Method of producing carbon nanotubes in fluidized bed reactor

Abstract

Provided is a method of producing carbon nanotubes by supplying a catalyst and a carbon source to a fluidized bed reactor. The fluidized bed reactor has an expanded zone. A flow velocity (linear velocity) of a raw material supplied to the fluidized bed reactor is equal to or higher than a terminal velocity of an internal material in the fluidized bed reactor.

Claims

1. A method of producing carbon nanotubes by supplying a catalyst and a carbon source to a fluidized bed reactor, wherein the fluidized bed reactor has an expanded zone, wherein a linear flow velocity of a raw material supplied to the fluidized bed reactor is equal to or higher than a terminal velocity of internal materials in the fluidized bed reactor, wherein the linear flow velocity of the raw material is equal to or more than 25 times a minimum fluidization velocity of the internal materials, and wherein the linear flow velocity of the raw material in the expanded zone is less than the terminal velocity of the internal materials.

2. The method according to claim 1, wherein the flow velocity of the raw material is 20 cm/s or higher.

3. The method according to claim 1, wherein the carbon source is one or more selected from the group consisting of saturated and unsaturated hydrocarbons having 1 to 4 carbon atoms.

4. The method according to claim 1, wherein the catalyst is a metal catalyst.

5. The method according to claim 4, the metal catalyst is any one metal selected from the group consisting of iron (Fe), molybdenum (Mo), titanium (Ti), vanadium (V), chromium (Cr), manganese (Mn), nickel (Ni), cobalt (Co), copper (Cu), cadmium (Cd), zinc (Zn), ruthenium (Ru), lead (Pd), silver (Ag), platinum (Pt) and gold (Au), or any one selected from alloys thereof.

6. The method according to claim 1, wherein the carbon nanotubes have a diameter of 0.4 nm to 10 nm.

7. The method according to claim 1, wherein the carbon nanotubes are comprised of 1 to 10 layers.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The above and other aspects, features, and advantages of the present disclosure will be more clearly understood from the following detailed description, taken in conjunction with the accompanying drawings, in which:

(2) FIGS. 1A to 1H schematically illustrate systems of fluidized bed reactors;

(3) FIGS. 2A and 2B illustrate a case in which flow velocity in a fluidized bed reactor is relatively high;

(4) FIG. 3 schematically illustrates a fluidized bed reactor having an expanded zone;

(5) FIGS. 4A to 4C schematically illustrate a behavior of internal materials according to a flow velocity in a fluidized bed reactor having an expanded zone. The particles are scattered from the reaction bed by the flow velocity of the terminal velocity U.sub.t or higher (4A). In the expanded zone, the flow velocity is decreased below U.sub.t to flow the particles downward again, and the particles a par to also agglomerate together (4B). In the original reaction bed and the expanded zone, the upward and downward flows, and the condensation and dispersion of the particles are repeatedly and mixedly proceeded (4C);

(6) FIGS. 5 and 6 illustrate yield and amount of carbon nanotubes obtained from a fluidized bed reactor; and

(7) FIG. 7 illustrates a purity of carbon nanotubes obtained from a fluidized bed reactor.

DESCRIPTION OF THE INVENTION

(8) Hereinafter, various exemplary embodiments in the present disclosure will be described with reference to the accompanying drawings. However, exemplary embodiments in the present disclosure may be variously modified, and the scope of the present disclosure is not limited to exemplary embodiments described below.

(9) In the present disclosure, a fluidized bed reactor may be provided with an expanded zone, and a flow velocity (linear velocity) of a raw material supplied to the fluidized bed reactor is preferably equal to or higher than a terminal velocity of internal materials in the fluidized bed reactor.

(10) In a case in which a flow velocity maintains a bubbling fluidization region, height of a bed of a dense phase may be relatively increased due to expansion of the bed. However, in a case of a gas flow velocity higher than the above-described velocity, scattering amounts of particles in carbon nanotubes (CNT) may be rapidly increased to maintain or slightly decrease the height of the thick phase, and to increase height including a transition region in which the dense phase and a lean phase are mixed. A flow velocity at which such a phenomenon begins to appear may be defined as a terminal velocity of the relevant CNT.

(11) The flow regime in the reaction bed may be changed, when the flow velocity is rapidly increased higher than the bubbling fluidized velocity to be equal to or higher than the terminal velocity U.sub.t (cases of (g) to (h) in FIG. 1). For example, particles and fluids may be mixed more vigorously, and the particles may begin to scatter out of the bed (FIGS. 2 and 3). When the particles flowing upward to a dilute region (a portion with fewer particles at the top of the bed) enter the expanded zone, the flow velocity may decrease rapidly to fall within the condition being lower than the terminal velocity U.sub.t, and then flow downward. It can be seen that such upward and downward flows are repeated (FIG. 4). In this case, the agglomeration and division of the internal materials may be repeated.

(12) When the effects on the fluidization velocity of the catalytic particles and particles of the prepared carbon nanotubes are similar to each other, for example, when a minimum fluidization velocity U.sub.mf and a terminal velocity U.sub.t are substantially similar to each other, in a case of the terminal velocity U.sub.t or higher, a mix characteristic may be good to dramatically increase yield of carbon nanotubes (FIGS. 5 and 6). Accordingly, it is preferable to operate the carbon nanotubes at the terminal velocity U.sub.t or higher to be advantageous in increasing the production amount, compared to the conventional flow velocity region.

(13) The flow velocity of the raw material supplied to the fluidized bed reactor is not particularly limited as long as it is equal to or higher than the terminal velocity of the internal materials in the fluidized bed reactor. The flow velocity of the raw material is preferably not less than 10 times the minimum fluidization velocity, more particularly, the flow velocity of the raw material is preferably 20 cm/s or higher. Meanwhile, the upper limit thereto may vary according to the design criteria of the expanded zone, but it is preferable that the expanded zone has a flow velocity equal to or lower than the terminal velocity.

(14) The fluidized bed reactor may produce carbon nanotubes at atmospheric pressure or at pressures in excess of the atmospheric pressure. The process may be carried out at an absolute pressure of 0.05 bar.Math.g to 1.5 bar.Math.g, with a pressure of 0.5 bar.Math.g to 1.0 bar.Math.g being particularly preferred.

(15) The reactor may be heated externally, the temperature may vary in the temperature range from 300 C. to 1600 C. This temperature should be high enough to allow deposition of carbon by decomposition to occur at a sufficient rate, and should not result in significant self-pyrolysis of gaseous hydrocarbons. This will result in the resulting material having an undesirably high content of amorphous carbon. An advantageous temperature range may be 500 C. to 800 C., and a decomposition temperature of 500 C. to 600 C. is particularly preferable.

(16) The catalyst may be reduced prior to entering an actual reaction chamber. The catalyst may be added primarily in the form of an oxide of a catalytically active metal, or even in the form of a precipitated hydroxide or carbonate. Transition metals or alloys thereof as broadly described in the literature referred to in the prior art may be generally suitable as a catalyst. In the present disclosure, it will be only mentioned some examples without limiting the general properties.

(17) This method is preferably used for catalysts containing manganese, iron, cobalt and support materials, wherein iron, cobalt and manganese are contained in an amount of 2 mol % to 98 mol %, based on the content of the active component in metal form. Further preferably, this method is used for catalyst further comprising molybdenum.

(18) The diameter of the catalyst supported on the support material is preferably 0.2 nm to 2000 nm, more preferably 10 nm to 1000 nm. The diameter of the catalyst may be measured by an atomic force microscope (AFM). As a combination of a catalyst supporting layer and the catalyst, from the viewpoint of productivity of carbon nanotubes, it is preferable that the catalyst supporting layer is Al.sub.2O.sub.3, and the catalyst is Fe. From the viewpoint of efficiently obtaining carbon nanotubes having a small diameter, it is preferable that the catalyst supporting layer is Al.sub.2O.sub.3, and the catalyst is Co.

(19) The support is composed of heat resistant beads having heat resistance. As materials of the support, it is preferable to include one or more element selected from the group consisting of Si, Al, Mg, Zr, Ti, O, N, C, Mo, Ta and W. Specific examples of the materials may include oxides such as SiO.sub.2, Al.sub.2O.sub.3 and MgO, nitrides such as SiN.sub.4 and AlN, and carbides such as SiC, or the like. A complex oxide such as Al.sub.2O.sub.3SiO.sub.2 is also preferred.

(20) The support preferably has a diameter of 100 m to 2000 m, more preferably 200 m to 2000 m. When the support has a diameter of 100 m or more, the support tends to be stably supported in the reaction tube and to flow efficiently, and the support and the carbon nanotubes tend to be easily separated from the same reaction tube. In the meantime, when the diameter of the support is 2000 m or less, the support tends to flow easily.

(21) In one embodiment of the present disclosure, a catalyst supporting material on the support may be included. In some embodiments, the catalyst supporting layer may be formed on the support in the catalyst supporting operation, the catalyst may be supported on the catalyst supporting layer, or the catalyst may be supported on the support without the catalyst supporting layer.

(22) The catalyst supporting material preferably contains one or more element selected from Si, Al, Mg, O, C, Mo and N. In particular, a precursor of the catalyst supporting material may be those for forming a catalyst supporting material layer containing an oxide such as SiO.sub.2, Al.sub.2O.sub.3 or MgO, a nitride such as Si.sub.3N.sub.4 or AlN, or a carbide such as SiC. The precursor of the catalyst supporting material may also be a catalyst supporting material layer containing a composite oxide of Al.sub.2O.sub.3SiO.sub.2. In particular, it is preferable that the precursor of the catalyst supporting material may form a catalyst supporting layer composed of Al.sub.2O.sub.3 from the viewpoint of stability of the catalyst particles. Specific examples of the precursor of the catalyst may include alkoxide such as aluminum isopropoxide and aluminum sec-butoxide, alkyl aluminum such as triethyl aluminum and triisobutyl aluminum, and aluminum chloride, and the like.

(23) An average thickness of the catalyst supporting layer formed on the support is preferably 1 nm to 100 nm, more preferably 1 nm to 50 nm. When the thickness of the catalyst supporting layer is 1 nm or more, the catalyst particles may be stably supported on the catalyst supporting layer, Ostwald ripening may be not easily generated, and the carbon nanotubes tend to grow in a longitudinal direction. Meanwhile, when the thickness of the catalyst supporting layer is 100 nm or less, the catalyst particles may be less likely to be received in the catalyst supporting layer during synthesis, and the carbon nanotubes tend to grow in a longitudinal direction.

(24) For the production of carbon nanotubes, aliphatic hydrocarbons, and light gaseous hydrocarbons such as olefins may be decomposed individually or as a mixture. However, alcohols, carbon oxides, in particular CO, heteroaromatic and aromatic compounds and functionalized hydrocarbons, such as aldehydes or ketones, may be used as long as they decompose on the catalyst. Mixtures of the hydrocarbons described above may also be used.

(25) Particularly suitable reactant gases may include, for example, methane, ethane, propane, butane or higher molecular weight aliphatics, ethylene, propylene, butene, butadiene or higher molecular weight olefins, or aromatic hydrocarbons or oxides of carbon, or hydrocarbons having alcohols or heteroatoms. For example, aliphatic or olefinic hydrocarbons each having 1 or 2 to 10 carbon atoms, or 1 nuclear or 2 nuclear aromatic hydrocarbons are preferably used. Aliphatic (C.sub.xH.sub.2x+2) and olefin (C.sub.xH.sub.y) having a carbon number x of 1 to 4, or 2 to 4, respectively, are particularly preferably used.

(26) In carrying out the process, the gaseous mixture may be passed through a suitable gas distributor to an apparatus disposed on a lower end of a reactor, by adding an inert gas such as, for example, nitrogen, hydrogen or argon. The molar ratio of the inert gas in the gas mixture is preferably 0.1 to 0.5.

(27) Hereinafter, preferred embodiments of the present disclosure will be described with reference to the accompanying drawings. The embodiments of the present disclosure may be modified into various other forms, and the scope of the present disclosure is not limited to the embodiments described below.

Example

(28) A fluidized bed reactor used for a reaction comprises an inlet portion extending linearly in the vertical direction and having an inner diameter of 0.15 m and a length of 2.0 m, an expanded zone slantedly connected to the inlet portion and having an inner diameter of 0.30 m and a length of 0.65 m, a dispersion plate formed with a through hole having an inner diameter of 25 mm to discharge carbon nanotubes (CNT), after end of reaction, and a structure in which gas is supplied at a lower end of the dispersion plate and gas is discharged at an upper end of the dispersion plate. Further, the heating portion is a heating device for covering the predetermined height position of the inlet portion and the expanded zone to heat the inlet portion and the expanded zone.

(29) A catalyst having a particle size of 130 microns and a density of 1300 kg/m3, in which iron and cobalt were supported on an Al.sub.2O.sub.3 support, was charged to a fluidized bed reactor having the structure shown in FIG. 3. The temperature of the catalyst in the reactor was maintained at 690 C., and hydrogen (molar ratio of 0.2) and ethylene as inert gases were introduced into the reactor at a temperature of 530 C. The physical properties of the catalysts and carbon nanotubes used are shown in Table 1.

(30) As a result of confirming the hydraulic characteristics in the cold model, the Ut value is expected to be 22 to 24 cm/s. As the flow regime is expected to change around this flow velocity, the reaction was carried out for 30 minutes while changing the fluidization velocity of the hydrocarbons and the catalyst as described in Table 2.

(31) As the flow velocity increases, and the flow rate increases (i.e., the higher the fluidization velocity), the reaction pressure in the same system slightly increases in a proportional relation. 250 g of carbon nanotubes manufactured by the same method were filled to perform a smooth fluidization. The catalyst was filled to maintain the same specific velocity according to the flow velocity.

(32) TABLE-US-00001 TABLE 1 Catalyst Carbon Nanotubes Size [micron] 130 400 Particle Density 1300 150 [kg/m.sup.3]

(33) TABLE-US-00002 TABLE 2 Conditions Value Initial Catalyst Temperature 690 [ C.] Reaction Time [min] 30 Molar Ratio of Inert Gas 0.2 (Hydrogen) (mol Ratio) Feed Temperature [ C.] 530 Fluidization Velocity [cm/s] 18 21 24 26 29 32 Reaction Pressure [bar.g] 0.2 0.3 0.3 0.4 0.5 0.6 Yield [%] 22.7 21.3 39.2 37.4 39.0 43.2 Carbon nanotubes per Catalyst 2.6 2.5 4.5 4.3 4.5 5.0 [g] Carbon nanotubes Purity [%] 72.5 70.1 84.8 85.1 84.0 85.2

(34) As a result of the reaction experiment, it was confirmed that the yield and the amount of carbon nanotubes per catalyst were dramatically increased when the value was lower than the predicted Ut value (see FIGS. 4 and 5). It was confirmed that the purity of the final product largely changed from this point as well (see FIG. 6).

(35) According to the present disclosure, in a case that carbon nanotubes are produced through a catalytic reaction in a fluidized bed, when the flow velocity is raised in the turbulent or fast fluidization region higher than the bubbling fluidization region, the yield, and the purity of the carbon nanotubes may be remarkably increased.

(36) While exemplary embodiments have been shown and described above, it will be apparent to those skilled in the art that modifications and variations could be made without departing from the scope of the present disclosure as defined by the appended claims.