JP2007000803A - Catalyst for synthesizing unsaturated aldehyde and unsaturated carboxylic acid - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a catalyst which is used for catalytically oxidizing a reactive raw material of a vapor phase by molecular oxygen to produce an objective substance in high yield and has high mechanical strength and to provide a method for manufacturing the catalyst and a method for producing unsaturated aldehyde and unsaturated carboxylic acid. <P>SOLUTION: The catalyst to be used for catalytically oxidizing propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether of a vapor phase by molecular oxygen to synthesize unsaturated aldehyde and unsaturated carboxylic acid contains a catalyst component containing molybdenum and bismuth and a scaly inorganic substance having 10 μm to 2 mm average particle size and the average thickness of 0.005-0.3 times of the average particle size. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  In the present invention, propylene, isobutylene, tertiary butyl alcohol (hereinafter also abbreviated as “TBA”) or methyl tertiary butyl ether (hereinafter also abbreviated as “MTBE”) is vapor-phased with molecular oxygen. Catalyst used for synthesizing unsaturated aldehyde and unsaturated carboxylic acid by catalytic oxidation (hereinafter also simply referred to as "catalyst"), method for producing the catalyst, and method for producing unsaturated aldehyde and unsaturated carboxylic acid About.

Propylene, isobutylene, TBA or MTBE (hereinafter collectively referred to as “reaction raw materials”) are vapor-phase catalytically oxidized with molecular oxygen to produce unsaturated aldehydes and unsaturated carboxylic acids (hereinafter collectively referred to as “objectives”). As a catalyst for producing a product, a composite oxide catalyst containing molybdenum and bismuth is known. For example, Patent Document 1 discloses a catalyst containing molybdenum and bismuth molded into a ring shape and containing inorganic fibers. It is also disclosed that as the inorganic fiber, at least one selected from glass fiber, alumina fiber and silica fiber having an average fiber length of 50 μm to 1.5 mm and an average diameter of 2 μm to 20 μm can be used.
JP 2002-273229 A

  However, the catalyst obtained by this method does not necessarily have a sufficient yield of the target product, and the mechanical strength is not always sufficient. Therefore, further improvement is desired from an industrial point of view.

  The present invention provides a catalyst having a high mechanical strength, a catalyst having a high mechanical strength, a method for producing the catalyst, an unsaturated aldehyde, and an unsaturated carboxylic acid. It aims at providing the manufacturing method of.

  That is, the present invention relates to a catalyst for synthesizing an unsaturated aldehyde and an unsaturated carboxylic acid by vapor-phase catalytic oxidation of propylene, isobutylene, TBA or MTBE with molecular oxygen and comprising a catalyst component containing molybdenum and bismuth. The catalyst contains a flaky inorganic substance having an average particle diameter of 10 μm to 2 mm and an average thickness of 0.005 to 0.3 times the average particle diameter.

  The present invention also provides a fired product obtained by drying and then firing a solution or slurry containing a catalyst raw material, and an average particle diameter of 10 μm to 2 mm and an average thickness of 0.005 to 0.3 of an average particle diameter. It is the manufacturing method of the said catalyst including the process which mixes and shape | molds a double scale-like inorganic substance.

  Furthermore, the present invention is a method for producing an unsaturated aldehyde and an unsaturated carboxylic acid in which propylene, isobutylene, TBA or MTBE is vapor-phase catalytically oxidized using molecular oxygen in the presence of the catalyst.

  According to the present invention, a target material can be produced in a high yield by vapor-phase catalytic oxidation of a reaction raw material with molecular oxygen, and a catalyst having high mechanical strength, a method for producing the catalyst, and an unsaturated aldehyde and unsaturated compound A method for producing a carboxylic acid can be provided.

  The catalyst of the present invention is a catalyst for synthesizing a target product by vapor-phase catalytic oxidation of propylene, isobutylene, TBA or MTBE with molecular oxygen, comprising a catalyst component containing molybdenum and bismuth and a specific scale-like inorganic substance It contains. In addition to molybdenum and bismuth, the catalyst components include, for example, iron, silicon, cobalt, nickel, chromium, lead, manganese, calcium, magnesium, niobium, silver, barium, tin, tantalum, zinc, phosphorus, boron, sulfur, Selenium, tellurium, cerium, tungsten, antimony, titanium, lithium, sodium, potassium, rubidium, cesium, thallium and the like may be contained.

As a catalyst component containing molybdenum and bismuth, those having the composition of the following formula (1) are preferable.
_{Mo a Bi b Fe c A d} X e Y f Z g Si h O i (1)
(In the formula (1), Mo, Bi, Fe, Si and O are molybdenum, bismuth, iron, silicon and oxygen, respectively, and the A element is at least one element selected from the group consisting of cobalt and nickel. The element is at least one element selected from the group consisting of chromium, lead, manganese, calcium, magnesium, niobium, silver, barium, tin, tantalum and zinc, and the Y element is phosphorus, boron, sulfur, selenium, tellurium, At least one element selected from the group consisting of cerium, tungsten, antimony and titanium, and Z element represents at least one element selected from the group consisting of lithium, sodium, potassium, rubidium, cesium and thallium, respectively. A, b, c, d, e, f, g, h and i represent the atomic ratio of each element, and a = 2 when b = 0.01-3, c = 0.01-5, d = 1-12, e = 0-8, f = 0-5, g = 0.001-2, h = 0-20. And i is an atomic ratio of oxygen necessary to satisfy the valence of each component.)

  In the composition of the formula (1), molybdenum, bismuth, iron, A element, Z element and oxygen are essential elements, and X element, Y element and silicon are optional elements. b is preferably 0.05-2. c is preferably 0.05-4. d is preferably 2 to 10. g is preferably 0.01 to 1.5. The atomic ratio (a and b to h) of each element in the target catalyst is arbitrarily set within the above range by adjusting the blending ratio of the raw materials for the catalyst components described below (hereinafter also referred to as “catalyst raw materials”). can do. The composition other than oxygen of the catalyst component (excluding additives such as scale-like inorganic substances from the catalyst) can be analyzed, for example, by dissolving the catalyst in aqueous ammonia by ICP emission spectrometry and atomic absorption spectrometry.

  In the present invention, the scale-like inorganic substance (hereinafter also referred to as “scale-like substance”) means a so-called scale-like inorganic substance called a flake shape or a flake shape. Scales have an average particle size in the range of 10 μm to 2 mm and an average thickness in the range of 0.005 to 0.3 times the average particle size. The average particle size of the scales is preferably in the range of 30 μm to 1 mm, more preferably in the range of 70 μm to 500 μm. The average thickness of the scales is preferably in the range of 0.007 to 0.2 times the average particle size, and more preferably in the range of 0.01 to 0.1 times the average particle size. The average particle diameter was measured on a volume basis by a laser diffraction method, and the average thickness was measured by observing 50 randomly extracted scales with an electron microscope.

  The average particle size of the scales is that in the produced catalyst, and it is preferable to produce the catalyst using scales having an average particle size of 10 μm to 2 mm, but the scales have an average particle size of 10 μm in the process of producing the catalyst. In the case of refining to ˜2 mm, the catalyst can be produced using scales having an average particle diameter exceeding 2 mm. Examples of the latter method include a method in which a scale component is cut by mixing a catalyst component, a precursor of the catalyst component, a catalyst raw material, and the like, and then vigorously stirring. However, in the latter case, the former method is preferred because the scales may not be uniformly dispersed in the catalyst.

  The component of the scale is not particularly limited as long as it is inorganic, and examples thereof include glass, alumina, silica, ceramic, carbon, etc. Among them, glass, alumina, and silica are preferable in terms of the yield of the target product, and particularly glass. Is preferred.

  One type of scaly object may be used, or two or more types may be used in appropriate combination. Examples of combinations of two or more types of scales include combinations of scales of different types, combinations of scales of the same type with different average particle sizes and thicknesses, and types of scales having different compositions such as glass composition. Combinations, combinations of scales of different components, and the like can be mentioned.

  The amount of scales contained in the catalyst is 0.1 to 15 parts by mass, preferably 1 to 10 parts by mass, and more preferably 3 to 8 parts by mass with respect to 100 parts by mass of the catalyst component. The greater the amount of scales, the more the mechanical strength tends to improve, and the smaller the amount, the greater the amount of catalyst component that can be charged into the reactor.

  The catalyst of this invention can be manufactured according to the method generally used for preparation of the catalyst for manufacture of a well-known unsaturated aldehyde and unsaturated carboxylic acid except the point which adds a scale thing.

  For example, a mixture obtained by mixing a catalyst component obtained by drying and / or calcining a catalyst raw material solution or slurry (hereinafter also referred to as “catalyst raw material liquid”) or a precursor thereof and molding a mixture is formed. A method of baking after the catalyst component precursor obtained by drying a catalyst material solution obtained by adding a scale material to a catalyst raw material solution, and drying and baking a catalyst material solution obtained by adding a scale material Examples include a method of molding the obtained catalyst component. Here, the catalyst component is a fired product, and the precursor of the catalyst component is a dried product of a catalyst raw material liquid containing molybdenum and bismuth.

  The method for preparing the catalyst raw material liquid is not particularly limited, and various methods such as a well-known precipitation method and oxide mixing method can be used as long as the components are not significantly unevenly distributed. As the catalyst raw material used for the preparation of the catalyst raw material liquid, oxides, sulfates, nitrates, carbonates, hydroxides, ammonium salts, halides, organic acid salts, alkali metal salts, and the like of each element can be used. . For example, examples of the molybdenum raw material include ammonium paramolybdate and molybdenum trioxide. The raw material of the catalyst component may be used alone or in combination of two or more for each element. Examples of the liquid mixed with the catalyst raw material when preparing the catalyst raw material liquid include organic solvents such as water, alcohols, ketones, and hydrocarbons, but water is preferable from the viewpoint of handleability. That is, the catalyst raw material liquid is preferably an aqueous solution or an aqueous slurry.

  The method for drying the catalyst raw material liquid is not particularly limited, and examples thereof include a method of drying using a spray dryer, a method of drying using a slurry dryer, a method of drying using a drum dryer, and a method of evaporating to dryness. Applicable. Among these, it is preferable to obtain dry spherical particles using a spray dryer because particles can be obtained simultaneously with drying, and the obtained particles have a spherical shape. Although the drying conditions vary depending on the drying method, when a spray dryer is used, the inlet temperature is preferably 100 to 500 ° C, and the outlet temperature is preferably 100 ° C or higher, more preferably 105 to 200 ° C.

  The dried product thus obtained may contain a salt such as nitric acid derived from the catalyst raw material, etc., and if the dried product is molded and then baked, the strength of the molded product may decrease due to decomposition of the salt. is there. For this reason, it is preferable to fire and form before forming. The firing conditions are not particularly limited, and known firing conditions can be applied. Calcination is preferably performed in the temperature range of 200 to 600 ° C. in the presence of oxygen, air, nitrogen, nitrogen oxides, etc., and the calcination time is appropriately selected depending on the target catalyst.

  The method of mixing the catalyst component or its precursor and the scale is not particularly limited, and examples thereof include a method using a double-arm kneader, a ribbon mixer, a Henschel mixer, etc., among which a double-arm kneader and a ribbon mixer are used. It is preferable to use it.

  The method for adding the scales is not particularly limited, and any method can be used as long as the scales can be dispersed and contained in the finished catalyst. In addition, scales may be added all at once, but for example, a part may be added to the catalyst raw material liquid and the remainder added to the catalyst component obtained by calcination. Good.

  The molding method is not particularly limited, and examples thereof include known methods such as extrusion molding, tableting molding, support molding, and rolling granulation. Of these, the tableting molding method and the extrusion molding method are preferred because of the high productivity of the catalyst. The shape of the molded product is not particularly limited, and examples thereof include a spherical shape, a cylindrical shape, a ring shape (cylindrical shape), and a star shape. Among them, a spherical shape, a cylindrical shape, and a ring shape with high mechanical strength are preferable. In the case of a ring shape, it has a through-hole in the vertical direction whose outer diameter is 3 to 10 mm, whose length is 0.5 to 2 times the outer diameter, and whose inner diameter is 0.1 to 0.7 times the outer diameter Is preferred. At the time of molding, polyvinyl alcohol, stearic acid, ammonium nitrate, graphite, water, alcohol and the like generally used as a molding aid can be used as necessary.

  The obtained molded product is preferably fired, but may be omitted if it is fired before molding. When omitted, this molded product is a catalyst, and when fired, the fired product is a catalyst. The firing method is not particularly limited, and known treatment methods and conditions can be applied. The firing conditions vary depending on the raw material compound used, the composition of the catalyst components, the preparation method, and the like, but are preferably 200 to 600 ° C. and 0.5 hours or longer under the flow of an oxygen-containing gas such as air or an inert gas. Here, the inert gas refers to a gas that does not decrease the reaction activity of the catalyst, and specifically includes nitrogen, carbon dioxide, helium, argon, and the like. The baking treatment may be performed using a heating device, or may be performed in a reactor after filling a molded product.

  Next, the manufacturing method of the unsaturated aldehyde and unsaturated carboxylic acid of this invention is demonstrated. In the method for producing the target product of the present invention, the target product is manufactured by vapor-phase catalytic oxidation of the reaction raw material with molecular oxygen in the presence of the catalyst of the present invention. Here, the unsaturated aldehyde and the unsaturated carboxylic acid specifically refer to acrolein and acrylic acid when the reaction raw material is propylene, and refer to methacrolein and methacrylic acid when the other reaction raw material is used. .

  The gas phase catalytic oxidation reaction is preferably performed in a fixed bed. The catalyst layer in that case is not particularly limited, and may be an undiluted layer containing only the catalyst, a diluted layer containing an inert carrier, or a single layer or a plurality of layers containing two or more different layers. In the reaction, a raw material gas containing a reaction raw material and molecular oxygen is used.

  Although the density | concentration of the reaction raw material in raw material gas is not specifically limited, 1-20 volume% is preferable. The reaction raw materials may be used singly or in combination of two or more.

Although it is economical to use air as the molecular oxygen source, air or the like enriched with pure oxygen can also be used if necessary. The molar ratio (volume ratio) of the reaction raw material and oxygen in the raw material gas is preferably in the range of 1: 0.5 to 1: 3.

  The source gas preferably contains water in addition to the reaction source and molecular oxygen. The concentration of water in the raw material gas is preferably 1 to 45% by volume. The source gas is preferably diluted with an inert gas such as nitrogen or carbon dioxide.

  The reaction pressure is preferably from atmospheric pressure to several hundred kPa. The reaction temperature is preferably 200 to 450 ° C, more preferably 250 to 400 ° C. The contact time is preferably 1.5 to 15 seconds, and more preferably 2 to 10 seconds.

  Hereinafter, the present invention will be specifically described with reference to Examples and Comparative Examples. In the examples and comparative examples, “part” is part by mass, and the raw material gas and the reaction gas were analyzed by gas chromatography. Moreover, the catalyst composition was calculated | required from the preparation amount of the catalyst raw material.

The reaction rate of propylene or isobutylene in Examples and Comparative Examples (hereinafter, also simply referred to as “reaction rate”), the selectivity of the unsaturated aldehyde or unsaturated carboxylic acid to be produced, the unsaturated aldehyde and unsaturated carboxylic acid to be produced The total yield (hereinafter simply referred to as “total yield”) was calculated by the following formula.
Reaction rate (%) = A / B × 100
Selectivity of unsaturated aldehyde (%) = C / A × 100
Selectivity of unsaturated carboxylic acid (%) = D / A × 100
Yield (%) = (C + D) / B × 100
Where A is the number of moles of propylene or isobutylene reacted, B is the number of moles of propylene or isobutylene supplied, C is the number of moles of unsaturated aldehyde formed, and D is the number of moles of unsaturated carboxylic acid formed.

The falling powder rate, which is an indicator of mechanical strength, is a stainless steel cylinder with an inner diameter of 2.75 cm and a length of 6 m, which is installed so that its longitudinal direction is vertical and the lower opening is closed with a stainless steel plate. If 100 g of the catalyst is dropped from the upper opening and filled into the cylinder, and the mass of the catalyst collected by opening the lower opening and not passing through the 1 mm sieve is Xg, the falling powder rate Is calculated as follows. The smaller the falling powder rate, the higher the mechanical strength, and the higher the falling powder rate, the lower the mechanical strength.
Falling powder rate (%) = {(100−X) / 100} × 100

Example 1
To 1000 parts of pure water, 500 parts of ammonium paramolybdate, 6.2 parts of ammonium paratungstate, 23.0 parts of cesium nitrate, 27.4 parts of antimony trioxide and 33.0 parts of bismuth trioxide were added and heated and stirred. (Liquid A). Separately, add 209.8 parts of ferric nitrate, 75.5 parts of nickel nitrate, 460.2 parts of cobalt nitrate, 31.3 parts of lead nitrate, and 5.6 parts of 85% phosphoric acid to 1000 parts of pure water and dissolve. (Liquid B). After liquid B was added to liquid A to form an aqueous slurry, this aqueous slurry was formed into dry spherical particles having an average particle diameter of 60 μm by a spray dryer. The dried spherical particles were fired at 300 ° C. for 1 hour and at 510 ° C. for 3 hours to obtain a fired product.

  To 500 parts of the obtained fired product, 15 parts of hydroxypropylmethylcellulose and 10 parts of curdlan were added and dry mixed. A slurry in which 190 parts of pure water having a temperature of 5 ° C. and 25 parts of glass flakes having an average particle diameter of 140 μm and an average thickness of 5 μm were uniformly mixed was added at 1.8 L / min. After mixing (kneading) with a kneader until it becomes a clay, it is molded using a piston-type extrusion molding machine, and formed into a ring shape having an outer diameter of 5 mm, an inner diameter of 2 mm, and an average length of 5 mm. Got the body.

Subsequently, the obtained molded object was dried at 110 degreeC with the hot air dryer, and the dried product of the molded object was obtained. A dried product of this molded body was calcined again at 400 ° C. for 3 hours to produce a catalyst. The composition of the catalyst excluding the glass flakes and oxygen (hereinafter the same) is Mo ₁₂ W _0.1 Bi _0.6 Fe _2.2 Sb _0.8 Ni _1.1 Co _6.7 Pb _0.4 P _0.2 Cs was _0.5 , and the fall powdering rate was 0.3%.

  This catalyst was filled in a stainless steel reaction tube, and a raw material gas of 5% by volume of isobutylene, 12% by volume of oxygen, 10% by volume of water vapor and 73% by volume of nitrogen was used. At atmospheric pressure, a contact time of 3.6 seconds, a reaction temperature of 340 The reaction was carried out at ° C. As a result, the reaction rate of isobutylene was 98.0%, the selectivity of methacrolein was 89.9%, the selectivity of methacrylic acid was 4.1%, and the total yield was 91.2%.

(Example 2)
A catalyst was produced in the same manner as in Example 1 except that a scaly glass having an average particle size of 50 μm and an average thickness of 4 μm was used in place of the scaly glass having an average particle size of 140 μm and an average thickness of 5 μm. went. The results are shown in Table 1.

(Example 3)
A catalyst was produced and reacted in the same manner as in Example 1 except that scaly glass having an average particle diameter of 1 mm and an average thickness of 7 μm was used in place of the scaly glass having an average particle diameter of 140 μm and an average thickness of 5 μm. It was. The results are shown in Table 1.

Example 4
A catalyst was produced and reacted in the same manner as in Example 1 except that the amount of scale-like glass was changed to 50 parts. The results are shown in Table 1.

(Example 5)
A catalyst was produced and reacted in the same manner as in Example 1 except that scaly silica having an average particle size of 140 μm and an average thickness of 5 μm was used in place of the scaly glass. The results are shown in Table 1.

(Comparative Example 1)
A catalyst was produced and reacted in the same manner as in Example 1 except that 10 parts of glass fibers having an average fiber diameter of 10 μm and an average fiber length of 500 μm were used instead of 25 parts of the glass flakes. The results are shown in Table 1. Compared with Examples 1-5, the yield and the intensity | strength of the catalyst fell.

(Comparative Example 2)
A catalyst was produced and reacted in the same manner as in Example 1 except that 25 parts of the glass flakes were not mixed. The results are shown in Table 1. Compared with Examples 1-5, the yield and the intensity | strength of the catalyst fell.

(Example 6)
To 500 parts of pure water, 500 parts of ammonium paramolybdate, 6.2 parts of ammonium paratungstate, 1.4 parts of potassium nitrate, 30.9 parts of antimony trioxide and 49.5 parts of bismuth trioxide were added and heated and stirred (Liquid A). ). Separately, 114.4 parts of ferric nitrate, 288.5 parts of cobalt nitrate and 42.1 parts of zinc nitrate were sequentially added and dissolved in 1000 parts of pure water (solution B). After liquid B was added to liquid A to form an aqueous slurry, this aqueous slurry was formed into dry spherical particles having an average particle diameter of 60 μm by a spray dryer. The dried spherical particles were fired at 300 ° C. for 1 hour to obtain a fired product.

  To 500 parts of the obtained fired product, 15 parts of hydroxypropylmethylcellulose and 10 parts of curdlan were added and dry mixed. A slurry in which 190 parts of pure water having a temperature of 5 ° C. and 25 parts of glass flakes having an average particle diameter of 140 μm and an average thickness of 5 μm were uniformly mixed was added at 1.8 L / min. After mixing (kneading) with a kneader until it becomes a clay, it is molded using a piston-type extrusion molding machine, and formed into a ring shape having an outer diameter of 5 mm, an inner diameter of 2 mm, and an average length of 5 mm. Got the body.

Subsequently, the obtained molded object was dried at 110 degreeC with the hot air dryer, and the dried product of the molded object was obtained. This molded body was calcined again at 510 ° C. for 3 hours to produce a catalyst. The composition of this catalyst was Mo ₁₂ W _0.1 Bi _0.9 Fe _1.2 Sb _0.9 Co _4.2 Zn _0.6 K _0.06 , and the fall powdering rate was 0.3%. .

  This catalyst is packed in a stainless steel reaction tube, and using 5% by volume of propylene, 12% by volume of oxygen, 10% by volume of steam and 73% by volume of nitrogen, under atmospheric pressure, contact time of 3.6 seconds, reaction temperature of 310 The reaction was carried out at ° C. As a result, the reaction rate of propylene was 99.0%, the selectivity of acrolein was 91.1%, the selectivity of acrylic acid was 6.5%, and the total yield was 96.6%.

(Example 7)
The scaly glass was not mixed with pure water, but dry-mixed with 500 parts of the fired product, and 190 parts of pure water having a temperature of 5 ° C. was added to 1.8 L / min. A catalyst was produced and reacted in the same manner as in Example 6 except that the mixture was mixed at a speed of 5 k and mixed with a kneader until it became a clay-like substance. The results are shown in Table 2.

(Example 8)
A catalyst was produced and reacted in the same manner as in Example 6 except that the catalyst shape was changed to a cylindrical shape having an outer diameter of 5 mm and an average length of 5 mm. The results are shown in Table 2.

(Comparative Example 3)
A catalyst was produced and reacted in the same manner as in Example 6 except that 10 parts of glass fibers having an average fiber diameter of 10 μm and an average fiber length of 500 μm were used instead of 25 parts of the glass flakes. The results are shown in Table 2. Compared with Examples 6-8, the yield and the intensity | strength of the catalyst fell.

(Comparative Example 4)
A catalyst was produced and reacted in the same manner as in Example 6 except that the scaly glass was not mixed. The results are shown in Table 2. Compared with Examples 6-8, the yield and the intensity | strength of the catalyst fell.

Claims (3)

  Catalyst for synthesizing unsaturated aldehyde and unsaturated carboxylic acid by vapor phase catalytic oxidation of propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether with molecular oxygen, comprising molybdenum and bismuth A catalyst containing a component and a flaky inorganic substance having an average particle diameter of 10 μm to 2 mm and an average thickness of 0.005 to 0.3 times the average particle diameter.   A fired product obtained by drying and then firing a solution or slurry containing a catalyst raw material, and a scaly inorganic material having an average particle size of 10 μm to 2 mm and an average thickness of 0.005 to 0.3 times the average particle size The method for producing a catalyst according to claim 1, comprising the steps of mixing and forming the catalyst.   A process for producing an unsaturated aldehyde and an unsaturated carboxylic acid, wherein propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether is vapor-phase catalytically oxidized with molecular oxygen in the presence of the catalyst according to claim 1.