WO2005115617A1

WO2005115617A1 - Catalyst mixer and catalyst mixing method

Info

Publication number: WO2005115617A1
Application number: PCT/JP2004/013465
Authority: WO
Inventors: Nariyasu Kanuka; Isao Teshigahara
Original assignee: Mitsubishi Chemical Corporation
Priority date: 2004-05-28
Filing date: 2004-09-15
Publication date: 2005-12-08
Also published as: JP2005334811A; JP4779309B2; CN1697686A

Abstract

A catalyst mixing method capable of solving problems resulting from hot spots in a gaseous phase catalytic oxidation reaction using a fixed bed multiple tube type reactor, wherein a composite oxide catalyst and an inert filler used for the gaseous phase catalytic oxidation reaction using the fixed bed multiple tube type reactor are mixed with each other by using a catalyst mixer in which a nonagitation type mixer (4) is arranged under a hopper (2). To store, in a classified state, the composite oxide catalyst and the inert filler used for the gaseous phase catalytic oxidation reaction using the fixed bed multiple tube type reactor, the inside of the hopper (2) is divided into two compartments by a partition wall (1), and the ratio of the cross section of one compartment to that of the other in the horizontal direction is made approximately equal to the ratio of the volume of the composite oxide catalyst to that of the inert filler.

Description

Specification

Catalyst mixer and catalyst mixing method

Technical field

The present invention relates to catalyst mixing, and in particular, to a mixer for mixing a composite oxide catalyst used for a gas-phase catalytic oxidation reaction using a fixed-bed multitubular reactor with an inert filler, and a mixer. The present invention relates to a mixing method and a divided package of a mixed composite oxide catalyst and an inert filler.

Background art

[0002] In the case of producing acrolein and acrylic acid from propylene using an oxidation catalyst, for example, it is conventionally known to dilute the catalyst with an inert filler. For example, Patent Document 1 discloses that the active catalyst is deactivated in order to improve the yield by increasing the flow rate of the reaction gas within a danger-free range and to prevent excessive oxidation and local overheating (hot spots). It is described to dilute with a material (inert packing) to reduce the activity of the catalyst.

[0003] However, when the catalyst and the inert filler are mixed and diluted according to such a conventional technique and used, the effect can be obtained to some extent, but the effect depends on the mixed state of the catalyst and the inert filler. It was not always satisfactory because it depends. That is, there is a problem that the effect of suppressing hot spots cannot be obtained satisfactorily because the catalyst and the inert filler are not uniformly mixed at a predetermined volume ratio. As a result, there is a need for more effective methods to adequately resolve the problems caused by hot spots. Patent Document 1 describes a mixing method and a mixed state when diluting a catalyst with an inert material, which are useful for solving such a problem.

Patent Document 1: Japanese Patent Publication No. 53-30688

Disclosure of the invention

Problems to be solved by the invention

The present invention has been made in view of the prior art as described above, and provides a more effective means for solving the problems caused by hot spots in a gas-phase catalytic oxidation reaction using a fixed-bed multitubular reactor. To provide.

Means for solving the problem

[0005] The present inventors have studied a method of mixing a catalyst and an inert filler in order to solve the above-mentioned problem. As a result, the inventors have adjusted the volume ratio of the catalyst and the inert filler to be mixed inside the hopper according to the volume ratio. It was found that the desired volume ratio can be easily mixed by mixing the catalyst and the inert filler with a catalyst mixer that combines this hopper and a non-stirring mixer. Was obtained.

[0006] The present invention provides a catalyst mixer in which a non-stirring mixer is arranged below a hopper, the catalyst mixer having a partition inside the hopper capable of substantially dividing an internal volume.

Further, a preferred embodiment of the present invention provides a catalyst mixer in which the partition wall is provided upright in a hopper so as to be adjustable in position.

[0008] The present invention is a method for mixing a plurality of types of packing using a catalyst mixer in which a non-stirring type mixer is arranged below a hopper, wherein the plurality of types of packing are separated and accommodated. For this purpose, the present invention provides a catalyst mixing method in which the inside of a hopper is divided into a plurality of sections by partition walls, and a horizontal sectional area ratio of each section is substantially equal to a volume ratio of each packing.

[0009] The present invention provides the above catalyst mixing method, wherein the plurality of types of packings are a composite oxide catalyst and an inert packing used for a gas-phase catalytic oxidation reaction using a fixed-bed multitubular reactor. I will provide a.

[0010] In a preferred embodiment of the present invention, a predetermined amount of the composite oxide catalyst and the inert packing to be filled per reaction tube of a fixed-bed multitubular reactor, or a plurality of the mixed oxide catalyst and the inert packing are filled in one reaction tube. The present invention provides a catalyst mixing method in which a predetermined amount of each reaction zone to be divided and filled into the reaction zones is mixed and bagged.

[0011] In a preferred embodiment of the present invention, the composite oxide catalyst and the inert filler are divided into eight parts and the volume ratio of the composite oxide catalyst to the inert filler is reduced. The present invention provides a catalyst mixing method wherein the coefficient of variation of the volume ratio of the catalyst is 10% or less.

The invention's effect

According to the method of the present invention, the composite oxide catalyst and the inert filler are mixed at a predetermined volume ratio. Since mixing can be performed, hot spots can be sufficiently suppressed in the gas-phase catalytic oxidation reaction using a fixed-bed multitubular reactor filled with the mixture. As a result, the catalyst performance can be maintained stably, and acrolein and Z or acrylic acid can be stably produced at a high yield from an oxidation reaction product such as propylene.

Brief Description of Drawings

FIG. 1 is a front view of a catalyst mixer according to an embodiment of the present invention.

FIG. 2 is a schematic diagram of the non-stirring mixer of FIG. 1.

FIG. 3 is an explanatory view of a circular system lj type splitter.

FIG. 4 is an explanatory view of a series-structured lj type splitter.

Explanation of symbols

[0014] 1 partition wall

2 Honoichi

3 Damper

4 Mixer without stirring

5 Input port

6 Housing

7 elements

8 Receiver

9 Weighing container

10 Rotary axis

11 pulley

BEST MODE FOR CARRYING OUT THE INVENTION

[0015] The present invention is characterized in that a composite oxide catalyst and another component other than the composite oxide catalyst are mixed by a catalyst mixer, and for example, gas phase catalytic oxidation using a fixed-bed multitubular reactor. Although the composite oxide catalyst used in the reaction (hereinafter sometimes simply referred to as a catalyst) and an inert filler are mixed by a catalyst mixer, the present invention is limited to the catalyst and the inert filler. What?

Hereinafter, the present invention will be specifically described with reference to the drawings. But the drawing is an invention The present invention is not limited to the drawings and the description thereof.

[0017] The catalyst mixer according to the present invention will be described with reference to FIG.

As shown in FIG. 1, the catalyst mixer of the invention has a non-stirring mixer 4 below a hopper 2. The hopper 2 has a capacity to receive a predetermined amount to be filled per reaction tube, or a predetermined amount of catalyst and inert packing in each reaction zone to be divided into a plurality of reaction zones per reaction tube. The bottom is openable and closable by dambar-3. Inside the hopper 2, a partition 1 is installed upright so that a plurality of types of packing, for example, a catalyst and an inert packing can be accommodated in a substantially separated manner. In this example, one partition 1 is provided to separate the catalyst and the inert packing, but the number of the partition 1 can be increased by the number of types of the packing. In this case, it is preferable that the partition wall 1 is provided so as to be adjustable in position, that is, movable. For this position adjustment, for example, although not shown, concave portions and grooves into which the partition wall 1 can be inserted are provided at regular intervals on the inner wall and the upper end of the hopper 2, and the partition wall 1 is replaced with these concave portions and grooves. Or a method in which the partition wall 1 is provided so as to be able to move in the hopper 2 in the lateral direction, and is fixed to a top end of the hopper 2 at a predetermined position by a screw or a hook. However. The position adjusting means of the partition 1 is not limited to these methods as long as the partition can be held at a predetermined position in the hopper.

The horizontal sectional area ratio of each section inside the hopper 2 divided by the partition 1 can be adjusted by changing the position of the partition 1. By adjusting the position of the partition 1, the horizontal cross-sectional area ratio of each section, preferably at least the horizontal cross-sectional area ratio at the outlet of the hopper 2, is made the same as the volume ratio of each of the plural types of packing materials. The ability to do S. Since the cross-sectional area ratio and the volume ratio are thus the same, the catalyst and the inert filler are accommodated in the corresponding compartments, so that the catalyst and the inert filler are packed at the same height of the packed bed. Can be charged inside the hopper 2.

[0019] The area of the partition 1 is not particularly limited as long as a plurality of types of packing can be substantially divided, but is preferably 60% or more, more preferably 80% or more, of the vertical section of the packing charged into the hopper. ° / ο or more, most preferably 95. / ₀ or more. If the area of the partition wall 1 is smaller than 60 ° / ο, the partitioning by the partition wall 1 becomes insufficient, and it becomes impossible to substantially uniformly mix a plurality of types of packing materials at a predetermined volume ratio. That the effect of There is power ^s .

Next, the non-stirring mixer 4 will be described with reference to FIG. As the non-stirring mixer 4, a non-stirring mixer shown in JIS_Z_8840 (pl4) can be used. Fig. 2 schematically shows a powerful non-stirring mixer, for example, using a static mixer in which a plurality of elements 7 are arranged inside a cylindrical housing 6 having an inlet 5 at the upper end. Let's do it. The inner diameter of the housing 6 is set so that the catalyst and the inert filler do not cause bridging in the housing. Usually, since the catalyst and the inert packing have a particle size of several mm to several tens of mm, the inner diameter is preferably 70 mm or more, more preferably 100 to 300 mm. Bridging may occur frequently in a housing with an inner diameter smaller than 70 mm. If the inner diameter is larger than 300 mm, the material required for the members increases, which is economically disadvantageous. The length of the housing 6 may vary depending on the element 7, but is preferably about 2 to 20 times the inner diameter.

The element 7 disposed inside the housing 6 may have a shape that allows passage of a catalyst and an inert filler having a particle diameter of several mm to several tens of mm, for example, a spiral element. Usually, 2 to 20 helical elements are used stepwise in the housing 6, but may be integrally formed. The catalyst and the inert filler to be mixed are supplied to the inlet 5 of the non-stirring mixer 4 by opening the damper 3 of the hopper 2 and mixed while falling along the spiral element 7 in the housing 6. Is done. In this case, since the catalyst and the inert filler are separated in the hopper 2 divided by the partition 1 in accordance with the respective mixing volume ratios, the catalyst and the inert filler can be supplied to the inlet 5 at a constant ratio. Such a mixing method using a helical element mixes the catalyst and the inert packing without stirring, and is effective for mixing without destroying the catalyst particles.

[0022] In the present invention, the mixed state of the catalyst and the inert filler is determined by a predetermined amount of the mixed catalyst and the inert filler to be filled per reaction tube (hereinafter, the catalyst and the inert gas per one reaction tube are mixed). The active packing is referred to as a “subdivided package”), which is conveniently divided into eight equal parts within the range of ± 15% by volume, and the volume ratio of each of the divided catalyst and the inert packing is determined. At this time, it is evaluated by the coefficient of variation of the catalyst capacity ratio. Here, the coefficient of variation is a value represented by (s / x X 100) where x is the average value of n data and s is the standard deviation. This variometer A large number means that the mixing ratio of the catalyst varies widely.

In the present invention, the coefficient of variation of the catalyst volume ratio is preferably 10% or less, more preferably 8% or less. If the variation coefficient is greater than 10%, the effect of suppressing hot spots in the gas-phase catalytic oxidation reaction becomes insufficient due to the heterogeneity of the catalyst, and when producing acrolein and / or acrylic acid from oxidation reaction products, for example, propylene. This is not preferable because the yield of the compound decreases.

[0024] As a method of equally dividing the contents of the subdivided package, for example, a divider shown in Figs. 3 and 4 can be used. Fig. 3 shows a type in which receivers 8 are arranged in a circle, and Fig. 4 shows a type in which receivers 8 are arranged in series. A measuring container 9 having an inner volume of 8 equal parts is placed in a receiver 8, and the contents of the subdivided package are put into the measuring container 9. When the weighing container 9 is filled, the rotating shaft 10 or the pulley 11 is moved, and subsequently, the weighing container 9 is set in the next receiver 8. By repeating this, the contents of the subdivided package can be equally divided into eight receivers 8 or measuring containers 9.

[0025] In addition, the volume of the packing in the present invention can be measured using a volume measuring device such as a measuring cylinder. In addition, the weight can be measured using a weighing device such as an electronic balance in terms of the bulk density, or a commercially available automatic weighing device can be used.

[0026] The inert filler used in the present invention may be any material that does not cause an unnecessary side reaction in the reaction. For example, high-temperature-treated oxides such as anoremina, zirconia, titania, magnesia, and silica may be used. High-temperature sintering materials such as tight, mullite, silicon carbide, and silicon nitride can be used.

[0027] A typical catalyst used in the present invention is a composite oxide catalyst used for a gas-phase catalytic oxidation reaction using a fixed-bed multitubular reactor. Specifically, for example, a catalyst used in a gas phase catalytic oxidation reaction for producing propylene perchlorein and acrylic acid can be mentioned. Preferred embodiments of the composite oxide catalyst include a catalyst represented by the following formula (1).

MoaBibCocNidFeeXfYgZhQiSijOk (1)

(In the formula, Mo is molybdenum, Bi is bismuth, Co is konorelate, Ni is nickel, Fe is iron, Si is silicon, O is oxygen, and X is any of Na, K, Rb, Cs, and T1. At least one Y indicates at least one of B, P, As and W, and Z indicates at least one of Mg, Ca, Zn, Ce and Sm. Q represents a halogen atom, ak represents the atom i of each element, and when a = 12, 0.5≤b≤7, 0≤c≤10, 0≤d≤10, l≤c + d ≤10, 0.05≤e≤3, 0.0005≤f≤3, 0≤g≤3, 0≤h≤l, 0≤i≤0.5, 0≤j≤4 8, and k is This is a value that satisfies the oxidation state of other elements. )

[0028] In the above, molybdenum (Mo), bismuth (Bi), silicon (Si), cobalt (Co), nickel (Ni), iron (Fe), magnesium (Mg), calcium ( Ca), zinc (Zn), cerium (Ce), samarium (Sm), sodium (Na), potassium (K), norebidium (Rb), cesium (Cs), thallium (T1), boron (B), phosphorus The elements (P), arsenic (As), tungsten (W), fluorine (F), chlorine (C1), bromine (Br), and iodine (I) are represented using the element symbols in Kakko. did. The molybdenum-bismuth composite oxide catalyst represented by the formula (1) itself is known and can be prepared by a known method.

[0029] Another representative catalyst used in the present invention is a molybdenum-based formula below, which is used in a reaction for producing a corresponding unsaturated carboxylic acid by subjecting an unsaturated aldehyde to a gas phase catalytic oxidation reaction. A composite oxide catalyst having (2).

MoaVbCucXdYeZfOg (2)

(In the formula, Mo is molybdenum, V is vanadium, Cu is copper, O is oxygen, X is at least one element selected from the group force of W and Nb force, Y is Fe, Co, Group power consisting of Ni and Bi is at least one element selected from the group consisting of: Ti, Zr, Ce, Cr, Mn, and Sb: at least one element selected from the group consisting of: a, b , C, d, e, f, and g represent the atom it of each element.When a = 12, l≤b≤12, 0≤c≤6, 0≤d≤12, 0≤e≤100, 0 ≤f≤100, g is the number of oxygen atoms required to satisfy the oxidation state of other elements.)

[0030] The method for preparing the catalyst used in the present invention is not particularly limited except for the calcination conditions. Usually, the required amount of the source compound containing each elemental component is appropriately dissolved or dispersed in an aqueous medium, and heated and stirred. After that, the mixture is evaporated to dryness, dried, and pulverized, and the obtained powder is molded by a method such as extrusion molding, granulation molding, tablet molding, or the like, to obtain a molded body. The shape and size of the catalyst are not particularly limited, and can be appropriately selected from known shapes and sizes. For example, regarding the shape, any of a spherical shape, a cylindrical shape, a ring shape, and the like may be used. this At this time, inorganic fibers such as glass fibers and various whiskers which are generally known to have an effect of improving the strength and the degree of powdering of the catalyst may be added. To control the physical properties of the catalyst with good reproducibility, additives generally known as powder binders such as ammonium nitrate, cellulose, starch, polybutyl alcohol, and stearic acid can be used.

[0031] In the present invention, the complex oxide represented by the above formula (1) can be used by itself. The compound can be used alone, such as phenol, silica, silica monoalumina, silicon carbide, titanium oxide, magnesium oxide, and aluminum sponge. It may be used by being supported on a carrier generally known as an inert carrier such as silica-titania. In addition, the above-mentioned inorganic fibers or the like may be added to improve the strength of the catalyst, or the above-mentioned additives such as ammonium nitrate may be used to control the physical properties of the catalyst with good reproducibility.

The composite oxide catalyst is prepared by calcining the catalyst, which is a molded body or a support, at a temperature of 300 to 650 ° C. for about 120 hours in a flowing atmosphere gas.

[0033] The gas-phase catalytic oxidation reaction using the Mo-Bi-Fe-based composite oxide catalyst is, specifically, a gas-phase catalytic oxidation of propylene, which is generally used when producing acrolein and acrylic acid. You can do that by For example, a mixed gas consisting of 1 to 15% by volume of propylene, 3 to 30% by volume of molecular oxygen, 0 to 60% by volume of steam, and 20 to 80% by volume of an inert gas such as nitrogen and carbon dioxide gas is supplied to each of the above reaction tubes. It may be introduced into the catalyst layer at 250-450 ° C, 0.01-IMPa under pressure and space velocity (SV) 300-5000hr- ¹ .

Example

[0034] Hereinafter, the present invention will be described specifically with reference to Examples, but the present invention is not limited to the following Examples.

In the following description, the conversion and the yield are defined as follows.

'Propylene conversion (mol ^_0/0) = (Monore number of moles / supplied propylene of reacted propylene) X 100

.Total yield of acrolein and acrylic acid (mol%) = (moles of acrolein and acrylic acid produced / moles of propylene supplied) x 100

Example 1

Catalyst for producing acrolein and acrylic acid using propylene as a raw material by gas phase catalytic oxidation reaction As a medium, Mo: Bi: Ni: Co: Fe: Na: B: K: Si = 12: 5: 2: 3: 0.5: 0.5: 0.1: 0.2: 0.1: 2

A composite oxide catalyst powder having an atomic ratio (excluding O) of 4 was prepared. To 100 parts by weight of this powder was added 2 parts by weight of graphite (molding aid), and the mixture was tableted into a ring having an outer diameter of 5 mm, an inner diameter of 2 mm, and a height of 4 mm. And calcined to obtain a catalyst.

Next, the catalyst and the inert filler (alumina balls having a diameter of about 5 mm) were mixed using the catalyst mixer shown in FIG. First, 500 ml of the catalyst and 500 ml of the inert filler were mixed and packed in small bags. A non-stirring mixer 4 was placed below the hopper 2, and a polyethylene bag (0.08 mm thick × 180 mm wide × 270 mm long) was set at the lower outlet of the non-stirring mixer 4. The position of partition 1 was adjusted so that the internal volume of hopper 2 was 1: 1. 500 ml of the catalyst was charged into one of the two sections divided by the partition 1, and 500 ml of the inert filler was charged into the other section. Next, the damper 3 was opened, and the catalyst and the inert filler were charged into the non-stirring mixer. The mixture of the catalyst and the inert filler discharged from the lower outlet of the non-stirring mixer 4 was received by a polyethylene bag, degassed, and sealed and heated to obtain a small package. The same operation was repeated six times to produce six subdivided packages, each of which was designated subdivided package A-11-A-6.

Table 1 shows the results of evaluating the mixed state of the catalyst and the inert filler of the subdivided packages A-11-A-5.

Next, the mixture of the catalyst and the inert filler divided into the above-mentioned subdivided packages A-6 is filled into the raw material gas inlet side of a stainless steel reaction tube having a diameter of 27 mm provided with a thermocouple. The outlet side was charged with 1000 ml of the catalyst.

[0039] Next, in order to confirm the catalyst performance, the gas space velocity lOOOOhr- ¹ (0 ° C reference), the inlet gouge pressure 100kPa, the reaction temperature 310 ° C, the propylene 8.5% by volume, Propylene was oxidized by flowing a mixed gas of 68% by volume of air, 15% by volume of steam and 8.5% by volume of nitrogen. The reaction results were as follows: propylene conversion: 98.8%; total yield of acrylic acid and acrolein: 92.6%. The maximum temperature of the reaction catalyst layer was 383 ° C.

[0040] Comparative Example 1

The partition wall 1 of the catalyst mixer shown in FIG. 1 was removed, and the same catalyst and the inert filler as in Example 1 were used to pack small portions according to the following method. First, 500 ml of the catalyst and 500 ml of the inert filler were mixed, and the mixture was packaged in small portions. A non-stirring mixer 4 was placed below the hopper 2, and a polyethylene bag (0.08mm thick x 180mm wide x 270mm long) was set at the lower outlet of the non-stirring mixer 4. Next, 500 ml of the catalyst was charged into the hopper 2, and subsequently 500 ml of the inert filler was charged into the hopper. Next, the damper 3 was opened, and the catalyst and the inert filler were charged into the mixer 4 without stirring. The mixture of the catalyst and the inert filler discharged from the lower outlet of the non-stirring mixer 4 was received by a polyethylene bag, degassed, and sealed and heated to obtain a small package. The same operation was repeated six times to produce six subdivided packages, each of which was designated subdivided package B-1-1 B-6.

Table 2 shows the results of evaluating the mixed state of the catalyst and the inert filler of the subdivided packages B-1-1 and B-5.

On the other hand, the mixture of the molding catalyst and the inert filler of the above-mentioned subdivided package B-6 is filled into the raw material gas inlet side of a 27 mm diameter stainless steel reaction tube provided with a thermocouple, and the raw material gas outlet side Was charged with 1000 ml of the catalyst.

[0042] Next, in order to confirm the catalyst performance, under the conditions of a gas hourly space velocity of 100 hr- ¹ (0 ° C reference), an inlet gauge pressure of 100 kPa, and a reaction temperature of 310 ° C, propylene 8.5% by volume, air 68 volume ^_0/0, the water vapor 15 volume%, was circulated nitrogen 8.5% by volume of the mixed gas, having conducted the oxidation of propylene. As for the reaction results, the propylene conversion was 98.6%, and the total yield of acrylic acid and acrolein was 91.1%. The maximum temperature of the reaction catalyst layer was 410 ° C.

[Table 1]

Small <divided package Volume ratio (%) Catalyst volume ratio

No. Coefficient of variation) O catalyst Inert packing

A- 1 48. 4 51. 6

50.0 50.0

53. 7 46. 3

49.2 50.86.4

53. 8 46. 2

43.8 56.2

47. 1 52. 9

52. 3 47. 7

A-2 47. 9 52. 1

51.7 48.3

53. 4 46. 6

48.0 52.07.3

45. 8 54. 2

49.5 50.5

46.7 53.3

57. 3 42. 7

44.6 55.4

52. 4 47. 6

56.3 43.7

51.5 48.5 7.8

51. 9 48. 1

44.7 55.3

46.5 53.5

50.7 49.3

A— 4 50. 7 49. 3

51. 9 48. 1

50. 1 49. 9

53.6 46.44.4

49.4 50.6

46. 8 53. 2

46.7 53.3

50.4 49.6

A— 5 53. 1 46. 9

54. 4 45. 6

47. 4 52. 6

49.6 50.45.9

45. 7 54. 3

46.5 53.5

50.7 49.3

52. 0 48. 0 2] Subdivision package Volume ratio (%) Catalyst volume ratio

No. Coefficient of variation (%)

Catalyst inert packing

B— 1n 60. 5 39. 5

57. 5 42. 5

45.3 54.7

42.8 57.2 14.9

44.5 55.5

47.2 52.8

42. 0 58. 0

60. 1 39. 9

B-2 54.5 55.5

53. 1 46. 9

53. 5 46. 5

56.7 43.3 11.2

53. 0 47. 0

48.3 51.7

47. 8 52. 2

38.0 62.0

B-3 60. 9 39.1

46.5 53.5

42. 1 57. 9

39.9 60.1 17.7

44.2 55.8

50.4 49.6

53. 5 46. 5

66. 6 33. 4

B— 4 49.5 50.5

52. 1 47. 9

56.4 43.6

51.0 49.0 11.6

51. 9 48. 1

53. 7 46. 3

44. 9 55. 1

36.2 63.8

48. 8 51. 2

52. 6 47. 4

55. 1 44. 9

55.4 44.6 14.7

57. 9 42. 1

52. 7 47. 3

45.3 54.7

33. 3 66. 7 Industrial Applicability

The present invention enables the catalyst and the inert filler to be mixed at a predetermined volume ratio, and provides a fixed-bed multitubular reactor. Since the effect of suppressing hot spots in the gas phase catalytic oxidation reaction using a reactor can be obtained, mixing of a catalyst with an inert filler in the case of producing acrolein and acrylic acid from oxidation reaction products such as propylene And a high yield can be achieved.

Claims

The scope of the claims

[1] A catalyst mixer in which a non-stirring mixer is arranged below a hopper, the catalyst mixer comprising a partition inside the hopper capable of substantially dividing an internal volume.

[2] The catalyst mixer according to claim 1, wherein the partition wall is provided upright in a hopper so as to be adjustable in position.

[3] A method of mixing a plurality of types of packing using a catalyst mixer in which a non-stirring type mixer is arranged below a hopper. A catalyst mixing method, wherein the inside of the upper is divided into a plurality of partitions by partition walls, and a horizontal sectional area ratio of each partition is made substantially equal to a volume ratio of each packing.

4. The catalyst mixture according to claim 3, wherein the plurality of types of packing are a composite oxide catalyst and an inert packing used in a gas-phase catalytic oxidation reaction using a fixed-bed multitubular reactor. Method

[5] The above-mentioned complex oxide catalyst and the inert packing are charged in a predetermined amount to be filled per reaction tube of a fixed-bed multitubular reactor, or divided into a plurality of reaction zones in one reaction tube. 5. The catalyst mixing method according to claim 4, wherein a predetermined amount of each reaction zone to be filled is divided, mixed and bagged.

[6] The coefficient of variation of the volume ratio of the composite oxide catalyst and the inert filler when the subdivided composite oxide catalyst and the inert filler are divided into 8 parts is 10% or less. 6. The method for mixing a catalyst according to claim 5, wherein

[7] A subdivided package that is packaged in subdivided bags according to the catalyst mixing method of claim 5 or 6.