KR101548410B1 - Homogeneously Supported Catalyst for CNT, a Method for Preparing Thereof and an Apparatus for Preparing Thereof - Google Patents

Abstract

The present invention relates to a homogeneous supported catalyst for carbon nanotubes, a method for producing the homogeneous supported catalyst, and a production apparatus used therefor. In particular, a homogeneous supported catalyst for carbon nanotubes in which the fine particles of the catalyst itself are minimized, A manufacturing method thereof, and a manufacturing apparatus used therefor.

Description

Technical Field [0001] The present invention relates to a homogeneous supported catalyst for carbon nanotubes, a method for producing the same, and a manufacturing apparatus used therefor.

The present invention relates to a homogeneous supported catalyst for carbon nanotubes, a method of producing the same, and a manufacturing apparatus used therefor. More particularly, the present invention relates to a homogeneous supported catalyst for carbon nanotubes A homogeneous supported catalyst, a method for producing the same, and a manufacturing apparatus used therefor.

Carbon nanotubes (hereinafter referred to as "CNTs") are understood to mean cylindrical carbon tubes having a diameter of 3 to 150 nm, specifically 3 to 100 nm, and a length several times the diameter, that is, 100 times or more. These tubes consist of a layer of aligned carbon atoms and have different types of cores. Such carbon nanotubes are also referred to as carbon fibrils or hollow carbon fibers, for example. Due to the size and specific nature of such carbon nanotubes, the carbon nanotubes described herein are of industrial importance in the manufacture of composites. There is an inherent additional possibility in electronic applications, energy applications and further applications.

The carbon nanotubes are generally manufactured by arc discharge, laser ablation, chemical vapor deposition, or the like. However, the arc discharge method and the laser evaporation method are difficult to mass-produce, and an excessive production cost of an arc or a cost of purchasing a laser device is a problem.

In addition, in the case of the above-mentioned chemical vapor deposition method, there is a problem that the synthesis rate is very slow and the CNT particles to be synthesized are too small in the case of a method using a gas phase dispersion catalyst. There is a limit to the mass production of CNTs.

A rotary kiln system in which CNTs are injected by injecting a hydrocarbon-based reaction gas into a reactor in the form of a rotating drum as a mass production method of CNTs, and a rotary kiln system in which a fluidizing medium is heated A fluidized bed reactor (hereinafter referred to as an FBR reactor) for forming a fluidized bed that forms a CNT in the fluidized bed is disclosed.

Particularly, in the case of a fluidized bed reactor, productivity is high as compared with the reactor volume, CNT mass production is easy, and continuous or batch operation is possible. Specifically, a carbon source, a reducing gas ) And an inert gas are preheated through a preheater to a temperature of about 200 to 500 ° C through a reaction gas supply pipe and then blown up to the upper part of the reactor and contacted with a catalyst injected into the reactor through a catalyst gas feeder CNT < / RTI >

The reaction gas supply pipe is not particularly limited as long as it can be used in a CNT manufacturing apparatus. Specifically, the reaction gas supply pipe may be a gas distributor or the like. When the preheater is used as described above, It is preferable that the supply pipe to be supplied is in the form of a gas distributor in view of the reaction efficiency.

The catalyst supplier is not particularly limited as long as it can be used in a CNT manufacturing apparatus, and may be a hopper type.

The catalyst can be a supported catalyst, a coprecipitation catalyst or the like, which mainly has a catalytically active component in an oxide form, a partially or fully reduced form, or a hydroxide form, and can usually be used for producing CNTs. If a supported catalyst is used, the bulk density of the catalyst itself is higher than that of the coprecipitation catalyst, and unlike the coprecipitation catalyst, the attrition that can occur in the fluidization process is small It is possible to reduce the possibility of generation of a fine particle by the catalyst, and the mechanical strength of the catalyst itself is also excellent, so that the operation of the reactor can be stabilized.

However, even using a fluidized bed reactor using such a supported catalyst, the conversion efficiency of the carbon source is at most about 80%, which limits the productivity. In order to improve the conversion of the carbon source in the reactor, there is a need for research to minimize the fine particles of the catalyst itself during the preparation of the supported catalyst.

In order to solve the problems of the prior art as described above, the present invention provides a homogeneous supported catalyst for carbon nanotubes in which fine particles of the catalyst itself are minimized in the preparation of a supported catalyst in consideration of a specific differentiation factor, a production method thereof, The purpose is to provide.

In order to attain the above object, the present invention provides a method for producing a catalyst, which comprises a support, a catalyst component, an active component and a precipitation-inhibiting component, wherein a difference (Dv-Dn) between a water- Or less, based on the total weight of the carbon nanotubes.

The present invention also relates to a method for preparing a metal precursor solution, comprising the steps of sequentially mixing an aqueous solution of a precursor of an active ingredient with a precipitation inhibiting component and an aqueous solution of a catalyst component precursor, Mixing said metal homogenized aqueous solution with a support and obtaining a mixture; And subjecting the mixture to rapid vacuum drying to obtain a supported catalyst having a catalyst component impregnated and coated on the surface of the support; And a method for producing a homogeneous supported catalyst for a carbon nanotube.

Furthermore, the present invention provides an apparatus for producing a homogeneous aqueous metal solution, comprising a catalyst component input means, an active component input means, a sedimentation suppression component input means, and a control means for the three input means; A mixing device for mixing the homogeneous aqueous metal solution and the support transferred from the production apparatus; A drying and firing apparatus for homogenously impregnating and coating the catalyst component on the surface of the support by drying and firing the mixture transferred from the mixing apparatus; Lt; / RTI >

Wherein the drying and calcining apparatus is a rapid vacuum drying apparatus. The present invention also provides an apparatus for manufacturing a homogeneous supported catalyst for a carbon nanotube.

Hereinafter, the present invention will be described in detail.

The homogeneous supported catalyst for a carbon nanotube of the present invention is characterized by comprising a support, a catalyst component, an active component and a precipitation inhibiting component, and satisfies a specific differentiation factor.

The support used in the present invention includes alumina, magnesium oxide, and silica , And it is preferable to use alumina as described in the following examples.

In addition, the catalyst component used in the present invention may be at least one kind selected from Fe, Co, and Ni, and it is preferable to use Fe as described in the following examples.

In addition, the active ingredient used in the present invention is preferably Mo.

On the other hand, in the present invention, the component to be added for suppressing the precipitation is not limited thereto, but is preferably at least one selected from dicarboxylic acid, tricarboxylic acid and tetracarboxylic acid.

Among other things, the specific differential factor provided by the present invention includes the difference (Dv-Dn) between the water volume average and the water droplet diameter average with respect to the water receiving diameter average (Dn). This means that the actual differential is generally expressed as% of the specific grains of Dn, but since there is a large deviation in the measurement, the accuracy of the differential measurement can be improved by the average value of the average particle diameter and the water volume average, (Dv-Dn) of the difference between the hydraulic average and the diameter average of the diameter average (Dn) as a tool for quantification.

Comparative Example 1 to Comparative Example 1 in which the differential factor was 0.6 in comparison with Example 1 in Example 1, 0.7 in Example 2, 0.9 in Example 3 and 0.9 in Example 4, which were 1.0 in the following examples, It can be confirmed that the content of 30 탆 or less, which is lower than the minimum particle diameter of the alumina used, is 10% or less, and the amount of impregnated coating of the catalyst component and the active component is relatively high, resulting in a high CNT yield.

It is preferable that the differential factor is 1.0 or less. Considering that Example 1 (differential factor 0.6) and Example 2 (differential factor 0.7) show the most improved effect of the actual differential within 5%, the differential factor Is preferably 1.0 or less, and most preferably 0.7 or less. The actual amount of the fine powder is important not only in the process but also in terms of the yield of the catalyst production.

For reference, when the impregnation catalyst supporting method using oven drying, which is conventionally used in the production of a metal catalyst for CNT production, is used, fine particles having a particle size smaller than that of the support are produced by precipitation reaction between the metal component and the active component at 100 ° C or higher.

For example, when Fe is used as a metal component and Mo is used as an active ingredient, a deep yellow precipitate of Fe ^{3 +} + 3MoO ^- -> Fe (MoO) ₃ ↓ is formed, so that a transparent homogeneous supported catalyst is produced .

On the other hand, the catalyst provided in the present invention is not only a supported catalyst suitable for use in a fluidized bed (FBR) reactor for producing carbon nanotubes, but also a homogeneous catalyst since it prevents such precipitation.

A method for producing such a homogeneous catalyst will be described in detail below.

First, the precipitation inhibiting component and the catalyst component precursor aqueous solution are sequentially compounded in the precursor aqueous solution of the active component to obtain a transparent metal homogeneous aqueous solution (first step). The obtained homogeneous aqueous solution of metal is mixed with a support and a mixture is obtained (second step). Then, the obtained mixture is rapidly vacuum dried and then calcined to impregnate and coat the catalyst component on the surface of the support, thereby obtaining a supported catalyst (Step 3).

The catalyst component used in the first step may be at least one kind selected from Fe, Co, and Ni, and it is preferable to use Fe as described in the following examples. Further, the active ingredient is preferably Mo.

Furthermore, it is preferable to use at least one polycarboxylic acid selected from dicarboxylic acid, tricarboxylic acid and tetracarboxylic acid as the precipitation inhibiting component.

More specifically, the first step using these components includes a step (a step) of producing an aqueous solution of Mo precursor, a step (step b) of mixing the precipitation inhibiting component in the aqueous solution of Mo precursor, and a step of mixing the Mo precursor and the precipitation- (Step c) of mixing the catalyst component precursor with the aqueous solution of the catalyst component (c).

The Mo precursor used in step a in the first step is not limited thereto, but nitrides such as (NH ₄ ) ₆ Mo ₇ O ₂₄ .4H ₂ O may be dissolved in distilled water.

It is preferable that the precursor aqueous solution of Mo is contained in the range of 0.5 to 12 mol% based on the active ingredient, considering the efficiency of the reaction.

The precipitation inhibiting component used in the step b) in the first step may contain at least one (M) selected from dicarboxylic acid, tricarboxylic acid and tetracarboxylic acid in a molar ratio (M / A) is in the range of 0.2 to 0.5.

In the case of Comparative Examples 1 to 4 in which the molar ratio of the precipitation inhibiting component (M) and the Mo precursor (A) in the following examples was less than 0.2 to 0.5 as compared with those of Examples 1 to 4, Precipitation occurs, and it is proven that the CNT yield is poor due to non-uniform catalyst preparation.

Then, the precursor of the catalyst component used in the step c in the first step may be at least one selected from Fe, Co, and Ni, specifically Co (NO ₃ ) ₂ .6H ₂ O, Fe (NO ₃ ) ₂ And nitrides such as .6H ₂ O, Fe (NO ₃ ) ₂ .9H ₂ O, or Ni (NO ₃ ) ₂ .6H ₂ O.

The specific amount used is preferably in the range of 10 to 40 mol% based on the catalyst component, considering the efficiency of the reaction.

The concentration of the metal homogeneous aqueous solution thus obtained is 0.4 g / ml or less, specifically, 0.3 g / ml, which is efficient considering the reactivity.

The support is mixed with the homogeneous aqueous metal solution obtained through the first step (second step).

The support used in the second step may include alumina, magnesium oxide, and silica , And it is preferable to use alumina as described in the following examples. Specifically, a support such as commercial Al ₂ O ₃ , MgO, SiO ₂ or the like is used to be mixed with the metal homogeneous aqueous solution through wet impregnation.

The resulting mixture is then rapidly vacuum dried and then calcined to impregnate and coat the catalyst component on the support surface to obtain a supported catalyst. In this case, the rapid vacuum drying step is preferably carried out at a temperature of 45 to 80 ° C by rotary evaporation, and the rapid vacuum drying time is preferably 30 minutes to 3 hours.

The supported catalyst may be a spherical type having an average particle diameter in the range of 30 to 150 μm and a surface particle size of 10 to 50 nm, but it is not limited to the particle size because it depends on the particle size of the support used.

Also, the firing conditions are preferably performed at 650 to 800 ° C for 30 minutes to 5 hours.

In particular, the present invention may further include an aging step (step 2 ') before performing the third step after the second step.

It is preferable that the aging condition is aged within 45 to 80 占 폚 through rotation or agitation within 20 minutes before rapid vacuum drying since it can optimally satisfy the differential factor. The aging conditions are proved to be lower than those of Examples 1 to 4 in which aging conditions are less than 20 minutes in the case of Comparative Example 5 in which aging conditions exceed 30 minutes in the following Examples.

Hereinafter, an apparatus for producing the above-described homogeneous supported catalyst will be described.

The apparatus for producing a catalyst used in the present invention is characterized in that it comprises an apparatus for producing a homogeneous aqueous metal solution, a device for mixing the homogeneous aqueous solution of metal and the supporter transferred from the apparatus for producing homogeneous aqueous solution of the solution, a device for drying the mixture transferred from the mixing device, And a sintering apparatus for the sintering process.

Such an apparatus for producing a homogeneous aqueous metal solution may be a solution stirring / mixing apparatus comprising a catalyst component injecting means, an active component injecting means, a sedimentation suppressing component injecting means, and a control means for the three kinds of injecting means.

At this time, the control means (1-4) of the three kinds of input means turns on the active component input means while turning off the catalyst component input means and the sedimentation suppression component input means so that the precursor of the active component Wherein the catalyst component injecting means and the active component injecting means are turned off and the sedimentation suppression component injecting means is turned on to complete the introduction of the sedimentation suppression component, The catalyst component injecting means is turned on while the inhibiting component injecting means is turned off and the precursor of the catalyst component is injected.

The homogeneous aqueous solution of metal transferred from the apparatus for producing a homogeneous metal solution and the support are mixed as a mixing device in an agitating and mixing device, and the mixture transferred from the agitating device is dried in a drying device and then burned through a burning device, The components are homogeneously impregnated and coated. The drying apparatus may be a rapid vacuum drying apparatus, specifically a rotary heating apparatus.

The rapid vacuum drying apparatus may be in the form of a straight wall or a baffle inside the apparatus, a shape that can be inclined at a predetermined angle with respect to the vertical direction and rotated at a predetermined speed.

In addition, the metal homogenous mixture can be aged by being conveyed to a drying apparatus and then rotated or stirred before drying. At this time, it is preferable to aged at a temperature of not more than 20 minutes by using a drying apparatus and then dried without using a separate device for aging.

The drying apparatus is not limited thereto, but a rapid vacuum drying apparatus can be used. After drying, the dried material is fired by using a high-temperature furnace or the like as a firing apparatus.

As described above, according to the present invention, there is provided an effect of providing a homogeneous supported catalyst for a carbon nanotube, a method for producing the same, and a manufacturing apparatus used therefor, in which the fine particles of the catalyst itself are minimized in the production of a supported catalyst in consideration of a specific differentiation factor have.

1 is a graph showing the relationship between the actual fine powder (wt%, particle diameter of the lower limit of the normal grain size of the alumina used as the support of less than 32 탆) and the differential factor measured in Examples and Comparative Examples of the present invention.
2 is a SEM image (X35) of a catalyst prepared according to Example 1 of the present invention.
3 is a SEM image (X100) of a CNT synthesized using the catalyst of Example 1 of the present invention.
4 is a SEM high-magnification image (X50,000) of a CNT synthesized using the catalyst of Example 1 of the present invention.

Hereinafter, preferred embodiments of the present invention will be described in order to facilitate understanding of the present invention, but the present invention is not limited thereto.

[ Example ]

Example  1 < CNT  Preparation of Catalyst - Differential Factor  0.6>

0.25 g (1.30 mmol) of citric acid was added to a flask A in which 0.64 g (0.52 mmol, Mo: 3.63 mmol) of (NH ₄ ) ₆ Mo ₇ O ₂₄ .4H ₂ O was dissolved in 15 ml of water. _{= 0.3), Fe (NO 3} ) 2 .9H 2 O 3.62 g [8.95 mmol] and the input are _{prepared, Al 2 O 3 (D50v =} 80 micron, D50n = 55 micron, pore volume: 0.64cm 3 / g, surface area: 237 m &lt; ² &gt; / g, manufactured by Saint Gobain), the catalyst metal precursor was sufficiently supported on Al ₂ O ₃ by adding the flask A to the flask B containing 2.5 g, and then stirred for 5 minutes in a 60 ° C thermostat It ages. At this time, the concentration of the metal aqueous solution was 0.3 g / ml.

Then, it is dried under vacuum drying for 30 minutes while maintaining the above temperature. The dried catalyst was calcined at 700 ° C for 3 hours to prepare a homogeneous supported catalyst. (Dv 50) of the prepared catalyst was 92 μm, and the average particle size (Dn 50) was 57 μm. The differential factor of (Dv-Dn) / Dn was calculated to be 0.61. The water volume average (Dv50) and the water droplet diameter average (Dn50) were measured after dispersing in water using a particle size analyzer (Microtrac, bluewave).

Meanwhile, an SEM image of the catalyst prepared according to Example 1 of the present invention is shown in FIG. It was confirmed that the catalyst prepared from the photograph of FIG. 2 was well coated with alumina without forming small agglomerates between the metal catalysts.

Example  2 < CNT  Preparation of Catalyst - Differential Factor  0.7>

Example 1 The same procedure as in Example 1 was repeated except that the aging time was omitted and the drying temperature was changed to 45 캜. (Dv 50) of the prepared catalyst was 93 탆, the number average particle diameter (Dn 50) was 57 탆, and the differential factor of (Dv-Dn) / Dn was calculated to be 0.652.

Example  3 < CNT  Preparation of Catalyst - Differential Factor  0.9>

The same procedure as in Example 1 was repeated except that the concentration of the metal aqueous solution in Example 1 was changed to 0.4 g / ml and the aging time was changed to 10 minutes. (Dv 50) of the prepared catalyst was 96 탆, the number average particle diameter (Dn 50) was 51 탆, and the differential factor of (Dv-Dn) / Dn was calculated to be 0.882.

Example  4 < CNT  Preparation of Catalyst - Differential Factor  1.0>

Example 1 The same procedure as in Example 1 was repeated except that the aging time was changed to 15 minutes. As a result of calculation of the differential factor of (Dv-Dn) / Dn, it was confirmed that the prepared catalyst had a water volume average (Dv50) of 102 mu m and a number average particle diameter (Dn50) of 50 mu m.

Comparative Example  1 < CNT  Preparation of Catalyst - Differential Factor  4.3>

Example 1 The same procedure as in Example 1 was repeated, except that the oven-drying was carried out under 120 ° C under 60 ° C. (Dv50) of the prepared catalyst was 80 占 퐉 and the number average particle diameter (Dn50) was 15 占 퐉. As a result, it was confirmed that the differential factor of (Dv-Dn) / Dn was 4.3.

Comparative Example  2 < CNT  Preparation of Catalyst - Differential Factor  1.5>

0.64 g (0.52 mmol, Mo: 3.63 mmol) of (NH ₄ ) ₆ Mo ₇ O ₂₄ .4H ₂ O and 0.50 g (2.6 mmol) of citric acid in Example 1 were added to adjust the molar ratio of Mo to citric acid to 0.7 The same procedure as in Example 1 was repeated. The Dv 50 and Dn 50 of the prepared catalyst were 99 탆 and 39 탆, respectively, and the differential factor of (Dv-Dn) / Dn was 1.53.

Comparative Example  3 < CNT  Preparation of Catalyst - Differential Factor  1.4>

The same procedure as in Example 1 was repeated except that the aging time of 20 minutes in Example 1 was replaced by aging for 35 minutes. (Dv50) of the prepared catalyst was 89 占 퐉 and the number average particle diameter (Dn50) was 37 占 퐉. As a result, it was confirmed that the differential factor of (Dv-Dn) / Dn was 1.405.

Comparative Example  4 < CNT  Preparation of Catalyst - Differential Factor  2.9>

The same procedure as in Example 1 was repeated except that 5 ml of water was added so that the concentration of the homogeneous aqueous metal solution in Example 1 was 1.0 g / ml. (Dv50) of the prepared catalyst was 104 占 퐉 and the number average particle diameter (Dn50) was 27 占 퐉. As a result, it was confirmed that the differential factor of (Dv-Dn) / Dn was 2.85.

Comparative Example  5 < CNT  Preparation of Catalyst - Differential Factor  3.6>

The same procedure as in Example 1 was repeated, except that MoO, Fe and CA were added in the order of Example 1 to obtain a metal aqueous solution containing a dark yellow precipitate. (Dv50) of the prepared catalyst was 92 占 퐉 and the number average particle diameter (Dn50) was 20 占 퐉. As a result, it was confirmed that the differential factor of (Dv-Dn) / Dn was 3.6.

In addition to the differential factor values calculated in Examples 1 to 4 and Comparative Examples 1 to 5, the particle diameters of the lower limit of normal grain size of alumina used as a support of less than 32 탆 were defined as actual differentials and the measured weight% Respectively. The relation between the actual differentiator (% by weight) and the differential factor is shown in Fig.

As shown in FIG. 1, the actual differentiation (weight%) and the differentiation factor are proportional to each other. Particularly, when the differential factor defined in the present invention is 1.0 or less, specifically 0.7 or less, Can be controlled to 4.5 wt% or less.

CNT Manufacturing example

Carbon nanotubes synthesis was tested in a laboratory scale fixed bed reactor using the CNT synthesis catalysts prepared in Examples 1-4.

The prepared CNT synthesis catalyst was mounted on the middle portion of a quartz tube having an inner diameter of 55 mm and then heated to a temperature of 700 to 700 ° C in a volume ratio of nitrogen and hydrogen to maintain the nitrogen and hydrogen and ethylene gas Was synthesized at a volume ratio of 50: 3: 10 for 1 hour to synthesize a predetermined amount of carbon nanotubes.

The synthesized carbon nanotubes were obtained at room temperature and their contents were measured. The reaction yield was calculated based on the weight of the CNT synthesis catalyst and the weight increase after the reaction according to the following formula.

CNT yield (%) = (total weight after reaction (g) - weight of used catalyst (g)) / weight of used catalyst (g) x 100

The CNTs collected in the CNT collector after the 1 hour reaction showed a CNT yield of 451% of the catalyst input amount in Example 1, and the average diameter of the obtained CNTs was 20 to 30 nm. The results of Examples 2 to 4 are summarized together in Table 1 below.

3 shows an SEM image of the CNT synthesized using the catalyst of Example 1 of the present invention. As shown in Fig. 3, it was confirmed that spherical CNTs were produced in a bulk state. Further, a high-magnification SEM image of the CNT synthesized using the catalyst of Example 1 of the present invention is shown in FIG. As shown in FIG. 4, it was confirmed that individual CNTs were produced.

Comparative Manufacturing Example  One

The procedure of Example 1 was repeated except that the catalysts of Comparative Examples 1 to 5 were used instead of the catalyst of Example 1.

The CNTs collected in the CNT collector after the 1 hour reaction showed a yield of 410% of the catalyst input amount in Comparative Example 1, and the average diameter of the obtained CNTs was 20 to 30 nm. The results of Comparative Examples 2 to 5 are also summarized in Table 1 below.

division Al ₂ O ₃ Example 1 Example 2 Example 3 Example 4 Comparative Example 1 Comparative Example 2 Comparative Example 3 Comparative Example 4 Comparative Example 5 dry
system - Rotary evaporation Rotary evaporation Rotary evaporation Rotary evaporation Oven drying Rotary evaporation Rotary evaporation Rotary evaporation Rotary evaporation Fe / Mo /
Al ₂ O ₃ 0/0/100 27/10/64 27/10/64 27/10/64 27/10/64 27/10/64 27/10/64 27/10/64 27/10/64 27/10/64 Mo mmol - 3.63 3.63 3.63 3.63 3.63 3.63 3.63 3.63 3.63 CA mmol - 1.30 1.30 1.30 1.30 1.30 2.60 1.30 1.30 1.30 CA / Mo - 0.36 0.36 0.36 0.36 0.36 0.72 0.36 0.36 0.36 Metal aqueous solution concentration
(g / ml) - 0.3 0.3 0.4 0.3 0.3 0.3 0.3 1.0 0.3 Aging (minutes) - 5 - 10 15 5 - 35 - 5 Drying (℃) - 60 45 60 60 150 60 60 60 60 Dv 80 92 93 96 102 80 99 82 104 92 Dn 55 57 59 51 50 15 39 40 27 20 Differential factor * 0.45 0.6 0.7 0.9 1.0 4.3 1.5 1.4 2.9 3.6 Actual differential (wt%) - 2.0 4.5 7.5 9.0 21.0 15.8 14.5 18.0 19.0 CNT yield (%) - 451 407 420 456 410 280 350 313 260

* Derivative factor = (Dv-Dn) / Dn

As shown in the above table, in the case of Examples 1 to 4 according to the present invention, it is possible to efficiently minimize the differentiability of Comparative Examples 1 to 5, and the CNT yield obtained is much improved.

Claims (16)

Characterized in that the difference (Dv-Dn) between the support body, the catalyst component, the active component and the precipitation inhibiting component, and the difference between the water volume average and the water- Supported catalyst.
The method according to claim 1,
The support comprises alumina, magnesium oxide, and silica Wherein the catalyst is selected from the group consisting of carbon nanotubes, carbon nanotubes, and carbon nanotubes.
The method according to claim 1,
Wherein the catalyst component is at least one selected from Fe, Co, and Ni.
The method according to claim 1,
Characterized in that the active component is Mo. The homogeneous supported catalyst for carbon nanotubes according to claim 1,
The method according to claim 1,
Wherein the precipitation inhibiting component is at least one selected from dicarboxylic acid, tricarboxylic acid, and tetracarboxylic acid.
The method according to claim 1,
Wherein the difference (Dv-Dn) between the water volume average and the water-soluble particle average to the water-soluble particle average (Dn) is 0.7 or less.
delete delete delete delete delete delete delete An apparatus for producing a homogeneous aqueous metal solution comprising a catalyst component input means, an active component input means, a sedimentation suppression component input means, and a control means for the three input means;
A mixing device for mixing the homogeneous aqueous metal solution and the support transferred from the production apparatus;
A drying device for homogenously impregnating and coating the catalyst component on the surface of the support by drying the mixture transferred from the mixing device; And
A firing device for transferring and firing the dried material; Lt; / RTI &gt;
Wherein the drying apparatus is a rapid vacuum drying apparatus, and the rapid vacuum drying apparatus is a rotary heating apparatus.
15. The method of claim 14,
The control means of the three kinds of injecting means turns on the active ingredient injecting means while turning off the catalyst ingredient injecting means and the sedimentation suppression ingredient injecting means to complete the injection of the precursor of the active ingredient, The active ingredient input means and the active ingredient input means are turned off and the sedimentation suppression component input means is turned on to complete the deposition of the sedimentation suppression component, wherein the catalyst component injecting means is turned on while the catalyst component injecting means is turned off to inject the precursor of the catalyst component.
delete

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