obtained.
Whatever technique may have been selected for introducing the lanthanide and element Me, the calcination between the introduction of the lanthanide and the introduction of the element Me is generally optional and if it is not effected, the partial transformation of the ions into the corresponding oxides takes place contemporaneously during the calcination effected at the end of the second step.
Catalytic compositions containing or consisting of Y-zeolite and Pd, Y-zeolite and Pt, Y-zeolite and Zn, Y-zeolite and Mo, Y-zeolite and Ni; Y-zeolite and Pd together with Ti, Y-zeolite and Zn together with Mo, Y-zeolite and Zn together with Cu, Y-zeolite and Mo together with Ni, Y-zeolite and La together with Zn and Mo, Y-zeolite and La together with Zn and Cu, are particularly preferred.
When the catalytic composition contains elements of group VIII, following the synthesis step, there may be an at least partial reduction step of the relative ions to the corresponding elements. Reduction to the element can be obtained by means of treatment of the catalytic composition with hydrogen or with a reducing agent, and it can be effected on the catalytic composition before its use or in the reactor itself in which the catalytic composition is used.
The catalytic composition of the present invention can be used in a mixture with suitable binders such as silica, alumina, clay. The catalytic composition and the binder are mixed in a proportion ranging from 5:95 to 95:5, preferably from 30:70 to 95:5, even more preferably from 50:50 to 90:10. The mixture of the two components is processed, according to the known techniques, into the desired end-form, for example cylindrical extruded products or other known forms.
The mixtures containing aromatic compounds which are suitable for being treated according to the process of the present invention, are for example fractions coming from thermal or catalytic conversion plants, and mineral oil fractions rich in aromatic compounds, such as for example pyrolysis gasolines or pygas, fractions coming from pyrolysis gasolines, in particular those from which the light aromatic compounds (from 6 to 8 carbon atoms) have been separated and residual fractions with a low commercial value coming from production plants of aromatic compounds and reforming.
In particular, pyrolysis gasolines are a by-product of steam cracking processes in which ethylene and propylene are obtained from light hydrocarbon cuts such as straight-run naphtha (oil fraction substantially containing C₅and C₆hydrocarbons), LPG (Liquefied Petroleum Gas, an oil fraction containing C₃and C₄hydrocarbons), propane or ethane.
Mixtures containing one or more alkanes with open chains or with cyclic structures and/or alkenes having one or more unsaturations with open chains or cyclic structures, which are suitable for being treated according to the process of the present invention, are those deriving from the fractionation of crude mineral oil or from the hydrogenation of mineral oil fractions or the hydrogenation of cracking plant fractions.
The hydrogenation of these fractions can be carried out with any of the known methods and catalysts, such as, for example, those based on Ni carried on alumina. The fractions deriving from this treatment prevalently or completely contain alkane compounds with a cyclic structure.
The charges suitable for being treated with the process of the present invention can be optionally mixed with heavier fractions, coming for example from fuel oil from steam cracking (FOK) or Light Cycle Oil (LCO) from fluid bed catalytic cracking. These heavy fractions contain polycyclic aromatic compounds having up to 20-21 carbon atoms. As these heavy fractions also contain sulfur, which is known to be poisonous for hydrogenation catalysts, an unexpected and extremely advantageous aspect is that the catalytic compositions of the present invention do not, on the contrary, undergo any deactivation due to the sulfur and are therefore capable of processing mixtures of aromatic hydrocarbons also containing heavier fractions, such as, for example, FOK and LCO.
During the treatment of these mixtures, there may be an at least partial transformation of the elements Me contained in the catalytic composition used, for example Mo, Zn, Cu, into the corresponding sulfides. As already mentioned, this transformation does not seem to invalidate the activity of the catalytic composition.
The dilution of very heavy mixtures (FOK, LCO) with lighter fractions is not indispensable. Another unexpected aspect of the present invention relates to the processing of heavier fractions, coming, for example, from fuel oil from steam cracking (FOK) or Light Cycle Oil (LCO) from fluid bed catalytic cracking, also without dilution with fractions coming from gasolines, provided a process is effected which avoids feeding heavier polycyclic components such as asphaltenes, to the conversion reactor to light paraffins. For this purpose, the fuel oil fraction can be subjected to treatment such as extraction with a solvent, distillation or, even better, evaporation with suitable equipment (Luwa thin film evaporator or similar equipment).
U.S. Pat. No. 5,932,090 describes, for example, a process for the conversion of heavy crude oils or distillation residues which, after a hydrocracking phase in the presence of hydrogen and a suitable catalyst, comprises distillation of the product to recover the most volatile hydrocarbons. By deasphalting the distillation residue, a mixture of hydrocarbons is obtained (called DAO, deasphalted oil), from which a feed can be obtained, which is suitable for the process of the present invention.
Also in these cases, the catalytic compositions of the present invention unexpectedly do not undergo any deactivation due to the sulfur which can be contained in these mixtures and there can be an at least partial transformation of the elements Me contained in the cataytic composition used into the corresponding sulfides without a loss in the catalytic activity.
The mixtures containing aromatic compounds which can be subjected to the process of the present invention, and in particular pyrolysis gasolines, generally prevalently contain toluene, ethyl benzene, xylenes, benzene and C₉aromatic compounds, but also naphthalene and alkyl derivatives of naphthalene, for example mono and polysubstituted methyl and ethyl derivatives. The intermediate fractions and fuel oils such as FOK and LCO can contain aromatic compounds with >20 carbon atoms, such as, for example, aromatic compounds with 2-4 condensed benzene rings, naphthalene, phenanthrene, anthracene, benzanthracene, with the relative alkyl derivatives (in particular methyl and/or ethyl derivatives) and phenyl derivatives, indene, biphenyl, fluorene, binaphthyl.
According to an aspect of the present invention, the resulting fraction of n-alkanes is prevalently made up of ethane, propane, n-butane and n-pentane.
According to a preferred aspect of the present invention, the fraction of linear alkanes containing from 2 to 5 carbon atoms ranges from 50 to 90% by weight of the resulting product.
The process of the present invention is carried out in the presence of hydrogen or a mixture of hydrogen and H₂S at a pressure ranging from 5 to 200 bar, preferably from 25 to 100 bar, at a temperature ranging from 200° C. to 700° C., preferably from 3000 to 600° C. A weight ratio H₂/charge ranging from 0.1 to 1.4, more preferably from 0.1 to 0.7, is preferably adopted.
According to a particular aspect of the invention, it is possible to operate with the use, in addition to hydrogen, of a diluent, and for this purpose, a paraffin, for example methane or ethane, can be used.
A particular advantageous aspect of the present invention relates to the possibility of using hydrogen or a diluent containing H₂S impurities. As specified above, the catalysts used in the present invention are not generally sensitive to the presence of sulfur.
The process is preferably carried out in continuous, in a fixed bed or fluid bed reactor, in gaseous or partially liquid phase, at a WHSV (Weight Hourly Space Velocity, expressed in kg of charge/hour/kg of catalyst) ranging from 0.1 to 20 hours⁻¹, preferably from 0.2 to 5 hours⁻¹, even more preferably from 0.5 to 3 hours⁻¹.
The alkenes with one or more unsaturations present in the feed are converted according to the process described in the present invention analogously to the other hydrocarbons, both alkanes and aromatic compounds. It has been verified however that the presence of compounds of this type can, in some cases, facilitate the formation of oligomers/polymers under the conditions in which the process, object of the invention, is carried out, and it may therefore be preferable to previously subject the mixtures containing them to hydrogenation in order to prolong the duration of the industrial run, without frequent stoppages and intermediate regenerations of the catalytic bed. The preliminary hydrogenating treatment can be carried out at a low temperature, in liquid phase, according to technologies already known, for example applied to the fractions of hydrocarbons destined for use as fuel for motor vehicles; this is generally light hydrogenating treatment normally but not exclusively effected with Pd-based catalysts on alumina.
Before use, the catalytic composition of the present invention is preferably activated in nitrogen at a temperature ranging from 300 to 700° C., for a time ranging from 1 to 24 hours and at a pressure varying from 0 to 10 barg.
In addition to or in substitution of the above, in particular when elements of group VIII are present, an activation with hydrogen can be effected at a temperature of 300-700° C., a pressure of 0-10 barg, for a time ranging from 1 to 24 hours.
The catalyst allows long operating periods before showing signs of deactivation; the catalyst however can be subjected to regeneration treatment, re-establishing its original performances. The most suitable method is by the combustion of the carbonaceous deposits accumulated in the operating period, according to what is known in the state of the art, operating, for example, at a temperature ranging from 450 to 550° C., at a pressure ranging from 1 to 3 bar, with mixtures of oxygen and nitrogen in a ratio ranging from 0.1 to 206 by volume and with a space velocity (GHSV=Gas Hourly Space Velocity, expressed in l of gas mixture/hour/l of catalyst) ranging from 3000 to 6000 hours⁻¹. Considering the low regeneration frequency, it is not necessary for the regeneration to be effected in the same reactor in which the catalyst is introduced for the reaction; the catalyst can be discharged during the periodic plant maintenance phases and regenerated elsewhere, in this way the reactor can be constructed without control devices necessary for carrying out the regeneration.
The catalytic compositions used in the present invention are new and a further object of the present invention therefore relates to a catalytic composition comprising:

(a) at least one element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti and metals of group VIII Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt,
(b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
with the exclusion of catalytic compositions comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and modified Y-zeolite.

These compositions can additionally contain one or more lanthanides.
An object of the present invention also relates to a process for the production of linear alkanes containing less than 6 carbon atoms from mixtures containing aromatic compounds having a structure with at least 6 carbon atoms using a catalytic composition essentially consisting of:

(a) at least one element Me selected from Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti in a mixture with one or more metals of group VIII,
(b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,
c) one or more lanthanides.

The catalytic compositions used in said process are also new and object of the present invention.
Some illustrative but non-limiting examples are provided for a better understanding of the present invention and for its embodiment, but should in no way be considered as limiting the scope of the invention itself.

EXAMPLES OF CATALYST PREPARATION

EXAMPLE 1

20 g of Y-zeolite in commercial extruded acidic form (Zeolyst CBV500 CY (1.6)) with a molar ratio SiO₂/Al₂O₃equal to 5.2, and a solution consisting of 160 ml of water and 11.2 g of an aqueous solution of tetra-amine palladium nitrate (Pd 5% max., Alfa Aesar), are charged into a glass flask. The solution is stirred for 4 hours at room temperature; at the end of this period, it is filtered on a Buckner funnel, washed and dried in an oven at 120° C. for 16 hours. Calcination is effected at a temperature of 400° C. in air, for 12 hours. A Y-zeolite is obtained, containing 2.1% by weight of Pd.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 2

30 g of the same Y-zeolite used in Example 1 are charged into a glass flask. A solution is prepared, using 4.6 g of ammonium heptamolybdate, 5.2 g of hexahydrated zinc nitrate and 62.4 g of demineralized water. The extruded zeolite is impregnated using the incipient wetness imbibition technique, with a third of the previous solution, dried at 120° C., impregnated again with a third of the solution, dried again, further impregnated with the remaining volume of the solution, dried and then calcined at 500° C. for 4 hours.
A catalyst is obtained with 7.0% by weight of Mo and 3.2% by weight of Zn.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 3

30 g of the same Y-zeolite used in Example 1 are charged into a glass flask. A solution is prepared, using 6.08 g of tri-hydrated copper nitrate, 4.76 g of hexahydrated zinc nitrate and 62.4 g of demineralized water. The extruded zeolite is impregnated using the incipient wetness imbibition technique, with a third of the previous solution, dried at 120° C., impregnated again with a third of the solution, dried again, further impregnated with the remaining volume of the solution, dried and then calcined at 500° C. for 4 hours.
A catalyst is obtained with 4.8% by weight of Cu and 3.1% by weight of Zn.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 4

30 g of the same Y-zeolite used in Example 1 are charged into a glass flask. A solution is prepared using 2.316 g of ammonium heptamolybdate and 62.4 g of demineralized water. The extruded zeolite is impregnated using the incipient wetness imbibition technique, with a third of the previous solution, dried at 120° C., impregnated again with a third of the solution, dried again, further impregnated with the remaining volume of the solution, dried and then calcined at 500° C. for 4 hours.
A catalyst is obtained with 4.0% by weight of Mo.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 5

30 g of the same Y-zeolite used in Example 1 are charged into a glass flask. A solution is prepared, using 2.72 g of hexa-hydrated zinc nitrate and 30 g of demineralized water. The extruded zeolite is impregnated using the incipient wetness imbibition technique, with a third of the previous solution, dried at 120° C., impregnated again with a third of the solution, dried again, further impregnated with the remaining volume of the solution, dried and then calcined at 500° C. for 4 hours.
A catalyst is obtained with 1.9% by weight of Zn.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 6

75 g of commercial Y-zeolite (Tosoh HSZ 320 HOA) with a molar ratio SiO₂/Al₂O₃equal to 5.5 and a sodium content, as Na₂O oxide, of 4% by weight, and 1500 g of a 2 molar aqueous solution of ammonium nitrate, are charged into a 2 liter glass flask. The suspension is maintained under reflux conditions for 3 hours, under stirring; after this period, it is filtered on a Buckner vacuum funnel, is dried in an oven and calcined at a temperature of 550° C. in air, for 5 hours, obtaining a Y-zeolite in acidic form. 20 g of the solid product thus obtained are exchanged with a solution consisting of 160 ml of water and 11.2 g of an aqueous solution of tetra-amine palladium nitrate (Pd 5% max., Alfa Aesar). The mixture is stirred for 4 hours, at room temperature. After this period, it is filtered on a Buckner funnel, washed and dried in an oven at 120° C. for 16 hours. Calcination is effected at a temperature of 400° C in air for 12 hours. 16 g of the catalyst thus obtained are mixed with 10.81 g of pseudoboehmite VERSAL 250 (UOP) and 64 g of an aqueous solution of acetic acid at 1.5%. The whole mixture is stirred for 30 minutes at room temperature, and is then dried on a heated plate. It is subsequently dried at 120° C. for 16 hours and is calcined at 500° C. for 4 hours.
A Y-zeolite is obtained, containing 1.5% by weight of Pd, bound with alumina, wherein the amount of binder corresponds to about 30% of the total weight of the catalytic composition.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 7

25 g of the same Y-zeolite used in Example 1 are treated with a solution containing 43.3 g of hexahydrated lanthanum nitrate in 500 g of demineralized water. The solution is maintained under reflux conditions for 3 hours under stirring. At the end of this period, the solution is filtered, the filtrate is washed with distilled water and is dried in an oven. The above operation is repeated three more times, with a total of four exchanges with the lanthanum nitrate solution.
The material obtained, after the last exchange, is dried in an oven and then calcined in a muffle at 550° C.
A solution is prepared, using 1.38 g of ammonium heptamolybdate, 1.56 g of hexahydrated zinc nitrate and 38 g of demineralized water. 18 g of the previously prepared zeolite containing lanthanum, are impregnated by means of the incipient wetness imbibition technique, with a third of the previous solution, dried at 120° C., impregnated again with a third of the solution, dried again, further impregnated with the remaining volume of the solution, dried and then calcined at 500° C. for 4 hours.
A catalyst is obtained with 4.4% by weight of La, 4.2% by weight of Mo and 1.6% by weight of Zn.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 8

75 g of the same Y-zeolite used in Example 6 and 1,500 g of a 2 molar aqueous solution of ammonium nitrate, are charged into a 2 liter glass flask. The suspension is maintained under reflux for 3 hours under stirring; after this period, it is filtered on a vacuum Buckner funnel, dried in an oven and calcined in air at a temperature of 5500C for 5 hours, obtaining a Y-zeolite in acidic form.
25 g of the solid product thus obtained are treated with a solution containing 43.3 g of hexahydrated lanthanum nitrate in 500 g of demineralized water. The solution is maintained under reflux conditions for 4 hours, under stirring. At the end of this period, the solution is filtered, the filtrate is washed with distilled water and dried in an oven. The above operation is repeated three more times, with a total of four exchanges with the lanthanum nitrate solution.
The material obtained after the last exchange, is dried in an oven and then calcined in a muffle at 550° C.
20 g of the calcined product are treated at room temperature with a solution consisting of 160 ml of water and 11.2 g of an aqueous solution of tetra-amine palladium nitrate (Pd 5% max., Alfa Aesar). The whole mixture is stirred for 4 hours, at room temperature. After this period, it is filtered on a Buckner funnel, washed and dried in an oven at 120° C. for 16 hours. Calcination is effected at a temperature of 400° C. in air for 12 hours.
16 g of the catalyst thus obtained are mixed with 10.81 g of pseudoboehmite VERSAL 250 (UOP) and 64 g of an aqueous solution of acetic acid at 1.5%. The whole mixture is stirred for 30 minutes at room temperature, and is then dried on an heated plate. It is subsequently dried at 120° C. for 16 hours and is calcined at 500° C. for 4 hours.
A Y-zeolite is obtained, containing 2.1% by weight of La and 1.0% by weight of Pd, bound with alumina, wherein the amount of binder corresponds to about 30% of the total weight of the catalytic composition.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLE 9

30 g of the same Y-zeolite used in Example 1 are charged into a glass flask. A solution is prepared using 2.3 g of ammonium heptamolybdate, 2.6 g of hexahydrated zinc nitrate and 62.4 g of demineralized water. The extruded zeolite is impregnated using the incipient wetness inbibition procedure, with a third of the previous solution, dried at 120° C., impregnated again with a third of the solution, dried again, further impregnated with the remaining volume of the solution, dried and then calcined at 500° C. for 4 hours.
A catalyst is obtained with 3.8% by weight of Mo and 1.7% by weight of Zn.
The material is crushed to granules within the 20-40 mesh range.

EXAMPLES OF CATALYTIC PERFORMANCES

The catalytic activity tests indicated in the following examples were carried out in the experimental equipment and with the operative conditions described hereunder.
Catalytic Test: Equipment and Operative Conditions
The conversion of hydrocarbon mixtures is carried out in a fixed bed tubular reactor having the following characteristics: material=AISI 316L stainless steel, length 400 mm, internal diameter=12 mm, external diameter of the internal thermocouple sheath=3 mm. The reactor is placed in an oven having differential-zone heating, which allows the selected reaction temperature to be reached.
The catalyst used for the test has a particle size of >10 mesh. The catalyst charge is of 2÷8 g and is placed in the reactor between two layers of granular corundum.
The flow rate of the hydrocarbon mix is regulated by means of an HPLC pump. The hydrogen flow rate is controlled by means of a thermal mass flow meter. The reactor is of the down-flow type. The two feedings are injected and mixed at the inlet of the reactor, in the zone filled with inert material (granular corundum) where the reaction temperature is reached before coming in contact with the catalyst. The plant pressure is controlled through a setting valve at the outlet of the reactor (back pressure valve control). After the pressure setting valve, the stream is sent to a volume flow meter. An aliquot of the gaseous stream is periodically deviated (about every two hours) to an on-line gas chromatograph, for analysis of the products.
In the starting phase of the activity test, the catalyst is heated to the reaction temperature, under a nitrogen stream or, alternatively, a hydrogen stream, at low pressure and for one hour, in order to dry the catalyst and remove air from the reactor. Hydrogen is subsequently fed, if nitrogen was used before, and the pressure is increased to the value established for the reaction. The feeding of the hydrocarbon mixture is then started, at the flow rate established for the reaction. The mix of hydrocarbons at the outlet of the reactor is partially cooled before reaching the pressure setting valve, it is then cooled to about 50° C., said temperature being maintained in the whole line to the gas chromatograph. Before reaching the flow volume meter, the gas is cooled to room temperature.
The composition of the hydrocarbon mix in the feeding is established through an out-of-line gas chromatographic analysis, with sample injection in liquid phase.
The catalytic performances are evaluated by calculating the conversion of the reagents and the yield of the products on the basis of the gas chromatographic analysis integrated with the process data, such as the inlet and outlet flow rates.
The regeneration of the catalyst is effected, when required, after the activity test. Regeneration is carried out in the same reactor used for the reaction. The regeneration operative conditions are the following: temperature=450÷550° C., pressure=1-3 bar, oxygen concentration=0.1÷20% and GHSV space velocity=3,000÷6,000 hours⁻¹. In particular, the treatment starts with a nitrogen flow, to which an equal air flow is progressively added (in about 1 hour), the nitrogen flow is then progressively reduced to zero (in about 1 hour) and the treatment is prolonged from 5 to 24 hours, in relation to the duration of the previous activity test. At the end of the treatment the reactor is purged with a nitrogen flow and the catalytic activity test can be re-started.
Catalytic Test: Performances
Examples of catalytic activity follow, using the catalysts whose preparation was described in Examples 1-9.
The results are indicated in the tables which specify the catalyst characteristics, references to the preparation example, the operative conditions and the catalytic performances obtained.
As far as the operative conditions are concerned, it should be pointed out that WHSV means the weight space velocity (Weight Hourly Space Velocity) expressed as kg of hydrocarbons fed/hour/kg of catalyst, and TOS means the working time of the catalyst (Time On Stream), calculated starting from the beginning of the test with fresh catalyst or, in the case of an operating period following a regeneration, from the re-starting of the test with the regenerated catalyst.
The performances are expressed in terms of total conversions of the hydrocarbon (or mix of hydrocarbons) fed and composition of the mix of hydrocarbons at the outlet of the reactor. In particular the concentration of the following products are specified: methane (CH₄), ethane (C₂H₆), propane (C₃H₈), n-butane (n-C₄H₁₀), isobutane (i-C₄H₁₀), summation of paraffins with more than 4 carbon atoms (Σ Par. >C₄) and summation of all linear paraffins with the exclusion of methane (Σ n-Par.>C₁).
In the following Table 1 (3 examples, from Ex. 10/A to Ex. 10/C) the operative conditions are indicated together with the catalytic performances obtained using a catalyst based on Pd on USY-zeolite, prepared as described in Example 1. In particular, the results shown were obtained under different operative conditions, by varying the reaction temperature between 400 and 450° C. and the molar ratio H₂/Hydrocarbons between 10.3 and 32.7. The results demonstrate that this catalyst can be advantageously used for the purposes of the present invention.
Tables 2-5 (12 examples, from Ex. 11/A to Ex. 14/C) specify the results obtained with catalysts having a composition different from that of Example 10. They are based on Zn/Mo, Zn/Cu, Mo and Zn, all on USY-zeolites; their preparation is described in examples 2-5. Also in this case, the results were obtained under different operative conditions, with reaction temperatures of 400÷450° C. and molar ratio H₂/Hydrocarbons of 9.8÷35.4. The results show that the purposes of the present invention can be achieved with all these catalysts, in a wide composition range.

TABLE 1

EXAMPLES 10/A-10/C

*Catalyst

Type and Preparation Reference Pd/USY Zeolyst CBV 500; See Ex. 1

Example 10/A

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 400

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 10.3

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

7 100 7.0 16.6 52.2 12.9 9.5 1.8 82.8

Example 10/B

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 10.3

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17.5 100 19.9 38.2 39.7 1.2 0.8 0.1 79.2

Example 10/C

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 32.7

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17 100 14.9 25.6 52.9 3.8 2.8 0.0 82.4

TABLE 2


EXAMPLES 11/A-11/C

*Catalyst

	Type and Preparation Reference	ZnMo/USY Zeolyst CBV500; See Ex. 2

Example 11/A

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	400
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	10.5

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

7	100	4.8	11.4	48.4	18.5	13.5	3.5	80.3

Example 11/B

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	10.7

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	100	16.1	30.9	49.9	1.8	1.2	0.1	82.7

Example 11/C

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	35.4

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17.5	100	14.6	19.9	47.2	10.9	7.0	0.4	78.3

TABLE 3


EXAMPLES 12/A-12/C

*Catalyst

	Type and Preparation Reference	ZnCu/USY Zeolyst CBV500; See Ex. 3

Example 12/A

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	9.8

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	99.2	4.6	4.5	31.2	14.1	18.7	23.4	57.6

Example 12/B

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	400
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	32.0

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

7	100	2.3	3.9	29.7	21.6	29.8	12.7	63.3

Example 12/C

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	32.0

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	100	6.7	8.8	46.8	19.9	15.1	2.6	77.2

TABLE 4


EXAMPLES 13/A-13/C

*Catalyst

	Type and Preparation Reference	Mo/USY Zeolyst CBV500; See Ex. 4

Example 13/A

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	400
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	10.0

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	100	1.4	9.4	40.1	21.3	18.7	9.0	76.0

Example 13/B

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	10.0

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	100	6.0	20.7	56.6	8.8	5.8	2.1	87.0

Example 13/C

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	31.9

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	100	12.9	26.3	47.8	7.7	5.1	0.2	81.9

TABLE 5


EXAMPLES 14/A-14/C

*Catalyst

	Type and Preparation Reference	Zn/USY Zeolyst CBV500; See Ex. 5

Example 14/A

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	10.1

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17.5	97.4	4.2	4.4	29.1	11.6	14.5	20.3	48.0

Example 14/B

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	400
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	32.8

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

7	99.6	1.5	2.2	31.4	21.5	29.1	12.0	59.2

Example 14/C

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	32.3

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

17	99.6	6.1	7.0	50.1	18.5	14.5	3.0	76.5

Table 6 (3 examples, from Ex. 15/A to Ex. 15/C) shows the operative conditions and the catalytic performances obtained using a catalyst based on Pd on USY-zeolite, prepared as described in example 6.

TABLE 6

EXAMPLES 15/A-15/C

*Catalyst

Type and Preparation Reference Pd/USY Tosoh HSZ 320 HOA; See Ex. 6

Example 15/A

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 400

WHSV (hours⁻¹) 0.7

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 10.1

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

7 100 7.9 16.0 48.8 14.2 11.0 2.1 79.0

Example 15/B

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.7

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 10.1

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17.5 100 17.0 32.4 47.4 1.9 1.3 0.2 81.7

Example 15/C

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.7

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 35.7

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17.5 100 11.5 21.2 51.7 9.1 6.5 0.1 82.0

Table 7 (3 examples, from Ex. 16/A to Ex. 16/C) shows the operative conditions and the catalytic performances obtained using a catalyst based on Zn/Mo on USY-zeolite previously exchanged with La, prepared as described in Example 7. Also in this case, the results obtained are extremely good and show that it is possible to operate in an advantageous way also using compositions having a more complex composition, as mentioned in the description of the present invention.
Table 8 (2 examples, from Ex. 17/A to Ex. 17/B) shows the results relating to the same catalyst used in Examples 16/A-16/C of Table 7, adopted in a test of a longer duration. The results of Example 17/A were obtained after 260 hours of operation after the last regeneration and it was demonstrated that an excellent catalytic performance is maintained. The results of Example 17/B (270 hours after the last regeneration), were obtained after increasing the reaction temperature to 500° C.; the yield to light paraffins, particularly ethane and propane, is extremely good and the methane production is reasonably contained.

TABLE 7

EXAMPLES 16/A-16/C

*Catalyst

Type and Preparation Reference Zn—Mo/La-USY Zeolyst CBV500; See Ex. 7

Example 16/A

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 400

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 10.1

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

7 100 2.7 8.3 41.8 22.1 18.2 6.9 76.4

Example 16/B

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 10.1

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17.5 100 11.4 24.2 56.6 4.3 2.9 0.6 85.5

Example 16/C

*Operative conditions

Hydrocarbons fed 100% 1,2,4-trimethyl benzene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 31.9

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17 100 12.6 18.8 46.6 13.1 8.2 0.7 78.9

TABLE 8


EXAMPLES 17/A-17/B

*Catalyst

	Type and Preparation Reference	Zn—Mo/La-USY Zeolyst CBV500; See Ex. 7

Example 17/A

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	31.6

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

260	100	6.9	17.7	48.5	15.1	10.1	1.3	81.8

Example 17/B

*Operative conditions

	Hydrocarbons fed	100% 1,2,4-trimethyl benzene
	Reaction temperature (° C.)	500
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar ratio	31.7

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(hr)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

270	100	17.1	33.8	46.1	1.8	1.1	0.0	81.7

Table 9 (Example 18) shows the results obtained with a Pd on an La-USY based catalyst, prepared according to the description in Example 8. The test was carried out with a feed consisting of dicyclopentadiene. The catalyst effectively converted the feed into low molecular weight paraffins.

TABLE 9

EXAMPLE 18

*Catalyst

Type and Preparation Reference Pd/La-USY Tosoh HSZ 320 HOA; See Ex. 8

*Operative conditions

Hydrocarbons fed 100% di-cyclo pentadiene

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.7

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 34.8

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ l-C₄H₁₀ Σ Par. > C4 Σn.Par > C1

17 100 4.3 10.0 39.1 19.7 13.1 13.8 74.1

Table 10 (8 examples, from Ex. 19/A to Ex. 19/H) indicates the results obtained with a Pd on USY based catalyst, prepared according to the description in Example 6. The test was carried out by repeatedly changing the feed, as shown in Table 10. 40÷50 working hours were effected with each different feed, and the catalyst was always regenerated before passing to the subsequent feed. The test clearly shows that the catalyst is capable of effectively converting all the hydrocarbons tested and, at the same time, that the catalyst can be repeatedly regenerated.

TABLE 10


Examples 19/A-19/H

Catalyst

	Type and Preparation Reference	Pd/USY Tosoh HSZ 320 HOA; See Ex. 6

*Operative conditions

	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.7
	Pressure (bar)	60
	TOS (hr)	17

*Catalytic performances

Feed

Conv.

Mix composition at the reactor outlet (weight %)

type	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	l-C₄H₁₀	Σ Par. > C4	Σn.Par > C1

19/A	100	8.6	21.1	63.9	3.6	2.6	0.3	88.7
19/B	98.1	1.2	7.9	21.7	11.2	7.7	19.9	42.7
19/C	100	0.9	8.4	30.7	18.4	20.6	17.9	66.3
19/D	100	2.1	11.3	42.2	20.6	15.9	8.0	77.1
19/E	100	12.2	14.5	44.3	16.6	11.7	0.8	75.6
19/F	100	10.4	22.1	48.1	11.2	7.9	0.2	81.6
19/G	100	2.9	11.2	36.0	23.2	18.1	8.6	73.7
19/H	100	5.1	14.3	44.9	19.8	13.2	2.6	80.0

19/A: hydrocarbon = 100% cumene, H₂/Hydrocarbon molar ratio = 10.1
19/B: hydrocarbon = 100% indane, H₂/Hydrocarbon molar ratio = 10.3
19/C: hydrocarbon = 100% indane, H₂/Hydrocarbon molar ratio = 19.5
19/D: hydrocarbon = 100% indane, H₂/Hydrocarbon molar ratio = 31.7
19/E: hydrocarbon = 100% 1,2,4-trimethyl cyclohexane H₂/Hydrocarbon molar ratio = 38.3
19/F: hydrocarbon = mix ethyl benzene + xylene isomers, H₂/Hydrocarbon molar ratio = 35.0
19/G: hydrocarbon = mix tetramethyl benzene isomers H₂/Hydrocarbon molar ratio = 34.8
19/H: hydrocarbon = 85% weight 1,2,4-trimethyl benzene + 15% weight naphthalene H₂/Hydrocarbon molar ratio = 36.0

Table 11 (5 examples, from Ex. 20/A to Ex. 20/E) indicates the results obtained with a catalyst based on Zn and Mo on USY-zeolite, prepared according to the description in Example 9. The test was carried out by feeding different types of hydrocarbons, as shown in the same Table 11.

20÷30 working hours were effected with each hydrocarbon, and the catalyst was always regenerated before passing to the subsequent feed. The test shows that the catalyst is capable of effectively converting all the hydrocarbons fed and that it can be regenerated.

TABLE 11


Examples 20/A-20/E

Catalyst

Type and Preparation Reference

ZnMo/USY Zeolyst CBV 500; See Ex. 9

*Operative conditions

	Reaction temperature (° C.)	420
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	TOS (hr)	11

*Catalytic performances

Feed

Conv.

Mix composition at the reactor outlet (weight %)

type	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	I—C₄H₁₀	ΣPar. >C4	Σn.Par >C1

20/A	100	6.4	15.5	57.9	10.9	7.7	1.6	84.9
20/B	100	10.3	17.1	55.7	9.6	6.5	0.7	82.9
20/C	100	6.4	12.0	42.1	19.2	13.2	7.0	77.7
20/D	100	10.4	18.7	53.0	10.1	6.9	0.9	82.4
20/E	100	3.4	11.5	44.9	20.5	15.5	4.0	79.3

20A: hydrocarbon = 100% decahydronaphthalene (decaline) H₂/Hydrocarbon molar ratio = 11.6
20B: hydrocarbon = 100% n-decane H₂/Hydrocarbon molar ratio = 14.3
20C: hydrocarbon = 100% di-cyclo pentadiene H₂/Hydrocarbon molar ratio = 33.5
20D: hydrocarbon = 100% weight 1,2,4-trimethyl cyclohexane H₂/Hydrocarbon molar ratio = 11.8
20E: hydrocarbon = 13.5% decahydronaphthalene + 13.1% n-decane + 12.7% di-cyclo pentadiene + 13.4% 1,2,4-trimethyl cyclohexane + 13.1% naphthalene + 34.2% 1,2,4-trimethyl benzene, H₂/Hydrocarbon molar ratio = 33.8

Table 12 (2 examples, from Ex. 21/A to Ex. 21/B) indicates the results obtained with the feed, consisting of two different high molecular weight hydrocarbon mixtures (the composition of the mixtures is specified in the same Table 12). A catalyst based on Zn and Mo on La-USY-zeolite was used in this case (prepared according to the description in Example 9). The results show the conversion obtained with aromatic compounds having more than one benzene ring.

TABLE 12


Examples 21/A-21/B

Catalyst

Type and Preparation Reference

ZnMo/USY Zeolyst CBV 500; See Ex. 9

*Operative conditions

	Reaction temperature (° C.)	450
	WHSV (hours⁻¹)	0.9
	Pressure (bar)	60
	TOS (hr)	for ex. 21/A = 21 h; for Ex. 21/B = 80 h

*Catalytic performances

Feed

Conv.

Mix composition at the reactor outlet (weight %)

type	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	I—C₄H₁₀	ΣPar. >C4	Σn.Par >C1

21A	100	9.0	17.7	47.0	15.1	9.8	1.4	80.7
21/B	100	5.3	15.7	46.3	18.0	12.3	2.3	81.5

21/A: hydrocarbon = 50% by weight of dimethyl naphthalenes + 50% by weight of trimethyl naphthalenes, H₂/Hydrocarbon molar ratio = 39.4
21/B: hydrocarbon = 84.5% by weight of 1,2,4-trimethyl benzene + 4.4% by weight of dimethyl naphthalenes + 4.4% by weight of trimethyl naphthalenes + 1.8% by weight of anthracene + 1.7% by weight of di-hydro anthracene + 2.5% by weight of di-hydro phenanthrene + 0.7% by weight of methyl anthracene, H₂/Hydrocarbon molar ratio = 30.1

Table 13 (Example 22) indicates the results obtained in a test of a longer duration with a catalyst based on Zn and Mo on USY-zeolite, prepared according to the description in Example 7. The feed composition was changed several times during the test, but the catalyst was never regenerated. The test was interrupted after 1,200 working hours. As indicated in Table 13, the feed contained; sulfurated compounds with concentrations of 5,000÷6,500 ppm, for long running periods, and the catalytic performance was always excellent for the purposes of the present invention.

Table 14 (Example 23) indicates the results obtained with a catalyst based on Zn and Mo on USY-zeolite, prepared according to the description in Example 7. The test was carried out with a mix of hydrocarbons containing ethyl benzene, xylenes, styrene, methyl styrenes, cumene, trimethyl benzene, methyl ethyl benzenes, indane, dicyclo pentadiene, naphthalenes and methyl naphthalenes, according to the composition shown in the same Table 14. The test clearly demonstrates that the catalyst is capable of effectively converting the entire hydrocarbon mix fed to low molecular weight paraffins.

TABLE 13

EXAMPLE 22

*Catalyst

Type and Preparation Reference Zn—Mo/La-USY Zeolyst CBV500; See Ex. 7

*Operative conditions

Reaction temperature (° C.) 450

WHSV (hours⁻¹) 0.8

Pressure (bar) 60

H₂/Hydrocarbons molar ratio 31.9

*Catalytic performances

TOS Conv. Mix composition at the reactor outlet (weight %)

(hr) (%) CH₄ C₂H₆ C₃H₈ n-C₄H₁₀ I—C₄H₁₀ ΣPar. >C4 Σn.Par >C1

Hydrocarbons fed = 100% 1,2,4-trimethyl benzene

17 100 8.7 17.4 46.7 15.7 10.3 1.2 80.6

275 100 6.5 16.7 47.2 16.6 11.0 1.6 81.0

479 100 6.3 15.4 45.9 17.7 11.9 2.0 80.2

Hydrocarbons fed = 99.4% 1,2,4-trimethyl benzene + 5000 ppm thio-octanol +

1500 ppm di-benzo thiophene

526 100 6.9 21.1 55.9 9.2 6.2 0.5 86.5

581 100 7.2 22.9 56.4 7.8 5.3 0.4 87.2

623 100 7.7 22.6 57.0 7.3 5.0 0.4 87.1

Hydrocarbons fed = 69.5% 1,2,4-trimethyl benzene + 30% naphthalene + 5000 ppm di-

benzo thiophene

625 100 7.8 22.7 56.8 7.3 5.0 0.3 87.0

819 100 6.3 20.7 57.2 8.8 6.1 0.6 87.1

999 100 5.7 19.2 57.3 9.8 6.7 0.8 86.6

1183 100 6.1 16.5 57.1 11.3 7.8 0.9 85.4

TABLE 14


Example 23

Catalyst

Type and Preparation Reference

ZnMo/La-USY Zeolyst CBV 500; See Ex. 7

*Operative conditions

	Reaction temperature (° C.)	420
	WHSV (hours⁻¹)	0.8
	Pressure (bar)	60
	H₂/Hydrocarbons molar	19.9
	ratio

*Catalytic performances

TOS

Conv.

Mix composition at the reactor outlet (weight %)

(h)	(%)	CH₄	C₂H₆	C₃H₈	n-C₄H₁₀	I—C₄H₁₀	ΣPar. >C4	Σn.Par >C1

11	100	3.7	16.6	47.5	16.8	11.7	3.2	82.5

Hydrocarbons fed = 5% ethyl benzene + 10% mix of xylenes + 20% styrene + 10% mix of methyl styrenes + 3% cumene + 12% mix of trimethyl benzenes and methyl ethyl benzenes + 10% indane + 25% di-cyclo pentadiene + 5% mix of naphthalenes and methyl naphthalenes

Claims

1. A process for the production of linear alkanes containing less than 6 carbon atoms comprising contacting a mixture comprising one or more hydrocarbons containing at least 6 carbon atoms, in presence of hydrogen, with a catalytic composition comprising:

a) at least one element Me selected from the group consisting essentially of Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals of group VIII Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt,

b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B,

with the exclusion of a catalytic composition comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B when the mixture treated is a mixture containing aromatic compounds.

2. The process according to claim 1, wherein the mixture comprises one or more hydrocarbons containing at least 6 carbon atoms, selected from the group consisting essentially of aromatic compounds, open-chain alkanes, alkanes with cyclic structures, alkenes having one or more unsaturations with open chains and alkenes with cyclic structures having one or more unsaturations.

3. The process according to claim 2, wherein the mixture comprises one or more hydrocarbons selected from the group consisting essentially of open-chain alkanes, alkanes with cyclic structures, open-chain alkenes having one or more unsaturations and alkenes with cyclic structures having one or more unsaturations.

4. The process according to claim 2, wherein the mixture contains aromatic compounds is contacted with a catalytic composition comprising:

a) at least one element Me selected from the group consisting essentially of Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals of group VIII,

with the exclusion of a catalytic composition comprising at least one lanthanide, at least one metal belonging to group VIII and a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B.

5. The process according to claim 4, wherein the mixtures containing aromatic compounds are contacted with catalytic compositions essentially consisting of:

b) a zeolite selected from Y-zeolite and Y-zeolite modified by partial or total substitution of the Si with Ti or Ge and/or partial or total substitution of the aluminum with Fe, Ga or B.

6. The process according to claim 1, wherein the catalytic composition comprises:

a) at least one element Me selected from the group consisting essentially of Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, metals of group VIII, Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt,

c) one or more lanthanides,

7. The process according to claim 6, wherein mixtures containing aromatic compounds are contacted with catalytic compositions containing:

a) at least one element selected from the group consisting essentially of Mo, Cu, Ga, In, W, Ta, Zr, Ti,

c) one or more lanthanides,

8. The process according to claim 7, wherein the catalytic composition essentially consists of:

a) at least one element Me selected from the group consisting essentially of Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti,

c) one or more lanthanides.

9. The process according to claim 1, wherein the zeolite is Y-zeolite.

10. The process according to claim 1, wherein the zeolite is partially in acidic form.

11. The process according to claim 9, wherein the molar ratio SiO₂/Al₂O₃in the zeolite ranges from 3 to 400.

12. The process according to claim 11, wherein the molar ratio between silicon oxide and aluminum oxide is from 5 to 50.

13. The process according to claim 1, wherein the Me is selected from the group consisting essentially of Pt, Pd, Ti, Zn, Mo, Cu, Ni, Zn/Mo, Cu/Zn, Pd/Ti and Ni/Mo.

14. The process according to claim 13, wherein the catalytic compositions contain Y-zeolite and Pd, Y-zeolite and Pt, Y-zeolite and Ni, Y-zeolite and Zn, Y-zeolite and Mo, Y-zeolite and Zn together with Mo, Y-zeolite and Zn together with Cu, Y-zeolite and Pd together with Ti, Y-zeolite and Mo together with Ni.

15. The process according to claim 6, wherein the catalytic compositions contain Y-zeolite and La together with Zn and Mo, Y-zeolite and La together with Zn and Cu.

16. The process according to claim 1, wherein the element Me is present in the catalytic composition in the form of an oxide, ion, metal or a mixture of these forms.

17. The process according to claim 1, wherein Zn, Mo, Cu, Ga, In, W, Ta, Zr or Ti are in a quantity from 0.1 to 50% by weight with respect to the total weight of the catalytic composition.

18. The process according to claim 17, wherein the quantity of the element Me is from 0.5 to 30% by weight.

19. The process according to claim 1, wherein the metal belonging to group VIII is in a quantity ranging from 0.001 to 10%, by weight.

20. The process according to claim 19, wherein the metal of group VIII is in a quantity from 0.1 to 5% by weight with respect to the total weight of the catalytic composition.

21. The process according to claim 6, wherein the lanthanide is lanthanum.

22. The process according to claim 6, wherein the lanthanide is in the form of an oxide, ion or a mixture of these forms.

23. The process according to claim 6, wherein the lanthanide is in a quantity, expressed as an element, from 0.5 to 20% by weight with respect to the total weight of the catalytic composition.

24. The process according to claim 23, wherein the lanthanide is in a quantity ranging from 1 to 15% by weight with respect to the total weight of the catalytic composition.

25. The process according to claim 1, wherein the catalytic composition contains a binder.

26. The process according to claim 25, wherein the binder is selected, from the group consisting essentially of silica, alumina, clay.

27. The process according to claim 3, wherein the alkanes, alkenes or mixtures thereof are mineral oil fractions, or derive from the hydrogenation of mineral oil fractions, or from the hydrogenation of fractions from conversion plants.

28. The process according to claim 2, wherein the mixtures containing aromatic compounds are fractions coming from thermal or catalytic conversion plants, or mineral oil fractions.

29. The process according to claim 28, wherein said fractions are pyrolysis gasolines, fractions coming from pyrolysis gasolines or residual fractions coming from production plants of aromatic compounds and reforming.

30. The process according to claim 2, wherein the aromatic compounds are toluene, ethyl benzene, xylenes, benzene, C₉aromatic compounds, derivatives of naphthalene and their mixtures.

31. The process according to claim 29, wherein said fractions are mixed with heavy fractions coming from fuel oil from steam cracking (FOK) or Light Cycle Oil (LCO) from fluid bed catalytic cracking.

32. The process according to claim 28, wherein the mixtures are heavy fractions coming from fuel oil from steam cracking (FOK) or Light Cycle Oil (LCO) from fluid bed catalytic cracking, previously treated to remove the asphaltenes.

33. The process according to claim 1, wherein the resulting fraction of n-alkanes are selected from the group consisting essentially of ethane, propane, n-butane and n-pentane.

34. The process according to claim 33, wherein the fraction of n-alkanes containing from 2 to 5 carbon atoms comprises from 50 to 90% by weight of the resulting product.

35. The process according to claim 1, carried out in the presence of hydrogen at a pressure ranging from 5 to 200 bar, at a temperature ranging from 200° C. to 700° C.

36. The process according to claim 35, carried out in the presence of hydrogen at a pressure ranging from 25 to 100 bar, at a temperature ranging from 300° C. to 600° C.

37. The process according to claim 35, carried out at a weight ratio H₂/charge ranging from 0.1 to 1.4.

38. The process according to claim 37, carried out at a weight ratio H₂/charge ranging from 0.1 to 0.7.

39. The process according to claim 35, wherein a paraffin is used as diluent.

40. Catalytic compositions comprising:

41. The catalytic compositions according to claim 40, additionally containing one or more lanthanides.

42. A process for preparing the catalytic composition according to claim 40, which comprises treating the zeolite with a compound of the element Me with ion exchange or impregnation, drying and calcining.

43. A process for preparing the catalytic composition according to claim 41, which comprises treating the zeolite with a lanthanide compound, treating the product thus obtained with a compound of the element Me, drying and calcining.

44. The process according to claim 43, wherein the lanthanide is inserted in the zeolite in acidic form by ion exchange, optionally calcining the product thus obtained, depositing the element Me by ion exchange, and drying and calcining the product.

45. A process for the production of linear alkanes containing less than 6 carbon atoms from mixtures containing aromatic compounds having a structure with at least 6 carbon atoms, in presence of hydrogen, using a catalytic composition consisting of:

a) at least one element Me selected from the group consisting essentially of Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, mixed with one or more metals of group VIII,

c) one or more lanthanides.

46. A catalytic composition consisting of:

c) one or more lanthanides.

47-48. (canceled)