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    • 专利摘要:
    improved oxidative dehydrogenation catalyst. oxidative dehydrogenation catalysts comprising movnbteo having an improved consistency of composition and a 25% conversion of ethylene at less than 420°c and a selectivity for ethylene of more than 95% are prepared by treating the catalyst precursor with h2o2 in an amount equivalent to 0.30 to 2.8 ml of h2o2 of a 30% solution per gram of catalyst precursor prior to calcination.
    公开号:BR112018003193B1
    申请号:R112018003193-3
    申请日:2016-08-04
    公开日:2021-07-20
    发明作者:Vasily Simanzhenkov；Xiaoliang Gao；David Sullivan；Hanna Drag；Leonid KUSTOV；Aleksey Kucherov；Elena Finashina
    申请人:Nova Chemicals (International) S.A.；
    IPC主号:
    专利说明:

    TECHNICAL FIELD
    [001] The present invention relates to an improved method for producing a catalyst for the oxidative dehydrogenation of lower alkanes to lower alkenes. Multicomponent metal oxide catalysts for the oxidative dehydrogenation of alkanes are known. Such catalysts are typically made by mixing metal solutions and then precipitating the metal oxide "mixture" from the solution and calcining it. As a result, catalysts are heterogeneous mixtures of various metal oxides and phases and may include some highly active species, but also some species that exhibit significantly lower activity. Applicants have found that by treating precipitated metal oxides with a controlled amount of hydrogen peroxide prior to calcination, catalyst activity is improved. FUNDAMENTALS OF THE TECHNIQUE
    [002] United States Patent 2,895,920 issued July 21, 1959 to Janoski, assigned to Sun Oil Company teaches a process for preparing a catalyst for the conversion of hydrocarbons, such as dehydrogenation. Catalysts comprise oxides of cobalt, iron, nickel, molybdenum, manganese, chromium, vanadium, tin and tungsten. Catalysts do not incorporate any niobium. In the process to form the catalysts a hydrogel of metal oxides which are difficult to reduce and metal oxides which are capable of existing in various oxidation states is prepared. A metal hydrogel is prepared and aged in the presence of hydrogen peroxide. The aged hydrogel is treated with a compound to precipitate the metals which are then filtered, dried and calcined. The sequence of treatments is different from the present invention. A hydrogel is not prepared in the process of the present invention.
    U.S. Patent 3,474,042 issued October 21, 1969 to Fattore et al., assigned to Montecatini Edison S.p.A. teaches a metal oxide catalyst comprising molybdenum or tungsten. Catalysts are prepared by the formation of peroxy - tungsten and molybdenum compounds, reacting the metal oxide with hydrogen peroxide or compounds that form hydrogen peroxide. The molar ratio of peroxide to metal oxide can range from 0.25 to 10, typically 1 to 3. The solution can be spray dried or impregnated on a carrier.
    US Patent 4,709,070 issued November 24, 1987 to Sasaki et al., assigned to Nitto Chemical Industry Co., Ltd. teaches a method for regenerating the activity of a complex metal oxide catalyst used for oxidation, the oxidative amoxidation and dehydrogenation of alkanes. Catalysts before reactivation are quite different from those presented here. They contain a number of elements not present in the catalysts of the present invention such as Fe, Sb, Cu and Co. The "deactivated" catalyst is treated with a Te compound, a Mo compound or a mixture thereof. The Te and Mo compounds can be oxides. In some cases, Te and Mo compounds can be prepared by contacting them with H2O2 in the presence of oxide, oxyacid, oxyacid salts, heteropolyacids or molybdenum salts thereof (Col. 9 lines 38-42). The patent teaches in addition to treating the entire catalyst precursor with H2O2.
    [005] United States Patent 8,105,972 issued January 31, 2012 to Gaffney et al. as of an application filed on April 2, 2009, assigned to Lummus Technology Inc. teaches a catalyst for the oxidative dehydrogenation of alkanes. The catalyst is formed in a conventional manner by hydrothermal treatment of metal oxide components. The resulting catalyst is recovered, dried and calcined. Then the calcined catalyst is treated with an acid. This process teaches beyond the object of the present invention, as it teaches a post-calcination treatment. Furthermore, the patent fails to teach H2O2 treatment.
    [006] The present invention seeks to provide an improved catalyst for oxidative dehydrogenation by treating the catalyst precursor with H2O2, prior to calcination. DISCLOSURE OF THE INVENTION
    [007] In an embodiment of the invention, a precursor for an oxidative dehydrogenation catalyst is prepared by the hydrothermal reaction of the compounds of Mo, V, Te and Nb and, before calcination, treating the precursor with H2O2.
    [008] In one embodiment, the present invention provides a method for improving the consistency of an oxidative dehydrogenation catalyst of the empirical formula (measured by PIXE):
    where d is a number to satisfy the valence of the oxide comprising treating a precursor, prior to calcination, with H2O2 in an amount equivalent to 0.30 to 2.8 mL of H2O2 of a 30% solution per gram of precursor of catalyst.
    [009] In another modality, the precursor is prepared by: i) forming an aqueous solution of ammonium heptamolybdate (tetrahydrate) and telluric acid at a temperature of 30 °C to 85 °C and adjusting the pH of the solution to 6 .5 to 8.5, preferably from 7 to 8, more preferably from 7.3 to 7.7 with a nitrogen-containing base to form soluble salts of the metals; ii) preparing an aqueous solution of vanadyl sulphate at a temperature from room temperature to 80°C (preferably 50°C to 70°C, more preferably from 55°C to 65°C); iii) mixing the solutions from steps i) and ii) together; iv) slowly (dropwise) adding a solution of niobium monoxide oxalate (NbO(C2O4H) 3) to the solution from step iii) to form a slurry; and v) heating the resulting slurry in an autoclave under an inert atmosphere at a temperature of 150 °C to 190 °C for not less than 10 hours.
    [010] In another modality, the solid resulting from step v) is filtered and washed with deionized water and the washed solid is dried for a period of 4 to 10 hours at a temperature of 70 to 100°C.
    [011] In a further modality, the precursor is calcined in an inert atmosphere at a temperature of 200°C to 600°C for a period of 1 to 20 hours.
    [012] In another embodiment, the precursor is treated with the equivalent of 0.3 to 2.8 mL of a 30% w/w solution of H2O2 per gram of catalyst precursor for a time period of 5 minutes at 10 hours at a temperature of 20 to 80°C.
    [013] In another embodiment in the catalyst, the molar ratio of Mo:V is from 1:0.22 to 1:0.29.
    [014] In another modality in the catalyst, the molar ratio of Mo:Te is greater than 1:0.11 and less than 1:0.15.
    [015] In another modality in the catalyst, the molar ratio of Mo:V is from 1:0.22 to 1:0.25.
    [016] In another modality in the catalyst, the molar ratio of Mo:Te is from 1:0.11 to 1:0.13.
    [017] In another modality, the catalyst has a bulk density of 1.20 to 1.53 g/cm3.
    [018] In another embodiment in the crystalline phase of the catalyst, the amount of the phase having the formula (TeO) 0.39 (Mo3.52V1.06Nb0.42) O14 is above 75% by weight. % of measured crystalline phase as determined by XRD.
    [019] In another embodiment in the crystalline phase of the catalyst, the amount of the phase having the formula (TeO) 0.39 (Mo3.52V1.06Nb0.42) O14 is above 85% by weight. % of measured crystalline phase as determined by XRD.
    [020] Another embodiment of the invention provides a method for the oxidative dehydrogenation of a mixed feed of ethane and oxygen in a volume ratio of 70:30 to 95:5 at a temperature below 420°C, preferably below 400 °C at a gas hourly space velocity of not less than 500 h-1 and a pressure of 0.8 to 1.2 atmosphere comprising passing said mixture over the above catalyst.
    [021] In another embodiment, a conversion to ethylene is not less than 90%.
    [022] In another modality, the hourly space velocity of the gas is not less than 1000 h-1.
    [023] In another modality, the calcined catalyst forms a fixed bed in the reactor.
    [024] In another modality, the catalyst has the empirical formula (measured by PIXE):
    where d is a number to satisfy the valence of the oxide and not less than 75% by weight. % of a crystalline component has the formula (TeO) 0.39 (Mo3.52V1.06Nb0.42) O14 as determined by XRD.
    [025] In another modality in the crystalline phase of the catalyst with the formula (TeO)0.71(Mo0.73V0.2Nb0.07)3O9 is from 2.4 to 12% by weight as determined by XRD.
    [026] In another modality, an (internal) surface of a reactor is seeded with the above catalyst.
    [027] In another embodiment, the reactor surface is selected from the group consisting of stainless steel, silica, alumina coating and polytetrafluoroethylene.
    [028] In another modality, the reactor contains particles (irregular such as flakes, granules, globules, filaments etc. or regular such as spheres, ellipticals, rods, rectangular prisms (right and not right), pentagonal prisms, pyramids, etc. .) of stainless steel, silica, alumina and polytetrafluoroethylene seeded with the above catalyst.
    [029] In another embodiment, a fully fluorinated ethylene propylene polymer reactor coating seeded with the above catalyst is provided. BRIEF DESCRIPTION OF THE DRAWINGS
    [030]Figure 1 is a schematic drawing of the reactor used to test the ODH catalysts.
    [031] Figure 2 is a graph of the temperature at which there is a 25% conversion of ethane to ethylene versus the 30% volume of H2O2 for 1.41 g of a catalyst with a temperature at which there is a 25% conversion less than 420°C and a selectivity for ethylene greater than 95% prepared in the examples.
    [032] Figures 3 are a graph of the selectivity for conversion to ethylene at the temperature at which there is a 25% conversion to ethylene versus the 30% volume of H2O2 for 1.41 g of catalyst with a temperature at which there is a conversion of 25% less than 420°C and a selectivity for ethylene greater than 95% prepared in the examples. BEST WAY TO CARRY OUT THE INVENTION number scales
    [033] In addition to the operational examples or where otherwise indicated, all numbers or expressions with respect to amounts of ingredients, reaction conditions, etc., used in the specification and claims shall be understood to be modified in all cases by the term "about". Accordingly, unless otherwise indicated, the numerical parameters presented in the following specification and in the appended claims are approximations which may vary depending on the properties which the present invention seeks to obtain. At the very least, and not as an attempt to limit the application of the equivalents doctrine to the scope of the claims, each numerical parameter should at least be interpreted in light of the number of significant digits reported and by applying common rounding techniques.
    [034] Notwithstanding the numerical ranges and parameters that define the broad scope of the invention are approximations, the numerical values presented in the specific examples are reported as accurately as possible. Any numerical value, however, inherently contains certain errors, necessarily resulting from the standard deviation found in the respective test measurements.
    [035]It should be understood that any numerical range mentioned herein is intended to include all subranges included in that range. For example, a range of "1 to 10" is intended to include all sub-ranges between and including the stated minimum value of 1 and the stated maximum value of 10; that is, having a minimum value equal to or greater than 1 and a maximum value equal to or less than 10. As the numerical ranges disclosed are continuous, they include all values between the minimum and maximum values. Unless otherwise stated, the various numerical ranges specified in this application are approximations.
    [036]All composition ranges expressed herein are limited in total and do not exceed 100 percent (percent by volume or percent by weight) in practice. Where multiple components may be present in a composition, the sum of the maximum quantities of each component may exceed 100 percent, with the understanding that, and as those skilled in the art readily understand, that the quantities of components actually used will conform to the maximum of 100 percent.
    [037]In the descriptive report, the phrase the temperature at which there is 25% conversion of ethane to ethylene is determined by plotting a graph of conversion to ethylene against temperature typically with data points below and above 25% conversion. Then a graph of the data is prepared or the data is fitted to an equation and the temperature at which there is a 25% conversion of ethane to ethylene is determined. In some cases, in the examples, the data had to be extrapolated to determine the temperature at which a 25% conversion occurred.
    [038]In the descriptive report, the phrase selectivity at 25% conversion is determined by graphically plotting the selectivity as a function of temperature. The data is then plotted on a graph of selectivity versus temperature or fit into an equation. Once you have calculated the temperature at which a 25% conversion occurs, you can determine from the graph or equation the selectivity at that temperature.
    [039] The calcined catalysts of the present invention typically have the formula: Mo1.0V0.22-0.33Te0.10-0.16Nb0.15-0.19Od as determined by PIXE where d is a number to satisfy the valence of the oxide . In some embodiments, the molar ratio of Mo:V in the calcined catalyst is 1:0.22 to 1:0.33, in other embodiments, the molar ratio of Mo:V in the calcined catalyst is 1:0.22 to 1:0.29, in some modes from 1:0.22 to 1:0.25. In other embodiments, the molar ratio of Mo:Te in the calcined catalyst is greater than 1:0.10 and less than 1:0.16, in other embodiments, the molar ratio of Mo:Te in the calcined catalyst is 1 : 0.11 to 1: 0.15.
    [040]The catalyst precursor is typically prepared by mixing solutions or suspensions (suspensions) of oxides or salts of the metal components.
    [041] In some embodiments, the precursor can be prepared by a process comprising the following steps: i) form an aqueous solution of ammonium heptamolybdate (tetrahydrate) and telluric acid at a temperature of 30 °C to 85 °C and adjusting the pH of the solution to from 6.5 to 8.5, preferably from 7 to 8, more preferably from 7.3 to 7.7 preferably with a nitrogen-containing base to form soluble salts of the metals; ii) preparing an aqueous solution of vanadyl sulphate at a temperature from room temperature to 80°C (preferably 50°C to 70°C, more preferably from 55°C to 65°C); iii) mixing the solutions from steps i) and ii) together; iv) slowly (dropwise) adding a solution of niobium monoxide oxalate (NbO(C2O4H) 3) to the solution from step iii) to form a slurry; v) heating the resulting slurry in an autoclave under an inert atmosphere at a temperature of 150 °C to 190 °C for not less than 10 hours.
    [042] In another modality, the sludge from step v) is filtered, washed with deionized water and dried for a period of 4 to 10 hours at a temperature of 70 to 100°C.
    [043] In another modality: after step i) one or more of the following steps can be incorporated into the process: a) evaporate the aqueous solvent to obtain a solid; b) drying the solid at a temperature of 80°C to 100°C; and c) redissolving the solid in water at a temperature of 40°C to 80°C (preferably 50°C to 70°C, more preferably 55°C to 65°C).
    [044] In another modality, after step ii) the solutions are cooled to a temperature of 20°C to 30°C.
    [045] In another modality, with part of step vi) the solution is cooled to a temperature of 20°C to 30°C.
    [046] In another modality, the precursor can be made by a process that comprises: i) forming an aqueous solution of ammonium heptamolybdate (tetrahydrate) and telluric acid at a temperature of 30 °C to 85 °C and adjusting the pH from the solution to from 7.3 to 7.7 (preferably from 7.4 to 7.5) with a nitrogen-containing base to form soluble salts of the metals; ii) evaporating the aqueous solvent to obtain a solid; iii) drying the solid at a temperature of 80°C to 100°C; iv) redissolving the solid in water at a temperature of 40°C to 80°C (preferably 50°C to 70°C, more preferably 55°C to 65°C). v) preparing an aqueous solution of vanadyl sulphate at a temperature from room temperature to 80°C (preferably 50°C to 70°C, more preferably from 55°C to 65°C); vi) cooling the solutions from steps iv) and v) to a temperature of 20 to 30 °C vii) mixing the cooled solutions from step vi together; viii) slowly (dropwise) adding a solution of niobium monoxide oxalate (NbO(C2O4H)3) to the solution from step vii) to form a slurry (brown); ix) heat the resulting slurry in an autoclave under an oxygen-free atmosphere at a temperature of 150 °C to 190 °C for not less than 10 hours. x) cool the autoclave to room temperature and filter and wash the resulting solid with deionized water; and xi) drying the washed solid for a time period of 4 to 10 hours at a temperature of 70 to 100°C.
    [047] In some embodiments, the reactor (catalyst) may be coated with a coating selected from the group consisting of stainless steel, silica, alumina coating and polytetrafluoroethylene, preferably polytetrafluoroethylene (TEFLON) seeded with catalyst with a conversion of 25% in ethylene at 420 °C or less and a selectivity to ethylene of not less than 90%.
    [048] The seed catalyst can be a catalyst with the empirical formula (measured by PIXE):
    where d is a number to satisfy the valence of the oxide and not less than 75% by weight of a crystalline component has the formula (TeO) 0.39 (Mo3.52V1.06Nb0.42) O14 as determined by XRD.
    [049] In some embodiments, the reactor (catalyst precursor) may be coated with a coating of a fully fluorinated ethylene propylene polymer (FEP) seeded with a catalyst having a 25% conversion to ethylene at 420 °C or less and a selectivity for ethylene of not less than 90%.
    [050]In some modalities, the seed catalyst has the empirical formula (measured by PIXE) Mo1.00V0.22-0.33Te0.10-0.16Nb0.15-0.18Od where d is a number to satisfy the valence of the oxide and has at least 75% by weight of a crystalline component has the formula (TeO)0.39(Mo3.52V1.06Nb0.42)O14 as determined by XRD.
    [051] Seed catalyst loadings can range from 1 to 15% by weight. of the reactor surface (eg steel, TEFLON or FEP).
    [052] In some cases, the reactor (catalyst precursor) contains stainless steel, silica, alumina and polytetrafluoroethylene particles seeded with a catalyst with a 25% conversion to ethylene at 420 °C or less and a selectivity to ethylene of not less to 90%.
    [053] In some modalities, the seed catalyst has the empirical formula (measured by PIXE) Mo1.0V0.22-0.33Te0.10-0.16Nb0.15-0.19Od where d is a number to satisfy the valence of the oxide and has at least 75% by weight of a crystalline component has the formula (TeO)0.39(Mo3.52V1.06Nb0.42)O14 as determined by XRD.
    [054] Particles can be (irregular such as flakes, granules, globules, filaments etc. or regular such as spheres, ellipticals, rods (stirring bars), rectangular prisms (right and not right), pentagonal prisms, pyramids, etc. )
    [055] The loadings of seed catalysts on the particles can vary from 1 to 15% by weight of the particles.
    [056] In some circumstances, it may be easier to replace particles where the seed catalyst, for whatever reason, has been depleted with new seed particles with an appropriate seed particle loading than to replenish the seed coating on the inner surface of the catalyst reactor.
    [057] A catalyst produced from a catalyst seeded hydrothermal reactor having a conversion of 25% to ethylene at 420 °C or less and a selectivity for ethylene of not less than 90% generally has the empirical formula determined by PIXE, Mo1V0 .34 -0.39Te0.09-0.14Nb0.14-0.16Od where d is a number to satisfy the valence of the oxide.
    [058] The peroxide treatment can take place at atmospheric pressure and at ambient temperature (eg 15 °C to 30 °C) to about 80 °C, in some cases 35 °C to 75 °C in other examples from 40°C to 65°C. The peroxide has a concentration of 10 to 30% by weight%, in some cases from 15 to 25% by weight. The treatment time can vary from 1 to 10 hours, in some cases from 2 to 8 hours, in other cases from 4 to 6 hours.
    [059] The catalyst precursor is treated with the equivalent of 0.3 to 2.8, in some embodiments of 0.3 to 2.5 mL of a 30% by weight solution of aqueous H2O2 per gram of precursor. The treatment must be in a slurry (eg the precursor is at least partially suspended) to provide an even distribution of H2O2 and to control temperature rise. For post-calcination treatment with H2O2, there is a sudden late reaction with H2O2. The process of the present invention is an instantaneous reaction that is more controlled and safer.
    [060]The treated catalyst precursor is then subjected to calcination to produce the active oxidative dehydrogenation catalyst. The treated precursor can be calcined in an inert atmosphere at a temperature of 200 °C to 600 °C for a time period of 1 to 20 hours. The purge gases used for calcination are inert gases, including one or more of nitrogen, helium, argon, CO2 (preferably of high purity > 90%), said gases or mixture containing less than 1% by vol. of hydrogen or air, at 200 to 600 °C, preferably at 300 to 500 °C. The calcination step can take from 1 to 20, in some cases from 5 to 15 in other cases from about 8 to 12 hours, usually about 10 hours. The resulting mixed oxide catalyst is a friable solid typically insoluble in water. Typically, the calcined product has a bulk density of 1.20 to 1.53 g/cm3. This bulk density is based on the amount of 1.5 ml of pressed and crushed catalyst that it weighs.
    [061] The resulting oxidative dehydrogenation catalyst is heterogeneous. It has an amorphous component and a crystalline component. The elemental analysis of the catalyst can be determined by any suitable technique. One useful technique is particle-induced X-ray emission (PIXE) analysis. From a PIXE analysis of the catalyst precursor before treatment and after treatment with H2O2, it is determined that the empirical molar ratio of Mo to V typically decreases from 1:0.33 to 1:0.40 to 1:0 .22 to 1: 0.33, in some cases from 1.0: 0.22 to 1.0: 0.25 compared to a calcined material that has not been treated with hydrogen peroxide. Furthermore, it has been found that the Mo:Te molar ratio is narrow and increased (over the base catalyst) from a range typically from 1:0.03 to 1:0.13 to more than 1:0.10 and less than 1:0.16, in some cases from 1.0:0.11 to 1:0 to 0.15 compared to a calcined oxidative dehydrogenation catalyst that has not been so treated.
    [062] The catalyst has one or more crystalline components and an amorphous component. The crystalline component can be analyzed using X-ray diffraction (XRD). There are several vendors of X-ray diffractometers, including Rigaku Shimadzu, Olympus and Bruker. A powder sample is irradiated with X-rays. The X-rays emitted from the sample pass through a diffraction grating and are collected in a goniometer (recorder). The results are usually analyzed using a computer program (usually provided by the instrument supplier) and compared to a database (International Diffraction Data Center ICDD) using a computer to determine the composition of the crystalline phases.
    [063]The 2θ X-ray diffraction pattern has a 2θ peak height ratio of 0 to 20° to the maximum peak height of less than 15%, in some cases less than 10%.
    [064]The crystalline phase of the catalyst is also heterogeneous. X-ray diffraction results can be analyzed by computer programs to identify the various likely crystalline species and their relative amounts compared to structures in a database (eg, deconvolutions).
    [065] The crystalline phase typically includes the following crystalline species:

    [066]The X-ray diffraction analysis of the precursor and the calcined catalyst show treatment results in a change in the composition of the crystalline phase. The treatment according to the present invention increases the phase of the crystalline component with the empirical formula (TeO) 0.39 (Mo3.52V1.06Nb0.42) to not less than 75% by weight, in some cases not less than that 85% by weight, in some cases not less than 90% by weight %, in some cases not less than 95% by weight of the crystalline phase.
    [067] In some embodiments, the crystalline component phase with the empirical formula TeO0.71 (Mo0.73V0.2Nb0.07) 3O9 is present in an amount of about 2.4 to 12% by weight, in some embodiments, the phase is present in amounts less than about 8% by weight, in other embodiments less than 3.5% by weight. The calcined catalyst product is a typically water-insoluble dry friable product. If necessary, the catalyst can be subjected to a sizing step, such as milling, to produce a desired particle size. Depending on how the catalyst is used, the particle size can be different. For example, for spray drying with a support, the particle size can range from about 5 to 75 µm, in some cases from 10 to 60 µm. For use in a bed in unsupported form, the particles may have a size of about 0.1 to 0.5 mm in some cases 0.2 to 0.4 mm.
    [068] In the present invention, the feed to the oxidative dehydrogenation reactor includes oxygen in an amount below the upper limit of explosive capacity/ability to become flammable. For example for the oxidative dehydrogenation with ethane, typically oxygen will be present in an amount of not less than about 16% by mol, preferably about 18% by mol, for example from about 22 to 27% by mol, or to 26% by mol. It is desirable not to have a large excess of oxygen as this can reduce selectivity arising from combustion of feed or end products. Furthermore, large excess oxygen in the feed stream may require additional separation steps at the downstream end of the reaction.
    [069] To maintain a viable fluidized or moving bed, the mass gas flow rate through the bed should be above the minimum flow required for fluidization, and preferably from about 1.5 to about 10 times Umf e more preferably from about 2 to about 6 times Umf. A faith used in accepted form as an abbreviation for the minimum mass gas flow necessary to achieve fluidization, C.Y. Wen and Y.H.Yu, "Mechanics of Fluidization", Chemical Engineering Progress Symposium Series, Vol. 62, p. 100-111 (1966). Typically, the required surface gas velocity ranges from 0.3 to 5 m/s.
    [070]The reactor can also be a fixed bed reactor.
    [071] The oxidative dehydrogenation process comprises the passage of a mixed feed of ethane and oxygen at a temperature lower than 420 °C in some cases lower than 410 °C, in some cases lower than 400 °C, in some cases less than 390 °C, in some instances less than 380 °C, in some cases as low as 375 °C, at an hourly space velocity of gas not less than 500 h-1, typically not less than 1000 h-1, desirably not less than 2800 h-1, preferably at least 3000 h-1 through one or more beds and a pressure of 0.8 to 1.2 atmosphere comprising passing said mixture over the oxidative dehydrogenation catalyst . In some embodiments, the oxidative dehydrogenation reactor operates at temperatures below 400 °C typically from 375 °C to 400 °C.
    [072] The reactor outlet pressure can be 105 kPa (15 psi) up to 172.3 kPa (25 psi) and the inlet pressure is increased by the pressure drop across the bed which depends on a number of factors including reactor configuration, bed particle size and space velocity. Generally, the pressure drop can be below 689 kPa (100 psi) preferably less than 206.7 kPa (30 psi).
    [073] The residence time of one or more alkanes in the oxidative dehydrogenation reactor is 0.002 to 20 seconds. The Support/Binder
    [074]If necessary, there are several ways in which the oxidative dehydrogenation catalyst can be supported or bound.
    [075] Preferred components for the formation of ceramic supports and for binders include titanium, zirconium, aluminum, magnesium, silicon oxides, phosphates, boron phosphate, zirconium phosphate and their mixtures, both for fluidized bed and fixed bed reactors. In the fluidized bed typically the catalyst is generally spray dried with the binder, typically forming spherical particles ranging in size (effective diameter) from 40 to 100 µm. However, care must be taken to ensure that the particle area is robust enough to minimize friction in the fluid bed.
    [076] The catalyst support for the fixed bed can also be a ceramic precursor formed from oxides, dioxides, nitrides, carbides selected from the group consisting of silicon dioxide, molten silicon dioxide, aluminum oxide, aluminum dioxide titanium, zirconium dioxide, thorium dioxide, lanthanum oxide, magnesium oxide, calcium oxide, barium oxide, tin oxide, cerium dioxide, zinc oxide, boron oxide, boron nitride, boron carbide, yttrium oxide, aluminum silicate, silicon nitride, silicon carbide and mixtures thereof.
    [077] In one modality, the support for the fixed bed may have a low surface area less than 20 m2/g, alternatively less than 15 m2/g, in some cases less than 3.0 m2/g for the oxidative dehydrogenation catalyst. This support can be prepared by compression molding. At higher pressures, the interstices within the ceramic precursor are in compressed collapse. Depending on the pressure exerted on the support precursor, the surface area of the support can be about 20 to 10 m 2 /g.
    [078]Low surface area support can be of any conventional shape such as balls, rings, saddle, etc.
    [079]It is important that the support is dried before use (ie before adding the catalyst). Generally, the support can be heated to a temperature of at least 200 °C for up to 24 hours, typically at a temperature of 500 °C to 800 °C for about 2 to 20 hours, preferably 4 to 10 hours) . The resulting support will be free of adsorbed water and should have a surface hydroxyl content of about 0.1 to 5 mmol/g of support, preferably 0.5 to 3 mmol/g.
    [080] The amount of hydroxyl groups on silica can be determined according to the method disclosed by J.B. Peri and A.L. Hensley, Jr., in J. Phys. Chem., 72(8), 2926, 1968, the entire contents of which are incorporated herein by reference.
    [081] The dry support for a fixed bed catalyst can be compressed into the required shape by compression molding. Depending on the particle size of the support, it can be combined with an inert binder to maintain the shape of the compressed part. Loads
    [082] Typically, loading catalyst on the support for a fixed bed catalyst provides from 1 to 30% by weight, typically from 5 to 20% by weight, preferably from 8 to 15% by weight of said catalyst and of 99 to 70% by weight, typically from 80 to 95% by weight, preferably from 85 to 92% by weight, respectively, of said support.
    [083]Catalyst can be added to the support in several ways. For example, the catalyst can be deposited from an aqueous slurry onto one of the low surface area support surfaces by impregnation, washing, brushing or spraying. The catalyst can also be concomitantly precipitated from a slurry with the ceramic precursor (eg, alumina) to form the low surface area supported catalyst.
    [084] Catalyst loading for the fluidized bed can be chosen based on a number of factors, including bed volume, alkane flow rate through the bed, bed energy balance, binder type, etc. For fluidized bed catalyst loading it can cover a wide range of values ranging from 10% by weight to 90% by weight, typically above 20% by weight desirable above 35% by weight.
    [085] The process must be operated to have a conversion of ethane to ethylene of at least 90%, in some cases 95%, desirably greater than 98% and a selectivity for ethylene not less than 95%, in some cases greater than 97%. Oxidative Dehydrogenation Processes
    [086] The catalyst of the present invention can be used with an exothermic fluidized bed or a fixed bed reaction. The fixed bed reactor is a tube reactor and, in a further embodiment, the fixed bed reactor comprises multiple tubes within a shell (eg a shell or tube heat exchanger type construction). In another embodiment, the fixed bed reactor may comprise a number of shells in series and/or in parallel. The reactions may involve one or more dehydrogenation steps including oxidative dehydrogenation and hydrogen transfer steps including the oxidative coupling of a hydrocarbon.
    [087] Typically, these reactions are conducted at temperatures from about 375°C to about 410°C, at pressures from about 100 to 21,000 kPa (15 to 3000 psi), preferably at an outlet pressure from 105 kPa (15 psi) to 172.3 kPa (25 psi) in the presence of an oxidative dehydrogenation catalyst. The hydrocarbon stream can contain a range of compounds including C2-4 aliphatic hydrocarbons.
    [088] In some embodiments, reactions include the oxidative coupling of aliphatic hydrocarbons, typically C1-4 aliphatic hydrocarbons particularly methane (eg when the ethane stream contains some methane) and the oxidative dehydrogenation of C2-4 aliphatic hydrocarbons. Such reactions can be conducted using a mixed hydrocarbon feed, in some embodiments, methane or ethane or both and oxygen in a volumetric ratio between 70:30 to 95:5 at a temperature less than 420 °C, preferably less than 400 °C at an hourly space velocity of the gas not less than 280 h-1, in some modes not less than 500 h-1, typically not less than 1000 h-1, desirable not less than 2800 h-1 , preferably at least 3000 h-1, and a pressure of 0.8 to 1.2 atmosphere. Typically, the process may have an overall conversion of about 50 to about 100%, typically about 75 to 98%, and a selectivity for ethylene not less than 90%, in some cases not less than 95%, in additional modalities not less than 98%. In some cases, the upper temperature control limit is less than about 400 °C, in some modalities less than 385 °C.
    [089] The resulting product stream is treated to separate the ethylene from the rest of the product stream which may also contain concomitant products such as acetic acid and unreacted feed which is recycled back to the reactor. Separation
    [090] The product stream from the reactor must have a relatively low ethane content less than 20% by weight in some cases less than 15% by weight, in some cases less than 10%. Furthermore, the product stream should have a low content of products such as water, carbon dioxide and carbon monoxide, generally cumulatively in a range of less than 5, preferably less than 3% by weight.
    [091]Power and products may need to be separated from the product stream. Some processes may use so-called diluted ethylene streams. For example, if the product stream does not contain much ethane, eg less than about 15% by volume, the stream can be used directly without further purification in a polymerization reactor, such as a gas phase process, of mud or in solution.
    [092] The most common technique would be to use a cryogenic C2 splitter.
    [093] Other known ethylene/ethane separation techniques may also be used including adsorption (oil, ionic liquids and zeolites).
    [094] The present invention will now be illustrated by the following non-limiting examples.
    [095] In the examples, the fixed bed reactor unit used for the oxidative dehydrogenation reaction is schematically shown in Figure 1. The reactor was a fixed bed stainless steel tube reactor having an outer diameter of 2 mm (% " ) and a length of 117 cm (46 inches) The reactor is in an electric furnace sealed with ceramic insulating material There are 7 thermocouples in the reactor indicated in numbers 1 to 7. The thermocouples are used to monitor the temperature in that zone of the reactor. Thermocouples 3 and 4 are also used to control the heating of the reactor bed. Feed flows from the top to the bottom of the reactor. At the inlet there is a ceramic cup 8 to prevent air currents in the reactor. Below the ceramic cup is a layer of quartz wool 9. Below the layer of quartz wool is a layer of catalytically inert quartz powder. Below the quartz powder is the fixed bed 10 which comprises the catalyst. Below the fixed bed is a layer of powder of quartz quartz 11, a layer of quartz wool 12 and a ceramic cup 13. At the bed outlet was a gas analyzer to determine the composition of the product stream. GHSV was 2685 h-1 and pressure was ambient pressure.
    [096]For the examples, the bed temperature was taken as an average of the temperatures of thermocouples 2, 3 and 4. The feed current was assumed to have the same temperature as the bed. The Nature of the Problem baseline experiences
    [097] Two different catalysts were prepared in the baseline in geographically separated laboratories.
    [098]The laboratory used a reactor coated with TEFLON® for the hydrothermal treatment that had on its surface crystals of the effective catalyst previously prepared.
    [099] The formation of the pre-catalyst in the glassware procedure was as follows:
    [0100] (NH4) 6Mo6TeO24.xH2O (6.4069 g) was added to 20 mL of distilled water in a 100 mL glass beaker and stirred in a warm water bath (80°C). VOSO4 x H2O (3.6505 g) was dissolved in 10 mL of distilled water in a 50 mL beaker at room temperature. The VOSO4 solution was poured into the (NH4) 6Mo6TeO24 solution and a brown solution resulted immediately (Solution 1).
    [0101]H3[NbO(C2O4) 3] 7.5 H2O (2.3318 g) was dissolved in 10 mL of warm water and added under an air atmosphere to Solution 1. A dark brown-gray slurry formed, which formed was stirred for 10 minutes under an air atmosphere. hydrothermal treatment
    [0102] The slurry samples were then heated in an autoclave with a TEFLON liner seeded with previously produced catalyst under an inert atmosphere at a temperature of 150 °C to 190 °C for not less than 10 hours. The slurry was filtered, washed with deionized water and dried for a period of 4 to 10 hours at a temperature of 70 to 100°C.
    [0103]Baseline catalyst sub-samples were immediately calcined.
    [0104]Two samples were prepared in this way.
    [0105] One sample (A) had a 25% conversion of ethane to ethylene at about 370 °C and a selectivity at this temperature of 98%.
    [0106]The second sample (B) had a 25% conversion of ethane to ethylene at about 354 °C and a selectivity at this temperature of 99%.
    [0107] This occurs even with catalyst seeds in hydrothermal treatment where there is variability. (This could be due to differences in seed crystals).
    [0108]Three samples of precatalyst A and four subsamples of precatalyst B were treated with varying amounts of H2O2 and then calcined and then used to oxidatively dehydrogenate a mixture of 78% ethane and 22% oxygen at a 600 cm3/h flow rate.
    [0109]The results are shown in Table 1 below. TABLE 1

    [0110] The treatment of a catalyst having a conversion of 25% at temperatures below 420 °C and a high selectivity with 30% hydrogen peroxide in amounts of 0.3 to 2.8 mL per gram of catalyst does not cause a measurable performance loss. Second Laboratory Pre-catalyst Preparation
    [0111] (NH4) 6Mo6TeO24.xH2O (6.4 g) was dissolved in 20 mL of water in a 100 mL round bottom flask with the help of a warm water bath. The clear solution was cooled to room temperature. VOSO4 x3.47 H2O (3.4 g) was dissolved in 10 mL of water in a 30 mL beaker (still with the help of a warm bath). The blue solution formed was cooled to room temperature. The VOSO4 solution was poured into the (NH4) 6Mo6TeO24 solution. The beaker was rinsed with water (2 x 0.5 mL) and the rinse solution was added to the flask. A brown solution formed was bubbled with nitrogen and stirred for 10 minutes. An aqueous solution of H3[NbO(C2O4)3] (0.3431 mmol/g solution, 13.29 g, 4.56 mmol Nb) was added slowly to the brown solution above with a pipette (in ~ 2.5 minutes). A red stone colored slurry formed which was stirred with N2 bubbling for about 10 minutes. Hydrothermal treatment in an unseeded TEFLON coated reactor
    [0112] The slurry was transferred to a 60 ml autoclave with a clear TEFLON liner, which was degassed and recharged with N2 (ambient pressure). The autoclave was heated with a heating sleeve with the contents magnetically stirred (300 rpm). The mixture was heated to 175 °C internal temperature for 48 hours. The autoclave was cooled to room temperature and the contents were filtered and washed with 500 ml of water. The cake was dried at 90°C overnight, ground and sieved through a 250 micron sieve. The purple solid was calcined at 600°C (O2 level in the nitrogen stream: 0.4 ppm). This catalyst appeared brown in color after calcination.
    [0113]The catalyst was tested as above.
    [0114]The ODH reaction was carried out at temperatures up to 420 °C to avoid the autoignition temperature of the feed gas. Conversion was low and the graph of conversion as a function of temperature had to be linearly extrapolated to get a rough estimate of the temperature at which there was 25% conversion. The estimated temperature at which there was 25% conversion was 635 °C. This would not be commercially viable as it is significantly above the autoignition temperature of a feed gas comprising 82% ethane and 18% oxygen. Seeded TEFLON coated reactor
    [0115] In the second laboratory, the procatalyst was prepared using the following general procedure.
    [0116]The procedure to prepare the catalyst was as follows.
    [0117] A paste prepared as above was poured into a 300 ml autoclave with a TEFLON coating. The reactor was dedicated and unwashed between hydrothermal treatments and it showed residual catalyst crystals made during previous use. The autoclave was closed. The headspace was oxygen purged with N2 (20 psi). After purging, the valve was closed and the autoclave was placed in an oven at 23 °C. The temperature was raised to 175°C and kept without stirring at this temperature for 50 hours. The autoclave was removed from the oven and cooled to room temperature. Autoclave pressure was released through a water bubbler. The autoclave was open. The solid was filtered, rinsed with 500 ml of water and dried at 80°C overnight. The brown solid (6.19 g) was loaded onto a quartz boat and calcined under a slow stream (30 mL/min) of purified nitrogen (RT at 600 °C, 4 hours, 600 °C held for 2 hours) . The solid obtained was a black powder, which was crushed and sieved through a 250 micron sieve (5.94 g). The resulting solid was loose (fluffy).
    [0118]The catalyst was tested in the ODH reactor using the above conditions.
    [0119]Of the experiments, the temperature at which there was 25% conversion into ethylene ranged from 370 °C to 383 °C and a selectivity at these temperatures was greater than 90%. This is quite tight considering the heterogeneous nature of the catalyst and the complexity of the crystalline phases and consistently below the auto-ignition temperature of the feed.
    [0120]The nature of the nucleation sites was unclear. It is believed that if the sites comprise a catalyst with a 25% conversion below 400°C and the selectivity for ethylene at this temperature above 95%, the resulting catalyst has a greater likelihood that the resulting catalyst has these properties.
    [0121] A quantity of catalyst samples prepared as above in a seeded TEFLON coated hydrothermal reactor was subjected to XRD analysis as described in the examples below to determine the crystalline phases in the catalyst. The results are shown in the table below.

    [0122] This shows that even if the reactor wall (coated with TEFLON or steel) in the hydrothermal reactor is seeded with catalyst, there can be significant variability in the final catalyst.
    [0123] Calcined catalyst samples obtained from a seeded reactor have the following empirical formula determined by PIXE:
    where d is a number to satisfy the valence of the oxide The samples had a conversion of 25% at a temperature of 372 °C to 383 °C and a selectivity for ethylene at these temperatures of 93 to 96%. In the Second Laboratory
    [0124]A series of catalysts were prepared in a clean glass reactor and subjected to hydrothermal treatment in a stainless steel reactor without TEFLON coating and without any seeding of catalyst. General Reaction Step:
    [0125] (NH4) 6Mo6TeO24.xH2O (19.2086 g, 15.15 mmol, 1.00 molar equivalents) was dissolved in 60 mL of distilled water in a 500 mL round bottom flask with the aid of a water-bath. warm mary. The resulting clear and colorless solution was allowed to cool to room temperature. VOSO4 x 3.47 H2O (10.2185 g, 62.59 mmol, 4.13 molar equivalents) was dissolved in 25 mL of distilled water in a 30 mL beaker with the help of a warm water bath. The light blue solution formed was cooled to room temperature.
    [0126]The VOSO4 solution was poured into the (NH4) 6Mo6TeO24 solution and a brown solution resulted immediately. The beaker containing the VOSO4 solution was rinsed with two 1 ml aliquots of water and these rinses were added to the vial. The resulting brown solution was stirred under the addition of bubbling nitrogen for 15 minutes. H3[NbO(C2O4)3] (0.3420 mmol(Nb) /g(solution), 39.9737 g(solution), 13.68 mmol(Nb), 0.903 molar equivalents) was added slowly (dropwise over seven minutes) under N2 bubbling into the brown solution through a pipette. An opaque purple colored slurry formed, which was stirred with N2 bubbling for 10 minutes. General hydrothermal treatment step
    [0127] The slurry was poured into a 600 mL steel autoclave that contained a TEFLON stir bar. The autoclave was closed and the atmosphere inside the autoclave was evacuated (vacuum) and filled with N2 (30 psi from the bulk nitrogen line) 10 times, followed by 10 additional repetitions of purging with N2 (30 psi from the line). of nitrogen in bulk) and releasing N2 pressure (positive pressure relief) to a water bubbler. The autoclave was left under ambient pressure of N2 atmosphere and the container was sealed using a needle valve in the head of the autoclave.
    [0128]The autoclave was placed in a heating blanket installation, where the heat is controlled by the heat controller through thermocouples inside and outside the autoclave. The heating blanket and autoclave are wrapped in thermal insulating ceramic fiber tape to ensure proper insulation. The temperature was raised to 173°C over a period of one hour and the reaction was allowed to proceed, with the addition of stirring, at this temperature for 48 hours.
    [0129]The autoclave was then cooled to room temperature slowly without agitation. Once cooled, excess pressure accumulated during the reaction process inside the autoclave was released through a water bubbler and the autoclave was opened. The solid (deep violet color) was filtered, rinsed with approximately 300 mL of distilled water (vibrant blue color of the filtrate) and dried in an oven at 90 °C overnight. General Calcination Step
    [0130]The dry catalyst solids were wetted using a mortar/pest and sieved through a 250 micron porosity filter. The dark purple solid of particle size less than 0.25 microns was loaded into a quartz boat and the boat was placed in the glass furnace tube that is used for calcining. To ensure the exclusion of air during calcination, the plant was purged under nitrogen. Calcination proceeded under a slow stream (30 mL/min) of purified nitrogen (ventilation through a water bubbler) under the following conditions: RT to 600 °C in 4 hours and held at 600 °C for 2 hours. The solid obtained was a black powder, which was ground and sieved through a 250 micron sieve, resulting in a powder that was loose and fluffy.
    [0131]Catalysts were tested as above. The temperature at which there was 25% conversion (measured or linearly extrapolated) ranged from 380 to 504 °C. This was wide spread at 25% conversion temperature as there was no obvious difference between the preparations. Of the five samples, two had a conversion temperature of 25% below 400 °C, which was considered a "reasonable" ceiling temperature for a large-scale commercial ODH reactor.
    [0132] These examples further illustrate the variability in the manufacture of catalysts with a conversion of 25% below 400 °C absent seed catalysts with the desired properties (temperature at which there is 25% conversion below 400 °C and a selectivity for ethylene at this temperature greater than 90%).
    [0133] In the literature this is known (Catalysis Communications 2005, 6, 215-220; Catalysis Communications 2012, 21, 22-26; Journal of Catalysis 2012, 285, 48 - 60) to treat ODH catalyst after calcination with peroxide hydrogen to improve performance.
    [0134] In the second laboratory, a sample of the catalyst prepared as the above catalyst was calcined at 600 °C for 2 to 4 hours. The calcined sample was then treated with about 12 to 16 mL of 30% w/w aqueous H 2 O 2 solution per gram of catalyst. The reaction was inconsistent in that there was no indication of a reaction (eg no heat or bubbling) or the incubation period to start the reaction was extremely unpredictable (eg 20 minutes to 3 hours) and when the reaction started it was extremely fast (in seconds) and violent (potentially explosive).
    [0135] The addition of H2O2 after calcining the catalyst is not a commercially viable route for catalyst preparation due to the above-described complication and safety implications the invention first laboratory
    [0136] In the first laboratory the portions of the baseline catalyst precursor prepared with a seeded TEFLON coating were treated with up to 5.6 ml of 30% w/w aqueous H2O2 solution per gram of precursor prior to calcining. Precursor treatment resulted in an immediate, controlled and observable reaction (bubbling and gentle heating that never exceeded about 60 °C). The treated precursor was then calcined in the normal manner.
    [0137]The catalysts were then tested in the ODH reactor.
    [0138]The treatment causes a small variation in selectivity (between 99% and 98%) up to the amount of peroxide 3.5 cm3, and only the use of a greater excess of H2O2 (5.6 cm3) causes a loss of selectivity measurable.
    [0139] Figure 2 is a graph of the temperature at which there is a 25% conversion of ethane to ethylene versus the 30% volume of H2O2 for 1.41 g of a catalyst with a temperature at which there is a 25% conversion lower than at 240 °C and a selectivity for ethylene higher than 95% prepared in the first laboratory.
    [0140] Figure 3 is a graph of the selectivity for the conversion to ethylene at the temperature where there is a 25% conversion to ethylene versus the 30% volume of H2O2 for 1.41 g of catalyst with a temperature where there is a conversion 25% lower than at 240 °C and a selectivity for ethylene higher than 95% prepared in the first laboratory.
    [0141] These graphs show the volumes of 30% H2O2 per 1.4 g of catalyst where the catalyst has a temperature at which there is a 25% lower conversion than at 240 °C and a higher ethylene selectivity than that 95% is relatively uncompromising up to about 5.6 mL of 30% H2O2 per 1.4 g of catalyst (i.e., 0.30 to 2.8 mL of H2O2 of a 30% solution per gram of catalyst ). In the Second Laboratory
    [0142] Portions of baseline catalyst precursor prepared as above and treated in a stainless reactor without a TEFLON coating and without seeding were treated with up to 0.35 to 1.42 mL of aqueous H2O2 solution at 30 % w/w per gram of precursor before calcination. Precursor treatment resulted in an immediate, controlled and observable reaction (bubbling and gentle heating that never exceeded about 60 °C).
    [0143] A series of PIXE characterizations of the baseline catalyst and catalyst treated according to the present invention from laboratory two were obtained.
    [0144] The typical untreated baseline catalyst had a PIXE characterization set forth below:

    [0145]In the baseline catalysts treated in an uncoated hydrothermal reactor, small amounts of iron and chromium were detected. Iron ranged from a minimum of 0.0026 to a maximum of 0.0416 mols/per mol of Mo. Chromium ranges from 0.000 to 0.0065 moles per mole of Mo.
    [0146]For the catalyst treated according to the present invention before calcination, the PIXIE analysis was (Mo1.00V0.28-0.29Te0.13Nb0.15-0.16Fe0.008) O8.17.
    [0147] It is believed that these amounts of iron and chromium in the aforementioned scaffold catalyst do not contribute to the oxidative dehydrogenation characteristics of the catalyst.
    [0148]Hydrogen peroxide treatment of a catalyst with a temperature at which there is a conversion 25% lower than 420 °C and a selectivity for ethylene higher than 95% prepared in laboratory 2. Sample 1 A:
    [0149] A catalyst precursor was prepared in the above manner and treated in a stainless steel hydrothermal reactor without a TEFLON coating and without seeding with a catalyst at a temperature where there is a 25% conversion of less than 240 °C and an ethylene selectivity of more than 95% was treated with hydrogen peroxide.
    [0150] 5,4672 g of crude purple catalyst precursor were used for the treatment with hydrogen peroxide. The catalyst precursor was added to a 400 mL beaker containing a stir bar and 20 mL of distilled water was added to create a dark paste. The slurry was stirred by stirring and 4 mL of H2O2 (30% w/w in H2O, ratio 1.41 gODH: 1 mL of H2O2) was added in one go, resulting in vigorous bubbles and heat. The reaction was self-heated and bubbled and changed from dark purple mud to black mud. The reaction was stirred and allowed to proceed for 5 minutes before processing. The solid was filtered, rinsed with approximately 100 mL of water and dried in an oven at 90 °C overnight to produce 4.4296 g of gray precursor for the calcination step. The sample was calcined as above. Sample 1 C:
    [0151]5.5679 g of crude purple catalyst precursor was treated in the same manner as Example 1A, except that the reaction was allowed to proceed for 2 hours before processing. A small bubbling was observed to have arisen from the reaction even after a reaction time of 2 hours. The solid was filtered (color of the filtrate was yellow), rinsed with approximately 100 mL of water and dried in an oven at 90 °C overnight to produce 4.6231 g of vibrant purple precursor for the calcination step. The resulting sample was calcined as above. Sample 1B
    [0152]A sample of the precursor prepared in a glass vial as above was not treated and calcined as above.
    [0153]The samples were then used in the oxidative dehydrogenation of ethylene.
    [0154]The results of the oxidative dehydrogenation test are shown in the table below.

    [0155]The treatment of a precursor to a catalyst having a temperature at which there is a 25% conversion of less than 420 °C and a selectivity to ethylene of more than 95% with 1 mL of 30% H2O2 per 1.4 g of catalyst precursor does not negatively affect the catalyst.
    [0156]The samples were then subjected to XRD analysis using a Rigaku Ultima X-ray diffractometer; 285 mm theta/theta radius goniometer; high speed D/teX-ULTRA detector; and ASC-48 automatic sample changer. The software used was the Rigaku "Standard Measurement" data acquisition application; MDI Jade 2010 analysis software version 2.6.6 2014; and the comparative database was ICDD PDF-4 + 2014 (with 354,264 inorganic data patterns).

    [0157]The table suggests that it is desirable to increase the phase content (TeO) 0.39(Mo3.52V1.062Nb) 0.42) O14 and reduce the phase content of (TeO) 0.71(Mo0.73V0. 2Nb) 0.07) 3O9.
    [0158]Another catalyst sample with a temperature where there is a 25% conversion of less than 420 °C and a selectivity to ethylene of more than 95% was tested. Example 2A
    [0159]7.0552 g of crude purple catalyst precursor was treated in the same manner as Example 1A, except that the reaction was allowed to proceed for 20 minutes before processing. The solid was filtered, rinsed with approximately 100 mL of water and dried in an oven at 90 °C overnight to yield 5.8907 g of black precursor for the calcination step. Example 2B
    [0160]Baseline catalyst has not been treated.
    [0161]The results of the oxidative dehydrogenation test are shown in the table below.

    [0162]The treatment of a precursor to a catalyst having a temperature at which there is a 25% conversion of less than 420 °C and a selectivity to ethylene of more than 95% with 1 mL of 30% H2O2 per 1.4 g of catalyst precursor does not negatively affect the catalyst. The samples were then subjected to XRD analysis as above.

    [0163]The treatment with H2O2 increases the relative proportion of the phase with the structure (TeO) 0.39(Mo3.52V1.062Nb) 0.42) O14 and improves the performance of the catalyst.
    [0164]Examples of treating a catalyst that does not have a temperature where there is a 25% conversion of less than 420 °C and a selectivity to ethylene of more than 95% with H2O2. The Baseline 3B
    [0165]A sample of catalyst precursor that was calcined without H2O2 treatment was tested in the oxidative dehydrogenation reactor. This was the catalyst above which had an estimated temperature for a 25% conversion of 504 °C. 3A
    [0166]5.9354 g of the crude purple catalyst precursor for the untreated sample was treated with hydrogen peroxide. The catalyst precursor was added to a 250 mL round bottom flask containing a stir bar and 20 mL of distilled water was added to create a dark slurry. The slurry was stirred by stirring and 8.5 mL of H2O2 (30% w/w in H2O, ratio 0.705 gODH: 1 mL of H2O2) was added at once, resulting in vigorous bubbles and heat. The reaction was self-heated and bubbled and changed from dark purple mud to black mud. The reaction was stirred for 2 hours before processing. The dark purple solid was filtered, rinsed with approximately 100 mL of water and dried in an oven at 90 °C overnight to yield 3.7494 g of gray solid for the calcination step. 3C
    [0167]4.9755 g of the crude purple catalyst precursor was treated as 3A above, except that 1.75 mL of H2O2 (30% w/w in H2O, ratio 2.82 gODH: 1 mL of H2O2) was added once and less bubbling and heat resulted. The reaction mud remained dark purple. The reaction was stirred for 2 hours before processing. The dark purple solid was filtered, rinsed with approximately 100 mL of water and dried in an oven at 90 °C overnight to yield 3.8326 g of gray solid for the calcination step.
    [0168]The samples were then tested in the oxidative dehydrogenation reactor. The results are shown in the Table below.


    [0169] The treatment of a precursor to a catalyst with a temperature at which there is a 25% conversion of more than 420 °C and a selectivity to ethylene of less than 95% with 1 mL of 30% H2O2 per 0.7 to 2.8 g of catalyst precursor significantly improves the catalyst.
    [0170]The samples were then subjected to XRD analysis as above.

    [0171]The data suggest that increasing the phase content of (TeO) 0.39(Mo3.52V1.062Nb) 0.42) O14 significantly increases the activity and selectivity of the catalyst. Example 4 Treatment of mother liquor with H2O2 without filtration
    [0172] A precursor sample was prepared as above. One portion was used as a baseline reference (no H2O2 treatment). Then 4.96 g of crude purple catalyst precursor and aqueous mother liquor (~500 mL) from the hydrothermal treatment were added to a 250 mL round bottom flask containing a stir bar to create a dark slurry. The dark mud was kept under a nitrogen atmosphere. The slurry was stirred by stirring and 3.6 mL of H2O2 (30% w/w in H2O, ratio 1.39 gODH: 1 mL of H2O2) was added in one go and no vigorous bubbling and heat resulted. The reaction changed from dark purple mud to black mud. The reaction was stirred for 3 hours before processing. The dark purple solid was filtered, rinsed with approximately 200 mL of water and dried in an oven at 90 °C overnight to yield 3.3720 g of gray solid for the calcination step.
    [0173]The catalysts were then tested for activity in the oxidative dehydrogenation reactor. The results are shown in the Table below.

    [0174]Treatment of a precursor with 1 mL of H2O2 (30% by weight) per 1.4 g of precursor before separation from the reactor before drying improves the activity of the calcined dehydrogenation catalyst. Example 5 100 g sample
    [0175] A number of catalyst samples (approximately 40, 40 and 20 g) were combined in a 5 L round bottom flask and 400 mL of distilled water was added to create a purple slurry. A 100 mL dropper funnel was attached to the flask and 39 mL of H2O2 (30% w/w, ~2.82 gODH/1 mL H2O2) was added slowly over 16 minutes dropwise to the stirring slurry. The mud changed from dark purple to black. The solids were filtered, rinsed with DI water and dried at 90°C in an oven overnight. The solids were then crushed with a mortar and pestle and captured through a 250 micron porosity filter to collect 101.7 g of a loose, fluffy powder for calcination.
    [0176]All the powder was loaded into a quartz tube, which acted like the boat, with some space above to allow the gas to flow. The quartz tube boat was placed inside a larger quartz tube and placed in a calcining unit. The calcining unit was completely purged under nitrogen, both bulk and purified to ensure a sufficiently anaerobic environment for calcination. Purified nitrogen flowed over the sample at 150 standard cubic centimeters per minute. The sample was heated from room temperature to 600 °C in 4 hours and held at 600 °C for 4 hours and cooled to room temperature in 4 hours.
    [0177] A small sample of approximately 2 g of the resulting 100 g catalyst was screened in the oxidative dehydrogenation reactor as described above and this had 25% conversion at 376.5 °C and the selectivity for ethylene in this conversion of 97% . INDUSTRIAL APPLICABILITY
    [0178] The invention provides an oxidative dehydrogenation catalyst for the production of alkenes with an improved activity.
    权利要求:
    Claims (20)
    [0001]
    1. Method to improve consistency of an oxidative dehydrogenation catalyst of the empirical formula (measured by PIXE):
    [0002]
    2. Method according to claim 1, CHARACTERIZED by the fact that the precursor is prepared by a method comprising: i) forming an aqueous solution of ammonium heptamolybdate (tetrahydrate) and telluric acid at a temperature of 30 °C to 85 °C and adjust the pH of the solution to 6.5 to 8.5 with a nitrogen-containing base to form soluble salts of the metals; ii) preparing an aqueous solution of vanadyl sulphate at a temperature from room temperature to 80°C; iii) mixing the solutions from steps i) and ii) together; iv) slowly adding a solution of niobium monoxide oxalate (NbO(C2O4H)3) to the solution from step iii) to form a slurry; and v) heating the resulting slurry in an autoclave under an inert atmosphere at a temperature of 150 °C to 190 °C for not less than 10 hours.
    [0003]
    3. Method according to claim 2, CHARACTERIZED by the fact that the solid resulting from step v) is filtered and washed with deionized water and the washed solid is dried for a period of 4 to 10 hours at a temperature of 70 °C at 100°C.
    [0004]
    4. Method according to claim 3, CHARACTERIZED in that it further comprises calcining the catalyst in an inert atmosphere at a temperature of 200 °C to 600 °C for a time period of 1 to 20 hours.
    [0005]
    5. Method according to claim 4, CHARACTERIZED by the fact that the precursor is treated with the equivalent of 0.30 to 2.8 mL of a 30% w/w aqueous solution of H2O2 per gram of catalyst precursor for a time period of 5 minutes to 10 hours at a temperature of 20°C to 80°C.
    [0006]
    6. Method according to claim 5, CHARACTERIZED by the fact that in the calcined catalyst, the molar ratio of Mo:V is from 1:0.22 to 1:0.29.
    [0007]
    7. Method, according to claim 6, CHARACTERIZED by the fact that in the calcined catalyst, the molar ratio of Mo:Te is greater than 1:0.11 and less than 1:0.15.
    [0008]
    8. Method according to claim 7, CHARACTERIZED by the fact that the calcined catalyst has a bulk density of 1.20 to 1.53 g/cm3.
    [0009]
    9. Method according to claim 8, CHARACTERIZED by the fact that in the crystalline phase of the catalyst the amount of the phase having the formula (TeO) 0.39(Mo3.52V1.06Nb0.42)O14 is above 75% in crystalline phase weight measured as determined by XRD.
    [0010]
    10. Method according to claim 9, CHARACTERIZED by the fact that in the crystalline phase of the catalyst the amount of the phase having the formula (TeO) 0.39 (Mo3.52V1.06Nb0.42)O14 is above 85% in crystalline phase weight measured as determined by XRD.
    [0011]
    11. Method for the oxidative dehydrogenation of a mixed feed of ethane and oxygen in a volume ratio of 70:30 to 95:5 at a temperature less than 400 °C at an hourly gas space velocity of not less than 500 h-1 and a pressure of 0.8 to 1.2 atmosphere, CHARACTERIZED by the fact that it comprises the passage of the mixed feed over a calcined oxidative dehydrogenation catalyst of the empirical formula (measured by PIXE):
    [0012]
    12. Method according to claim 11, CHARACTERIZED by the fact that it has a selectivity for ethylene of not less than 90%.
    [0013]
    13. Method according to claim 11, CHARACTERIZED by the fact that the hourly space velocity of the gas is not less than 3000 h-1.
    [0014]
    14. Method according to claim 11, CHARACTERIZED by the fact that the calcined oxidative dehydrogenation catalyst forms a fixed bed in the reactor.
    [0015]
    15. Method according to claim 11, CHARACTERIZED by the fact that the hourly space velocity of the gas is not less than 3000 h-1, the calcined oxidative dehydrogenation catalyst forms a fixed bed in the reactor and the selectivity for ethylene is not less to 90%.
    [0016]
    16. Method according to claim 11, CHARACTERIZED by the fact that the molar ratio of Mo:V is from 1:0.22 to 1:0.29 in the calcined oxidative dehydrogenation catalyst.
    [0017]
    17. Method according to claim 11, CHARACTERIZED by the fact that the molar ratio of Mo:Te is greater than 1:0.11 and less than 1:0.15 in the calcined oxidative dehydrogenation catalyst.
    [0018]
    18. Method according to claim 11, CHARACTERIZED by the fact that the calcined oxidative dehydrogenation catalyst has a bulk density of 1.20 to 1.53 g/cm3.
    [0019]
    19. Method according to claim 11, CHARACTERIZED by the fact that in the crystalline phase of the calcined oxidative dehydrogenation catalyst, the amount of the phase having the formula (TeO) 0.39 (Mo3.52V1.06Nb0.42)O14 is above 75% by weight of the measured crystalline phase as determined by XRD.
    [0020]
    20. Method according to claim 11, CHARACTERIZED by the fact that in the crystalline phase of the calcined oxidative dehydrogenation catalyst, the amount of the phase having the formula (TeO)0.39(Mo3.52V1.06Nb0.42)O14 is above 85% by weight of the measured crystalline phase as determined by XRD.
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    法律状态:
    2020-03-24| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2021-06-29| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-07-20| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 04/08/2016, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    CA2900775|2015-08-20|
    CA2900775A|CA2900775A1|2015-08-20|2015-08-20|Improved oxidative dehydrogenation catalyst|
    PCT/IB2016/054717|WO2017029572A2|2015-08-20|2016-08-04|Improved oxidative dehydrogenation catalyst|
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