JP4954750B2 - Method for producing molybdenum, bismuth, iron, silica-containing composite oxide catalyst - Google Patents

Description

  The present invention relates to a method for producing a composite oxide catalyst containing molybdenum, bismuth, iron and silica as essential components.

A composite oxide catalyst containing molybdenum, bismuth, iron and silica as essential components is produced by subjecting the target product (an aldehyde, a carboxylic acid, a nitrile compound, etc. corresponding to the organic compound) by an oxidation reaction (for example, an ammoxidation reaction) of the organic compound. Have been widely used in the production of catalysts, and catalysts having various compositions have been proposed.
For example, taking a catalyst used for the synthesis of acrylonitrile by propylene ammoxidation as an example, Patent Document 1 discloses an oxide catalyst containing molybdenum, bismuth and iron, and Patent Document 2 discloses an oxidation containing iron and antimony. A product catalyst is disclosed.
Improvements to these catalysts have also been made energetically. For example, Patent Documents 3 to 8 disclose an improved catalyst in which other components are added in addition to molybdenum, bismuth, and iron, and Patent Document 9 discloses an improved catalyst in which other components are added in addition to iron and antimony. ing.
Furthermore, efforts are being made to improve the yield of the desired product by improving the catalyst production process. For example, Patent Documents 10 to 18 disclose a method for adjusting the pH of a slurry containing a catalyst component to a predetermined range, a method for mixing specific elements after pH adjustment, a heat treatment, and a method for performing a concentration treatment, Patent Document 19 discloses a method of holding a slurry for a certain period of time under a specific condition during the process. Patent Document 20 discloses a method in which a catalyst or catalyst precursor prepared in advance is impregnated with a specific component and then fired.
Japanese Patent Publication No. 38-17967 Japanese Examined Patent Publication No. 38-19111 JP 48-49719 A JP 55-56839 A JP 54-95513 A JP 58-67349 A JP 7-47272 A JP-A-10-43595 JP-A-4-118051 Japanese Patent Laid-Open No. 1-265058 JP-A-2-59046 JP-A-2-214543 JP-A-2-251250 JP 2000-37631 A JP 2000-42414 A Japanese Patent Laid-Open No. 1-265067 JP 2002-306968 A JP 2002-306969 A JP 2006-55732 A JP 11-309374 A

However, these prior art catalysts, although having some effect in improving the yield of the target product, are still not sufficient from an industrial point of view. In addition, when the same type of catalyst is repeatedly produced, the catalyst activity of the resulting catalyst varies greatly, and the yield of the target product when the target product is manufactured using the catalyst also varies. The problem of low reproducibility is also a problem, and improvement is desired in this respect as well.
This invention is made | formed in view of the said situation, and makes it a subject to provide the manufacturing method which can manufacture the complex oxide catalyst with the high yield of a target product with sufficient reproducibility.

The present invention includes the following aspects.
[1] A catalyst for the synthesis of an aldehyde, carboxylic acid or nitrile compound by an oxidation reaction of an organic compound, and a method for producing a composite oxide catalyst containing molybdenum, bismuth, iron and silica,
Mixing step of mixing a solution or slurry containing at least molybdenum and a solution or slurry containing at least bismuth and iron within a temperature range of 30 to 70 ° C. to obtain a mixed solution containing at least molybdenum, bismuth and iron When,
Holding the mixture for 2 hours or more in a temperature range of 0 to 25 ° C .;
After the holding step, a drying step of drying the mixed liquid to obtain a dried product,
A method for producing a composite oxide catalyst, comprising a firing step of firing the dried product.
[2] The method for producing a composite oxide catalyst according to [1], wherein the composite oxide catalyst has a composition represented by the following general formula (I).
_{Mo a Bi b Fe c A d} B e C f D g O h (SiO 2) i ... (I)
[Wherein, Mo, Bi, Fe and O represent molybdenum, bismuth, iron and oxygen, respectively, A represents at least one element selected from the group consisting of lithium, sodium, potassium, rubidium and cesium; B represents at least one element selected from the group consisting of cobalt, nickel, copper, zinc, magnesium, strontium, calcium, barium and manganese, and C represents chromium, vanadium, tungsten, niobium, zirconium, lanthanum, cerium, praseodymium Represents at least one element selected from the group consisting of neodymium and samarium, D represents at least one element selected from the group consisting of thallium, silver, boron, aluminum, indium, antimony, phosphorus and tellurium; ₂ represents silica . The symbols a, b, c, d, e, f, g, and h each represent the atomic ratio of the element with the symbol, i represents the atomic ratio of silica, and when a = 12, 0. 1 ≦ b ≦ 5, 0.1 ≦ c ≦ 10, 0.01 ≦ d ≦ 3, 2 ≦ e ≦ 12, 0.5 ≦ f ≦ 5, 0 ≦ g ≦ 5, 20 ≦ i ≦ 200, h is an atomic ratio of oxygen necessary to satisfy the valences of Mo, Bi, Fe, A, B, C, and D. ]
[3] The method for producing a composite oxide catalyst according to [1] or [2], wherein the composite oxide catalyst is a catalyst for acrylonitrile synthesis by propylene ammoxidation reaction.

  According to the present invention, a complex oxide catalyst having a high yield of the target product can be produced with good reproducibility.

Hereinafter, the present invention will be described in detail.
The method for producing a composite oxide catalyst of the present invention (hereinafter sometimes referred to as the catalyst production method of the present invention) comprises a solution or slurry containing at least molybdenum and a solution or slurry containing at least bismuth and iron. A mixing step of mixing within a temperature range of ˜70 ° C. to obtain a mixed solution containing at least molybdenum, bismuth and iron, and a holding step of holding the mixed solution in a temperature range of 0 to 25 ° C. for 2 hours or more After the holding step, the method includes a drying step of drying the mixed liquid to obtain a dried product, and a firing step of firing the dried product.
In the present invention, the mixing step and the holding step are particularly important, and the other steps are performed in accordance with a conventional catalyst preparation method (for example, the catalyst preparation method described in the above-mentioned patent document). That's fine.

[Mixing process]
In the mixing step, a solution or slurry containing at least molybdenum (hereinafter sometimes referred to as Mo liquid) and a solution or slurry containing at least bismuth and iron (hereinafter sometimes referred to as BF liquid) are mixed. To obtain a mixed solution containing at least molybdenum, bismuth and iron.
The lower limit of the temperature during the mixing is 30 ° C, preferably 35 ° C, more preferably 40 ° C. Moreover, an upper limit is 70 degreeC, Preferably it is 65 degreeC, More preferably, it is 60 degreeC.
When the temperature at the time of mixing is lower than the lower limit of the above temperature range or higher than the upper limit, the effect of the present invention is not sufficiently exhibited and the target product yield is reduced. Furthermore, when the temperature of the Mo liquid is too high, precipitation may occur, which may hinder the production of the catalyst.
The liquid temperature may rise due to the mixing of the Mo liquid and the BF liquid. In this case, the temperature of each solution or slurry before mixing is adjusted so that the maximum temperature falls within a predetermined range.

The Mo liquid only needs to contain at least molybdenum, and may contain a catalyst component other than molybdenum among the elemental components constituting the catalyst (hereinafter also referred to as catalyst component). However, for the effect of the present invention, it is preferable that the Mo liquid does not contain bismuth and iron.
Moreover, Mo liquid does not necessarily need to contain the whole quantity of molybdenum, and may mix a part by another process. However, in order to fully exhibit the effects of the present invention, it is preferable to mix 50% or more of the total molybdenum amount in this step.

The BF liquid only needs to contain at least bismuth and iron, and may contain a catalyst component other than bismuth and iron. However, for the effect of the present invention, the BF liquid preferably does not contain molybdenum.
Further, the BF liquid does not necessarily need to contain the total amount of bismuth and iron, and a part thereof may be mixed in another process. However, in order to fully manifest the effects of the present invention, it is preferable to mix 50% or more of the total amount of bismuth and 50% or more of the total amount of iron in this step.

  An aqueous liquid such as silica sol is particularly preferably used as a raw material for the silica component, and may be mixed with the Mo liquid or BF liquid before or during the mixing process, or added in any process from the mixing process to the drying process. May be.

  When the composite oxide catalyst to be produced by the catalyst production method of the present invention contains other catalyst components other than molybdenum, bismuth, iron and silica, these catalyst components are contained in the Mo liquid and / or the BF liquid. In addition, a solution or slurry containing the catalyst component may be prepared separately, and this may be added when preparing the Mo liquid and / or BF liquid. It may be added during or after mixing.

Each solution or slurry can be prepared by a known method. For example, it can be prepared by adding the raw materials of each catalyst component in an aqueous medium in the form of a solid or a solution, and dissolving and / or suspending. Examples of the aqueous medium include water and nitric acid. In addition, as the aqueous medium, a raw material in which some of the catalyst component materials are previously dissolved and / or suspended in the aqueous medium, for example, an aqueous liquid containing the silica described above may be used.
Each solution or slurry may be further subjected to pH adjustment, atomization treatment, and the like. The pH adjustment is preferably performed so that the pH of the mixed solution (mixed solution retained in the retaining step) is in the range of 0 to 5, and is performed in the range of 0.5 to 2.5. Is more preferable.
In addition, after mixing Mo liquid and BF liquid, you may heat-process, but when the temperature of the solution or slurry used in this process and those liquid mixture exceeds 70 degreeC, this invention The effect of may not be fully manifested. Therefore, it is preferable that the temperature of the solution or slurry used in this step and the mixed solution thereof be 70 ° C. or lower throughout the mixing step.

The raw material of each catalyst component used for the preparation of each solution or slurry is not particularly limited and can be appropriately selected according to the catalyst properties and the preparation method.
For example, as a raw material of the molybdenum component, an oxide such as molybdenum trioxide, molybdic acid or its salt such as ammonium molybdate, ammonium paramolybdate or ammonium metamolybdate, molybdenum such as phosphomolybdic acid or silicomolybdic acid Heteropolyacid containing or a salt thereof can be used.
As raw materials for the bismuth component, bismuth salts such as bismuth nitrate, bismuth carbonate, bismuth sulfate, bismuth acetate, bismuth trioxide, metal bismuth, and the like can be used. These raw materials can be used in the form of a solid or as an aqueous solution, an aqueous nitric acid solution, or a slurry of a bismuth compound generated from the aqueous solution, but it is preferable to use nitrate, a solution thereof, or a slurry generated from the solution.
As raw materials for iron components, ferrous oxide, ferric oxide, ferrous nitrate, ferric nitrate, iron sulfate, iron chloride, iron organic acid salt, iron hydroxide, etc. can be used. Iron may be dissolved in heated nitric acid. The solution containing the iron component may be used after adjusting the pH with aqueous ammonia or the like. When adjusting the pH, it is possible to prevent the iron component from being precipitated by allowing a chelating agent to coexist in a solution containing the iron component. Examples of chelating agents that can be used here include ethylenediaminetetraacetic acid, lactic acid, citric acid, tartaric acid, and gluconic acid. When preparing an aqueous solution containing iron ions and a chelating agent, it is preferable to use these raw materials by dissolving them in an acid or water.
Although there is no restriction | limiting in particular as a raw material of a silica component, As mentioned above, a silica sol is preferable and it can select from a commercially available thing suitably and can be used.
When the composite oxide catalyst to be produced by the catalyst production method of the present invention contains a catalyst component other than molybdenum, bismuth, iron and silica, the raw material for the other catalyst component is an oxidation of the catalyst component. Or chlorides, sulfates, nitrates, ammonium salts, carbonates, hydroxides, organic acid salts, oxyacids, oxyacid salts, heteropolyacids, heteropolyacid salts or the like that can be converted to oxides when ignited A mixture of the above can be used.

The mixing method of each solution or slurry is not particularly limited, and a known method can be used.
In the mixed solution, the total concentration of each catalyst component is preferably 10 to 50% by mass in terms of the oxide of each catalyst component.

The mixed solution prepared in this step contains at least molybdenum, bismuth, and iron. The mixed solution does not necessarily need to contain all the catalyst components constituting the catalyst. The catalyst component not included in the mixed solution at this time, or a part of the catalyst component is included in the total amount. The catalyst component that is not contained may be added in the steps after the holding step.
For example, in the present invention, the mixed liquid does not necessarily contain silica as described above. However, since the composite oxide catalyst produced by the catalyst production method of the present invention contains silica as an essential component, when the mixed solution does not contain silica, silica is separately added in the steps from the holding step to the drying step. It is necessary to add.

[Holding process]
Next, the liquid mixture obtained in the holding step is cooled to a predetermined holding temperature, and the holding temperature is held for a predetermined time.
The lower limit of the holding temperature is 0 ° C, preferably 5 ° C. The upper limit of the holding temperature is 25 ° C, preferably 20 ° C. When the holding temperature is lower or higher than the lower limit of the above range, the effect of the present invention is not sufficiently exhibited, the target product yield is lowered, and the performance of the obtained catalyst is greatly fluctuated.
The lower limit of the holding time (holding time) at the predetermined holding temperature is 2 hours, preferably 3 hours, and more preferably 5 hours. The upper limit is not particularly limited, but it is usually within 100 hours because a certain effect cannot be obtained even if the holding time is extended more than necessary.
It is preferable to stir the slurry while the temperature is maintained within a predetermined temperature range.
The holding time here refers to the time from when the temperature of the mixed solution is within the holding temperature range until drying in the next drying / firing step.
If the drying time is long, the resulting catalyst will be an assembly of catalysts with different retention times.In that case, the average retention time of the entire assembly is calculated and this is the retention time. Define that there is.

[Drying process]
Next, the mixed solution after the holding step is dried. Thereby, a dried product (catalyst precursor) is obtained.
When the composite oxide catalyst produced by the method for producing a catalyst of the present invention is used as a catalyst for fluidized bed reaction, particularly when the catalyst is used for acrylonitrile synthesis, the catalyst precursor is formed into spherical particles by spray drying. It is preferable to do. At the time of spray drying, a spray dryer such as a pressure nozzle type, a two-fluid nozzle type, or a rotary disk type is used.
As for the temperature of the hot air circulated in the spray dryer drying chamber, the lower limit of the temperature in the vicinity of the inlet to the drying chamber is preferably 130 ° C, more preferably 140 ° C, and the upper limit is preferably 350 ° C, more preferably. 300 ° C. The lower limit of the temperature in the vicinity of the drying chamber outlet is preferably 100 ° C., more preferably 110 ° C., and the upper limit is preferably 200 ° C., more preferably 180 ° C. Furthermore, the difference between the temperature near the inlet and the temperature near the drying chamber outlet is preferably maintained at 20 to 120 ° C, more preferably 30 to 110 ° C. If each of the above temperatures is not within the predetermined range, the target product yield or the activity of the resulting catalyst may decrease, or the bulk density, particle strength, etc. of the finally obtained catalyst particles may decrease. May occur.

[Baking process]
Next, the obtained dried product (catalyst precursor) is fired. Thereby, a fired product (catalyst) containing at least molybdenum, bismuth and iron is obtained.
The lower limit of the firing temperature is preferably 500 ° C, more preferably 520 ° C. The upper limit is preferably 700 ° C, more preferably 680 ° C. When the temperature is lower than the lower limit, sufficient catalytic performance is not exhibited, and the target product yield may be reduced. On the other hand, if it is higher than the upper limit, the yield of the target product may be reduced, or the activity of the catalyst may be excessively low. In addition, ammonia combustibility may increase in the ammoxidation reaction.
The lower limit of the firing time is preferably 0.1 hour, more preferably 0.5 hour. When the calcination time is shorter than the lower limit, sufficient catalyst performance is not exhibited, and the target product yield may be reduced. The upper limit is not particularly limited, but is usually within 20 hours because the effect obtained even if the time is extended more than necessary does not become a certain level.
A general-purpose firing furnace can be used for firing, and a rotary kiln, fluidized firing furnace or the like is particularly preferably used.
The gas atmosphere used in the firing may be an oxidizing gas atmosphere containing oxygen or an inert gas atmosphere such as nitrogen, but it is convenient to use air.

[Temperary firing process]
In this invention, before performing a baking process after a drying process, Preferably it has the temporary baking process of pre-baking the said dried material in the range of 200-490 degreeC, More preferably, in the range of 220-470 degreeC. preferable. This may improve the target product yield.
A general-purpose firing furnace can be used for the temporary firing as in the firing step.
The gas atmosphere used in the preliminary firing may be an oxidizing gas atmosphere containing oxygen or an inert gas atmosphere such as nitrogen, but it is convenient to use air.

[Addition process]
In the present invention, in the mixed solution after the holding step, the catalyst precursor before the firing step (including the dried product obtained in the drying step, and the provisionally calcined product when the preliminary firing step is performed), or the firing step. You may perform the addition process which adds a catalyst component with respect to the catalyst obtained.
What is necessary is just to set suitably the kind and addition amount of the catalyst component added at this time according to the catalyst composition to manufacture.
The catalyst component can be added by a conventionally known method. For example, a method of mixing a raw material of a predetermined catalyst component in a solid, solution or slurry state with the mixed solution, the catalyst precursor or the catalyst, A predetermined amount of a solution containing a raw material of the catalyst component can be added and impregnated.

  The shape and size of the composite oxide catalyst obtained as described above are not particularly limited, and may be appropriately set depending on the application. For example, in the case of a catalyst for a fluidized bed reaction, particularly when the catalyst is used for acrylonitrile synthesis, the particle size of the calcined product is preferably in the range of 5 to 200 μm, more preferably in the range of 10 to 150 μm.

The composite oxide catalyst produced by the catalyst production method of the present invention is not particularly limited as long as it contains at least molybdenum, bismuth, iron and silica, but may have a composition represented by the following general formula (I). preferable. When the catalyst production method of the present invention is applied to the production of a catalyst having the composition represented by the following general formula (I), the properties of the obtained catalyst are preferable, and the yield of the desired product is improved when used in the reaction. The effects of the present invention are sufficiently exhibited.
_{Mo a Bi b Fe c A d} B e C f D g O h (SiO 2) i ... (I)
[Wherein, Mo, Bi, Fe and O represent molybdenum, bismuth, iron and oxygen, respectively, A represents at least one element selected from the group consisting of lithium, sodium, potassium, rubidium and cesium; B represents at least one element selected from the group consisting of cobalt, nickel, copper, zinc, magnesium, strontium, calcium, barium and manganese, and C represents chromium, vanadium, tungsten, niobium, zirconium, lanthanum, cerium, praseodymium Represents at least one element selected from the group consisting of neodymium and samarium, D represents at least one element selected from the group consisting of thallium, silver, boron, aluminum, indium, antimony, phosphorus and tellurium; ₂ represents silica . The symbols a, b, c, d, e, f, g, and h each represent the atomic ratio of the element with the symbol, i represents the atomic ratio of silica, and when a = 12, 0. 1 ≦ b ≦ 5, 0.1 ≦ c ≦ 10, 0.01 ≦ d ≦ 3, 2 ≦ e ≦ 12, 0.5 ≦ f ≦ 5, 0 ≦ g ≦ 5, 20 ≦ i ≦ 200, h is an atomic ratio of oxygen necessary to satisfy the valences of Mo, Bi, Fe, A, B, C, and D. ]

  When two or more elements are included as A, d represents the total atomic ratio of the two or more elements. When B contains two or more elements, e represents the total atomic ratio of the two or more elements. When C contains two or more elements, f represents the total atomic ratio of the two or more elements. When D contains two or more elements, g represents the total atomic ratio of the two or more elements.

In order to make the composition of the catalyst the above composition, for example, the addition amount of the catalyst raw material in the mixing step may be adjusted, or the addition step may be performed, and the addition amount of each catalyst component at that time may be appropriately adjusted.
The composition of the catalyst can be confirmed by conducting elemental analysis by ICP (inductively coupled radio frequency plasma) emission analysis, fluorescent X-ray analysis, atomic absorption analysis or the like. In the case where an extremely volatile element is not used, it may be calculated from the amount of each raw material used at the time of catalyst production.

According to the composite oxide catalyst produced by the catalyst production method of the present invention, acrylonitrile can be produced in high yield in acrylonitrile synthesis by propylene ammoxidation reaction.
Therefore, the catalyst production method of the present invention is particularly suitable for producing an acrylonitrile synthesis catalyst by propylene ammoxidation reaction.

The synthesis of acrylonitrile by the ammoxidation reaction of propylene can be carried out, for example, by using the composite oxide catalyst as a fluidized bed catalyst and supplying a raw material gas containing propylene, ammonia and oxygen to the catalyst layer.
Although it does not specifically limit as source gas, The source gas of the range whose propylene / ammonia / oxygen is 1 / 1.1-1.5 / 1.5-3 (molar ratio) is preferable.
It is convenient to use air as the oxygen source.
The source gas may be used after being diluted with an inert gas such as water vapor, nitrogen or carbon dioxide, saturated hydrocarbon or the like, or may be used with an increased oxygen concentration.
The reaction temperature of the ammoxidation reaction is preferably 370 to 500 ° C. The reaction pressure is preferably within the range of normal pressure to 500 kPa.
The apparent contact time (apparent volume density-based catalyst volume / supplied raw material gas amount) is preferably 0.1 to 20 seconds.

EXAMPLES Hereinafter, although an Example and a comparative example demonstrate this invention concretely, this invention is not limited to an Example.
In the following examples and comparative examples, “parts” means parts by mass.
The compositions of the catalysts produced in the examples and comparative examples were determined from the amount of each raw material used for the production of the catalyst.
Moreover, the activity test was implemented in the following procedures about the catalyst obtained by the following Example and comparative example.
[Catalyst activity test]
A catalyst is packed in a fluidized bed reactor having an inner diameter of 25 mm and a height of 40 mm in the catalyst fluidized portion, and the composition is propylene / ammonia / oxygen (supplied as air) / water vapor = 1/1 in the fluidized bed reactor. A mixed gas of 1 / 2.2 / 0.5 (molar ratio) is fed at a gas linear velocity of 4.5 cm / sec (sec.), Under reaction conditions of a reaction temperature of 440 ° C. and a reaction pressure of 200 kPa, Acrylonitrile was synthesized by ammoxidation of propylene.
In this synthesis reaction, the contact time between the raw material gas and the catalyst particles, the propylene conversion rate, and the acrylonitrile yield are defined by the following equations.
Contact time (sec.) = Apparent volume density-based catalyst volume (mL) / feed gas amount converted to reaction conditions (mL / sec.)
Propylene conversion rate (%) = (carbon mass of supplied propylene−carbon mass of unreacted propylene) / carbon mass of supplied propylene Acrylonitrile yield (%) = (carbon mass of produced acrylonitrile / carbon of supplied propylene) Mass) × 100
Each carbon mass in the above formula was analyzed by gas chromatography.
The composition of the catalyst obtained in each Example and Comparative Example is shown in Table 1. The slurry preparation conditions (mixing temperature), slurry holding conditions (holding temperature, holding time), final calcination conditions (temperature, time), and activity test results Is shown in Table 2. The numerical values in Table 1 indicate the atomic ratio of each element.

[Example 1]
Composition is Mo ₁₂ Bi _0.6 Fe _1.5 K _0.2 Co _1.5 Ni _4.5 Mg _0.5 Zn _0.5 Cr _0.6 W _0.4 La _0.2 Ce _0.5 P ₀ A catalyst represented by _.2 O _x (SiO ₂ ) ₃₅ (the oxygen atomic ratio x is a value naturally determined by the valence of other elements; the same shall apply hereinafter) was produced in the following manner.
In 900 parts of pure water, 433.5 parts of ammonium paramolybdate was dissolved (solution A).
Separately, 17 mass% nitric acid 520 parts, ferric nitrate 124.0 parts, cobalt nitrate 89.3 parts, nickel nitrate 267.7 parts, magnesium nitrate 26.2 parts, zinc nitrate 30.4 parts, chromium nitrate 49 .1 part, 17.7 parts of lanthanum nitrate, 44.4 parts of cerium nitrate, 4.1 parts of potassium nitrate and 59.6 parts of bismuth nitrate were sequentially added and dissolved (solution B).
The temperature of A liquid, B liquid, 40 mass% silica sol, 50 mass% ammonium metatungstate aqueous solution part, and 85 mass% phosphoric acid was adjusted to 40 degreeC.
Under stirring, A liquid, B liquid, 50 mass% ammonium metatungstate aqueous solution 38.0, and 4.7 mass parts of 85 mass% phosphoric acid were sequentially added to 1076 parts of 40 mass% silica sol to obtain an aqueous slurry.
The temperature of the resulting slurry was adjusted to 20 ° C. and held for 12 hours with stirring.
The slurry after holding was spray-dried with a rotary disk spray dryer at an inlet temperature of 270 ° C. and an outlet temperature of 180 ° C. The obtained dried powder was baked by standing in an electric furnace at 250 ° C. for 2 hours and at 450 ° C. for 2 hours, and finally fluidly baked at 590 ° C. for 3 hours to obtain a catalyst.
The obtained catalyst was subjected to an activity test.

[Example 2]
Composition is Mo ₁₂ Bi _1.2 Fe _1.8 K _0.1 Rb _0.05 Co ₁ Ni ₅ Cu _0.2 Mn _0.3 Cr _0.8 W _0.3 V _0.1 Zr _0.2 Ce ₀ A catalyst represented by _{.4B 0.2} O _x (SiO ₂ ) ₅₀ was produced in the following manner.
In 750 parts of pure water, 359.3 parts of ammonium paramolybdate were dissolved (solution C).
Separately, 360 parts of 17% by weight nitric acid, 123.3 parts of ferric nitrate, 49.4 parts of cobalt nitrate, 246.6 parts of nickel nitrate, 8.2 parts of copper nitrate, 14.6 parts of manganese nitrate, 54 parts of chromium nitrate .3 parts, 9.1 parts of zirconium oxynitrate, 29.5 parts of cerium nitrate, 1.7 parts of potassium nitrate, 1.3 parts of rubidium nitrate and 98.7 parts of bismuth nitrate were sequentially added and dissolved (solution D).
Separately, 2.0 parts of ammonium metavanadate and 2.1 parts of boric acid were sequentially added to 500 parts of pure water and dissolved (solution E).
The temperature of C liquid, D liquid, E liquid, 40 mass% silica sol, and 50 mass% ammonium metatungstate aqueous solution was adjusted to 50 degreeC.
Under stirring, liquid D, 1273 parts of 40 mass% silica sol, liquid E, and 23.6 parts of 50 mass% aqueous ammonium metatungstate solution were sequentially added to liquid C to obtain an aqueous slurry.
The temperature of the resulting slurry was adjusted to 10 ° C. and held for 20 hours with stirring.
The slurry after holding was spray-dried with a rotary disk spray dryer at an inlet temperature of 270 ° C. and an outlet temperature of 180 ° C. The obtained dried powder was baked by standing in an electric furnace at 250 ° C. for 2 hours and at 450 ° C. for 2 hours, and finally fluidly baked at 620 ° C. for 3 hours to obtain a catalyst.
The obtained catalyst was subjected to an activity test.

[Example 3]
Composition _{Mo 12 Bi 0.8 Fe 1.1 K 0.08} Cs 0.07 Co 2 Ni 5 Mn 0.2 Cr 1 W 0.5 Ce 0.4 Pr 0.1 Nd 0.1 In 0.1 A catalyst represented by Te _0.1 O _x (SiO ₂ ) ₄₀ was produced in the following manner.
400.7 parts of ammonium paramolybdate were dissolved in 1000 parts of pure water (F solution).
Separately, 450 parts of 17 mass% nitric acid, 84.0 parts of ferric nitrate, 110.1 parts of cobalt nitrate, 275.0 parts of nickel nitrate, 10.9 parts of manganese nitrate, 75.7 parts of chromium nitrate, 32. 9 parts, 8.2 parts of praseodymium nitrate, 8.3 parts of neodymium nitrate, 2.2 parts of indium nitrate, 1.5 parts of potassium nitrate, 2.6 parts of cesium nitrate and 73.4 parts of bismuth nitrate were dissolved successively. (G liquid).
Separately, 4.3 parts of telluric acid was dissolved in 100 parts of pure water (solution H).
The temperature of the F liquid, G liquid, H liquid, 40 mass% silica sol, and 50 mass% ammonium metatungstate aqueous solution was adjusted to 60 degreeC.
Under stirring, liquid F, liquid G, liquid H, and 43.8 parts of a 50 mass% aqueous solution of metatungstic acid were sequentially added to 1136 parts of 40 mass% silica sol to obtain an aqueous slurry.
The temperature of the resulting slurry was adjusted to 15 ° C. and held for 18 hours with stirring.
The slurry after holding was spray-dried with a rotary disk spray dryer at an inlet temperature of 270 ° C. and an outlet temperature of 180 ° C. The obtained dried powder was baked by standing in an electric furnace at 250 ° C. for 2 hours and 450 ° C. for 2 hours, and finally fluidly baked at 560 ° C. for 3 hours to obtain a catalyst.
The obtained catalyst was subjected to an activity test.

[Example 3-2]
In order to confirm reproducibility, a catalyst having the same composition as in Example 3 was produced in the same manner as in Example 3, and an activity test was performed.

[Example 4]
The composition is Mo ₁₂ Bi _0.4 Fe _1.5 K _0.1 Rb _0.06 Co ₁ Ni ₅ Ba _0.2 Mn _0.5 Cr _0.7 W _0.3 Ce _0.7 Sm _0.1 Sb ₀ A catalyst represented by _.2 O _x (SiO ₂ ) ₆₀ was produced in the following manner.
In 650 parts of pure water, 332.6 parts of ammonium paramolybdate were dissolved (solution I).
Separately, ferric nitrate 95.1 parts, cobalt nitrate 45.7 parts, nickel nitrate 228.2 parts, barium nitrate 8.2 parts, manganese nitrate 22.5 parts, chromium nitrate 44. 0 parts, 47.7 parts of cerium nitrate, 7.0 parts of samarium nitrate, 1.6 parts of potassium nitrate, 1.4 parts of rubidium nitrate and 30.5 parts of bismuth nitrate were sequentially added and dissolved (solution J).
The temperatures of the liquid I, liquid J, 40 mass% silica sol, and 50 mass% ammonium metatungstate aqueous solution were adjusted to 40 ° C.
Under stirring, I solution, J solution, 12.3 parts of 50 mass% ammonium metatungstate aqueous solution and 4.6 parts of antimony trioxide powder were sequentially added to 1415 parts of 40 mass% silica sol to obtain an aqueous slurry.
The temperature of the resulting slurry was adjusted to 20 ° C. and held for 6 hours with stirring.
The slurry after holding was spray-dried with a rotary disk spray dryer at an inlet temperature of 270 ° C. and an outlet temperature of 180 ° C. The obtained dried powder was baked by standing in an electric furnace at 250 ° C. for 2 hours and 450 ° C. for 2 hours, and finally fluidized and fired at 600 ° C. for 3 hours to obtain a catalyst.
The obtained catalyst was subjected to an activity test.

[Comparative Example 1]
A catalyst having the same composition as in Example 2 was produced in the same manner as in Example 2 except that the slurry holding temperature was 50 ° C., and an activity test was performed.

[Comparative Example 2]
A catalyst having the same composition as in Example 2 was produced in the same manner as in Example 2 except that the aqueous slurry was obtained by setting the temperature of Liquid C and Liquid D to 10 ° C., and an activity test was performed.

[Comparative Example 3]
A catalyst having the same composition as in Example 2 was produced in the same manner as in Example 2 except that the aqueous slurry was obtained by setting the temperature of liquid C and liquid D to 80 ° C., and an activity test was performed. In addition, when C liquid was 80 degreeC, it has confirmed that white precipitation was producing | generating in C liquid.

[Comparative Example 4]
A catalyst having the same composition as in Example 3 was produced in the same manner as in Example 3 except that the slurry retention time was 0.5 hour, and an activity test was performed.

[Comparative Example 5]
A catalyst having the same composition as in Example 3 was produced in the same manner as in Example 3 except that the slurry holding temperature was 60 ° C. and the holding time was 0.5 hour, and an activity test was performed.

[Comparative Example 5-2]
In order to confirm reproducibility, a catalyst having the same composition as Comparative Example 5 was produced in the same manner as Comparative Example 5, and an activity test was performed.

As described above, all of the catalysts obtained in Examples 1 to 4 had a high yield of acrylonitrile. Moreover, the catalyst obtained in Example 3 and the catalyst obtained in Example 3-2 had substantially the same acrylonitrile yield, and it was confirmed that the same catalyst could be produced with good reproducibility.
On the other hand, although the catalysts obtained in Comparative Examples 1 to 3 had the same composition as the catalyst obtained in Example 2, the yield of acrylonitrile was lower than that in Example 2.
Moreover, although the catalyst obtained in Comparative Examples 4, 5, and 5-2 had the same composition as the catalyst obtained in Example 3, the yield of acrylonitrile was lower than that in Example 3. Further, when the catalyst obtained in Comparative Example 5 and the catalyst obtained in Comparative Example 5-2 were compared, there was a difference in the yield of acrylonitrile even though the catalyst having the same composition was produced by the same production method. It was.

Claims (3)

A catalyst for the synthesis of an aldehyde, carboxylic acid or nitrile compound by an oxidation reaction of an organic compound, a method for producing a composite oxide catalyst containing molybdenum, bismuth, iron and silica,
Mixing step of mixing a solution or slurry containing at least molybdenum and a solution or slurry containing at least bismuth and iron within a temperature range of 30 to 70 ° C. to obtain a mixed solution containing at least molybdenum, bismuth and iron When,
Holding the mixture for 2 hours or more in a temperature range of 0 to 25 ° C .;
After the holding step, a drying step of drying the mixed liquid to obtain a dried product,
A method for producing a composite oxide catalyst, comprising a firing step of firing the dried product. The method for producing a composite oxide catalyst according to claim 1, wherein the composite oxide catalyst has a composition represented by the following general formula (I).
_{Mo a Bi b Fe c A d} B e C f D g O h (SiO 2) i ... (I)
[Wherein, Mo, Bi, Fe and O represent molybdenum, bismuth, iron and oxygen, respectively, A represents at least one element selected from the group consisting of lithium, sodium, potassium, rubidium and cesium; B represents at least one element selected from the group consisting of cobalt, nickel, copper, zinc, magnesium, strontium, calcium, barium and manganese, and C represents chromium, vanadium, tungsten, niobium, zirconium, lanthanum, cerium, praseodymium Represents at least one element selected from the group consisting of neodymium and samarium, D represents at least one element selected from the group consisting of thallium, silver, boron, aluminum, indium, antimony, phosphorus and tellurium; ₂ represents silica . The symbols a, b, c, d, e, f, g, and h each represent the atomic ratio of the element with the symbol, i represents the atomic ratio of silica, and when a = 12, 0. 1 ≦ b ≦ 5, 0.1 ≦ c ≦ 10, 0.01 ≦ d ≦ 3, 2 ≦ e ≦ 12, 0.5 ≦ f ≦ 5, 0 ≦ g ≦ 5, 20 ≦ i ≦ 200, h is an atomic ratio of oxygen necessary to satisfy the valences of Mo, Bi, Fe, A, B, C, and D. ]   The method for producing a composite oxide catalyst according to claim 1 or 2, wherein the composite oxide catalyst is a catalyst for acrylonitrile synthesis by ammoxidation reaction of propylene.