Catalyst and method of producing nicotinic acid

FIELD: chemistry.

SUBSTANCE: invention relates to vanadium-titanium oxide catalysts, used for producing nicotinic acid through gas phase oxidation of β-picoline with oxygen and methods of producing nicotinic acid using said catalysts. The catalyst contains vanadium oxide, titanium oxide and modifying additives - cerium oxide or one or more metal oxides, chosen from groups IV and V of the periodic table of elements with total content of oxides of modifying elements in the range 1.0 to10.0 wt %, vanadium oxide in amount of 5.0 to 75.0 wt %, and titanium oxide - the rest. A method is described for producing nicotinic acid through oxidation of β-picoline with oxygen in one or more successive layers of catalyst with different grain-size in a tube reactor in the presence of the catalyst described above.

EFFECT: increased activity of catalyst and selectivity on nicotinic acid.

13 cl, 2 tbl, 15 ex

 

The invention relates to an oxide analytically catalysts for the production of nicotinic acid by gas-phase oxidation of 3-methylpyridine (β-picoline, β) oxygen and the method of production of nicotinic acid using these catalysts.

Nicotinic acid and its derivative - nicotinamide - are vital b vitamins and is used in medicine as a medicinal preparations as food supplements and premixes for the animal, and is widely used in the syntheses of a number of valuable organic compounds.

The traditional way of production of nicotinic acid is the liquid-phase oxidation of β-picoline nitric or sulfuric acid or potassium permanganate. These methods, regardless of the type of oxidant, suffer from common drawbacks, a large number of sinks, the difficulty of selection of product, technological complexity and high energy processes. A better method for the production of nicotinic acid through gas-phase oxidative ammonolysis of β-picoline 3-lepirudin with its subsequent hydrolysis is a multistage, with a large number of harmful liquid effluents and gaseous emissions (R. Chuck, Technology development nicotinate in production, Applied catalysis A: General 280 (2005) 75-82).

The method of direct oxidation of β-picoline to nicotinic acid by oxygen in the presence of a solid the second catalyst has several advantages over these methods:

in this way there are no liquid effluents,

- gas emissions do not contain harmful impurities,

as the oxidant is air,

- nicotinic acid is produced directly after the reactor,

- does not require separation of product from catalyst

production is compact, occupies a small area.

There is a method of oxidation of β-picoline to nicotinic acid oxygen (O2: β-picoline=15-40) in the presence of water vapor (H2O / β-picoline=10-70) at a temperature of 250-290°C. is Used a catalyst containing, wt.%: the vanadium oxide 5-75, titanium oxide - rest (RF 2049089, C07D 213/803, 26.01.94). Nicotinic acid allocate immediately after the crystallization reactor cooling capacity at a temperature of 160-180°C. the Output of nicotinic acid is 82-86%.

There is a method of oxidation to nicotinic acid by oxygen (O2: β-picoline=5-100) in the presence of water vapor (H2O / β-picoline=25-75) at the temperature of inlet 150 up to 450°C. the Catalyst contains vanadium oxide 5-50 wt.% and the titanium oxide - rest. (US 6229018, C07D 213/80, 08.05.2001). The output of nicotinic acid at temperatures 265-290°C is 49-96%.

The closest is the way of the oxidation of β-picoline to nicotinic acid by oxygen (O2: β-picoline=15-40) in the presence of water vapor (H2O / β-picoline=10-70) at a temperature of 250-290°C. is Used the catalyst composition: nV 2O5mTiO2pMxOy, where n=5-75 wt.%, m=95-25%by weight, R 0-1 wt.%, M - alkaline or transition metal (EP 747359 A1, C07D 213/55, 11.12.1996). Nicotinic acid allocate immediately after the crystallization reactor cooling capacity at a temperature of 160-200°C. the Output of nicotinic acid is 82-86%.

In the known methods the catalytic experiment is carried out on the powder catalyst is 0.5 to 1 mm or 1.0 to 1.6 mm, Such grain sizes are unacceptable for use in industrial tubular reactor due to the high hydrodynamic resistance layer and a high parametric sensitivity of the catalyst. The transition to acceptable on the hydrodynamic properties of the size of the granules, for example 4×5 mm, reduces the degree of use of the V-Ti catalyst to 20-30%, i.e. the activity decreases by 3-5 times.

The invention solves the problem of increasing the activity and selectivity of the catalyst. The problem is solved

1) by promotion supplements the basic structure

2) the use of the catalyst in the form of a ring,

3) the creation of an optimal porous structure.

The problem is solved as the composition of the catalyst.

Proposed a catalyst based on oxides of vanadium and titanium for the production of nicotinic acid by oxidation of β-picoline oxygen-containing vanadium oxide, titanium oxide and modifying additives, as modifying doba is OK it contains cerium oxide or one or more metal oxides, selected from group IV and V of the period of the Periodic table, with the total weight content of oxides of reactive elements in the range from 1.1 to 10.0 wt.%, mainly 1,1-3.0 wt.%, the vanadium oxide in the amount of 5.0 is 75.0 wt.%, the rest is titanium oxide.

In particular, as the modifying compounds it contains one of the oxides of molybdenum, or tellurium, or antimony, and cerium, or silicon, or tin, or zirconium, or niobium, or any mixture.

The catalyst has a surface no more than 40 m2/g, preferably 10-40 m2/g, and the free pore volume of at least 0.4 cm3/year

The increase in the activity per unit volume of catalyst may be achieved by increasing activity unit of its surface, and the increased value of the catalyst surface. However, with the increase in the activity of the catalyst increases interdiffuse braking and reduced utilization of grain, which leads to a fall in the observed activity of the catalyst and selectivity of the reaction for the target product. To increase the degree of utilization of the catalyst is possible by optimization of the shape of the hollow grain with the minimum possible wall thickness. For the oxidation of β-picoline the course of the reaction in the area close to the kinetic, provides ring 4×2,4×5 mm (external diameter × hole diameter × height).

Thus, the catalyst may and shall be used in the form of a continuous cylinder, areas, however, the additional increase in its activity and selectivity is provided by the use in the form of granules, which have one or more through holes, and the equivalent diameter of the granules, defined as 6V/S (V is the volume of the catalyst pellet, S - area of the outer surface of the catalyst pellet), is in the range of 2.0-3.9 mm, mostly in the range of 2.4 to 3.5 mm, They can be in the form of Raschig rings or trilistniku, or chetyrehlistnik, or spoked wheels or cylinders with a few holes. The task is also solved by a method of production of nicotinic acid by oxidation of β-picoline oxygen in one or more successive layers of the above-described catalysts of different chemical composition, different size or different shape.

Another way to reduce interdiffuse braking is to create an optimal porous structure of the catalyst. The catalyst must not contain pores of less than 100 Å, while the pore volume should not be less than 0.4 cm3/, Such a structure is achieved step by calcining the catalyst in the special conditions.

The task is also solved by a method of production of nicotinic acid by oxidation of β-picoline oxygen in one or more successive layers of the above-described catalyst of different chemical composition or different shapes.

The catalysts can be prepared in various ways, for example, through the following stages:

1 - preparation of a solution of salts of vanadium and promoter;

2 - preparation of a suspension of titanium dioxide in a solution of salts of vanadium and promoter;

3 - drying the catalyst slurry;

4 - mixing powder of the dried slurry to the forming additives;

5 - granulation of the catalyst;

6 - the crop has wilted catalyst in air;

7 - heat treatment of the catalyst at a temperature of 450-550°C.

The process is carried out in the presence of water vapor at a water vapor / β-picoline=10-70.

The process is carried out at a temperature of 250-290°C. the Process is carried out at a ratio of oxygen : β-picoline=15-40. Nicotinic acid allocate immediately after the crystallization reactor cooling capacity at a temperature of 100-180°C.

In this invention the catalytic activity is characterized by the degree of conversion of β-picoline (X %), the reaction rate constant of the first order (K, ml/g*sec) and the selectivity is at nicotinic acid (S, %). Contact time is defined as the ratio of the weight of catalyst in grams to the flow of the original reaction mixture in ml/sec.

The catalytic activity of the samples is determined in flow-through installation in the temperature has reached 270-290°C. when the content in the original reaction mixture of β-picoline 0,8 vol.%, oxygen 18,0%, water 20%, the rest is nitrogen at different contact times. The acid crystallizes directly after the reactor is cooled tube. The specific surface of the catalyst (SUD,m2/g) determined by the BET method by thermal desorption of argon.

The invention is illustrated by the following examples.

The experiment in examples 1-12 performed in a glass reactor ø 25 mm with coaxial thermocouple pocket d 4 mm, the catalyst Loading is 20 g, the contact time varies with the flow of the reaction mixture within 14-21 l/h

Example 1 (comparative).

Charged to the reactor oxide analytically catalyst composition, wt.%: 20 V2O5, 80 TiO2with the surface 25 m2/g, made in the form of cylinders 4×5 mm (diameter × height). The equivalent diameter of the catalyst pellet is 4.3 mm, an Initial reaction mixture containing, vol.%: 0,8 β-picoline (β), 18 oxygen, 20 water vapor, the rest is nitrogen, is directed into the reactor, the conditional contact time of 5.0 sec*g/ml, temperature of the tour in the reactor 275°C. Conversion β 83%, the selectivity for nicotinic acid 85%, the reaction rate constant of 0.35 ml/g*sec.

Example 2 (comparative).

Charged to the reactor oxide analytically catalyst composition, wt.%: 20 V2O5, 80 TiO2with the surface 25 m2/g, made in the form of rings 4×2,4×5 mm Equivalent diameter of the catalyst pellet is 2.0 mm, the Initial reaction mixture, vol.%: 0,8 β-picoline (β), 18 oxygen, 20 water vapor, the rest is nitrogen, is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 88,2%, the selectivity for nicotinic acid 91%, the reaction rate constant of 0.53 ml/g*sec.

Example 3 (comparative).

Charged to the reactor oxide analytically catalyst composition, wt.%: 20 V2O5, 80 TiO2from surface to 120 m2/g, made in the form of rings 4×2,4×5 mm Equivalent diameter of the catalyst pellet is 2.0 mm, the Initial reaction mixture, vol.%: 0,8 β-picoline, 18 oxygen, 20 water vapor, the rest is nitrogen, is directed into the reactor, the conditional contact time of 3.5 sec*g/ml, the temperature in the reactor 275°C. Conversion β 92,2%, the selectivity for nicotinic acid 66%, the reaction rate constant to 0.73 ml/g*sec.

Example 4.

Charged to the reactor oxide analytically catalyst composition, wt.%: 16,5 V2 O5, 73,5 TiO2, 2,0 SiO2, 8,0 TeO2from surface to 30 m2/g, made in the form of rings 4×2.4×5 mm Equivalent diameter of the catalyst pellet is 2.0. The original reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.5 sec*g/ml, the temperature in the reactor 275°C. Conversion β 95%, the selectivity for nicotinic acid 86%, the reaction rate constant of 0.66 ml/g*sec.

Example 5.

Charged to the reactor oxide analytically catalyst composition, wt.%: 19,9 V2O5, 80,0 TiO2, 1,1, Moo3with the surface 25 m2/g, made in the form of rings 4×2,4×5 mm Equivalent diameter of the catalyst pellet is 2.0. The original reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 90,3%, the selectivity for nicotinic acid 90%, the reaction rate constant of 0.58 ml/g*sec.

Example 6.

Charged to the reactor oxide analytically catalyst composition, wt.%: 18 V2O5, 80 TiO2, 2.0 Moo3with the surface 28 m2/g, made in the form of rings 4×2,4×5 mm Equivalent diameter of the catalyst pellet is 2.0. The original reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 921%, selectivity for nicotinic acid 89%, the reaction rate constant 0.63 ml/g*sec.

Example 7.

Charged to the reactor oxide vanadium-titanium catalyst composition, wt.%: 18 V2O5, 80 TiO2, 2,0 TeO2with the surface 35 m2/g, made in the form of rings 4×2,4×5 mm Equivalent diameter of the catalyst pellet is 2.0. The original reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 93,4%, the selectivity for nicotinic acid 86%, the reaction rate constant of 0.67 ml/g*sec.

Example 8.

Charged to the reactor oxide analytically catalyst composition, wt.%: 16,8 V2O5, 80 TiO2, 3,2 Sb2O3with surface 32 m2/g, made in the form of rings 4×2,4×5 mm, an Initial reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 91.5%, the selectivity for nicotinic acid 87%, the reaction rate constant of 0.62 ml/g*sec.

Example 9.

Charged to the reactor oxide analytically catalyst composition, wt.%: 17,5 V2O5, 80 TiO2, 2,5 ZrO2with surface 26 m2/g, manufactured in the form of rings 4×2,4×5 mm, an Initial reaction mixture of standard composition is directed into the reactor, the conditional time pin the KTA 4,0 sec*g/ml, the temperature in the reactor 275°C. Conversion β 90,5%, the selectivity for nicotinic acid 89%, the reaction rate constant of 0.59 ml/g* sec.

Example 10.

Charged to the reactor oxide analytically catalyst composition, wt.%: 21,1 V2O5, 76,9 TiO2, 2,0 CeO2with the surface 22 m2/g, made in the form of rings 4×2,4×5 mm, an Initial reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 90,0%, the selectivity for nicotinic acid 92%, the reaction rate constant of 0.58 ml/g*sec.

Example 11.

Charged to the reactor oxide analytically catalyst composition, wt.%: 25 V2O5, 72 TiO2, 3,0 Nb2O5with the surface 24 m2/g, made in the form of rings 4×2,4×5 mm, an Initial reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 s*g/ml, the temperature in the reactor 275°C. Conversion β 92,0%, the selectivity for nicotinic acid 90%, the reaction rate constant 0.63 ml/g*sec.

Example 12.

Charged to the reactor oxide analytically catalyst composition, wt.%: 21,8 V2O577 TiO2and 1.2 SnO2with the surface 30 m2/g, made in the form of rings 4×2,4×5 mm, an Initial reaction mixture of standard composition is directed into the reactor, the conditional contact time of 4.0 seconds*GDF, the temperature in the reactor 275°C. Conversion (β 93,4 .0%, the selectivity for nicotinic acid 87%, the reaction rate constant of 0.67 ml/g*sec.

The data in examples 1-12 see table 1.

Examples 13 and 14 demonstrate how the implementation process in the industrial element of the reactor. The reactor is a steel tube outer diameter of 25 mm and a height of the reaction zone of 2.4 m, the Temperature in the reactor is measured movable thermocouple placed in coaxial pocket. Heating of the reactor tubes carry the heated fluidized bed of sand. Nicotinic acid is crystallized after the reactor vessel at 100-180°C.

The data are shown in table 2.

Example 13.

Charged to the reactor 1450 oxide analitichnogo catalyst composition, wt.%: 21,8 V2O5,77 TiO2and 1.2 SnO2from surface to 30 m2/g, made in the form of rings 4×2,4×m the Original reaction mixture, vol.%: 0,8 β-picoline (β), 18 oxygen, 20 water vapor, the rest is nitrogen, is directed into the reactor, the flow 1160 l/h, the conditional contact time of 4.5 sec*g/ml, the temperature in the hot spot in the reactor 280°C. Conversion β 96%, the selectivity for nicotinic acid 84%, the reaction rate constant of 0.71 ml/g*sec.

Example 14.

Charged to the reactor, 500 g of the oxide analitichnogo catalyst composition, wt.%: 21,8 V2O5, 77 TiO2and 1.2 SnO2/sub> from surface to 30 m2/g , made in the form of rings 4×2,4×5 mm and 950 g of a catalyst of the same composition with the surface 30 m2/g, made in the form of a ring 3,5×2×4mm in the Original reaction mixture, vol.%: 8 β-picoline (β), 18 oxygen, 20 water vapor, the rest is nitrogen, is directed into the reactor, the flow 1160 l/h, the conditional contact time of 4.5 sec*g/ml, the temperature in the hot spot in the reactor 278°C. the Conversion β 98,3%, the selectivity for nicotinic acid 86%, the reaction rate constant of 0.89 ml/g*sec.

These examples demonstrate the advantages of the annular shape of the catalyst prior to cylindrical (examples 1 and 2), macroporous catalyst before microporous (examples 2 and 3)promoted catalysts before binary (examples 2 and 4-12).

Example 14 shows the advantage of the layer-by-layer load in the course of the reaction flow less active catalyst (large ring) and then a more active catalyst (smaller ring) compared with uniform loading (example 13).

Table 1
No. AveThe catalyst composition, wt.%S, m2/gReaction conditions Conversion picoline, %The rate constant, ml/g*sSelectivity, %
V2O5TiO2Additivet, s*g/ mlT, °CWithβ,.%CO2vol.%.vol.%.
120800255.02750.8182083.00.3585
218820254.02750.8182088.20.5391
32080 01203.52750.8182092.20.7366
416.573.52.0 SiO2+8.0 TeO2304.52750.8182095.00.6686.
518.980.01.1 Moo3254.02750.8182090.30.5890.
618802.0 Moo3284.02750.8 182092.10.6389
718802.0 TeO2354.02750.8182093.40.6786
816.8803.2 Sb2O3324.02750.8182091.50.6287
917.5802.5 ZrO2264.02750.8182090.50.5989
1021.176.92.0 CeO2224.02750.8182090.00.5892.
1125.0723.0 Nb2O5244.02750.8182092.00.6390
1221.80771.2 SnO2304.02750.8182093.40.6787

Table 2
No. Ave Reaction conditionsConversion picoline, %The rate constant, ml/g*sSelectivity, %
t, s*g/T, °CWithβ,.%vol.%vol.%
ml
134.52800.5182096.00.7184
144.52780.5182098.20.8986

1. The catalyst based on oxides of vanadium and titanium for the production of nicotinic acid by oxidation of β-picoline oxygen-containing vanadium oxide, titanium oxide and modifying additives, characterized in that it contains as modifying additives cerium oxide or one or more of the LCO oxides of elements selected from group IV and V of the period of the Periodic table, with the total weight content of oxides of reactive elements in the range from 1.1 to 10.0 wt.%, the vanadium oxide in the amount of 5.0 is 75.0 wt.%, the rest is titanium oxide.

2. The catalyst according to claim 1, characterized in that the total content of oxides of reactive elements mainly of 1.1 to 3.0 wt.%.

3. The catalyst according to claim 1, characterized in that the modifying compounds it contains one of the oxides of molybdenum, or tellurium, or antimony, and cerium, or silicon, or tin, or zirconium, or niobium, or any mixture.

4. The catalyst according to claim 1, characterized in that the catalyst has a surface no more than 40 m2/g and the free pore volume of at least 0.4 cm3/year

5. The catalyst according to claim 1, characterized in that it has the form of granules with one or more through-holes, and the equivalent diameter of the granules, defined as 6V/S, where V is the volume of the catalyst pellet S is the area of the outer surface of the catalyst pellet is in the range of 2.0-3.9 mm, mostly in the range of 2.4 to 3.5 mm

6. The catalyst according to claim 6, characterized in that its granules have the form of Raschig rings, or trilistniku, or chetyrehlistnik, or spoked wheels or cylinders with a few holes.

7. Method of production of nicotinic acid by oxidation of β-picoline oxygen in one and several successive layers of the catalyst of different chemical composition or different shapes, characterized in that the process is carried out in the presence of a catalyst according to any one of claims 1 to 6.

8. The method according to claim 7, characterized in that the process is carried out in the presence of water vapor.

9. The method of claim 8, wherein the process is carried out at a ratio of water vapor / β-picoline=10-70.

10. The method according to 7, wherein the process is carried out at a temperature of 250-290°C.

11. The method according to claim 7, characterized in that the process is carried out at a ratio of oxygen : β-picoline=15-40.

12. The method according to 7, characterized in that nicotinic acid allocate immediately after the crystallization reactor cooling capacity at a temperature of 100-180°C.



 

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30 cl, 1 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to vanadium-titanium oxide catalysts, used in production of methanoic acid through gas-phase oxidation of formaldehyde using oxygen and methods of obtaining methanoic acid using these catalysts. Described is a catalyst based on vanadium and titanium oxides, mainly containing nano VOx particles in form of a monolayer surface coating of titanium oxide. Content of the crystalline phase of vanadium oxide is not more than 20 wt %, and mainly not more than 8.0 wt % of its total content. Described also is a method of obtaining methanoic acid through oxidation of formaldehyde using oxygen in one or several serial pipe reactors in the presence of the above described catalyst.

EFFECT: increased catalyst activity and increased output of methanoic acid.

7 cl, 12 ex, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to vanadium-titanium oxide catalysts, used in production of methonoic acid through gas-phase oxidation of formaldehyde with oxygen and methods of obtaining methanoic acid using these catalysts. Described is a catalyst based on vanadium and titanium oxides, containing 7.0-50.0 wt % vanadium oxide and in form of granules with one or several through-holes and equivalent diametre of the granules defined by the ratio 6V/S, where V is the volume of the catalyst granule and S is the outer surface area of the catalyst granule. The equivalent diametre lies between 2.0 and 3.9 mm and mainly between 2.4 and 3.5 mm. Described also is a method of obtaining methanoic acid through oxidation of formaldehyde with oxygen in one or several serial pipe reactors in the presence of the above described catalyst.

EFFECT: increased catalyst activity and increased output of methanoic acid.

7 cl, 10 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: present invention relates to vanadium-titanium oxide catalysts, used in production of methonic acid through gas-phase oxidation of formaldehyde with oxygen and methods of obtaining methanoic acid using the said catalysts. Description is given of a catalyst containing 7.0-50.0 wt % vanadium oxide and modifying compounds: one or more oxides of group IV and V metals with total weight content of oxides of modifying metals between 0.1 and 10.0 wt %, and mainly between 0.1 and 3 wt %. Described also is a method of obtaining methanoic acid through oxidation of formaldehyde using oxygen in one or several serial pipe reactors in the presence of the above described catalyst.

EFFECT: increased catalyst activity and increased output of methanoic acid.

8 cl, 18 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: catalyst includes manganese and zirconium, and at least, 50 wt % of catalyst in its reduced condition consists of manganese oxide and zirconium oxide, in which ratio Mn/Zr constitutes between 0.05 and 5.00. Method of synthesis-gas processing includes stage of synthesis-gas contact with catalyst in presence of water steam, said catalyst being used. Claimed catalyst has higher activity, high adhesion properties relative to other ceramic materials, and metals. Catalyst is suitable for production of catalytic equipment, which can be used in stationary and automobile installations.

EFFECT: possibility to control productivity of hydrogen and carbon monoxide by controlling temperature and amount of steam in synthesis-gas.

14 cl, 7 tbl, 34 ex

FIELD: technological processes; chemistry.

SUBSTANCE: method involves reaction of raw material containing organic component with a catalyst composition. Processing method is selected out of alkylation, acylation, hydrotreatment, demetallisation, catalytic deparaffinisation, Fischer-Tropsch process and cracking. Catalyst composition includes mainly mesoporous silicon dioxide structure containing at least 97 vol.% of pores with size in the interval from ca. 15 Å to ca. 300 Å, and at least ca. 0.01 cm3/g of micropores. Mesoporous structure features at least one catalytically and/or chemically active heteroatom in amount of at least ca. 0.02 mass %, selected out of a group including Al, Ti, V, Cr, Zn, Fe, Sn, Mo, Ga, Ni, Co, In, Zr, Mn, Cu, Mg, Pd, Ru, Pt, W and their combinations. The catalyst composition radiograph has one 0.3° to ca. 3.5° peak at 2θ.

EFFECT: highly efficient method of organic compound processing in the presence of catalyst composition without zeolite.

20 cl, 31 ex, 17 tbl, 22 dwg

FIELD: chemical industry; other industries; production of the vanadium catalysts for oxidation of sulfur dioxide and sulfur trioxide.

SUBSTANCE: the invention is pertaining to production of the vanadium catalysts for oxidation of sulfur dioxide and sulfur trioxide used in production of the sulfuric acid by the contact method, in particular, to the fusion mixture for production of the catalyst. The technical problem of the present invention is improvement of the operational properties of the catalyst of the conversion of SO2 into SO3, namely - improvement of the strength of the extruded calcined granules of the ready catalyst without deterioration of its catalytic activity at the expense of decrease of the minimal working humidity of the contact mass at extrusion. The fusion mixture for preparation of the catalyst of conversion of SO2 into SO3 includes vanadium oxides and oxides of the alkali metals (K, Na, Rb, Cs), sulfur, polyethyleneoxide, silicon dioxide in the form of the natural and-or synthetic silica. The contents in it of the polyethyleneoxide is within the limits from 0.005 up to 0.195 mass %, in terms of the dry substance.

EFFECT: the invention ensures the improved operational properties of the catalyst of the conversion of sulfur dioxide into sulfur trioxide and the improved strength of the extruded calcined granules of the ready catalyst without deterioration of its catalytic activity.

10 ex, 1 tbl, 1 dwg

FIELD: chemical industry; non-ferrous metallurgy industry; other industries; methods of production of the catalyst for oxidization of the vanadium oxide particles in the gaseous phase with the definite size distribution.

SUBSTANCE: the invention is pertaining to the method of production of the catalyst for oxidization in the gaseous phase of the vanadium oxide particles with the definite size distribution. The invention describes the method of production of the catalyst for oxidization in the gaseous phase, at which on the fluidized inert carrier they deposit the suspension of TiO2 and V2O5 particles, in which, at least, 90 volumetric % of the particles of V2O5 have the diameter of 20 microns or less and, at least, 95 volumetric % of the particles of V2O5 have the diameter of 30 microns or less. The technical result of the invention is that the certain particle-size distribution allows to achieve the high efficiency of the coating.

EFFECT: the invention allows to achieve the high efficiency of the coating.

6 cl, 2 ex

FIELD: redox reaction catalysts.

SUBSTANCE: invention relates to methods for preparing vanadium-titanium oxide catalysts for redox reactions, e.g. for industrial processes of production of phthalic anhydride via oxidation of o-xylene, selective reduction nitrogen oxides, and detoxification of organochlorine compounds. Method of invention comprises following stages: providing titanyl sulfate solution; adding ammonia and then vanadium peroxide solution to titanyl sulfate solution or adding to the same vanadyl sulfate or oxalate and then ammonia solution; optionally ageing suspension resulting after mixing of solutions; filtration; and calcinations at 450°C.

EFFECT: increased heat resistance of active chlorobenzene oxidation catalyst and reduced catalyst preparation time (10-12 h instead 72 h as in a known method).

1 tbl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention can be used for hydrogen recombination in reactor sections of nuclear power stations and other facilities. Description is given of a catalyst for recombination of hydrogen and oxygen, containing a solid porous carrier with hydrophobisated catalytic coating of a platinoid metal. This catalyst is distinguished by that, the carrier is made from a valve metal, obtained using powder metallurgical technique, with specific surface are of 0.05-1.50 m2/g; the catalyst carrier is made from porous plates of titanium or o tantalum, or niobium, or zirconium of thickness 0.3-2.0 mm. Described also, is a method of making the said catalyst, involving saturation of the carrier with a solution of platinoid compound, reduction of the said compound to a metal, as well as hydrophobisation of the catalytic coating by moistening it with a suspension of fluorine-containing polymer with an organic stabiliser and subsequent calcination. This method is distinguished by that, the carrier is kept in the suspension for 5-30 s. The carrier is held in a single position and all stages for preparation of hydrophobisated catalytic coating are carried out in that position. Translational oscillations at frequency 1-2 Hz are imparted when saturating the carrier.

EFFECT: provision for reliable functioning of the catalyst for recombination of hydrogen and oxygen in conditions of prolonged contact with wet medium, as well as cutting on preparation time.

3 cl, 1 tbl, 1 ex, 2 dwg

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