CA2284883A1 - Catalysts with modified molybdenum oxycarbide base prepared from oriented molybdenum and method for producing same - Google Patents

Abstract

The invention concerns a catalyst with modified molybdenum oxycarbide base having a specific surface area more than 5 m?2¿/g and improved catalytic activity, in particular in velocity constant, characterised in that it is prepared from molybdenum oxide MoO¿3? with a structure essentially comprising preferentially oriented monocrystalline plates resulting from sublimation condensation. The invention also concerns a method for producing such a catalyst.

Description

MODIFIED MOLYBDENE OXYCARBON CATALYSTS PREPARED FROM
ORIIDATED MOLYBDENE OXIDE AND PROCESS FOR OBTAINING SAME
"FIELD OF THE INVENTION
S The invention relates to a catalyst for chemical reactions or petrochemicals, based on large surface metal oxycarbons specific, its preparation process and its use. This catalyst is particularly suitable for refining and processing products tankers, in particular the isomerization of saturated hydrocarbons, hydrogenation and decyclization of cyclic hydrocarbons and aromatic, and has improved catalytic properties, in particular the specific speed.
STATE OF THE ART
We know from the patents FR 266620 and 2712587, reactions catalyzed isomerization of linear hydrocarbons ranging from four to more of twenty carbon atoms, and hydrogenation and decyclization of aromatics using an oxycarbide catalyst molybdenum, the latter being obtained by direct activation treatment of the precursor oxide (MoOs) by the reaction mixture itself.
It may be recalled that the catalysts based on oxycarbide of Mo have a major interest since they always offer a high selectivity in particular even when conversion rates are high. In addition, there are many cheaper and less susceptible to poisons than conventional catalysts to base of Pt.
However in petrochemical reactions catalyzed by oxycarbide of Mo, the specific speed of the reaction expressed in moles of product transformed per g of catalyst per second is still insufficient.

2 As an indication, when this speed is 150 for a conventional catalyst at base of Pt on a zeolite support, it is generally around 50 for a oxycarbide of Mo prepared in a standard way.
Also the inventors asked themselves the question of improving the activity catalytic of this type of catalyst, seeking in particular to increase, in the petrochemical reactions, the specific speed reduced to the unit of weight of catalyzer.
DESCRIPTION OF THE INVENTION
A first aspect of the invention is a modified molybdenum oxycarbide of elevated specific surface characterized in that ü is prepared from a molybdenum oxide MoOs having a structure comprising essentially platelets with preferred orientation.
The most favorable MoOs oriented plan to obtain a more oxycarbide effective is the plan (010) with preferential development in the direction (001).
Said plates generally have a length in the direction of orientation preferential of at least 1 gym; it is remarkable that they can reach or exceed 10 000 Nm. The thickness of the pads is generally at least minus 0.1 Nm and Fear width of at least 0.5 Nm; the latter can sometimes up to 6000 Nm. They are generally monocrystalline, more or less less agglomerated.
The BET specific surface of this oxycarbide is greater than 5 m2 / g, generally at 20 m2 / g and can even reach 90 m2 / g and is clearly higher than that of the MoOs oriented at the start.
It is difficult to know what peculiarity of microstructure the characterizes and provides the unexpected results observed. We can however note that it is substantially free of Mo02 oxide which can be considered as a harmful reduction byproduct, whereas generally the oxycarbide obtained from polycrystalline MoOa contains it.

WO 98142438 PCTlFR98 / 00551

3 Another aspect of the invention is a process for obtaining oxycarbide from modified meybdenum with a high specific surface, characterized in that part of usual polycrystalline molybdenum oxide, or optionally a composed of molybdenum (for example ammonium hepfiamolybdate) which is transformed into oxide, the said oxide is heat treated molybdenum by sublimation-condensation at a temperature between 500 and 800 ° C in an enclosure under an oxidizing gas atmosphere for at minus Sh to obtain an oriented recrystallized oxide, which is then treaty under current of a mixture of hydrocarbon and hydrogen to give a modified molybdenum oxycarbide.
The sublimation-condensation stage is usually carried out under an atmosphere static or under current of dry or wet oxidizing gas at low speed, said gas may be air. This performs a recrystallization of the oxide of molybdenum on site, without appreciable transfer of material.
In order to obtain a supported catalyst, it is possible to mix or deposit the starting oxide or a precursor, with or on an inert material opposite of oxide, this material serving as a support for the modified oxycarbide catalyst.
This material is usually a refractory, for example alumina, but of preferably a carbide with a large specific surface such as pure SiC or dope.
The recrystallized oxide obtained is an oriented structure oxide comprising mainly elongated monocrystalline wafers with preferential orientation.
The preparation of the oxycarbide from the recrystallized oxide is done according to the methods described in the patents cited above.
Another aspect of the invention is the use of this oxycarbide of modified large surface area molybdenum prepared from MoOa oriented as a catalyst in petrochemical reactions in particular for the isomerization of hydrocarbons or the hydrogenation, in particular WO 98/42438 PCT / FIt98100551

4 that of aromatics to obtain a high selectivity at a high rate of conversion.
Filial catalysts according to the invention have a marked activity S improved compared to the usual polycrystalline molybdenum oxycarbide.
In especially their specific speed can reach almost 10 times that of MoOC
obtained from polycrystalline MoOa; in other words for the same reaction the amount of catalyst required is more than 10 times lower. The speed specific is also superior, sometimes at least 4 times, to that obtained with the usual catalysts based on Pt on zeolite.
The selectivity or conversion rate characteristics specific to MoOC
(high conversion selectivity much higher than that of Pt) are usually not changed.
The catalyst according to the invention can be prepared as it is (that is to say by bulk) or supported for example on an SiC support with a high specific surface, as has already been said.
DETAILED DESCRIPTION OF THE INVENTION
Different methods of preparing the oxide phase, MoOs as is or supported, having the correct orientation to allow (obtaining a highly active and selective modified Mo oxycarbide catalyst isomerization reaction, are described below.
A first method of preparation consists of heating under low air flow of a polycrystalline Mo03 powder as it is at a temperature preferably between 650 and 750 ° C during a period ranging from 5 to 240h. The molybdenum oxide used can be replaced either by a precursor salt (heptamolybdate), either by a metal powder or metal plates which are oxidized. Molybdenum oxide after that treatment is in the form of powder or platelets having r.

S
the preferred orientation desired. The air flow can be replaced by any other oxygen-containing gas. The gas flow, generally of low speed, can either be used as dry gas or contain water vapour. The synthesis can also be carried out under an atmosphere static air or a mixture of oxygen with an inert gas.
A second method of preparation consists of heating either of a polycrystalline MoOs powder but an intimate mixture of MoOs polycristaün and grains of SiC. The treatment is identical to that described in the first method of preparation. The resulting product consists of SiC grains covered by oriented MoOs platelets preferentially.
A third method of preparation consists in impregnating a support based on of SiC by a solution containing a molybdenum salt, for example a heptamolybdate solution. The support is then dried in a drying oven.
120 ° C for 12 hours then calcined under air flow. The temperature is rise of ambient at the calcination temperature (650-750 ° C) with a slope of 60 ° Cmin- ~ then kept at this temperature for a period additional 24h. The gas mixtures used are identical to those employed in the first two methods.
The general conditions for the preparation of molybdenum oxides, mass or supported, presenting a preferential orientation are the following - the oxidizing gas used is generally air, but can be oxygen pure or more or less diluted by an inert gas. There is no need to overdo it dilute the oxygen and preferably use a gas containing at least 10%
oxygen. The gas mixture can be used in anhydrous form or containing water vapor as already mentioned;

- the treatment temperature must be between 500 ° C and 800 ° C. We have showed that at a temperature below 500 ° C., the treatment for to be effective, should have an unacceptable duration while the temperatures higher than 800 ° C cause too strong evaporation of the product;
- the duration of treatment is more than 5 hours; it is usually understood between 24 and 72 hours when the treatment is carried out in the presence of humid air, and between 48 and 120 h in the presence of dry air. But it can be higher, the catalyst performance increasing with the duration of the treatment.
Treatment in the presence of moist air increases the speed of transformation into oriented oxide and thus obtaining larger quantities of recrystallized oxide only in the presence of dry air.
Example 1 This example illustrates first obtaining molybdenum oxide (MoOs) as it is oriented according to the invention, using the first method, then modified meybdenum oxycarbide gall which catalyzes isomerization of n-heptane.
The oriented oxide was prepared as follows: a mass of 1000 mg of polycrystalline MoOs was introduced into a quartz tube located at inside a tubular oven. The whole was swept by a draft dry (10 cm3 min- '). The oven temperature has risen from ambient to b80 ° C with a speed of 20 ° C min-. The temperature was maintained during a period of 100h. The oven temperature was then lowered at room temperature always under air flow. At room temperature the oriented or monocrystalline MoOs oxide obtained was extracted from the oven and stored in a glove box to be subsequently transformed into a modified oxycarbide according to the invention.
The carburetion and the use of part of the oxide as directed obtained in presence of dry air were then carried out under the following conditions A mass of 12 mg of oriented molybdenum oxide (in the form of plates) prepared above was introduced into a tubular reactor in stainless steel between two layers of silica wool. The reactor was purged under a stream of hydrogen (purity greater than 99.95%) at room temperature for 30 min at atmospheric pressure. Then system pressure was raised under hydrogen flow to 6 bars, the reaction temperature is 350 ° C. Once the temperature and pressure affected, n-heptane was injected into the hydrogen stream, such so that the molar ratio between H2 and n-heptane in the mixture is 30, to obtain the molybdenum oxycarbide.
Then the catalytic performances obtained during the reforming of n-heptane were measured over time to assess a possible aging of the modified Mo oxycarbide catalyst. The obtained results as well as the details of the reaction products obtained are presented in the Table 1.
Furthermore, FIG. 1 gives the selectivity for n-hepfane isomers (iC ~) in % in function of the conversion of said nC ~.
In table l, the time since the start of the operation is shown in head of the columns. The lines indicate successively - the total conversion rate of the system (% of n-heptane molecules transformed either by isomerization or by cracking) - specific speed: number of starting hydrocarbon molecules processed per g of catalyst per second - the total selectivity in C ~ isomers (% of isomerized molecules compared total molecules transformed) the yield of C ~ isomers (product of selectivity in isomerization and of conversion, %) - the percentages of isomerized chemical species compared to the total of isomers obtained (C ~ isomers,%) oh DMPen - 2,2-dimethyl pentane + 2,3-dimethyl pentane +
2,4-dimethyl-pentane 2MHex - 2-methyl hexane 3MHex - 3-methyl hexane 3EPent - 3-ethyl-pentane Cyclic - methyicyciohexane + toluene - the percentages of cracked chemical species obtained reported in total cracked products obtained (cracked products,%).
The BET specific surface is 80 m2 / g.

Isomerization of the modified n-heptane suc oxycarbide of Mo, as it is, prepared at go of MoOa tef which oriented in the presence of dry air Time (h) 2.0 15.5 19.5 25.0 41.5 Conversion (%) 2.3 16.2 16.1 16.3 16.0 Specific speed (10- ~ 71.0 613.5 620.0 608.4 606.0 mol g- 's- ~) Selectivity in i- C ~ (%) 95 96 96 9b 95 Reaction yield in 2.2 15.6 15.5 15.5 15.4 i- C ~ (%) Distribution of products reaction Isomers in C ~ (~ J

DMPen Q, 5 9.6 9.5 9.6 9, b 2Mhex 40.4 40.3 40.1 40.2 40.1 3Mhex 46.4 46.5 46.3 46.7 46.4 3EPen 3.2 3.1 3.1 3.1 3.0 Cracked products (% J

Cyclical 0.7 0.5 0.9 0.5 0.8 Ce + C ~ 18.0 17.0 14.0 16.0 19.1 Cs + C2 17.9 18.9 13.7 13.1 15.3 C4 + Cs 60.5 60.8 66.6 67.2 63.5 Others 3.6 3.3 5.7 3.7 2.2 Examination of Table i makes the following comments 1. The number of transformed n-heptane molecules is very low during ~ fa first hour of the reaction. After about 2 hours under flow of n-heptane and hydrogen at 350 ° C, the catalyst begins to be active, this which reflects a significant change in its surface. This activation corresponds to the reduction and the carburetion of molybdenum oxide oriented into reactive modified oxycarbide, by reaction with the mixture reaction (n-heptane / hydrogen), as in the case of an oxide of i0 polycrystalline molybdenum.
2. the selectivity for C ~ isomers is very important from the start of the reaction and remains above 95%. The isomeric products formed are composed essentially monobranched molecules (2-methyl hexane and 3-methyl hexane) and dibranched (dimethylpentanes) while the cyclic molecules are formed in very small quantities (<1%).
The examination of FIG. 1 shows that the selectivity for isomers of n-C7 remains very high regardless of the conversion of the reaction.
Example 2 This example illustrates first obtaining Mo oxide oriented according to the invention supported on a SiC-based support using the third method, then of molybdenum oxycarbide modified and supported on said SiC
to catalyze the isomerization of n-heptane.
SiC granules with a BET specific surface area of 19 m2 / g were impregnated with an aqueous solution of ammonium heptamolybdate then calcined at 350 ° C.
for 2 hours to decompose the heptamolybdate into MoOs oxide.
The SiC granules impregnated with pofycrystalline MoOs thus obtained, placed in a ceramic tray, were introduced into a quartz tube placed in a tubular oven. The whole was swept by a draft dry with a flow rate of 20 cm3 min- '. The rise in temperature and the rest of the assembly are identical to those used in Example 1. The temperature used was 700 ° C. The system was maintained at this temperature during a 72 hour period. The oven temperature was then lowered to room temperature always under dry air flow. At the temperature S ambient the product, in this case oriented MoOa, or monocrystalline, supported on SiC, was removed from the oven and stored in a glove box for subsequently be transformed into modified oxycarbide.
The carburetion followed by the use of the oriented and supported oxide obtained in presence of dry air were then carried out as previously.
10 The specific speed and the selectivity for C ~ isomers obtained on the catalyst as a function of time under flow are presented in Table 2. The details concerning the distribution of the reaction products are also included in this board.

1 S Isomerization of n-heptane on modified Mo oxycarbide supported on SiC
prepared for go of MoOa support sure SiC
East in presence of air dry Time (h) 2 6 10 21 25 49 Conversion (% i 13.5 20.2 22, b 23.6 22.7 23.5 Specific speed (10- ~ 81.0 121.2 872.4 904.2 880.2 896.4 mol g- ~ of MoOa s- ~

Selectivity in i- C ~ (% j 94 94 95 95 95 94 Reaction efficiency in 12.7 19.0 21.5 22.5 21.8 22.1 i- C ~%

Distribution of products reaction Isomers in C7 (%) DMPen 9.1 10.2 9.4 9.0 8.8 8.7 2MHex 34.5 41, b 40.5 41.2 40.5 40.2 3Mhex 34.8 44.5 46.5 46.2 46.5 47.2 3EPen 19.5 3.5 3.0 3.0 3.1 3.1 Cyclic 2.1 0.2 0.6 0.6 l, l 0.8 Cracked products / ~ /

C6 + Cf 12.9 11.9 12.0 12.4 14.5 17.0 Cs + C2 15.7 20.2 20.6 21.9 21.6 19.1 Ca + C3 70.9 b5.9 62.0 60.8 59.7 59.9 Others 0.5 2.0 5.7 4.9 4.2 4.0 '' Such oxycarbure supported on SiC offers the advantage of greater solidity (abrasion resistance, mechanical strength, etc.), better conditions of use (no blockage of reactors ...) and better efficiency of use (less quantity used compared to the product treated).
Example 3 This example illustrates the results obtained with a molybdenum oxycarbide.
as modified according to the invention using an intermediate oriented oxide i 0 obtained in the presence of a humid oxidizing atmosphere. For that we have used the method of Example 1 in which the stream of dry air was replaced by a humid air flow of 30 cm3 / min at 3% (by volume) of water vapour;
The oriented oxide was obtained after 48 h of treatment and was then i5 transformed into oxycarbide then used for the isomerization of n-heptane, as in example 1.
The results are given in Table 3 r WO 98/42438 PCT / FR98l00551 Isomerization of n-heptane on modified Mo oxycarbide, as is, prepared for go MoOa as it is oriented in the presence of humid air Time (h) 2.75 14.75 19.25 23.25 42 Conversion (%) 9.9 21.6 21 20.9 20.9 Specific speed (10- ~ 177.7 362.4 353.7 352.8 352.7 mol g- ~ s- ') Selectivity in i- C ~ (%} 88 93 93 93 93 Reaction efficiency in 8.7 20.1 19.5 19.4 19.4 i- C ~ (%}

Distribution of products reaction isomers in C ~ (~) DMPen 14 13.5 13.3 13.3 13.3 2Mhex 41.5 39.7 39.6 39.6 39.6 3Mhex 40.9 43.1 43.2 43.2 43.2 3EPin 2.7 2.9 2.9 3 2.9 Cracked products (~ J

Cyclical 0 0.4 0.4 0.5 0.4 Ce + C i 5.9 11.3 10.6 11.3 11.2 Cs + Ci 8.9 10.8 10.9 10.7 10.8 Ca + Cs 79.5 74.4 74.5 74.8 74.7 Others 5.6 3.5 4 3.2 3.3 We can see that the specific speed is always high although lower than that obtained when the oriented Mo oxide is produced in the presence of dry air. By against the development of said oriented oxide requires a period clearly lower.
Example 4 In this example, we compared the specific speeds obtained with a oxycarbide catalyst as modified, prepared from bulk MoOs precursor oriented in the presence of dry air of Example 1 and activated under the mixture of n-heptane and hydrogen at 6 bars and 350 ° C, and the speeds obtained with a catalyst prepared from MoOs as it is polycrystalline of the prior art activated under the same conditions.

The specific velocities and the selectivities in C ~ isomers obtained with the two catalysts and details of the reaction products are presented in Table 4.
Table 4 Isomerization of n-heptane on modified Mo oxycarbide, as it is, prepared at go of MoOs East in presence of air dry and of MoOa polycrystaln MoOxC ifi MoOXCv mod art previous Time (h) 2.0 15.5 25.0 2.0 10.0 25.0 Conversion (%) 2.3 16.2 16.1 26.4 43.0 43.2 Specific speed 71.0 613.5 608.4 37.3 53.1 53.2 (10- 'mol g-' s- ' ) Selectivity in i- C ~ 95 96 96 93 93 94 (%at) Efficiency in i- C ~ 2.2 15.6 15.5 24.6 40.0 40.6 %

Distribution of products reaction Isomers in C ~ (~) DMPen 9.5 9.6 9.6 13.3 13.5 13.4 2MHex 40.4 40.3 40.2 41.4 39.2 39.1 3MHex 46.4 46.5 46.7 42.4 44.1 44.2 3EPen 3.2 3.1 3.1 2.9 3.2 3.2 Cyclical 0.7 0.5 0.5 0 0 0 Cracked products (%) C6 + C ~ 18 17 16 20 25 25 Cs + Ci 18 19 13 11 14 16 Ca + Cs 60 61 b7 67 58 56 Others 4 3 4 2 3 2 Examination of this table makes it possible to draw the following conclusions 1. The specific speed for the isomerization reaction of n-heptane obtained on a modified molybdenum oxycarbide prepared from oriented Mo03 according to the invention is much greater than that obtained on the same active phase but prepared from pofycrystalline MoOa (608 instead of 53.10- 'mol g- ~ s-' j.

2. The distribution of the reaction products (isomers and cracked) is practically identical between the two catalysts. This shows that the active phase formed is of identical chemical nature, namely molybdenum oxycarbide.
Example 5 The same type of comparison as in example 4 (oxycarbide modified / oxycarbide prior art) has been made.
We thus compared the specific velocities in the case of an oxycarbide of Mo modified, supported on SiC, obtained from a supported Mo oxide and modified in the presence of humid air (as in Example 3) and in the case of an oxycarbide obtained from Poiycrystalline MoOs supported on the same SiC.
The operating conditions for the activation and isomerization of n-heptane are the same as those of Example 4.
The results are given in Table 5.

Board

5 Isomerization from n-heptane from on MoOs oxycarbide from Mo support prepared East in the presence of air wet and of Polycrystalline MoOa, supporfs on SiC

MoOxCy MoOxCy previous ur modifi s SiC
sure SiC

Time 2 5.75 24 2 6 25 Conversion% 10.7 42.3 41.4 13.5 20.2 22.7 Specific speed 79.7 420.2 421.9 91.5 131.1 146.7 (10-7 mol / g / sec Selectivity in i-C7 85 92 93 94 94 96 (%) Reaction efficiency 9.1 38.9 38.5 12.7 19 21.8 in i-C7 (%) Distribution of products reaction Isomers in C7 (~) DMPen 14.3 13.7 13.1 9.1 10.2 8.8 2MHex 40.5 40.2 39.7 34.5 41.6 40.5 3mhex 39.8 42, fi 43.5 34.8 44.5 46.5 3EPen 2.7 2.9 3 19.5 3.5 3.1 Cracked products (~) Cyclical 1.8 0.3 0.3 2.1 0.2 1.1 C6 + C 1 5.3 11 12.5 12.9 11.9 16 C5 + C2 7.5 11.5 11.7 15.7 20.2 21.6 C4 + C3 81.5 73 7i, 3 70.9 65.9 59.7 Others 5.8 4.6 4.5 0.5 2 2.7 5 We can see that here again the specific speed obtained with the oxycarbide amended supported is significantly increased compared to that of oxycarbide obtained from polycrystalline MoOs.
Example 6 10 This example illustrates the use of molybdenum oxycarbide as such amended according to the invention in the hydrogenation and decyclization reaction of benzene.
In this example, the modified oxycarbide catalyst is obtained from 15 Mo03 oriented (in the form of plates) synthesized in the presence of dry air in i WO 98/42438 PCTlFR98 / 00551 Example 1 and is used in the hydrogenation and decyclization benzene. The reaction temperature and the working pressure are 350 ° C and 60 bar respectively. The results obtained are reported in the Table 6. The catalyst is first activated at 6 bar under a mixture of n-heptane / hydrogen (see example 3) then placed under a benzene / hydrogen mixture at 60 bars.
Table b Hydrognation of benzene sure oxycarbide of Mo modified, Phone what, prepared go of MoOa East in presence of air dry and after activation under not-heptanelhydrogen (cf example 3d Time (h) 2 5 8 22 28 Conversion (%) 45.5 60.3 70.5 75.0 74.1 Selectivity in C6 (%) 99 98 97 98 98 Reaction efficiency in 45.0 59.1 68.4 73.5 72.6 C6 (%) Distribution of products reaction Selectivity in products

6 atoms of C (~ j Methylcciopentane 42.4 24.0 22.8 23.0 33.0 Cyclohexane 45.6 55.3 63.8 64.9 64.7 Cyclization 12.0 11.7 12.2 12.3 12.3 Cracked products (%) Cs + Ci 49.7 51.0 52.0 51.2 50.0 Ca + C2 25.7 26.0 27.0 26.8 27.3 2Ca 10.0 9.2 10.0 9, b 10.2 Others 14.6 12.8 11.0 12.4 12.5 Two points should be emphasized - the very high selectivity in terms of product with 6 carbon atoms, always greater than 97%

- a significant decyclization rate without cracking around 12%; this value is exceptionally high for such a difficult reaction and leaves at think that this catalyst can be used for reactions of decyclization of aromatics in petroleum refining, knowing that the benzene is the most difficult aromatic to decyclize.

Claims

1. Catalyst based on modified molybdenum oxycarbide characterized in that that it is prepared from a molybdenum oxide MoOs having a structure consisting essentially of monocrystalline wafers oriented in a preferential direction, said oxide then being treated under cover of a mixture of hydrocarbon and hydrogen, and that it has a specific surface of at least 80 m2/g.

2. Catalyst according to claim 1 characterized in that the oxycarbide is supported on a support, said support preferably having a surface high BET specificity.

3. Catalyst according to claim 2 characterized in that the support is pure or doped silicon carbide.

4. Process for obtaining catalyst based on molybdenum oxycarbide modified characterized in that the usual molybdenum oxide is started polycrystalline or optionally a precursor molybdenum compound which is transformed into oxide, which is heat-treated said oxide of molybdenum by sublimation-condensation at a temperature between between 500 and 800°C in an enclosure under an oxidizing gas atmosphere for at least 5 hours to obtain an oriented recrystallized oxide, which is then treated under current with a mixture of hydrocarbon and hydrogen to give a modified molybdenum oxycarbide.

5. Method according to claim 4 characterized in that the oxide of polycrystalline molybdenum or the precursor molybdenum compound of the oxide is mixed with or deposited on a support before treatment thermal.

5. Method according to any one of claims 4 or 5 characterized in that the oxidizing gas atmosphere is a low velocity current or a static atmosphere.

7. Method according to any one of claims 4 to 6 characterized in what the oxidizing gas is dry or moist air.

8. Use of catalysts based on oriented molybdenum oxycarbide claims 1 to 3 or obtained according to the process of claims 4 to 7 catalysis of petrochemical reactions.

9. Use according to claim 8 characterized in that the reactions petrochemicals are isomerization, hydrogenation of hydrocarbons linear and cyclic or the decyclization of aromatics.