JP2009207995A - Catalyst for producing unsaturated aldehyde and unsaturated carboxylic acid and its manufacturing method - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a catalyst for producing unsaturated carboxylic acid at higher selectivity while keeping the total selectivity of the objective unsaturated aldehyde and unsaturated carboxylic acid and a method for manufacturing the catalyst. <P>SOLUTION: The catalyst, which is used for producing corresponding unsaturated aldehyde and unsaturated carboxylic acid by subjecting propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether to vapor phase catalytic oxidation by using molecular oxygen, contains molybdenum, bismuth, iron and antimony at the least, at least one element (M) selected from the group consisting of cobalt, nickel, manganese, lead, calcium, magnesium, strontium, barium and zinc, and crystals of MMoO<SB>4</SB>, Fe<SB>2</SB>(MoO<SB>4</SB>)<SB>3</SB>and BiSbO<SB>4</SB>at the least. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  In the present invention, propylene, isobutylene, tertiary butyl alcohol (hereinafter also referred to as TBA) or methyl tertiary butyl ether (hereinafter also referred to as MTBE) is subjected to gas phase catalytic oxidation using molecular oxygen, respectively. The present invention relates to a catalyst used in the synthesis of an unsaturated aldehyde and an unsaturated carboxylic acid corresponding to the above and a method for producing the same.

  Acrylic acid and methacrylic acid are very useful substances as industrial raw materials. One of the industrial methods for producing acrylic acid and methacrylic acid is a direct oxidation method using propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether. In this method, a two-stage oxidation reaction is used. For example, in the synthesis of methacrylic acid, methacrolein and a small amount of methacrylic acid were oxidized mainly by oxidation of isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether in the first stage, and methacrolein formed in the first stage was oxidized in the first stage to methacrylic acid. An acid is produced.

If the methacrylic acid, which is the final product, can be produced with high selectivity as much as possible in the first stage, the efficiency of this production method will increase. For example, by increasing the conversion rate under the reaction conditions, the selectivity of methacrylic acid increases, but unnecessary CO and CO ₂ increase, resulting in a decrease in efficiency. Therefore, improvement of the catalyst is essential to improve it.

  Catalysts used for producing acrolein and acrylic acid by vapor-phase catalytic oxidation of propylene, and catalysts used for producing methacrolein and methacrylic acid by vapor-phase catalytic oxidation of isobutylene, TBA or MTBE, etc. Many reports have been made.

  Multicomponent bismuth, molybdenum, and iron-based catalysts are the most famous as catalyst components, and this structure is reported to be composed of bismuth and molybdenum oxides, II-valent metals and molybdenum oxides, iron and molybdenum oxides, etc. (Non-Patent Documents 1 and 2).

  Catalyst components other than bismuth, molybdenum, and iron are also reported. For example, a mixture of bismuth antimonate and barium molybdate has also been reported (Patent Document 1). However, in order to increase the selectivity of acrolein and methacrolein, the conversion is carried out under conditions where the conversion rate of propylene and isobutylene is low.

Japanese Patent Publication No.49-28170 M.M. W. J. et al. Wolfs, Ph. A. Batist, J.M. Catalysis, 32, 25 (1974) I. Matsuura, Proc. 7th Inter. Congr. Catalysis 2, P1099 (1981), Kodansha-Elsevier

  The object of the present invention is to provide the total selectivity of the target unsaturated aldehyde and unsaturated carboxylic acid in the gas phase catalytic oxidation of propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether using molecular oxygen. An object of the present invention is to provide a catalyst excellent in selectivity for unsaturated carboxylic acid while maintaining it, and a method for producing the same.

In the present invention, propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether is subjected to gas phase catalytic oxidation using molecular oxygen to produce the corresponding unsaturated aldehyde and unsaturated carboxylic acid, respectively. And at least one element selected from the group consisting of cobalt, nickel, manganese, lead, calcium, magnesium, strontium, barium and zinc (M) ) Containing at least MMoO ₄ , Fe ₂ (MoO ₄ ) ₃ and BiSbO ₄ .

The present invention also provides the method for producing the catalyst, wherein the catalyst is produced using BiSbO ₄ as a raw material for the bismuth and antimony.

  Further, the present invention produces unsaturated aldehyde and unsaturated carboxylic acid corresponding to each by subjecting propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether to gas phase catalytic oxidation using molecular oxygen. A method for producing an unsaturated aldehyde and an unsaturated carboxylic acid, wherein the gas phase catalytic oxidation is carried out in the presence of the catalyst.

  ADVANTAGE OF THE INVENTION According to this invention, the catalyst excellent in the unsaturated carboxylic acid selectivity and its manufacturing method can be provided, maintaining the total selectivity of the target unsaturated aldehyde and unsaturated carboxylic acid.

[catalyst]
The catalyst of the present invention can produce propylene, isobutylene, tertiary butyl alcohol or tertiary butyl ether by vapor phase catalytic oxidation using molecular oxygen to produce the corresponding unsaturated aldehyde and unsaturated carboxylic acid, respectively. . When propylene is used as a raw material, methacrolein and methacrylic acid are obtained when acrolein and acrylic acid, isobutylene, tertiary butyl alcohol or tertiary butyl ether are used as raw materials.

  The catalyst contains at least molybdenum, bismuth, iron, antimony, and at least one element (M) selected from the group consisting of cobalt, nickel, manganese, lead, calcium, magnesium, strontium, barium, and zinc. It is a complex oxide containing.

  Further, the catalyst includes at least one element selected from the group consisting of chromium, niobium, silver, tin and tantalum (hereinafter referred to as X), phosphorus, boron, sulfur, selenium, tellurium, cerium, tungsten and titanium. At least one element selected from the group consisting of (hereinafter referred to as Y), at least one element selected from the group consisting of lithium, sodium, potassium, rubidium, cesium and thallium (hereinafter referred to as Z), Silicon may be included.

  The composition of the catalyst is not particularly limited, but preferably has a composition represented by the following formula (1).

Mo _a Bi _b Fe _c Sb _{d Me} X _f Y _g Z _h Si _i O _j (1)
(In the formula, Mo, Bi, Fe, Sb, Si, and O represent molybdenum, bismuth, iron, antimony, silicon, and oxygen, respectively, a to i indicate the atomic composition ratio, and when a is 12, b is 0. 0.01 to 5, c is 0.01 to 5, d is 0.01 to 5, e is 1 to 12, f is 0 to 5, g is 0 to 5, h is 0.001 to 2, i is 0 -20, and j represents the oxygen atomic ratio necessary to satisfy the valence of the whole atom.)

  The composition of the catalyst other than oxygen can be measured by dissolving the catalyst in aqueous ammonia and analyzing it by ICP emission spectrometry or atomic absorption spectrometry. In addition, when there is a standard sample analyzed by ICP emission spectrometry or atomic absorption spectrometry, it can be calculated by comparing with the standard sample using a fluorescent X-ray analyzer.

The catalyst of the present invention contains at least crystals of MMoO ₄ , Fe ₂ (MoO ₄ ) ₃ and BiSbO ₄ . When there is no crystal of MMoO ₄ or Fe ₂ (MoO ₄ ) ₃ , the reaction rate of raw materials such as propylene is low, and the target unsaturated aldehyde and unsaturated carboxylic acid are hardly produced. Further, when BiSbO ₄ crystals are not present, the unsaturated carboxylic acid selectivity cannot be further improved while maintaining the total selectivity of unsaturated aldehyde and unsaturated carboxylic acid. In the case where a plurality of M is present, it may be at least one MMoO ₄ exists.

  The presence or absence of each crystal can be analyzed by using an X-ray diffractometer (XRD). The presence or absence of each crystal is determined by whether or not there is a peak of the XRD pattern at 2θ corresponding to the lattice plane spacing d value described in the reference recorded on an ICDD (International Center for Diffraction Data) card. However, the strength is actually strong among the d values and is confirmed at several points that do not overlap with the d values of other crystals.

Specifically, the d value of Fe ₂ (MoO ₄ ) ₃ is 4.08 ° (2θ when using a Cu tube is 21.8 °, and the values in parentheses below are the same), 3.87 ° (23. 0 °), 3.46 ° (25.7 °), and the d value of BiSbO ₄ is 3.26 ° (27.3 °), 2.90 ° (30.8 °), and 1.81 ° (50.5 °). is there. The d value of MMoO ₄ varies depending on M. For example, when M is Co, it is 3.81 ° (23.3 °), 3.36 ° (26.5 °), 3.14 ° (28.4 °). is there.

[Method for producing catalyst]
Hereafter, the manufacturing method of the catalyst in this invention is demonstrated.

  First, at least each raw material of molybdenum, bismuth, iron, antimony and the element (M) is dissolved or dispersed in water to prepare a raw material solution or slurry. The raw material to be used is not particularly limited, and nitrates, carbonates, acetates, ammonium salts, oxides, halides and the like of each element can be used in combination. As the molybdenum raw material, for example, ammonium paramolybdate, molybdenum trioxide, molybdic acid, molybdenum chloride, or the like can be used. Examples of the bismuth raw material that can be used include bismuth trioxide, bismuth nitrate, and bismuth subcarbonate. Examples of the iron raw material that can be used include ferric nitrate, iron hydroxide, and iron trioxide. As the antimony raw material, for example, antimony trioxide, antimony tetroxide, antimony pentoxide and the like can be used. The raw material of each element may be 1 type, and may use 2 or more types together.

In addition, composite oxides containing the above elements can also be used as raw materials. Examples include Bi ₂ Mo ₃ O ₁₂ , Bi ₂ Mo ₂ O ₉ , Bi ₂ MoO ₆ , Fe ₂ Mo ₃ O ₁₂ , MMoO ₄ , BiSbO ₄ , FeSbO ₄ , and M ₃ Sb ₂ O _8. Then, it is preferable to use BiSbO ₄ as a raw material for bismuth and antimony. By using BiSbO ₄ as a raw material, it is possible to produce a catalyst that can further improve the selectivity of unsaturated carboxylic acid while maintaining the total selectivity of unsaturated aldehyde and unsaturated carboxylic acid. BiSbO ₄ may be all or a part of the bismuth raw material or antimony raw material.

Although the manufacturing method of BiSbO ₄ is not particularly limited, for example, it is manufactured as follows. Bismuth trioxide as a bismuth raw material and antimony trioxide as an antimony raw material are mixed in equimolar amounts in terms of metal, calcined at 600 ° C. for 48 hours, pulverized and mixed, and further calcined at 850 ° C. for 12 hours. Is obtained.

  Next, the raw material solution or slurry is heat-treated to form a catalyst precursor. A method for heat treatment is not particularly limited, and for example, a method using a spray dryer, a slurry dryer, or a drum dryer, a method of pulverizing a lump-like dried product by evaporation to dryness, or the like can be applied. Among these, a method of obtaining dry spherical particles using a spray dryer is preferable from the viewpoint that particles are obtained simultaneously with drying and the shape of the obtained particles is a spherical shape suitable as a catalyst. Although the drying conditions vary depending on the drying method, when a spray dryer is used, the inlet temperature can be, for example, 100 to 500 ° C, and the outlet temperature can be, for example, 100 ° C or higher, preferably 105 to 200 ° C.

  The catalyst precursor thus obtained is calcined to obtain a catalyst. The calcination conditions can be performed in a temperature range of 200 to 600 ° C., for example, and the calcination time is appropriately selected depending on the target catalyst.

  Furthermore, the fired particles may be formed into a catalyst molded body. The fired particles may be molded after being supported on a support. In order to carry the fired particles on the carrier, the fired particles and the carrier component can be heated and mixed as necessary. As the carrier component, silica, alumina, silica-alumina, magnesia, titania and the like can be used.

  Furthermore, when manufacturing a catalyst molded body, as other additives, for example, organic compounds such as polyvinyl alcohol and carboxymethyl cellulose, inorganic compounds such as graphite and diatomaceous earth, inorganic fibers such as glass fibers, ceramic fibers, and carbon fibers. It may be added.

  As a method for molding the catalyst molded body, the calcined particles or the calcined particles supported on the carrier are mixed with additives to be added as necessary. Then, using a powder molding machine such as a tableting machine, an extrusion molding machine, a rolling granulator, etc., a method of molding into an arbitrary shape such as a spherical shape, a ring shape, a cylindrical shape, a star shape, etc. Can do. The molded catalyst obtained as described above may be fired again. Firing can be performed, for example, in a temperature range of usually 200 to 600 ° C.

[Method for producing unsaturated aldehyde and unsaturated carboxylic acid using catalyst]
Unsaturated aldehydes and unsaturated carboxylic acids can be produced by subjecting raw material propylene, isobutylene, TBA or MTBE to gas-phase contact reaction with molecular oxygen in the presence of the catalyst produced by the above method. For this gas phase contact reaction, it is preferable to use a tubular reactor filled with a catalyst, and a multitubular reactor can be used.

  Although it is industrially advantageous to use air as the molecular oxygen of the source gas, pure oxygen can also be mixed and used as necessary.

  It is economical to use the source gas diluted with an inert gas such as nitrogen or carbon dioxide, water vapor or the like. The concentration of propylene or the like in the raw material gas can be varied within a wide range, and can be, for example, 1 to 20% by volume, preferably 3 to 10% by volume. The molar ratio between propylene and the like in the source gas and molecular oxygen is preferably in the range of 1: 0.5-3.

  The catalyst filled in the reactor can be diluted with an inert substance such as silica, alumina, silica-alumina, silicon carbide, ceramic balls, stainless steel and the like.

  The reaction pressure is preferably from normal pressure to several atmospheres. The reaction temperature can be selected in the range of 200 to 450 ° C, but the range of 250 to 400 ° C is preferable.

  The contact time between the raw material gas and the catalyst is preferably 0.5 to 10 seconds, more preferably 1 to 5 seconds.

  Hereinafter, although the manufacture example of the catalyst of this invention and the reaction example using the catalyst are demonstrated concretely, these do not limit this invention at all. Hereinafter, in the examples, “part” means “part by mass”.

  The analysis of the raw material gas and the product was performed by gas chromatography. The atomization treatment was performed using a rotary homogenizer “TK homomixer MARKII” (trade name, manufactured by Tokushu Kika Kogyo Co., Ltd.) (hereinafter referred to as a homomixer atomizer) at a rotational speed of 12000 rpm. The average median diameter of the particles contained in the powder and the catalyst slurry was measured using a particle size distribution analyzer “SALD-7000” (trade name, manufactured by Shimadzu Corporation). The catalyst crystals were analyzed using an X-ray diffractometer "X'Pert Pro" (trade name, manufactured by Panalical). The composition of the catalyst (excluding oxygen) was measured for the catalyst dissolved in aqueous ammonia by ICP emission spectrometry and atomic absorption spectrometry.

  Moreover, the reaction rate of the raw material (isobutylene) in an Example and a comparative example, the produced | generated unsaturated aldehyde (methacrolein), unsaturated carboxylic acid (methacrylic acid), unsaturated aldehyde (methacrolein), and unsaturated carboxylic acid (methacrylic acid) Acid) total selectivity (hereinafter referred to as total selectivity) was calculated by the following equation.

Raw material reaction rate (%) = A / B × 100
Selectivity of unsaturated aldehyde (%) = C / A × 100
Selectivity of unsaturated carboxylic acid (%) = D / A × 100
Total selectivity (%) = (C + D) / A × 100.

  Here, A is the number of moles of reacted raw material (isobutylene), B is the number of moles of supplied raw material (isobutylene), C is the number of moles of generated unsaturated aldehyde (methacrolein), and D is the generated unsaturated carboxylic acid It is the number of moles of (methacrylic acid).

[Example 1]
[Preparation of BiSbO ₄ ]
10.0 parts of bismuth trioxide and 6.2 parts of antimony trioxide were mixed and baked in air at 600 ° C. for 24 hours. After mixing, it was further calcined in air at 850 ° C. for 12 hours, and the resulting mass was pulverized to obtain a powder having an average particle size of 37 μm.

When the obtained powder was measured by XRD, a pattern peculiar to BiSbO ₄ was mainly confirmed.

[Preparation of catalyst]
Prepared in advance to 500 parts of pure water at 60 ° C., 500 parts of ammonium paramolybdate, 12.4 parts of ammonium paratungstate, 23.0 parts of cesium nitrate, 13.7 parts of antimony trioxide, 11.0 parts of bismuth trioxide 37.3 parts of BiSbO ₄ was added and stirred to obtain Liquid A. Separately, 1000 parts of pure water at room temperature, 209.8 parts of ferric nitrate, 75.5 parts of nickel nitrate, 453.3 parts of cobalt nitrate, 31.3 parts of lead nitrate, and 85 mass% phosphoric acid aqueous solution 5.6 parts were sequentially added and dissolved to obtain a liquid B (raw material solution).

  Liquid B was added to and mixed with liquid A, and atomization was performed with the homomixer atomizer at a rotational speed of 12000 rpm until the average median diameter became 3.5 μm, to obtain a catalyst precursor. Thereafter, this catalyst precursor slurry was aged for 1.5 hours while being heated to 95 ° C. and stirred, and then spray-dried with a spray dryer equipped with a rotating disk type centrifugal atomizer. At this time, the atomizer rotation speed of the spray dryer was 11000 rpm, the inlet temperature was 165 ° C., and the outlet temperature was 125 ° C.

The dried spherical particles thus obtained were calcined for 1 hour at 300 ° C. in an air atmosphere using a rotary kiln to form catalyst calcined powder, and the catalyst calcined powder was pressure-molded and crushed. Among the crushed particles, particles that passed through a sieve having an aperture of 2.36 mm and did not pass through a sieve having an aperture of 0.71 mm were obtained. Thereafter, the particles having a specific size thus classified were calcined again at 500 ° C. for 6 hours in an air atmosphere to obtain a catalyst. The composition of elements other than oxygen in the obtained catalyst was Mo ₁₂ W _0.2 Bi _0.6 Fe _2.2 Sb _0.8 Ni _1.1 Co _6.6 Pb _0.4 P _0.2 Cs _0.5 . Moreover, the presence of CoMoO ₄ , Fe ₂ (MoO ₄ ) ₃ , and BiSbO ₄ crystals was confirmed by XRD measurement.

  10 g of this catalyst was packed into a stainless steel reaction tube having an inner diameter of 15 mm. Supply a source gas of 5% isobutylene (raw material), 12% molecular oxygen, 10% water vapor and 73% (volume%) nitrogen, and supply isobutylene under conditions of normal pressure, contact time of 2.6 seconds, and reaction temperature of 340 ° C. Gas phase catalytic oxidation with molecular oxygen. As a result, the reaction rate of isobutylene was 98.5%, the selectivity of methacrolein was 88.8%, the selectivity of methacrylic acid was 4.3%, and the total selectivity of methacrolein and methacrylic acid was 93.1%.

[Comparative Example 1]
A catalyst was prepared in the same manner as in Example 1 except that 27.4 parts of antimony trioxide, 33.0 parts of bismuth trioxide were added, and BiSbO ₄ was not added.

According to XRD measurement, the presence of crystals of CoMoO ₄ and Fe ₂ (MoO ₄ ) ₃ was confirmed in the catalyst, but the presence of crystals of BiSbO ₄ was not confirmed. The composition of elements other than oxygen in the catalyst was the same as in Example 1.

  The reaction was evaluated under the same conditions as in Example 1 except that this catalyst was used and the contact time was 3.6 seconds. As a result, the reaction rate of isobutylene was 98.1%, the selectivity of methacrolein was 90.5%, the selectivity of methacrylic acid was 2.5%, and the total selectivity of methacrolein and methacrylic acid was 93.0%. The total selectivity of methacrolein and methacrylic acid was almost the same as in Example 1, but the selectivity of methacrylic acid was about 60% lower than that in Example 1.

[Comparative Example 2]
The reaction was evaluated under the same conditions as in Comparative Example 1 except that the contact time was 7.2 seconds. As a result, the reaction rate of isobutylene was 100%, the selectivity of methacrolein was 77.6%, the selectivity of methacrylic acid was 5.1%, and the total selectivity of methacrolein and methacrylic acid was 82.7%. Although the selectivity of methacrylic acid was higher than in the examples, the total selectivity of methacrolein and methacrylic acid was remarkably low.

[Comparative Example 3]
A solution A was obtained by adding 500 parts of ammonium paramolybdate to 2000 parts of pure water at 60 ° C. and stirring to dissolve. Separately from this, 247 parts of barium nitrate was added to 8000 parts of pure water at room temperature and dissolved by stirring to obtain Liquid B.

Liquid B was added to liquid A and mixed, and then most of the water was evaporated. The obtained cake-like substance was dried at 120 ° C. for 16 hours, pulverized, and baked at 540 ° C. for 16 hours. Equal amounts of the obtained powder and BiSbO ₄ obtained in Example 1 were mixed, the catalyst calcined powder was pressure-molded and crushed, among these crushed particles, passed through a sieve with an aperture of 2.36 mm, And what did not pass a sieve with an aperture of 0.71 mm was obtained.

The presence of BaMoO ₄ and BiSbO ₄ was confirmed by XRD measurement, but Fe ₂ (MoO ₄ ) ₃ was not confirmed. The composition of elements other than oxygen in the catalyst was Mo ₁₂ Bi ₁₆ Ba ₁₂ Sb ₁₆ .

  The reaction of the catalyst thus obtained was evaluated under the same conditions as in Example 1 except that the contact time was 10.0 seconds. As a result, the reaction rate of isobutylene was 5.4%, the selectivity of methacrolein was 78.5%, the selectivity of methacrylic acid was 0.0%, and the total selectivity of methacrolein and methacrylic acid was 78.5%. Compared to Example 1, the reaction rate, methacrolein selectivity, and methacrylic acid selectivity were all significantly lower. In particular, no methacrylic acid was produced.

  As described above, the catalyst of the present invention can produce an unsaturated carboxylic acid with high selectivity while maintaining the total selectivity of the target unsaturated aldehyde and unsaturated carboxylic acid.

Claims (3)

Used in the production of the corresponding unsaturated aldehydes and carboxylic acids by vapor phase catalytic oxidation of propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether with molecular oxygen. A catalyst containing at least molybdenum, bismuth, iron, antimony and containing at least one element (M) selected from the group consisting of cobalt, nickel, manganese, lead, calcium, magnesium, strontium, barium and zinc A catalyst containing at least crystals of MMoO ₄ , Fe ₂ (MoO ₄ ) ₃ and BiSbO ₄ . 2. The method for producing a catalyst according to claim 1, wherein the catalyst is produced using BiSbO ₄ as a raw material for the bismuth and antimony. A process for producing unsaturated aldehydes and unsaturated carboxylic acids corresponding to propylene, isobutylene, tertiary butyl alcohol or methyl tertiary butyl ether by vapor phase catalytic oxidation using molecular oxygen, respectively. ,
A method for producing an unsaturated aldehyde and an unsaturated carboxylic acid, wherein the gas phase catalytic oxidation is carried out in the presence of the catalyst according to claim 1 or 2.