SYNTHESIS OF A MOVTENB CATALYTIC CONVERTER FROM LOW-PRICE METAL OXIDES

Description

[0001] The invention relates to a novel process for producing a mixed oxide material containing molybdenum, vanadium, tellurium and niobium as a catalyst for the oxidative dehydrogenation of ethane to ethene or the oxidation of propane to acrylic acid and a process for producing the mixed oxide material.

[0002] MoVNbTe mixed oxides for the oxidation of propane to acrylic acid or for the oxidative dehydrogenation of ethane to ethylene are state-of-the-art. More than 200 patents and numerous scientific publications deal with catalysts based on MoVNbTe mixed oxides. The promotion of these mixed oxides with other metals of the periodic table is known. The highest reported yields for acrylic acid are 60% and for ethylene are approximately 80%.

[0003] The four-element MoVNbTe catalyst system was proposed by Mitsubishi for the ammoxidation of propane to acrylonitrile (1989, EP 318295 A1) and the oxidation to acrylic acid (1994, EP 6088038 A2). JP H07-053414 (Mitsubishi) discloses a catalytic process for the production of ethylene by the oxidative hydrogenation of ethane at low temperature, with high yield and high selectivity. This process for producing ethylene by contacting ethane with a molecular oxygen-containing gas in the presence of a catalyst composition at elevated temperature comprises the catalyst composition containing a mixed metal oxide having as essential components molybdenum, vanadium, tellurium, and oxygen and exhibiting a powder X-ray diffractogram having essentially the following relative peak intensities: 2θ (+-0.4°), rel. Int.: 22.1° (100), 28.2° (400~3), 36.2° (80~3), 45.1° (40~3), 50° (50~3).

[0004] MoVNbTe catalysts consist primarily of two orthorhombic phases, called "M1" and "M2" (T. Ushikubo, K. Oshima, A. Kayou, M. Hatano, Studies in Surface Science and Catalysis 112, (1997), 473). The M1 phase appears to play the essential role in the selective oxidation reactions.

[0005] According to P. De Santo et al., Z. Kristallogr. 219 (2004) 152, the main phases M1 and M2 in multimetal oxide catalysts for selective oxidation can be described, for example, with the following molecular formulas: M1: Mo 1 V 0.15 Te 0.12 Nb 0.128 O 3.7 or Mo 7.8 V 1.2 Te 0.937 Nb 1 O 28.9 M2: *Mo 1 V 0.32 Te 0.42 Nb 0.08 O 4.6 or Mo 4.31 V 1.36 Te 1.81 Nb 0.33 O 19.81

[0006] The two main phases can also occur with slightly different stoichiometry. For example, both vanadium and molybdenum are located at the center of an octahedron of oxygen atoms and are therefore partially interchangeable in structure, so that the same structure, e.g., the M1 phase, is also possible with a higher vanadium content. A detailed investigation of these relationships can be found in P. Botella et al., Solid State Science 7 (2005) 507-519. The M2 phase in particular is not active for the oxidative dehydrogenation of ethane (see J.S. Valente et al., ACS Catal. 4 (2014), 1292-1301, especially p. 1293). For the oxidative dehydrogenation of ethane, a catalyst consisting of the purest possible M1 phase is therefore desirable. Attempts are therefore being made to produce these crystal phases cleanly and separately.

[0007] EP 529853 A2 discloses a catalyst suitable for producing a nitrile from an alkane, the catalyst having the empirical formula MoV b Te c X x O n , wherein X is at least one of Nb, Ta, W, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pd, Pt, Sb, Bi, B and Ce, b is 0.01 to 1.0, c is 0.01 to 1.0; x is 0.01 to 1.0 and n is a number according to which the total valence of the metal elements is satisfied and the catalyst has X-ray diffraction peaks at the following 2θ angles in its X-ray diffraction pattern: Diffraction angle at 2θ (22.1° + / - 0.3°, 28.2° + / - 0.3°, 36.2° + / - 0.3°, 45.2° + / - 0.3°, 50.0° + / - 0.3°).

[0008] JP H07-232071 discloses a catalytic process for producing a nitrile, at a relatively low temperature and with a high yield, using an alkane as a raw material and a certain catalyst. The main component of the catalyst is a mixed metal oxide of molybdenum, vanadium, tellurium, oxygen and X (X is one or more elements selected from the group of niobium, tantalum, etc.), where the ratio of the main components, excluding oxygen, is expressed by the formulas I to IV: I) 0.25 < rMo < 0.98, II) 0.003 < rV < 0.50, III) 0.003 < rTe < 0.50, IV) 0 ≤ rX < 0.5, (rMo, rV, rTe and rX are the molar parts of molybdenum, vanadium, tellurium and X respectively) and in the XRD, XRD bands of this mixed oxide at the different 2θ angles 9.0°±0.3°, 22.1°±0.3°, 27.3°±0.3°, 29.2°±0.3° and 35.4°±0.3°. Accordingly, a nitrile can be prepared by reacting an alkane without the presence of a halogenated substance, e.g.with water etc., in the reaction system, at a low temperature with a high yield.

[0009] Other successful attempts to produce a pure M1 phase are based on separating the M2 phase from the phase mixture. These attempts are described, for example, in EP 1301457 A2, EP 1558569 A1, or WO 2009106474 A2.

[0010] AC Sanfiz et al., Top. Catal. 50 (2008) 19-32, describe hydrothermal syntheses of MoVNbTe oxide. These syntheses start exclusively with soluble compounds. Telluric acid Te(OH) 6 is typically used as the soluble tellurium compound. In the most common tellurium oxide compound, TeO 2 , tellurium has an oxidation state of +4. Unfortunately, tellurium dioxide (TeO 2 ) is poorly soluble in water. In telluric acid, however, tellurium has an oxidation state of +6. Therefore, tellurium must be highly oxidized to produce telluric acid. The usual synthesis is by oxidizing tellurium oxide with hydrogen peroxide, which poses safety problems on a large scale because hydrogen peroxide can disproportionately decompose into water and oxygen. Therefore, telluric acid is difficult to produce in large quantities. US 2014 / 336411 A1 1 discloses a process for producing a mixed oxide material containing the elements molybdenum, vanadium, niobium and tellurium.The synthesis was carried out under hydrothermal conditions using molybdenum trioxide, vanadium pentoxide, niobium oxalate and Te(OH) 6 as starting materials, and in the presence of oxo ligands such as ethylene glycol and citric acid.

[0011] A synthesis of the MoVNbTe mixed oxide without the use of telluric acid therefore has the potential to be significantly more cost-effective.

[0012] The Nb component used in the synthesis of MoVNbTe mixed oxides is usually ammonium niobium oxalate. Niobium oxide, on the other hand, is poorly soluble and therefore only of limited use as a starting material.

[0013] Watanabe (Applied Catal. A General, 194-195 (2000) 479-485) describes, among other things, the hydrothermal synthesis from the sparingly soluble precursors MoO 3 , V 2 O 5 and TeO 2 . The hydrothermal synthesis produces a precursor for an ammoxidation catalyst that has twice the activity after calcination compared to a catalyst prepared by the known dry method. The mixed oxides prepared by the solid-state reaction show rather low activity. It has been suggested that the higher activity of the catalyst prepared by hydrothermal synthesis is primarily due to its higher surface area.

[0014] The object of the present invention is to provide a mixed oxide material containing molybdenum, vanadium, tellurium and niobium ("MoVTeNb mixed oxide") with a high content of M1 phase, which has the highest possible activity and selectivity as a catalyst material especially for the oxidation of ethane to ethylene.

[0015] This object is achieved by a process for producing a mixed oxide material, comprising the steps: a) preparing a mixture of starting compounds containing starting compounds containing molybdenum, vanadium, niobium and tellurium and two chelating oxo ligands, b) hydrothermally treating the mixture of starting compounds at a temperature of 100 °C to 300 °C to obtain a product suspension, c) separating and drying the solid contained in the product suspension resulting from step b), d) activating the solid obtained from step c) in an inert gas.

[0016] The mixture of starting compounds is preferably present as an aqueous suspension and is subsequently treated hydrothermally. The term "hydrothermal" primarily refers to reaction conditions for producing a catalyst material in the presence of water and under elevated temperature and / or elevated pressure, for example, in an autoclave. The pressure can be in the range from 5 to 30 bar, preferably from 10 to 27 bar. Exemplary pressure ranges are 11 to 20 bar.

[0017] The hydrothermal treatment (step b)) produces a product suspension containing the MoVNbTe mixed oxide as a solid. In the process according to the invention, the solid from the suspension can be separated in step c) by one or more filtration steps, e.g., filtering it off from the mother liquor. Drying can be carried out in one step or in two steps in flowing or static air. The first drying step is preferably carried out at 60°C to 150°C (particularly preferably at 80°C to 120°C) and the second drying step at 200°C to 350°C (particularly preferably at 220°C to 280°C). In addition, step c) of the process according to the invention can include one or more steps of washing, calcining (thermal treatment), and / or grinding. Calcination can be carried out at 200 to 500 °C, preferably 250 °C to 350 °C in air.

[0018] After drying the filtrate in step c), the dried mixture is activated, for example, in a flowing or static inert gas atmosphere at approximately 500°C to 700°C for at least 1 hour (step d). Nitrogen, helium, or argon are particularly suitable as inert gases. It is preferred if the activation takes place in the range of 550°C to 650°C. For example, activation can take place at approximately 600°C for approximately 2 hours.

[0019] The starting compounds are molybdenum trioxide, vanadium pentoxide, niobium pentoxide and a tellurium-containing starting compound, wherein the tellurium-containing starting compound is tellurium dioxide.

[0020] Tellurium dioxide can preferably be present in any degree of hydration.

[0021] Tellurium dioxide preferably has a particle size with a D 90 < 100 µm.

[0022] It is particularly preferred that the D 50 value for the tellurium dioxide used as starting compound is below 35 µm.

[0023] Niobium oxide can also have a particle size with a D 90 < 100 µm, preferably D 90 < 75 µm, particularly preferably D 90 < 50 µm. Optionally, niobium oxide can have a particle size D 50 < 50 µm or < 35 µm.

[0024] In addition, all starting compounds used can have a particle size of D 90 < 100 µm, preferably D 90 < 75 µm, particularly preferably D 90 < 50 µm. Optionally, the starting compounds can have a particle size of D 50 < 50 µm or < 35 µm.

[0025] The starting compounds are in powder form and exhibit a particle size distribution. The particle size D 90 is defined as the particle diameter limit in the particle size distribution below which 90% of all particles lie. The particle size of the meridian, i.e., the particle size below which half of all particles lie in the particle size distribution, is also referred to as the particle size D 50. It is particularly preferred that the particle size D 50 for the tellurium dioxide used as the starting compound be below 35 µm.

[0026] The desired particle size D 90 or D 50 of the starting compound can be obtained by starting with a powder with a coarser particle size distribution and mechanically comminuting the particles. This can be achieved by grinding, using any suitable means familiar to the person skilled in the art, such as impact mills, planetary mills, mortars, etc.

[0027] An advantage of the preparation process according to the invention is that a synthesis of the M1 phase from the insoluble and inexpensive oxides MoO 3 , V 2 O 5 , Nb 2 O 5 , and TeO 2 is used as starting compounds. Citric acid, glycol, and oxalic acid have proven particularly suitable as chelating oxo ligands.

[0028] The two chelating oxo ligands should preferably be present in the mixture of starting compounds in a Mo / oxo ligand ratio of 1:0.01 to 1:1, preferably 1:0.08 to 1:0.4, more preferably 1:0.15 to 1:0.25. The two chelating oxo ligands can each have the same Mo / oxo ligand ratio or a different one.

[0029] The synthesis according to the invention not only provides a MoVTeNb mixed oxide with a high phase purity with respect to the M1 phase, but the obtained MoVTeNb mixed oxide also represents a catalyst material with improved activity for the oxidation of ethane to ethylene. A further advantage of the synthesis of the M1 phase according to the invention is the high efficiency of the conversion of the starting materials by hydrothermal synthesis.

[0030] If the stoichiometry of the reactants is in the range Mo / V / Nb / Te = 1:0.22:0.1:0.1 to 1:0.3:0.17:0.17, Mo, V, Nb, and Te are almost completely converted to the M1 phase, so that less than 100 ppm of all metals remain in the mother liquor. The possible stoichiometry of the M1 phase is well known from the literature and can be described by the formula Mo 1 V a Nb b Te c O x with a = 0.2 to 0.3, b = 0.1 to 0.2, c = 0.1 to 0.25, and x, depending on the oxidation state of the metals (Mo, V, Nb, and Te), is a value that leads to charge balance.

[0031] It has also been found that hydrothermal crystallization is excellent when MoO 3 , V 2 O 5 , Nb 2 O 5 , and TeO 2 are used with citric acid, glycol, and oxalic acid. Crystallization is particularly successful in the absence of ammonium ions. Therefore, the absence of ammonium ions during synthesis is preferred.

[0032] By the process according to the invention, a mixed oxide material comprising the elements molybdenum, vanadium, niobium and tellurium is obtained for the oxidation of ethane, with the following stoichiometry: Mo 1 V a Nb b Te c O x with 0.27 < a < 0.31; 0.08 < b < 0.12; 0.08 < c < 0.12, which has diffraction peaks h, i, k and 1 in the XRD, the vertices of which are approximately at the diffraction angles (2·) 26.2° ± 0.5° (h), 27.0° ± 0.5° (i), 7.8° ± 0.5° (k) and 28.0° ± 0.5° (1).

[0033] The MoVTeNb mixed oxide according to the invention can be used as a catalyst material for the oxidation and / or oxidative dehydrogenation ("ODH") of hydrocarbons, in particular for the oxidative dehydrogenation of ethane to ethylene. It can have a BET surface area of ​​5 to 25 m 2 / g, particularly preferably 5 to 15 m 2 / g.

[0034] The MoVTeNb mixed oxide produced by the process of the invention can be used as a catalyst or catalyst material. It can be used in a variety of ways in a commercial catalyst. For example, it can be processed into catalyst tablets by tabletting, which can then be introduced into a reactor.

[0035] The catalyst material can also be processed into an extrudate (tablets, molded bodies, honeycomb bodies, and the like) together with a suitable binder. Any binder familiar to the person skilled in the art and deemed suitable can be used as the binder. Preferred binders include pseudoboehmite and silicate binders such as colloidal silicon oxide or silica sol.

[0036] The catalyst material can further be processed together with other components, preferably with a binder, particularly preferably with an organic binder, for example an organic adhesive, polymers, resins, or waxes, to form a washcoat, which can be applied to a metallic or ceramic support. Additional impregnation or calcination steps can optionally be carried out.

[0037] The X-ray diffractogram of the MoVTeNb mixed oxide formed by the process according to the invention, when using Cu-Kα radiation, has diffraction reflections h, i, k and l, the vertices of which are approximately at the diffraction angles (2θ) 26.2° ± 0.5° (h), 27.0° ± 0.5° (i), 7.8° ± 0.5° (k) and 28.0° ± 0.5° (1), wherein the intensities P h , P i , P k , P l of the diffraction reflections h, i, k and l can satisfy the following relationships, with R x (x = 1 to 3) as the intensity ratio defined by the relationships: and / or and / or

[0038] In the X-ray diffraction pattern (XRD) of embodiments of the mixed oxide material, the diffraction peak i may have the second highest intensity and / or the diffraction peak h may have the third highest intensity.

[0039] The MoVNbTe mixed oxide according to the invention is used as catalyst material in the examples and is therefore sometimes referred to as catalyst in the experimental data. Figure 1 : XRD of the MoVTeNb mixed oxide from Example 1. Figure 2 : XRD of the MoVTeNb mixed oxide from Example 2. Figure 3 : XRD of the MoVTeNb mixed oxide from Comparative Example 1. Figure 4 : Pore distribution of the MoVTeNb mixed oxide from Example 1. Figure 5 : Pore distribution of the MoVTeNb mixed oxide from Example 2. Figure 6 : Pore distribution of the MoVTeNb mixed oxide from Comparative Example 1. Figure 7 : Comparison of the catalytic activity of the MoVTeNb mixed oxides according to Example 2 and Comparative Example 1 in the ODH of ethane.

[0040] The MoVTeNb mixed oxide produced by the novel process according to the invention is clearly more active. It achieves a higher activity, standardized to 1 g of catalyst, than the prior art catalyst according to the comparative example ( Figure 7 This demonstrates that the process according to the invention produces a mixed oxide material with novel properties. However, the new properties of the new mixed oxide material cannot be readily captured using conventional characterization methods. Characterization methods:

[0041] The following methods are used to determine the parameters of the catalysts according to the invention: 1. BET surface area

[0042] The determination was carried out using the BET method according to DIN 66131; a publication of the BET method can also be found in J. Am. Chem. Soc. 60, 309 (1938). The measurements were carried out on a Sorptomatic 1990 device at 77 K. Before the measurement, the sample was evacuated for 2 h at 523 K. Linear regression of the isotherms according to the BET method was performed in a pressure range of p / p 0 = 0.01 - 0.3 (p 0 = 730 Torr). 2. Powder X-ray diffraction (XRD)

[0043] The X-ray diffraction patterns were recorded on a PANalytical Empyrean equipped with a Medipix PIXcel 3D detector in Θ-Θ geometry over an angular range of 2Θ = 5 - 70°. The X-ray tube generated Cu-K radiation. The Cu-Kβ radiation was suppressed by using a Ni filter in the beam path of the incident X-ray beam, so that only Cu-Kα radiation with a wavelength of 15.4 nm (E = 8.04778 keV) was diffracted at the sample. The height of the source-side beam path was adjusted using a programmable divergence slit (PDS) so that the sample was irradiated over the entire angular range over a length of 12 mm. The width of the detector-side X-ray beam was limited to 10 mm by a fixed aperture. Horizontal divergence was minimized by using a 0.4 rad Soller slit.

[0044] The height of the detector-side beam path was adjusted analogously to the source-side beam path using an automatic anti-scatter slit (programmable anti-scatter slit - PASS) so that the X-ray beam reflected on the sample over a length of 12 mm was detected over the entire angular range.

[0045] Depending on the amount available, the samples were prepared either on an amorphous silicon sample plate or tableted as flatbed samples. 3. Pore distribution

[0046] The pore size distribution was determined using nitrogen sorption measurements on a Sorptomatic device or a TriStar 3000 device at 77 K. Before the measurement, the sample was evacuated for 2 h at 523 K. Both adsorption and desorption isotherms were determined and used for evaluation according to the Barrett-Joyner-Halenda method (BJH).

[0047] The invention will now be explained in more detail with reference to the following non-limiting embodiments. Examples of implementation: Example 1:

[0048] TeO 2 (Alfa Aesar) was slurried in 200 g of distilled H 2 O and ground in a planetary ball mill with 1 cm balls (ZrO 2 ). The portion was then transferred to a beaker with 500 ml of distilled H 2 O. The Nb 2 O 5 was slurried in 200 g of distilled H 2 O and ground in the same ball mill. The portion was then transferred to a beaker with 500 ml of distilled H 2 O. The next morning, the mixture was heated to 80 °C, 107.8 g of oxalic acid dihydrate were added to the Nb 2 O 5 suspension and stirred for approximately 1 h. 6 L of distilled H 2 O were placed in an autoclave (40 L) and heated to 80 °C while stirring (stirrer speed 90 rpm). Once the water had reached the desired temperature, 61.58 g of citric acid, 19.9 g of ethylene glycol, 615.5 g of MoO 3 (Sigma Aldrich), 124.5 g of V 2 O 5 , the ground TeO 2 , and the ground Nb 2 O 5 in oxalic acid were added successively. 850 ml of distilled water was used to transfer and rinse the vessels. The total water volume in the autoclave was 8.25 L.Subsequently, the mixture was blanketed with nitrogen. Hydrothermal synthesis was carried out in a 40 L autoclave at 190 °C for 48 h. After synthesis, the mixture was filtered using a vacuum pump with a blue band filter, and the filter cake was washed with 5 L of distilled water.

[0049] Drying was carried out at 80 °C in a drying oven for 3 days, and the product was then ground in an impact mill. A solids yield of 0.8 kg was achieved.

[0050] The subsequent calcination was carried out at 280 °C for 4 h in air (heating rate 5 °C / min air: 1 L / min).

[0051] Activation was carried out in a retort at 600 °C for 2 h (heating rate 5 °C / min N 2 : 0.5 L / min).

[0052] The product had a BET surface area of ​​9 m 2 / g and a pore volume of 0.04 cm 3 / g. Example 2:

[0053] 75 mL of bidistilled water was placed in a 100 mL PTFE beaker, 177.8 mg of (mono)ethylene glycol were added dropwise, and then 5397.9 mg of MoO 3 , 1023.9 ​​mg of V 2 O 5 , 599.1 mg of TeO 2 , 549.5 mg of Nb 2 O 5 xH 2 O (Nb = 63.45 wt%), 540.9 mg of citric acid, and 338.3 mg of oxalic acid were slurried. The Teflon beaker was sealed and transferred to a stainless steel autoclave bomb. This was sealed pressure-tight and clamped onto a horizontally rotating shaft in an oven preheated to 190 °C. After 48 hours, the autoclave bomb was removed from the oven and immediately quenched under running water and then cooled in an ice bath for 45 minutes.

[0054] The resulting product suspension was filtered through filter paper (pore size 3 µm) and the solid was washed with 200 mL of double-distilled water.

[0055] The product obtained in this way was dried for 16 h in a drying cabinet at 80 °C and then ground in a hand mortar.

[0056] The solid yield was 6.2 g. Activation was carried out at 600 °C for 2 h (heating rate 10 °C / min N 2 : 100 mL / min). The XRD diffractogram of the product is shown in Figure 2 shown, the BET surface area was 7.3 m 2 < / g, the pore volume was below 0.012 cm 3 < / g. Comparison example 1:

[0057] 3.3 L of distilled H2O are placed in an autoclave (40 L) and heated to 80°C while stirring. 725.58 g of ammonium heptamolybdate tetrahydrate (from HC Starck) are added and dissolved (AHM solution). In three 5 L beakers, 1.65 L of distilled H2O are each heated to 80°C while stirring on a temperature-controlled magnetic stirrer. 405.10 g of vanadyl sulfate hydrate (GfE, V content: 21.2%), 185.59 g of ammonium nioboxalate (HC Starck, Nb content: 20.6%), and 94.14 g of telluric acid are then added to each of these beakers and dissolved (V solution, Nb solution, and Te solution).

[0058] Subsequently, the V solution, the Te solution, and finally the Nb solution were pumped into the AHM solution using a peristaltic pump. Pumping time: V solution: 4.5 min at 190 rpm (tubing diameter: 8 x 5 mm), Nb solution: 6 min at 130 rpm (tubing diameter: 8 x 5 mm).

[0059] The resulting suspension was then stirred for a further 10 min at 80 °C. The stirrer speed during precipitation was 90 rpm.

[0060] Subsequently, the autoclave was blanketed with nitrogen by building up a pressure of approximately 6 bar with nitrogen and opening the drain valve sufficiently to allow N2 to flow through the autoclave (5 min). Finally, the pressure was released again via the vent valve to a residual pressure of 1 bar.

[0061] The hydrothermal synthesis in a 40 L autoclave was carried out at 175 °C for 20 h (heating time: 3 h), with an anchor stirrer at a stirrer speed of 90 rpm.

[0062] After synthesis, the mixture was filtered using a vacuum pump with a blue band filter and the filter cake was washed with 5 L of distilled H 2 O.

[0063] The drying was carried out at 80 °C in a drying cabinet for 3 days and then ground in an impact mill; the solid yield was 0.8 kg.

[0064] Calcination was carried out at 280 °C for 4 h (heating rate of 5 °C / min, air: 1 L / min). Activation was carried out in a retort at 600 °C for 2 h (heating rate of 5 °C / min, N 2 : 0.5 L / min).

[0065] The BET surface area of ​​the product was 9 m 2 / g, the pore volume = 0.055 cm 3 / g. Example 3:

[0066] The catalytic activity of the catalysts from Example 2 and the comparative example in the oxidative dehydrogenation of ethane was investigated in a tubular reactor at atmospheric pressure in the temperature range 330 to 420 °C. For this purpose, 25 mg (Example 2) or 200 mg (Comparative Example 1) of catalyst (particle size 150 to 212 µm) were diluted with silicon carbide (particle size 150 to 212 µm) in a mass ratio of 1:5. A layer of 250 mg of silicon carbide of the same particle size was filled above and below the catalyst bed, and the ends of the tubular reactor were sealed with quartz wool plugs.

[0067] The reactor was purged with inert gas before the start of the experiment and then heated to 330 °C under a helium flow of 50 sccm. After the desired temperature was reached and stable for one hour, the reactor was switched to the reaction gas mixture.

[0068] The input gas composition was C 2 H 6 / O 2 / He = 9.1 / 9.1 / 81.8 (v / v) at a total volume flow of 50 sccm.

[0069] The analysis of the product gas stream was determined in a gas chromatograph equipped with Haysep N and Haysep Q columns, a molecular sieve column 5A and a thermal conductivity detector.

[0070] The ethylene formation rates under the conditions described above are in Figure 7 shown.

Claims

1. A process for preparing a mixed oxide material comprising the steps of: a) Preparation of a mixture of starting compounds containing molybdenum trioxide, vanadium pentoxide, niobium pentoxide and a starting compound containing tellurium and two chelating oxoligands, b) hydrothermal treatment of the mixture of starting compounds at a temperature of 100 °C to 300 °C to obtain a product suspension, c) separating and drying the solid contained in the product suspension resulting from step b), d) activating the solid obtained from step c) in inert gas, characterized in that the tellurium-containing starting compound is tellurium dioxide.

2. Process according to claim 1, characterized in that the activation in step d) is carried out at a temperature between 450 °C to 700 °C, preferably 550 °C to 650 °C.

3. Process according to claim 2, characterized in that the niobium pentoxide has a particle size D90 of less than 100 µm.

4. Process according to claim 1, characterized in that the tellurium dioxide has a particle size D90 of less than 100 µm.

5. Process according to one of the preceding claims, characterized in that one of the chelating oxoligands is ethylene glycol.

6. Process according to one of the preceding claims, characterized in that one of the chelating oxoligands is citric acid.

7. A mixed oxide material for the oxidation of ethane comprising the elements molybdenum, vanadium, niobium and tellurium, having the following stoichiometry:         Mo1VaNbbTecOx with 0.27< a < 0.31; 0.08 < b < 0.12; 0.08 < c < 0.12, which in XRD, using Cu-Kα-radiation, has diffraction reflections h, i, k and l, the apexes of which lie approximately at the diffraction angles (2θ) 26.2° ± 0.5° (h), 27.0° ± 0.5° (i), 7.8° ± 0.5° (k) and 28.0° ± 0.5° (1), obtainable by process of claim 1.

8. Use of a catalyst according to claim 7 for the oxidative dehydrogenation of ethane to ethene.

9. Use of a catalyst according to claim 7 for the oxidation of propane.