JP5020514B2 - Method for producing fluidized bed catalyst and method for producing nitriles - Google Patents

Description

  The present invention relates to a method for producing a catalyst used in a fluidized bed. The present invention also relates to a method for producing nitriles in which ammoxidation is performed in the presence of a fluidized bed catalyst.

  The fluidized bed reaction is widely practiced in the petrochemical industry, such as production of nitriles by ammoxidation reaction of organic compounds and production of high octane gasoline by fluid catalytic cracking of heavy oil.

As a method for producing a catalyst used in a fluidized bed reaction, many methods have been developed conventionally. For example, as a catalyst used for the production of nitriles, in Patent Document 1, a molybdenum compound and other raw materials are mixed at a temperature of about 66 ° C. or lower, and then spray-dried at about 537.7 ° C. or lower and calcined. A method is described.
Patent Document 2 describes a method in which a raw slurry containing an antimony compound, another catalytically active component-containing compound and a catalyst carrier raw material is spray-dried and then fluidized and fired at a temperature of 400 to 1100 ° C.
Patent Document 3 describes a method of adjusting the pH of a raw slurry containing a soluble tungsten compound, iron, cobalt and the like and silica sol to 5 or less, spray drying, and firing at 400 to 1000 ° C.
Patent Document 4 describes a method in which a raw material slurry having a solid content concentration of 40% by mass or less is spray-dried at 300 ° C. or lower, pre-fired at 250 to 500 ° C., and then post-fired at 650 to 710 ° C. ing.
Patent Document 5 describes a method of adjusting the pH of a raw material slurry containing a raw material such as iron and a molybdenum compound to 7 or more and then spray-drying and firing the slurry.
Patent Document 6 describes a method in which the pH of a solution or raw material slurry containing molybdenum and iron component raw materials is adjusted to 5 or less, heat-treated in a temperature range of 50 to 120 ° C., spray-dried, and fired. ing.
Patent Document 7 describes a method in which the pH of a raw material slurry containing iron, antimony and nitric acid is adjusted to 0.5 to 3, heat-treated, spray-dried, and fired.
Patent Document 8 describes a method of concentrating a raw slurry containing molybdenum, bismuth, iron and silica, followed by spray drying and firing.
JP 48-155783 A Japanese Patent Publication No. 50-3756 Japanese Patent Publication No.52-10431 JP 50-125984 A JP-A-2-59046 Japanese Patent Laid-Open No. 1-265067 JP-A-10-231125 JP 2002-306969 A

According to the catalyst production methods described in Patent Documents 1 to 8, although some effects were obtained in improving the yield of the target product and maintaining the reaction results over a long period of time, the level is not necessarily industrially. It was not satisfactory. Therefore, there has been a strong demand for a fluidized bed catalyst in which the target product can be stably obtained over a long period of time with a high yield. Further, industrial fluidized bed catalysts have been required to have high strength and the like from the viewpoint of handleability.
In addition, when a fluidized bed catalyst having a low yield is not obtained stably for a long time with a high yield, the productivity of the nitriles will be low. was there.

  The present invention has been made to solve these problems, and the target product can be stably obtained over a long period of time with a high yield, and also can be used to produce a fluid bed catalyst with high strength. It aims at providing the manufacturing method of a catalyst. Moreover, it aims at providing the manufacturing method of nitriles with high productivity by the contact reaction using a fluidized bed.

The method for producing a fluidized bed catalyst of the present invention comprises a raw material slurry preparation step of preparing a raw material slurry containing a catalyst raw material,
A heating step of filling the raw material slurry in a container and heating at a pressure of 300 to 50000 Pa (gauge pressure) at a heating temperature of 50 ° C. or more for 10 minutes or more;
It has the drying and baking process of spray-drying and baking the heated raw material slurry, It is characterized by the above-mentioned.
The method for producing nitriles of the present invention is characterized in that the raw organic compound is ammoxidized in the fluidized bed in the presence of the fluidized bed catalyst obtained by the fluidized bed catalyst producing method described above.

According to the method for producing a fluidized bed catalyst of the present invention, a target product can be stably obtained over a long period of time with a high yield, and a fluidized bed catalyst having high catalyst strength and the like can be produced.
According to the method for producing nitriles of the present invention, nitriles can be produced with high productivity by a catalytic reaction using a fluidized bed.

<Method for producing fluidized bed catalyst>
The method for producing a fluidized bed catalyst (hereinafter abbreviated as catalyst) of the present invention comprises a raw material slurry preparation step for preparing a raw material slurry containing a catalyst raw material, a heating step for heating the raw material slurry, and a heated raw material slurry. A drying / firing step of spray drying and baking.

(Raw material slurry preparation process)
In the raw material slurry preparation step, for example, the raw material slurry is obtained by preparing the catalyst raw material in water as it is in the solid state, or by preparing it after dissolving in water or dilute nitric acid to form a solution.
The catalyst raw material can be appropriately selected according to the compound produced by the obtained catalyst. For example, it is an oxide, or nitrate, carbonate, organic acid salt, water that can be easily converted into an oxide by ignition. Oxides, ammonium salts, etc., or mixtures thereof are preferably used. Although the catalyst raw material may be single, it is preferable that it is plural.
The catalyst raw material does not necessarily include all elements constituting the catalyst. The elements not added here may be added before the drying / firing process.

  In the raw material slurry preparation step, if necessary, the pH may be adjusted by adding nitric acid, aqueous ammonia or the like. If the pH of the raw slurry is adjusted to 5 or less before the heating step, the performance of the resulting catalyst may be improved and the target product yield may be higher.

(Heating process)
In the heating step, the raw material slurry is heated at a pressure of 300 to 50000 Pa.
When the pressure is less than 300 Pa, the effect of the present invention is not exhibited. On the other hand, even if the pressure exceeds 50000 Pa, an effect corresponding to the increase in pressure cannot be obtained, and a device having high pressure resistance is required.
A preferable lower limit of the pressure is 400 Pa, a more preferable lower limit is 500 Pa, and a preferable upper limit is 40000 Pa.
The pressure referred to here is a pressure at which atmospheric pressure (pressure in the atmosphere outside the container) is 0 Pa, that is, gauge pressure.

In order to set the pressure within the above range, for example, the raw material slurry charged in the container is heated and pressurized with water vapor generated thereby, and the water vapor in the container is exhausted using a pressure regulating valve or the like to a predetermined pressure. And a method of adjusting the pressure to the above. When the pressure in the container does not reach a predetermined range only by heating, it is preferable to apply a method of supplying pressurized air, inert gas, or the like into the container.

  The heating temperature in the heating step is 50 ° C. or higher, preferably 60 ° C. or higher, more preferably 70 ° C. or higher. When the heating temperature is lower than the lower limit, the effect of the present invention is not exhibited. The upper limit of the heating temperature is not particularly limited, but is preferably 120 ° C. or lower.

The heating time is 10 minutes or more, preferably 15 minutes or more, and more preferably 30 minutes or more. When the heating time is shorter than the lower limit value, the effect of the present invention is not exhibited. The upper limit of the heating time is not particularly limited, but even if heating is performed for more than 10 hours, the corresponding effect is not exhibited and waste is increased.
The heating time in the present invention refers to a time for maintaining the temperature after reaching a predetermined temperature.

In the heating step, in addition to heating at the predetermined pressure and temperature for a predetermined time, heating may be performed under conditions other than the pressure and temperature as necessary.

The heating step may be performed under reflux with a reflux condenser. Moreover, you may concentrate a raw material slurry by this heating process.

(Drying and firing process)
In the spray drying of the raw material slurry in the drying / firing process, for example, a rotary disk type, a nozzle type or the like can be used. The spray drying conditions are preferably selected as appropriate so as to obtain a particle size distribution preferable as a catalyst.

  The firing temperature of the dried particles obtained by the drying is preferably 200 to 1000 ° C., and the firing time is preferably 0.5 to 20 hours. There is no restriction | limiting in particular about the furnace used for baking, A box furnace, a rotary kiln, a fluidized-fired furnace, etc. can be used. Among these, a fluidized firing furnace is preferable in that it can be fired uniformly. Firing may be performed twice or more under different conditions or under the same conditions. When the calcination is performed twice or more, the activity and strength of the resulting catalyst tend to be higher.

(Composition of catalyst)
The catalyst produced by the production method of the present invention preferably has a composition represented by the following formula (I) or (II), more preferably a composition represented by the following formula (I).
When the catalyst has a composition represented by the following formula, the yield of the target product is further improved during the reaction, and the strength of the catalyst is further increased.

Fe ₁₀ Sb _i X _x Y _y Z _z O _j (SiO ₂ ) _k (I)
In the formula, Fe, Sb and SiO ₂ represent iron, antimony and silica, respectively.
X represents at least one element selected from the group consisting of vanadium, molybdenum and tungsten.
Y is magnesium, calcium, strontium, barium, titanium, zirconium, niobium, chromium, manganese, cobalt, nickel, copper, silver, zinc, boron, aluminum, gallium, indium, thallium, germanium, tin, lead, phosphorus, arsenic, It represents at least one element selected from the group consisting of bismuth and tellurium.
Z represents at least one element selected from the group consisting of lithium, sodium, potassium, rubidium, and cesium.
O represents oxygen.

The subscripts i, x, y, z, j and k represent an atomic ratio. The lower limit of i is preferably 3, more preferably 5, and the upper limit is preferably 100, more preferably 90.
The lower limit of x is preferably 0.1, more preferably 0.3, and the upper limit is preferably 15, more preferably 12.
The lower limit of y is preferably 0.1, more preferably 0.3, and the upper limit is preferably 20, more preferably 15.
The lower limit of z is 0, and the upper limit is preferably 3, more preferably 2.
j is the number of oxygen in the metal oxide formed by combining the above components.
The lower limit of k is preferably 10, more preferably 30, and the upper limit is preferably 200, more preferably 180.

_{Mo 10 Bi a Fe b C c} D d E e F f O g (SiO 2) h ··· (II)
In the formula, Mo, Bi, Fe, and Si represent molybdenum, bismuth, iron, and silicon, respectively.
C represents at least one element selected from the group consisting of nickel, cobalt, zinc, magnesium, manganese and copper.
D represents at least one element selected from the group consisting of lanthanum, cerium, praseodymium, neodymium and samarium.
E represents at least one element selected from the group consisting of lithium, sodium, potassium, rubidium and cesium.
F is calcium, strontium, barium, cadmium, titanium, zirconium, vanadium, niobium, tantalum, chromium, tungsten, germanium, tin, yttrium, aluminum, gallium, ruthenium, rhodium, palladium, rhenium, osmium, iridium, platinum, silver, It represents at least one element selected from the group consisting of boron, phosphorus, antimony and tellurium.
O represents oxygen.

The subscripts a, b, c, d, e, f, g and h represent the atomic ratio, and the lower limit of a is preferably 0.1, more preferably 0.2, and the upper limit is preferably 2.5, Preferably it is 2.
The lower limit of b is preferably 0.1, more preferably 0.3, and the upper limit is preferably 15, more preferably 12.
The lower limit of c is preferably 2, more preferably 2.5, and the upper limit is preferably 12, more preferably 10.
The lower limit of d is preferably 0.05, more preferably 0.1, and the upper limit is preferably 5, more preferably 3.
The lower limit of e is preferably 0.05, more preferably 0.07, and the upper limit is preferably 2, more preferably 1.5.
The lower limit of f is preferably 0, and the upper limit is preferably 10, and more preferably 8.
g is the number of oxygen of the metal oxide produced | generated by said each component couple | bonding.
The lower limit of h is preferably 20, more preferably 30, and the upper limit is preferably 200, more preferably 150.

  In order to make the catalyst into the composition, for example, the amount of the catalyst raw material added in the raw material slurry preparation step is appropriately selected, or the element constituting the catalyst added after the raw material slurry preparation step and before the drying and firing step is used. Examples thereof include a method of appropriately selecting the amount of the compound contained.

As described above, in the method for producing a catalyst of the present invention, since the raw material slurry containing the catalyst raw material is heated for a specific time at a specific pressure and temperature, the target product is produced in a high yield during the reaction. A catalyst obtained stably can be produced. In addition, a catalyst having high strength and suitable properties for a fluidized bed can be produced.
The catalyst obtained by the method for producing a catalyst of the present invention is suitably used for reactions in which a fluidized bed is used, for example, catalytic cracking of heavy oil, production of nitrites described later, and the like.

<Method for producing nitriles>
The method for producing nitriles of the present invention is a method in which a starting organic compound is ammoxidized in a fluidized bed in the presence of the catalyst. Here, ammoxidation is a reaction in which an organic compound is nitrified in the presence of ammonia and oxygen.
Examples of the raw material organic compound include olefins, alcohols, ethers, aromatic compounds, and heteroaromatic compounds. Specific examples include propylene, isobutene, methanol, ethanol, tertiary butanol, methyl tertiary butyl ether, toluene, xylene, picoline, and quinaldine.
Here, the nitriles obtained when propylene is ammoxidized is acrylonitrile, and the nitriles obtained when methanol is ammoxidized is hydrocyanic acid. The present invention is particularly effective for ammoxidation of propylene or methanol.
Air is preferred as the oxygen source. The air may be diluted with water vapor, nitrogen, carbon dioxide, saturated hydrocarbon, or the like, or may be enriched with oxygen in advance.

In the method for producing nitriles of the present invention, it is preferable to supply a raw material gas having a composition range of raw material organic compound / ammonia / air of 1 / 0.1 to 5/1 to 20 (molar ratio) to the catalyst.
The reaction temperature is preferably 370 to 500 ° C., the reaction pressure is preferably atmospheric pressure to 500 kPa, and the apparent contact time 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.

Example 1
Catalysts having the compositions shown in Table 1 were produced by the following procedure.
64.5 g of copper powder was dissolved in 6500 g of 63% by mass nitric acid. 6300 g of pure water was added to this solution and then heated to 60 ° C., and 566.9 g of electrolytic iron powder and 142.5 g of metal tellurium powder were added little by little and dissolved. After confirming dissolution, 885.5 g of nickel nitrate, 52.1 g of magnesium nitrate, 10.3 g of potassium nitrate, and 3.5 g of lithium nitrate were sequentially added and dissolved (solution A).
Separately, a solution (solution B) in which 265.0 g of ammonium paratungstate was dissolved in 6700 g of pure water, and a solution (solution C) in which 89.6 g of ammonium paramolybdate were dissolved in 300 g of pure water were prepared.
While stirring, 18295.6 g of 20 mass% silica sol, 4438.7 g of antimony trioxide powder, B liquid, and C liquid were sequentially added to the A liquid to obtain a raw material slurry.
To this raw material slurry, 15% by mass of ammonia water was added dropwise to adjust the pH to 2.0, and then the raw material slurry after pH adjustment was heated in a vessel at the boiling point for 3 hours under reflux. At that time, the pressure in the container was adjusted to 1280 Pa (gauge pressure).
The raw material slurry after heating was cooled to 80 ° C., and 58.5 g of 85 mass% phosphoric acid and 6.3 g of boric acid were added.
Thereafter, the raw material slurry was spray-dried by a spray dryer at a drying air temperature of 330 ° C. at the dryer inlet and 160 ° C. at the dryer outlet. Next, the obtained dry particles were calcined at 250 ° C. for 2 hours and at 400 ° C. for 2 hours, and finally fluidized and calcined at 800 ° C. for 3 hours in a fluid calcining furnace to obtain a particulate catalyst.

(Example 2)
Catalysts having the compositions shown in Table 1 were produced by the following procedure.
After 3200 g of pure water was added to 4900 g of 63 mass% nitric acid, the mixture was heated to 60 ° C., and 442.3 g of electrolytic iron powder and 202.1 g of metal tellurium powder were added and dissolved little by little. After confirming dissolution, 460.5 g of nickel nitrate, 230.5 g of cobalt nitrate, and 11.7 g of rubidium nitrate were sequentially added and dissolved (solution D).
Separately, 279.6 g of ammonium paramolybdate and 18.5 g of ammonium metavanadate were sequentially added to 5000 g of pure water and dissolved (solution E).
While stirring, 19030.1 g of 20% by mass silica sol, 4617.0 g of antimony trioxide powder, and E solution were sequentially added to the D solution to obtain a raw material slurry.
To the obtained raw material slurry, 15% by mass ammonia water was dropped to adjust the pH of the raw material slurry to 2.2, and then the raw material slurry after pH adjustment was heated in a vessel at the boiling point for 3 hours under reflux. . At that time, the pressure in the container was adjusted to 2320 Pa (gauge pressure).
The raw material slurry after heating was cooled to 80 ° C., and 19.6 g of boric acid was added.
Thereafter, the raw material slurry was spray-dried by a spray dryer at a drying air temperature of 330 ° C. at the dryer inlet and 160 ° C. at the dryer outlet. Next, the obtained dried particles were calcined at 250 ° C. for 2 hours and at 400 ° C. for 2 hours, and finally fluidly calcined at 740 ° C. for 3 hours in a fluidized calcining furnace to obtain a particulate catalyst.

(Example 3)
Catalysts having the compositions shown in Table 1 were produced by the following procedure.
140.8 g of copper powder was dissolved in 6050 g of 63% by mass nitric acid. 5900 g of pure water was added to this solution, and then heated to 60 ° C., and 495.0 g of electrolytic iron powder and 56.5 g of metal tellurium powder were added little by little and dissolved. After confirming dissolution, 113.6 g of magnesium nitrate, 86.0 g of bismuth nitrate, 17.3 g of cesium nitrate, and 4.5 g of potassium nitrate were sequentially added and dissolved (solution F).
Separately, a solution in which 125.2 g of ammonium paramolybdate was dissolved in 300 g of pure water (solution G), a solution in which 115.7 g of ammonium paratungstate was dissolved in 3000 g of pure water (solution H), and ammonium metavanadate in 3500 g of pure water. A solution (solution I) in which 7 g was dissolved was prepared.
With stirring, 20 mass% silica sol 266424.4 g, antimony trioxide powder 3229.7 g, G liquid, H liquid, and I liquid were sequentially added to the F liquid to obtain a raw material slurry.
15 mass% ammonia water was dripped at the obtained raw material slurry, pH of the raw material slurry was adjusted to 1.9, and the raw material slurry after pH adjustment was then heated at 99 ° C. for 3 hours under reflux in a container. At that time, the pressure in the container was adjusted to 620 Pa (gauge pressure).
The raw material slurry after heating was cooled to 80 ° C., and 30.7 g of 85 mass% phosphoric acid was added.
Thereafter, the raw material slurry was spray-dried by a spray dryer at a drying air temperature of 330 ° C. at the dryer inlet and 160 ° C. at the dryer outlet. Next, the obtained dried particles were calcined at 250 ° C. for 2 hours and at 400 ° C. for 2 hours, and finally fluidly calcined at 770 ° C. for 3 hours in a fluidized calcining furnace to obtain a particulate catalyst.

Example 4
Catalysts having the compositions shown in Table 1 were produced by the following procedure.
131.6 g of copper powder was dissolved in 4900 g of 63% by mass nitric acid. To this solution, 4700 g of pure water was added and then heated to 60 ° C., and 385.5 g of electrolytic iron powder and 70.5 g of metal tellurium powder were added little by little and dissolved. After confirming dissolution, 200.7 g of nickel nitrate, 110.5 g of chromium nitrate, 25.9 g of aluminum nitrate, 3.5 g of potassium nitrate, and 5.1 g of rubidium nitrate were sequentially added and dissolved (solution J).
Separately, a solution (solution K) in which 219.4 g of ammonium paratungstate was dissolved in 600 g of pure water and a solution (solution L) in which 90.1 g of ammonium paratungstate was dissolved in 2500 g of pure water were prepared.
While stirring, 12441.2 g of 20 mass% silica sol, 6036.7 g of antimony trioxide powder, K solution, and L solution were sequentially added to the J solution to obtain a raw material slurry.
15 mass% ammonia water was dripped at the obtained raw material slurry, pH was adjusted to 2.2, and the raw material slurry after pH adjustment was then heated at 99 ° C. for 3 hours under reflux in a container. At that time, the pressure in the container was adjusted to 830 Pa (gauge pressure).
Thereafter, the raw material slurry was spray-dried by a spray dryer at a drying air temperature of 330 ° C. at the dryer inlet and 160 ° C. at the dryer outlet. Next, the obtained dried particles were calcined at 250 ° C. for 2 hours and at 400 ° C. for 2 hours, and finally fluidly calcined at 750 ° C. for 3 hours in a fluidized calcining furnace to obtain a particulate catalyst.

(Comparative Example 1)
A catalyst having the same composition as in Example 1 was produced in the same procedure as in Example 1 except that the pressure in the container during heating was changed to normal pressure (0 Pa).

(Comparative Example 2)
A catalyst having the same composition as in Example 2 was produced in the same procedure as in Example 2, except that the pressure in the container during heating was changed to normal pressure (0 Pa).

(Comparative Example 3)
A catalyst having the same composition as in Example 3 was produced in the same procedure as in Example 3 except that the pressure in the container during heating was changed to normal pressure (0 Pa).

(Example 5)
Catalysts having the compositions shown in Table 2 were produced by the following procedure.
A solution (solution X) in which 3896.3 ammonium paramolybdate was dissolved in 10000 g of pure water, and a solution (solution Y) in which 288.1 g of ammonium paratungstate was dissolved in 7500 g of pure water were prepared.
Separately, 1500 g of 63 mass% nitric acid and 4000 g of pure water were mixed, and 980.7 g of ferric nitrate, 3208.7 g of nickel nitrate, 321.1 g of cobalt nitrate, 126.7 g of manganese nitrate, 383.3 g of cerium nitrate, Potassium nitrate 22.3 g, lanthanum nitrate 286.7 g, rubidium nitrate 32.5 g, chromium nitrate 706.5 g, zirconium oxynitrate 118.0 g, and bismuth nitrate 642.4 g were sequentially added and dissolved (solution Z).
Solution X, solution Y and solution Z were sequentially added to 23203.3 g of 20% by mass silica sol with stirring, and then heated at 99 ° C. for 3 hours under reflux in a container. The pressure in the container at the time of heating was adjusted to 660 Pa (gauge pressure).
The raw material slurry thus obtained was spray-dried with a spray drier at a drying air temperature of 330 ° C. at the dryer inlet and 160 ° C. at the dryer outlet, and the resulting dried particles were heated at 250 ° C. for 2 hours, 400 The particles were calcined for 2 hours and finally fluidized and calcined for 3 hours at 640 ° C. to obtain a particulate catalyst.

(Comparative Example 4)
A catalyst having the same composition as in Example 5 was produced in the same procedure as in Example 5 except that the pressure in the container during heating was changed to normal pressure (0 Pa).

  The catalysts of Examples 1 to 5 and Comparative Examples 1 to 4 were evaluated as follows. The evaluation results are shown in Table 3.

(Catalyst compressive strength test)
Using a micromesh high precision sieve, particles having a particle size of 45 to 50 μm were collected and measured for compressive strength (mN / particle). The measurement conditions were as follows.
Test device: MCTM-200 manufactured by Shimadzu Corporation
Measurement conditions: Upper pressure indenter Diamond 500 μm flat indenter
Lower pressure plate SUS plate
Loading speed 7.1 mN / sec The compressive strength in Table 3 was measured for 30 samples for each sample, and the average value was shown.

(Catalyst activity test)
The activity of the catalyst was evaluated by synthesizing acrylonitrile by propylene ammoxidation.
The catalyst is packed in a fluidized bed reactor having an inner diameter of 25 mm and a height of 400 mm, and the composition is propylene / ammonia / oxygen (supplied as air) / water vapor = 1 / 1.1 / 2.2 / 0. 5 (molar ratio) was supplied at a gas linear velocity of 4.5 cm / sec, and the reaction pressure was 200 kPa to carry out the reaction.
The reaction product was quantified using gas chromatography.
The contact time, propylene conversion rate, and acrylonitrile yield were determined by the following formula.
Contact time (second) = catalyst volume based on apparent bulk density (ml) / feed gas flow rate converted to reaction conditions (ml / second)
Propylene conversion rate (%) = (number of moles of propylene consumed in reaction / number of moles of propylene supplied) × 100
Acrylonitrile yield (%) = (number of moles of acrylonitrile produced / number of moles of propylene fed) × 100

In the methods of Examples 1 to 5 in which the raw material slurry containing the catalyst raw material was heated at a specific pressure and temperature for a specific time, acrylonitrile was obtained in a high yield in the ammoxidation of propylene, and the strength was high. A suitable catalyst could be obtained.
On the other hand, the catalysts obtained by the methods of Comparative Examples 1 to 4 that were not pressurized during the heating step were compared with Examples under the same reaction conditions (Comparative Example 1 was Example 1 and Comparative Example 2 was Example 2). Comparative Example 3 was low in acrylonitrile yield as compared with Example 3 and Comparative Example 4 as compared with Example 5. In addition, the strength of the catalyst obtained in the comparative example was low.

Claims (2)

A raw material slurry preparation step of preparing a raw material slurry containing a catalyst raw material;
A heating step of filling the raw material slurry in a container and heating at a pressure of 300 to 50000 Pa (gauge pressure) at a heating temperature of 50 ° C. or more for 10 minutes or more;
A method for producing a fluidized bed catalyst, comprising: drying and baking a heated raw material slurry and spray-drying. A method for producing a nitrile, comprising ammoxidizing a raw material organic compound in a fluidized bed in the presence of the fluidized bed catalyst obtained by the method for producing a fluidized bed catalyst according to claim 1.