JP6238354B2 - Catalyst for producing unsaturated aldehyde and / or unsaturated carboxylic acid, method for producing the same, and method for producing unsaturated aldehyde and / or unsaturated carboxylic acid - Google Patents

Description

The present invention relates to the production of a corresponding unsaturated aldehyde and / or unsaturated carboxylic acid by subjecting an alkene to gas phase catalytic partial oxidation with molecular oxygen or a molecular oxygen-containing gas in the presence of a catalyst containing molybdenum and bismuth. The present invention relates to a catalyst used and a method for producing the same, and a method for producing an unsaturated aldehyde and / or an unsaturated carboxylic acid using the catalyst.

Various problems arise when acrolein and acrylic acid are produced industrially by subjecting propylene to gas phase catalytic partial oxidation with molecular oxygen. As one of them, it is known that the deterioration of the catalyst accelerates as the temperature to which the composite metal oxide catalyst (hereinafter referred to as “catalyst”) is exposed increases. It is also widely known that an excessive oxidation reaction occurs and the yield of the target product is lowered. Therefore, in order to increase the productivity of the target product, it is necessary to increase the concentration of the raw material and the space velocity, and accordingly increase the reaction bath temperature. However, as described above, when the reaction bath temperature is high, there is a problem that the catalyst life is shortened. Furthermore, since the gas phase partial oxidation of propylene or the like is an exothermic reaction, a local high temperature portion (hot spot) is generated in the catalyst layer, and the catalyst deterioration and the yield reduction become remarkable. Various proposals have been made in the prior art for these problems. For example, Japanese Patent Application Laid-Open No. 2001-226302 (Patent Document 1) prepares a plurality of types of catalysts having different occupied volumes, firing temperatures, and / or types and / or amounts of alkali metal elements, and multitubular oxidation reaction. Describes a method of suppressing the hot spot temperature by filling the tube so that the activity increases from the source gas inlet toward the outlet in the direction of the tube axis of the vessel. This method is intended to suppress excessive heat generation by filling a catalyst with reduced activity on the inlet side where a high-concentration source gas is introduced. However, in the activity adjustment based on the occupied volume, the size of the occupied volume of the catalyst is limited by the diameter of the reaction tube, so that a sufficient effect may not be obtained, or the reaction field designed by uniformly filling the catalyst may not be achieved. It may not be realized and sufficient catalyst performance may not be exhibited. In JP-A-6-192144 (Patent Document 2), the hot spot temperature at the raw material gas inlet side is increased by increasing the amount of catalyst supported from the raw material gas inlet side to the outlet side to rank the catalyst activity. In the outlet side filled with a highly active catalyst, a gas phase catalytic partial oxidation reaction is reached up to the conversion rate of the raw material required for the process. However, the catalyst on the raw material gas inlet side, which has a low loading amount, has a short life, while the catalyst on the raw material gas outlet side has a large amount of active component, so the reaction heat is stored in the catalyst by thickening the layer of the catalytic active component. However, there is a problem that selectivity is lowered. Moreover, according to Japanese Patent Publication No. 2007-511565 (Patent Document 3), by using a ring-shaped catalyst, a hot spot temperature is suppressed and a method capable of dealing with a reaction under a high load condition is described. However, ring-shaped catalysts are difficult to pack uniformly due to the characteristics of the shape when packed into a multi-tubular oxidation reactor, and because of the low mechanical strength due to the characteristics of the molding method, the catalyst collapses. It is a big problem that not only the reaction performance tube is clogged but also the catalytic activity is not sufficiently exhibited due to the catalyst active component falling off. Furthermore, in Japanese Patent Application Laid-Open No. 2001-048817 (Patent Document 4), a catalyst in which the amount of bismuth and iron is changed in a reaction zone provided by dividing the catalyst layer in each reaction tube into two or more layers in the tube axis direction. By filling the raw material gas inlet to the outlet so that the total amount of bismuth and iron decreases, the sublimation of the molybdenum component is suppressed, and acrolein and acrylic acid are produced in a stable and high yield over a long period of time. Techniques to do this are disclosed.

JP 2001-226302 A JP-A-6-192144 Special table 2007-511565 gazette JP 2001-048817 A

Some of the processes for producing the corresponding unsaturated aldehydes and / or unsaturated carboxylic acids by the gas-phase catalytic partial oxidation reaction of alkenes have already been partially industrialized, but further improvements in catalyst performance and usage are required. ing. When using a multi-tubular oxidation reactor to produce a large amount of the corresponding unsaturated aldehyde and / or carboxylic acid from the alkene, the supply load of the alkene per unit catalyst volume is increased, and the reaction bath temperature must be increased. Occurs. As a result, the temperature in the catalyst layer is raised, and the yield of the target product is lowered by bringing about a decrease in catalytic activity and / or selectivity over time. It becomes. Improvement in the activity of the catalyst makes it possible to lower the reaction bath temperature, lower the running cost, and extend the life of the catalyst, and improving the yield of the target product can greatly reduce the production cost. In addition, if the mechanical strength of the catalyst used in the gas phase catalytic partial oxidation reaction is low, as a result of the compression molding, extrusion molding, coating molding or any other method, the catalyst can be When filling the oxidation reactor, the inside of the multi-tubular oxidation reactor is clogged due to catalyst pulverization and separation of the catalytically active component, leading to an abnormal pressure increase. In other words, a catalyst having high mechanical strength is required in order to exhibit the excellent activity and selectivity inherent in the catalyst. Furthermore, in order to lower the reaction bath temperature, a highly active catalyst is required. However, in the prior art, since the selectivity of the catalyst is greatly reduced due to the high activation of the catalyst, a highly active catalyst maintaining high selectivity is required. There are challenges in the technology of producing and combining them effectively to produce the desired product. In particular, if a highly active catalyst is not used after a thorough examination of the method of use, the hot spot temperature will be too high, leading to a decrease in yield, and may cause a runaway reaction. Therefore, the present invention provides a technique capable of producing an unsaturated aldehyde and / or unsaturated carboxylic acid, preferably acrolein and / or acrylic acid, methacrolein and / or methacrylic acid in high yield. It is aimed.

That is, the present invention
(1) A catalyst for producing an unsaturated aldehyde and / or unsaturated carboxylic acid containing molybdenum and bismuth as essential active components, wherein the composition of the catalytic active component is represented by the following general formula (I)
_{Mo 12 Bi a U b X c} Y d Z e O f (I)
(Where Mo, Bi, and O represent molybdenum, bismuth, and oxygen, U is at least one element selected from cobalt, nickel, and iron, and X is magnesium (Mg), calcium (Ca), manganese ( Mn), copper (Cu), zinc (Zn), cerium (Ce), and samarium (Sm), at least one element selected from the group consisting of boron (B), phosphorus (P), arsenic (Y) As), antimony (Sb), tungsten (W), silicon (Si) and at least one element selected from the group consisting of aluminum (Al), and Z is sodium (Na), potassium (K), rubidium ( Rb) and at least one element selected from the group consisting of cesium (Cs) are shown respectively, wherein (a) to (e) represent the atomic ratio of each component, and 0 a ≦ 10, 0 ≦ b ≦ 40, 0 ≦ c ≦ 10, 0 ≦ d ≦ 10, 0 ≦ e ≦ 6, and f is a numerical value determined by the degree of oxidation of the catalyst component. A catalyst for producing an unsaturated aldehyde and / or an unsaturated carboxylic acid, wherein the turbidity of a mixture of ammonium molybdate and water used as a molybdenum raw material is 30 NTU or less,
(2) A mixture of ammonium molybdate and water was prepared under conditions of 0 ° C. to 60 ° C., and then the mixture was mixed with other component elements and water as required to obtain a mixture, which was then dried, A process for producing an unsaturated aldehyde and / or unsaturated carboxylic acid production catalyst according to (1), which comprises a step of calcining;
(3) A process for producing an unsaturated aldehyde and / or an unsaturated carboxylic acid, characterized by subjecting an alkene to gas phase catalytic oxidation in the presence of the catalyst according to (1),
About.

By using the catalyst of the present invention, unsaturated aldehyde and / or unsaturated carboxylic acid can be produced in high yield in the production of unsaturated aldehyde and / or unsaturated carboxylic acid.

Hereinafter, the unsaturated aldehyde and / or unsaturated carboxylic acid production catalyst and the production method thereof according to the present invention will be described in detail. However, the scope of the present invention is not limited to these explanations, and the present invention is not limited to the following examples. The present invention can be changed and implemented as appropriate without departing from the spirit of the invention.

The catalyst for producing an unsaturated aldehyde and / or unsaturated carboxylic acid in the present invention is a catalyst containing molybdenum and bismuth as essential components, and the composition of the catalytically active component can be represented by the following general formula (I).
_{Mo 12 Bi a U b X c} Y d Z e O f (I)
(Where Mo, Bi, and O represent molybdenum, bismuth, and oxygen, U is at least one element selected from cobalt, nickel, and iron, and X is magnesium (Mg), calcium (Ca), manganese ( Mn), copper (Cu), zinc (Zn), cerium (Ce), and samarium (Sm), at least one element selected from the group consisting of boron (B), phosphorus (P), arsenic (Y) As), antimony (Sb), tungsten (W), silicon (Si) and at least one element selected from the group consisting of aluminum (Al), and Z is sodium (Na), potassium (K), rubidium ( Rb) and at least one element selected from the group consisting of cesium (Cs) are shown respectively, wherein (a) to (e) represent the atomic ratio of each component, and 0 a ≦ 10,0 ≦ b ≦ 40,0 ≦ c ≦ 10,0 a ≦ d ≦ 10,0 ≦ e ≦ 6, f is a numerical value determined by degree of oxidation of the catalyst component.)
Furthermore, the catalyst of the present invention is a catalyst obtained using ammonium molybdate having a turbidity of 30 NTU or less as a mixture of molybdenum raw material and water. Here, turbidity represents the degree of turbidity of water, and is classified into visual turbidity, transmitted light turbidity, scattered light turbidity, and integrating sphere turbidity. JIS K0101 (“industrial water” There are provisions in "Test methods"). In the present invention, NTU based on the formazine solution was used as a measure of turbidity. This NTU is a (Nephelometric Turbidity Units) turbidimetric turbidity unit, which is a unit of measurement when scattered light is measured using formazine as a standard solution. The turbidity (NTU) described in the present invention is 2.3% of purified water with respect to 1 part by weight of ammonium molybdate in a mixture of ammonium molybdate and water in which the concentration of ammonium molybdate is 30% by weight. After adding parts by weight and stirring at 23 ° C. for 15 minutes, it is a numerical value measured with a turbidimeter using purified water as a reference solution (though not particularly limited, it is preferable to use 2020e manufactured by LaMote).

The catalyst of the present invention is obtained by further mixing a bismuth-containing compound with a mixture of ammonium molybdate having a turbidity of 30 NTU or less and water as a catalyst for producing an unsaturated aldehyde and / or unsaturated carboxylic acid. Preferably, it is obtained by mixing a compound comprising at least one element selected from iron, cobalt, and nickel.

When ammonium molybdate having a turbidity of 30 NTU or more is used, it is presumed that molybdenum is not uniformly arranged in a catalyst containing molybdenum and bismuth, and a catalyst having excellent performance cannot be obtained.

Hereinafter, the method for producing the catalyst according to the present invention will be described more specifically.
Step a) Preparation In general, the starting materials of each element other than molybdenum constituting the catalyst are not particularly limited. As the molybdenum component material, ammonium molybdate is used. The ammonium molybdate includes a plurality of types of compounds such as ammonium dimolybdate, ammonium tetramolybdate, and ammonium heptamolybdate. Among them, ammonium heptamolybdate is preferably used. As the bismuth component raw material, bismuth salts such as bismuth nitrate, bismuth carbonate, bismuth sulfate and bismuth acetate, bismuth trioxide, metal bismuth, etc. can be used. There is a tendency to be obtained. As raw materials for iron, cobalt, nickel and other elements, oxides, nitrates, carbonates, organic acid salts, hydroxides and the like that can be converted into oxides by heat or mixtures thereof can be used. For example, when mixing ammonium molybdate and water, a high-performance catalyst can be obtained by mixing ammonium molybdate with water at 0 ° C. to 60 ° C., preferably 20 ° C. to 60 ° C. In addition, ammonium molybdate may be mixed with water under the conditions of 0 ° C to 60 ° C, and once the mixture of ammonium molybdate and water is prepared, the temperature of the mixture is adjusted to 0 ° C to 60 ° C. You may do it. When the temperature of the water to be mixed exceeds 60 ° C., ammonia that forms a complex is easily detached from the mixture of ammonium molybdate, and the catalyst performance may deteriorate. On the other hand, even if the temperature is too low, the solubility of ammonium molybdate may decrease and the catalyst performance may decrease. Further, since it takes time to dissolve ammonium molybdate, the production efficiency of the catalyst is lowered, which is not preferable. A mixture of this ammonium molybdate and water mixed with water at a desired ratio of 10 to 80 ° C. with an iron component raw material and / or a cobalt component raw material and / or a nickel component raw material, and / After mixing the Z component raw material and heating and stirring for about 1 hour under the condition of 20 ° C. to 90 ° C., add the mixture containing the bismuth component raw material and, if necessary, the X component raw material and the Y component raw material. To obtain a mixture containing the catalyst components. In the case of adding the X component and the Y component, it is preferable to use an oxide, a nitrate, a carbonate, an organic acid salt, a hydroxide or the like or a mixture thereof that can be converted into an oxide when heated. Hereinafter, these mixtures are referred to as preparation liquid (A). Here, the preparation liquid (A) does not necessarily need to contain all the catalyst constituent elements, and a part of the elements or a part thereof may be added in a step after preparation. In addition, when preparing the preparation liquid (A), the amount of water mixed with each component raw material, and when adding an acid such as sulfuric acid, nitric acid, hydrochloric acid, tartaric acid or acetic acid for mixing, the raw material dissolves. If the acid concentration in the mixture is not suitable, for example, in the range of 5 wt% to 99 wt%, the form of the preparation (A) may become a clay-like lump, which is an excellent catalyst. Must not. As the form of the preparation liquid (A), a mixture is preferable as an excellent catalyst.

Step b) Drying Next, the prepared liquid (A) obtained above is dried to obtain a dry powder. The drying method is not particularly limited as long as the preparation liquid (A) can be completely dried, and examples thereof include drum drying, freeze drying, spray drying, and evaporation to dryness. Among these, in the present invention, spray drying which can be dried from the mixture into powder or granules in a short time is particularly preferable. The drying temperature of spray drying varies depending on the concentration of the mixture, the liquid feeding speed, etc., but the temperature at the outlet of the dryer is generally 70 ° C to 150 ° C. Moreover, it is preferable to dry so that the average particle diameter of the dry powder obtained at this time may be 10 μm to 700 μm. A dry powder (B) is thus obtained.

Step c) The preliminarily calcined dry powder (B) is calcined at 200 ° C. to 600 ° C., preferably 300 ° C. to 600 ° C. under air flow, thereby improving the catalyst moldability, mechanical strength, and catalyst performance. Tend to. The firing time is preferably 1 hour to 12 hours. Thus, the pre-fired powder (C) is obtained.

Step d) Although there is no particular limitation on the molding method, a method using a tableting molding machine, an extrusion molding machine or the like is preferable when molding into a cylindrical shape or a ring shape. More preferably, it is a case of forming into a spherical shape, and the pre-fired powder (C) may be formed into a sphere with a molding machine, but the pre-fired powder (C) (including a molding aid and a strength improver if necessary). A method in which is supported on a carrier such as an inert ceramic is preferred. Here, as the loading method, a rolling granulation method, a method using a centrifugal fluidized coating apparatus, a wash coating method and the like are widely known, and particularly if it is a method capable of uniformly supporting the pre-fired powder (C) on a carrier. Although not limited, when considering the production efficiency of the catalyst and the performance of the catalyst to be prepared, it is more preferable to rotate the disk at a high speed with an apparatus having a flat or uneven disk at the bottom of the fixed cylindrical container. Thus, the carrier charged in the container is vigorously stirred by repeating the rotation and revolution of the carrier itself, and the pre-fired powder (C) and, if necessary, a molding aid and / or a strength improver are added thereto. Thus, a method in which the powder component is supported on a carrier is preferable. In addition, it is preferable to use a binder for carrying. Specific examples of the binder that can be used include water, ethanol, methanol, propanol, polyhydric alcohol, polyvinyl alcohol as a polymeric binder, silica sol aqueous solution of an inorganic binder, and the like. Ethanol, methanol, propanol, polyhydric alcohol A diol such as ethylene glycol or a triol such as glycerin is more preferable. By using an appropriate amount of an aqueous glycerin solution, the moldability becomes good, and a high-performance catalyst with high mechanical strength is obtained. Specifically, when an aqueous solution having a glycerin concentration of 5% by weight or more is used, the performance is particularly high. There is a tendency to obtain a catalyst. The amount of these binders used is usually 2 to 80 parts by weight with respect to 100 parts by weight of the pre-fired powder (C). The inert carrier is usually about 2 to 8 mm, and the pre-calcined powder (C) is supported on the inert carrier. The amount supported is a reaction condition such as a catalyst use condition, for example, a reaction material space velocity and a raw material concentration. However, it is usually 20% by weight to 80% by weight. Here, the supporting rate is expressed by the following formula (3).
Formula (3) Loading ratio (% by weight) = 100 × weight of pre-fired powder (C) used for molding / (weight of pre-fired powder (C) used for molding + weight of inert carrier used for molding)
In this way, a molded object (D) is obtained.

Step e) The fired molded body (D) tends to improve catalytic activity and selectivity by firing at a temperature of 200 ° C. to 600 ° C. for about 1 to 12 hours. The baking temperature is preferably 400 ° C. or higher and 600 ° C. or lower, and more preferably 500 ° C. or higher and 600 ° C. or lower. Since the optimal calcination temperature of catalysts having different atomic ratios is different, when the atomic ratio of the catalyst is changed, a catalyst having excellent performance tends to be obtained when calcination is performed at the optimal temperature at the atomic ratio. As the gas to be circulated, air is simple and preferable. In addition, nitrogen, carbon dioxide, nitrogen oxide-containing gas, ammonia-containing gas, hydrogen gas and mixtures thereof can be used as the inert gas. In this way, a catalyst (E) is obtained. The mechanical strength of the catalyst (E) is greatly influenced by the atomic ratio of the catalyst composition, that is, the kind of the compound produced by adjusting the atomic ratio and the phase structure of the crystal structure are different even in the same compound. receive. In addition, since the diameter of the composite metal oxide particles produced in the preparation process and the drying process, the geometric structure of the particles, and the aggregation form thereof change, the micro physical properties such as the strength of the compound crystals in the composite metal oxide For example, it is also affected by macroscopic physical property changes such as the particle size distribution of the pre-fired powder. The combined physical properties including not only the preparation method of each step but also the influence of the atomic ratio determine the mechanical strength of the catalyst finally prepared.

The catalytic gas phase oxidation reaction of alkene using the composite metal oxide obtained by this method as a catalyst is performed by using 1% by volume to 10% by volume alkene as a raw material gas composition, 5% by volume to 18% by volume molecular oxygen, 0% A temperature of 250 ° C. to 450 ° C. is applied to a catalyst prepared as described above by mixing a gas mixture of vol% to 60 vol% of water vapor and 20 vol% to 70 vol% of an inert gas such as nitrogen and carbon dioxide. under range and pressure atmospheric to 10 atmospheres, but is accomplished by introducing a feed load alkene at a space velocity of ^{60hr -1 ~200hr} -1, to more effectively exhibit the present invention is 100 hr ^-1 It is preferable to set the space velocity to ˜200 hr ⁻¹ , and it is more preferable to execute at a space velocity of 120 hr ^{−1 to} 200 hr ⁻¹ . Here, the alkene space velocity (SV ₀ ) means a raw material load. For example, when the alkene space velocity (SV ₀ ) is introduced at 100 hr ⁻¹ , the alkene is 100 times the unit catalyst volume per hour (standard state conversion). And performing a gas phase catalytic oxidation reaction. In the present invention, the alkene includes alcohols that generate alkene in the intramolecular dehydration reaction, such as tertiary butanol.

Examples have been described below with specific examples, but the present invention is not limited to the examples without departing from the gist thereof.

Example 1
Catalyst 1
1000 g of ammonium heptamolybdate having a turbidity of 6 NTU was mixed with 3800 g of pure water heated to 50 ° C. Next, 4.5 g of potassium nitrate was mixed with 51.2 g of pure water and added to the above solution. Next, 333.7 g of ferric nitrate, 714.3 g of cobalt nitrate, and 384.3 g of nickel nitrate were dissolved in 759.1 ml of pure water heated to 60 ° C. These solutions were mixed gradually with stirring. Subsequently, 97.4 g of nitric acid (60% by weight) was added to 323.1 ml of pure water, and 382.4 g of bismuth nitrate was added and completely dissolved, and the mixture was stirred and mixed. The obtained mixture was dried by a spray drying method, and the obtained dried powder was pre-baked at a maximum temperature of 440 ° C. for 6 hours. After adding 5% by weight of crystalline cellulose to the pre-fired powder and mixing well, using a 33% by weight glycerin solution as a binder by the tumbling granulation method, the diameter is 4 based on silica and alumina. A spherical support was formed on a 5 mm inert spherical carrier so that the amount supported was 50% by weight. Next, calcination was performed at 510 ° C. for 4 hours to obtain a spherical catalyst 1 having an average particle diameter of 5.2 mm of the present invention. The catalyst calculated from the charged raw materials was a composite metal oxide having the following atomic ratio.
Mo: Bi: Fe: Co: Ni: K = 12: 1.7: 1.8: 5.2: 2.8: 0.1

Comparative Example 1
Catalyst 2
A comparative catalyst 2 was obtained by using a catalyst 1 having a turbidity of 47 NTU of a mixture of ammonium heptamolybdate and water.

Comparative Example 2
Catalyst 3
The catalyst 3 for comparison was obtained by using the catalyst 1 having a turbidity of a mixture of ammonium heptamolybdate and water of 105 NTU.

Example 2
In a jacket for causing alumina powder to flow by air as a heat medium, 68 ml of catalyst 1 was filled in a stainless steel reactor having an inner diameter of 22.2 mm, and the reaction bath temperature was 327 ° C. Here, a gas in which the supply amounts of propylene, air, and water are set so that the raw material molar ratio is propylene: oxygen: nitrogen: water = 1: 1.7: 6.4: 3.0 at a space velocity of 862 h ⁻¹ . Table 1 shows the results of introduction into the oxidation reactor and determination of the acrolein yield and acrylic acid yield.

Comparative Example 3
Table 1 shows the results of carrying out the oxidation reaction of propylene in the same manner as in Example 2 except that the catalyst was changed to the catalyst 2, and obtaining the acrolein yield and the acrylic acid yield.

Comparative Example 4
Table 1 shows the results of carrying out the oxidation reaction of propylene in the same manner as in Example 2 except that the catalyst 3 was changed to the acrolein yield and acrylic acid yield.

Thus, in the method for producing an unsaturated aldehyde and / or unsaturated carboxylic acid by using the technique of the present invention, it becomes possible to produce the unsaturated aldehyde and / or unsaturated carboxylic acid in a high yield. .

Claims (4)

A process for producing an unsaturated aldehyde and / or unsaturated carboxylic acid production catalyst comprising molybdenum and bismuth as essential active ingredients, wherein the composition of the catalytic active ingredient is represented by the following general formula (I)
_{Mo 12 Bi a U b X c} Y d Z e O f (I)
(Where Mo, Bi, and O represent molybdenum, bismuth, and oxygen, U is at least one element selected from cobalt, nickel, and iron, and X is magnesium (Mg), calcium (Ca), manganese ( Mn), copper (Cu), zinc (Zn), cerium (Ce), and samarium (Sm), at least one element selected from the group consisting of boron (B), phosphorus (P), arsenic (Y) As), antimony (Sb), tungsten (W), silicon (Si) and at least one element selected from the group consisting of aluminum (Al), and Z is sodium (Na), potassium (K), rubidium ( Rb) and at least one element selected from the group consisting of cesium (Cs) are shown respectively, wherein (a) to (e) represent the atomic ratio of each component, and 0 a ≦ 10, 0 ≦ b ≦ 40, 0 ≦ c ≦ 10, 0 ≦ d ≦ 10, 0 ≦ e ≦ 6, and f is a numerical value determined by the degree of oxidation of the catalyst component. A mixture of ammonium molybdate and water is prepared, and the iron component raw material and / or cobalt component raw material and / or nickel component raw material is mixed with water under conditions of 10 ° C. or higher and 80 ° C. or lower to the mixture satisfying a turbidity of 30 NTU or lower. After mixing, the method further comprises the steps of adding a bismuth component raw material and then optionally preparing a mixture containing the X component raw material and / or the Y component raw material, drying, pre-baking, molding, and baking. A method for producing a catalyst for producing an unsaturated aldehyde and / or an unsaturated carboxylic acid. A mixture of ammonium molybdate and water satisfying a turbidity of 30 NTU or less according to claim 1 with an iron component raw material and / or a cobalt component raw material and / or a nickel component raw material and / or a Z component raw material at 20 ° C or higher and 90 ° C or lower. Bismuth component raw material is added after mixing with water under the above conditions, and then a mixture is optionally prepared by adding X component raw material and / or Y component raw material, followed by drying, pre-baking, molding, and baking The manufacturing method of the catalyst for unsaturated aldehyde and / or unsaturated carboxylic acid production characterized by including the process to carry out. The method for producing a catalyst for producing an unsaturated aldehyde and / or unsaturated carboxylic acid according to claim 1 or 2, wherein a mixture of ammonium molybdate and water is prepared under conditions of 0 to 60 ° C. A method for producing an unsaturated aldehyde and / or an unsaturated carboxylic acid, comprising subjecting an alkene to gas phase catalytic oxidation in the presence of the catalyst obtained by the production method according to any one of claims 1 to 3.