English
Tiếng Việt
(en)The present invention relates to a system for optimizing and controlling the particle size distribution and scale-up of production of nanoparticle in an aerosol flame reactor. The method provides nanoparticles with desired, optimized and controlled particle size and the specific surface area in aerosol reactors using a simulation tool with programmed instructions. The said simulation tool couples flame dynamics model and particle population balance model.
1.ApplicationNumber: US-201113180401-A
1.PublishNumber: US-2012009118-A1
2.Date Publish: 20120112
3.Inventor: RUNKANA VENKATARAMANA
BUDDHIRAJU VENKATA SUDHEENDRA
VARMA NADIMPALLI NAGARAVI KUMAR
4.Inventor Harmonized: RUNKANA VENKATARAMANA(IN)
BUDDHIRAJU VENKATA SUDHEENDRA(IN)
VARMA NADIMPALLI NAGARAVI KUMAR(IN)
5.Country: US
6.Claims:
(en)The present invention relates to a system for optimizing and controlling the particle size distribution and scale-up of production of nanoparticle in an aerosol flame reactor. The method provides nanoparticles with desired, optimized and controlled particle size and the specific surface area in aerosol reactors using a simulation tool with programmed instructions. The said simulation tool couples flame dynamics model and particle population balance model.
7.Description:
(en)CROSS REFERENCE TO RELATED APPLICATION[S]
This application claims priority to Indian Patent Application to Runkana, et al., serial number 1984/MUM/2010, filed Jul. 12, 2010, the disclosure of which is hereby incorporated entirely herein by reference.
FIELD OF INVENTION
The present invention relates to a system and a method for optimizing and controlling the particle size distribution and for scale-up of production of nanoparticles in an aerosol flame reactor. More particularly the present invention relates to a system and a method for optimization of mean particle size, specific surface area, and distribution of nanoparticles in aerosol reactors.
BACKGROUND OF THE INVENTION AND PRIOR ART
In the recent years, nanotechnology has gained importance and has become one of the major research focus areas for its fundamental and practical applications. The smaller size of the particles especially less than 100 nm is one of the key parameters that is responsible for various properties such as electronic, electric, optical, magnetic chemical and mechanical properties that makes nanoparticles suitable for several applications in the fields of ceramics, catalysis, coatings, electronics, chemical and mechanical polishing, data storage, fuel cells, etc.
Many commodity and specialty chemicals and materials such as carbon black, titania, silica and zinc oxide are produced in the form of fine particles, which find applications in a wide variety of industrial and domestic products ranging from tyres, printing inks, paints and pigments, plastics, optical fibers, catalysts, pharmaceutical ingredients and cosmetics.
For many practical applications, it is desirable to have particles of small size as well as of narrow size distribution because smaller particles with narrow size distribution result in better properties of finished products. For example, activity of catalysts, hardness and strength of metals, electrical conductivity of ceramics improve as the particle size decreases.
These special properties of the nanoparticles can vary markedly from those of the analogous bulk materials. The physical and chemical properties of the nanomaterials tend to be exceptionally dependent on their size and shape or morphology. As a result, materials scientists are focusing their efforts on developing simple and effective methods for producing nanomaterials with controlled particle size and morphology and hence, improving their properties.
Many techniques and methods have been employed for the synthesis of nanoparticles on the laboratory scale. Some of the well known methods and systems are as follows:
a) Gas phase synthesis process: It is one of the routinely employed techniques used for large scale production of nano powders, as it is a single step process without any moving parts and any extensive solid-liquid separation processes. b) Chemical and mechanical routes such as microemulsion-based synthesis and grinding.
Amongst the above mentioned methods and techniques, flame aerosol synthesis is one of the commonly and widely used technologies for synthesis of fine powders on an industrial scale, as it offers many control parameters like flame temperature, flame structure, stoichiometry, pressure level, residence time distribution, turbulence etc.
The typical method of synthesis of nanoparticles in flame aerosol synthesis is as follows:
a) Injecting the precursor or reactant into the reactor in the form of a vapor or liquid using a carrier gas along with air and fuel. b) Chemical reactions occur in the gas phase in the flame at high temperatures and results in product molecules; c) Growth of the particles by coagulation and/or surface reaction to form product particles due to decrease in the temperature at downstream in the reactor
The temperature decrease at the downstream of the reactor results in the particle growth mainly by coagulation and results in irregularly structured particles and particle distribution.
Further, the powders produced in the aerosol flame reactors have a relatively large particle size and have wide size distribution, with particle size ranging from a few nanometers to micrometers, the said wide particle size distribution is influenced by several factors, namely, burner geometry, nature of flame and its configuration, inlet reactant flow rate and its concentration, and turbulence characteristics, gas and particle velocities, pressure and temperature profiles and residence time distribution inside the reactor.
Yet another challenging task lies in scaling up of the process to produce nanoparticles in large quantities, while at the same time maintaining the particle size in the nanometer range.
Hence, there is a need for controlling the product particle size distribution by manipulating and designing the process input variables.
Further, there is also a need for scaling up the process of synthesis of nanoparticles with desired characteristics.
Some of the prior arts that propose a system, method and scale-up process for synthesis of nano-particles are as follows:
U.S. Pat. No. 5,498,446 (Axelbaum et al) teaches a method and apparatus for reacting sodium vapor with gaseous chlorides in a flame to produce nanoscale particles of un-oxidized metals, composites and ceramics. The flame is operated under conditions which lead to condensation of a NaCl by-product onto the particles. The condensate encapsulates the particles and aids in controlling desired particle size and preventing undesirable agglomeration among the particles during synthesis. Following synthesis, oxidation of the particles is inhibited by the encapsulation and handling character of the products is greatly enhanced. Though the '446 patent discloses a method and apparatus for synthesis of nanoparticles, it does not disclose the means for optimization, and controlled particle size distribution of nanoparticles. Further, '446 patent does not address challenging aspect for the scale-up of production of nanoparticles with the desired particle size.
EP 1122212 (Hendrik et al) teaches a method to control particle characteristics of flame made nanostructured powders and investigated at high production rates addressing the required safety concerns. The influence of increasing the fuel and production rate, burner configuration and total oxidant flow on particle size morphology and composition is presented for synthesis of silica in a commercial oxy-hydrogen burner. Hence, the said patent application discloses a method to control particle characteristics of flame made nanostructured powders experimentally, which is expensive and time consuming.
“Computational fluid-particle dynamics for the flame synthesis of alumina particles” by Johannessen et al (2000) discloses a mathematical model for the dynamics of particle growth during the synthesis of the ultra fine particles in diffusion flame. The said article combines a simple batch model for coagulation and coalescence of aerosol particles along with the computational fluid dynamics model (Fluent) in a decoupled manner to simulate the gas composition, temperature and velocity profiles in a flame reactor and integrate the simple monodisperse population balance (MPB) model along a set of “characteristic trajectories” only and not for the entire flame structure. Further, the said article discloses the computational fluid-particle dynamics for the flame synthesis using specific burner with three concentric quartz tubes. Further, the said article does not determine the particle characteristics throughout the reactor and does not determine the particle characteristics using various burners and does not address the challenging aspect for the scale-up of production of nanoparticles with the desired particle size. Further, the simple kinetics used in the article only applies for a limited range of temperature and particle size.
Thus, in light of the above mentioned prior arts it is evident that there is a need to have a customizable solution for optimizing and controlling the particle size distribution in a continuous process rather than a batch process and scale-up of production of nanoparticle in an aerosol flame reactor.
Further, there is a need to have a customizable solution to optimize and control the particle size distribution and scale-up of production of nanoparticles in aerosol flame reactor in a coupled manner i.e. by solving the particle dynamics equations in each and every cell of the computational domain.
It is also evident that the process equipment design and scale-up, pilot scale studies are tedious and expensive. Hence, there is growing demand to have a customizable solution for synthesis and scale-up of nanoparticles with desired particle size and shape by improving the process design and scale-up which provides the basic process understanding and dynamic behavior of the flame reactor to reduce the efforts on pilot plant studies for the synthesis of any material.
In the present invention we propose a novel approach for optimizing and controlling the particle size distribution and scale-up of production of nanoparticles in aerosol flame reactor to overcome the above mentioned limitations for synthesis of nanoparticles with controlled particle size, shape and particle size distribution.
In order to address the long felt need for such a solution, the present invention provides a system and method for optimizing and controlling the particle size and scale-up of production of nanoparticles in an aerosol flame reactor, described more particularly herein after.
OBJECTS OF THE INVENTION
The principle object of the invention is to provide a system and method for optimizing and controlling the particle size and specific surface area of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide a system and method for scaling up the synthesis of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide cost effective system and method for optimizing and controlling the particle size and specific surface area of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide cost effective method for scaling up synthesis of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide system and method which optimizes and controls the particle size and specific surface area of nanoparticles in an aerosol flame reactor requiring less experimentation and utilizing less time.
Another object of the invention is to provide a method for scaling up synthesis of nanoparticles in an aerosol flame reactor which requires less experimentation.
Yet another object of the invention is to provide a simulation tool with programmed instructions for production of nanoparticles with controlled properties.
SUMMARY OF THE INVENTION
The present invention discloses a system and method for optimizing and controlling mean particle size and specific surface area and for scale-up of nanoparticle production in an aerosol flame reactor.
A system for optimizing and controlling mean particle size and specific surface area and for scale-up of nanoparticle production in aerosol flame reactor comprising of:
an aerosol flame reactor integrated with process instruments, wherein the said reactor further comprises of
at least one burner; at least one precursor or reactant fed to the said aerosol flame reactor; at least one stream input fed along with at least one precursor or reactant to the said aerosol flame reactor;
a simulation tool with programmed instructions to cause the processor to couple flame dynamics model and particle population balance model in order to optimize and control mean particle size and specific surface area and for scale-up of nanoparticle production in aerosol flame reactor.
A method for optimizing and controlling the mean particle size and specific surface area and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments, wherein the said method comprises the steps of:
a) Determining
i) the operating data for physical process parameters from the said process instruments integrated with aerosol flame reactor; ii) the mixing characteristics of the precursor or reactant at a particular concentration and the stream input fed to the burner of the said aerosol flame reactor with the process instruments; iii) the flame temperature and different species mass-fractions throughout the said reactor using the Flame dynamics model coupled to the simulation tool with programmed instructions; iv) the data for influence of burner configuration and the design of the reactor on the properties of nanoparticles.
b) Feeding the determined data of step i) to the simulation tool with the programmed instructions to obtain the simulated data for optimizing and controlling the mean particle size and specific surface area and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments; c) Implementation of the simulated data obtained from the said simulation tool with programmed instructions for optimizing and controlling the mean particle size and specific surface area and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments; d) Estimating the rate kinetics of the precursor oxidation reaction using the precursor to product conversion kinetics coupled to Particle population balance model of the said simulation tool with programmed instructions; e) Obtaining the output as product particle size and specific surface area of the reactor from the simulation tool with the programmed instructions to optimize and control the particle size distribution and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments.
BRIEF DESCRIPTION OF THE DRAWINGS
The foregoing summary, as well as the following detailed description of preferred embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the invention, there is shown in the drawings, exemplary constructions of the invention; however, the invention is not limited to the specific methods disclosed. In the drawings:
FIG. 1 of the present invention illustrates the structure of the simulation tool with programmed instructions.
FIG. 2 illustrates the typical diffusion flame burner.
FIG. 3 illustrates the typical aerosol flame burner configurations (Source of figure: T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 4 illustrates the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration B (Source for Flame B figure: T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 5 illustrates the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration C (Source for Flame C figure: T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 6 illustrates the comparison of axial temperature profile in a laboratory scale flame reactor determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 7 illustrates the comparison of alumina aggregate particle sizes determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 8 illustrates the burner configuration with five concentric tubes for silica nanoparticles synthesis from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
FIG. 9 illustrates the effect of TEOS (precursor) concentration on silica particle specific surface area and compares the data determined by the simulation tool of the present invention with the experimental data from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
FIG. 10 illustrates Titanium dioxide particle diameter as a function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
FIG. 11 illustrates Silica particle diameter as function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
FIG. 12 illustrates the influence of the different burner designs on the velocities of the oxidant and the fuel on carbon black particle size.
DETAILED DESCRIPTION OF THE INVENTION
Before the present method, and hardware enablement are described, it is to be understood that this invention in not limited to the particular methodologies, and hardware described, as these may vary. It is also to be understood that the terminology used in the description is for the purpose of describing the particular versions or embodiments only, and is not intended to limit the scope of the present invention which will be limited only by the appended claims. The words “comprising,” “having,” “containing,” and “including,” and other forms thereof, are intended to be equivalent in meaning and be open ended in that an item or items following any one of these words is not meant to be an exhaustive listing of such item or items, or meant to be limited to only the listed item or items. The disclosed embodiments are exemplary to the invention, which may be embodied in various forms.
The present invention provides a system for optimizing and controlling particle size distribution and for scale-up of nanoparticle production in an aerosol flame reactor comprising of:
an aerosol flame reactor integrated with process instruments, wherein the said reactor further comprises of
at least one burner; at least one precursor or reactant fed to the said aerosol flame reactor; at least one stream input fed along with at least one precursor or reactant to the said aerosol flame reactor;
a simulation tool with programmed instructions to cause the processor to couple flame dynamics model and particle population balance model in order to optimize and control mean particle size and specific surface area and for scale-up of nanoparticle production in an aerosol flame reactor.
According to one of the embodiments of the present invention, the process instruments comprises of precursor flow rate gauze, precursor pressure gauze, air flow rate gauze, air pressure gauze, fuel flow rate gauze, fuel pressure gauze, carrier gas flow rate gauze, carrier gas pressure gauze and temperature sensors.
The process instruments integrated with the aerosol flame reactor provides the operating data for variables such as precursor flow rate, precursor pressure, air flow rate, air pressure, carrier gas flow rate, carrier gas pressure to the simulation tool with programmed instructions to manage the process.
FIG. 1 of the present invention illustrates the structure of the simulation tool with programmed instructions.
According to one of the embodiments of the present invention, simulation tool with programmed instructions ( 10 ) couples flame dynamics model ( 20 ) and particle population balance model ( 30 ) to optimize and control the mean particle size and specific surface area and for scale-up of the production of nanoparticles with the desired characteristics.
Flame dynamics model ( 20 ) coupled to the simulation tool with programmed instructions determines the flame temperature and different species mass-fractions throughout the reactor and further determines and simulates the physical process parameters such as but not limited to fluid flow rate, heat transfer rate, etc.
Further, the Flame dynamics model ( 20 ) is coupled with fuel combustion kinetics ( 70 ) for managing operating data obtained from the various process instruments of the aerosol flame reactor.
The governing equations for the flame dynamics model are as follows:
The equation of motion according to Bird et al., (2002)
∂
∂
t
(
ρ
u
)
=
-
[
∇
·
ρ
uu
]
-
∇
p
-
[
∇
·
τ
]
-
[
∇
·
τ
(
t
)
]
+
ρ
g
(
1
)
Wherein ρ is gas density (kg/m 3 ), u is velocity (m/s), τ (t) is turbulent momentum flux tensor (kg/s 2 /m), τ is stress tensor (kg/s 2 /m) and g is gravitational acceleration (m/s 2 ).
Further, as per Launder and Spalding (1974), the k-ε model is used for calculating the turbulent kinetic energy, k (m 2 /s 2 ) and its dissipation rate, ε (m 2 /s 3 )
∂
∂
t
(
ρ
k
)
+
∇
·
(
ρ
uk
)
=
∇
·
[
(
μ
+
μ
t
σ
k
)
∇
k
]
+
P
k
-
ρɛ
(
2
)
∂
∂
t
(
ρɛ
)
+
∇
·
(
ρ
u
ɛ
)
=
∇
·
[
(
μ
+
μ
t
σ
k
)
∇
ɛ
]
+
ɛ
k
(
C
ɛ
1
P
k
-
C
ɛ
2
ρɛ
)
(
3
)
where P k is turbulence production due to viscous and buoyancy forces (kg/s 3 ) which is obtained using the following equation:
P
k
=
μ
t
∇
u
·
(
∇
u
+
∇
u
T
)
-
2
3
∇
·
u
(
3
μ
t
∇
·
u
+
ρ
k
)
+
P
kb
(
4
)
where μ t is turbulent viscosity (kg/m/s) given by
ρ
C
μ
k
2
ɛ
and P kb is turbulence production due to buoyancy forces (kg/s 3 ).
The continuity equation for component i as given by (CFX 11.0 User's Manual):
∇·(ρ {right arrow over (v)}Y i )=−∇· {right arrow over (J)} i +R i +S i (5)
where R i is the net rate of production of species i by a chemical reaction, S i is the rate of creation by addition from the dispersed phase, Y i is mass fraction of component i and J i is diffusion flux of species i, which arises due to concentration gradients.
The equation of energy in terms of the specific enthalpy h (J/kg) is given by (CFX 11.0 User's Manual):
∂
∂
t
(
ρ
h
)
+
∇
·
ρ
hu
=
∇
·
(
k
g
∇
T
)
+
∂
p
∂
t
+
u
·
∇
p
+
τ
:
∇
u
+
S
E
(
6
)
where k g is thermal conductivity of the gas (J/m/s/K), S E is source term that denotes the rate of heat liberated due to chemical reaction and heat absorption due to radiation. τ:∇u is always negative and is called the viscous dissipation.
The P-1 radiation model according to Siegel and Howell (1992) is incorporated in the enthalpy balance to account for radiant energy absorption and irradiation. The radiation flux is expressed by expanding the radiation intensity in series of orthogonal harmonics in this model. The radiation flux is then directly incorporated into the enthalpy balance to account for the radiation heat transfer process.
The rate of fuel combustion is calculated using the eddy-dissipation model (EDM) proposed by Magnussen and Hjertager (1976). The chemical reaction is fast relative to the transport processes. The fuel combustion model consists of two rate expressions, Equations 7 and 8 given below. Equation 7 represents the reaction rate R 1 (kmol/m 3 /s) that accounts for the mixing of the reactants in the turbulent eddies.
R
1
=
A
EDM
ɛ
k
min
(
[
I
]
v
I
)
(
7
)
where [I] (kmol/m 3 ) is concentration of the reactant I, v I is the stoichiometric coefficient of component I and A EDM is a numerical constant.
Equation 8 represents the reaction rate R 2 (kmol/m 3 /s) that accounts for the mixing of the hot product gases with the cold reactant gases when heat transport to the unreacted gases is the limiting factor.
R
2
=
A
EDM
B
EDM
ɛ
k
(
∑
P
[
I
]
W
I
∑
P
v
I
W
I
)
(
8
)
where P loops over all product components in the reaction. In Eq. 8, W I (kg/kgmol) is molar mass of the component I and B EDM is a numerical constant. The rate of combustion is determined by the smaller of the two rates R 1 and R 2 .
Particle population balance model ( 30 ) coupled to the simulation tool with programmed instructions determines the properties of evolved particles.
The governing equations for particle population balance model ( 30 ) are as follows:
The rate of change of particle number concentration (N) is given by:
∂
N
∂
t
+
∂
u
j
N
∂
x
j
=
∂
∂
x
j
(
η
∂
N
∂
x
j
)
+
I
-
1
2
β
N
2
(
9
)
where η (m 2 /sec) is diffusion coefficient, β (m 3 /sec) is coagulation rate coefficient and I (#/m 3 -sec) is rate of nucleation (Ji et al., 2007):
I=k n ( S− 1) N n (10)
where k n (#·s −1 ·m 3 ) is nucleation rate constant, S is degree of supersaturation and the exponent N n is taken as 1. The last term on the RHS of Eq. 9 represents the reduction of particle number concentration N by coagulation. The coagulation rate coefficient β is calculated using the Fuchs equation (Fuchs, 1964; Seinfield, 1986).
β
=
8
π
Dr
c
(
r
c
2
r
c
+
2
t
p
+
2
D
cr
c
)
(
11
)
The particle diffusion coefficient D is calculated as given by Johannessen (1999):
D
=
K
b
T
6
π
μ
r
c
[
5
+
4
Kn
+
6
Kn
2
+
18
Kn
3
5
-
Kn
+
(
8
+
π
)
Kn
2
]
(
12
)
where Kn is the Knudsen number (λ/r c ), λ (m) is the gas mean free path and μ (Pa·s) is viscosity of the gas. The total surface area density of the particles A (m 2 /m 3 ) decreases by coalescence but remains unaffected by coagulation.
∂
A
∂
t
+
∂
u
j
A
∂
x
j
=
∂
∂
x
j
(
η
∂
A
∂
x
j
)
+
Ia
p
-
1
τ
f
(
A
-
A
min
)
(
13
)
where a p is the monomer surface area (m 2 ), τ f is characteristic coalescence time (s) and A min is minimal total surface area density, given by:
A min =(π N ) 1/3 (6 V) 2/3 (14)
where V is total particle volume density (m 3 /m 3 ). The characteristic coalescence time τ f depends on temperature, primary particle size, material, sintering mechanism, etc. Particle coalescence occurs due to a combination of mechanisms, namely, surface diffusion, grain boundary diffusion, solid state diffusion and viscous flow.
The characteristic coalescence time τ f of two separate, contacting spherical particles is given by Johannesssen et al. (2000):
τ
f
=
k
0
d
p
m
T
T
0
exp
(
E
A
R
(
1
T
-
1
T
0
)
)
(
15
)
where E A is activation energy, d p is initial diameter of the two primary contacting spherical particles in an aggregate, k 0 is pre-exponential term, T 0 is temperature and R is universal gas constant.
The total particle volume density V (m 3 /m 3 ) increases by nucleation and chemical reaction.
∂
V
∂
t
+
∂
u
j
V
∂
x
j
=
∂
∂
x
j
(
η
∂
V
∂
x
j
)
+
Iv
p
+
S
V
(
16
)
where v p is the monomer volume (m 3 ) and S V is rate of increase of total particle mass per unit volume of the system (kg/m 3 ·s), given by the following equation:
S V =(π/2) AGρ (17)
where G is total growth rate of a particle (m/s). The total growth rate G under the combined control of chemical reaction and mass transfer is calculated as
G
=
G
M
G
C
G
M
+
G
C
(
18
)
where G M is growth rate of a particle under the control of mass transfer (m/s) and G C is growth rate of a particle under the control of chemical reaction kinetics (m/s). The linear growth rate of a particle under the control of mass transfer G M (m/s) is given by:
G
M
=
4
V
mol
D
A
-
O
2
1.013
×
10
5
8.314
T
d
n
Y
A
*
(
S
-
1
)
(
19
)
where V mol is molar volume of the product molecule produced (m 3 /mol): TiO 2 , SiO 2 or Carbon black, D A-O2 is diffusion coefficient of A (product molecule) through O 2 (m 2 /s), S is degree of supersaturation, d n is number-averaged particle size (m), Y* A is mole fraction of A at saturation temperature T. The growth rate of a particle under the control of chemical reaction kinetics, G C is given by the following expression:
G c =k gc ( S− 1) N g (20)
where k gc is particle growth rate constant (m/s). The exponent N g is assumed to be 1. When S≦1, G C is set equal to zero.
Particle population balance model ( 30 ) determines the properties of the evolved particles on the basis of the above discussed equations for particle number concentration, particle volume and particle surface area.
Particle population balance model ( 30 ) is further coupled to precursor to product conversion kinetics ( 80 ) for monitoring and controlling the particle size distribution of nanoparticles and further estimates the rate kinetics of the precursor oxidation reaction.
The combined eddy dissipation-finite rate chemistry model available in CFX 11.0 represents the oxidation of precursor to product molecules. The rate of oxidation is taken as the minimum of the rates obtained using the Arrhenius expression, given below, and the eddy dissipation model (Eqs. 7 and 8).
R
A
=
A
exp
(
-
E
RT
)
C
precursor
C
O
2
(
21
)
where A is pre-exponential factor, E (J/kmol-K) is activation energy, C precursor (kmol/m 3 ) is the concentration of the precursor, C O 2 (kmol/m 3 ) is concentration of oxygen and R (J·kmol −1 ·K −1 ) is the universal gas constant.
In one of the embodiments of the present invention, the simulation tool with programmed instructions is developed on a FORTRAN platform to simulate and determine the physical processes.
Nanoparticles with desired particle size and shape are produced in the aerosol flame reactors on provision of the various optimized operating conditions ( 40 ) such as but not limited to flame temperature, pressure, optimum gas flow rate, and reactant or precursor concentrations.
The values for various optimized operating conditions are provided to the simulation tool with the programmed instructions so as to simulate and determine the influence of these various operating parameters on the particle size and specific surface area of the nanoparticles.
Further, according to another embodiment of the present invention, the geometry and design ( 50 ) of the reactor and burner also influences the particle size, particle size distribution and shape of the nanoparticles. The various sizes of burners, the number of concentric tubes of the burner, the spacing between each tube, diameter of the tubes of the burner are fed to the simulation tool with the programmed instructions so as to simulate and determine the influence of the variable geometry and design of the burner and reactor on the particle size.
Further according to one of the embodiments of the present invention, the burners are designed and configured for various stream inputs to the aerosol flame reactor.
Further according to one of the embodiments of the present invention the burner geometry is designed and implemented in co-ordination with the simulation tool with programmed instructions in terms of number of concentric tubes, diameters of each tube and spacing between each tube.
According to another embodiment of the present invention the various characteristics and properties of the physical constants and materials ( 60 ) are fed to the simulation tool with the programmed instructions so as to simulate and determine the influence of the characteristics and properties of the materials ( 60 ) on the particle size distribution.
The simulation tool with the programmed instructions provides output ( 90 ) as product particle size and specific surface area of the reactor.
FIG. 2 of the present invention illustrates the typical diffusion flame burner, wherein carrier gas along with precursor or reactant is injected through the centre tube; fuel is injected through the second tube and oxidant through the third tube; wherein the diameter of centre tube, second tube and third tube are represented by d 1 , d 2 and d 3 respectively.
According to one of the embodiments of the present invention, the simulation tool with programmed instructions of the present invention determines the influence of the three burners with varying diameters of the central tube, the annulus and the outer tube, for scale-up of production of nanoparticles. The inner diameter of the central tube (d 1 ) can be in the range 1.5-5.5 mm, the inner diameter of the outer most tube (d 3 ) can range from 5 mm to 25 mm while the inner diameter of the tube in between the central and outer tubes (d 2 ) could be in the range 3 mm-12 mm.
FIG. 3 of the present invention illustrates the typical aerosol flame burner configurations according to Johannssen et al., (2000).
According to one of the embodiments, four typical aerosol flame reactor burner configurations are illustrated in FIG. 3 with respect to the various modes of stream inputs.
Flame A illustrates the injection of carrier gas along with precursor and air from the centre tube and fuel through the third tube, whereas no stream input is provided through the second tube.
Flame B illustrates the injection of carrier gas along with precursor from the centre tube and air through the second tube while fuel through the third tube.
Flame C illustrates the injection of carrier gas along with precursor from the centre tube and fuel through the second tube while air through the third tube.
Flame D illustrates the injection of carrier gas along with precursor and fuel from the centre tube and air through the third tube, whereas no stream input is provided through the second tube.
Any of the four typical aerosol flame reactor burner configuration values and geometries as illustrated in FIG. 3 can be fed to the simulation tool with programmed instructions of the present invention to simulate, and determine the influence of the burner configuration and geometries on the particle size distribution in the aerosol flame reactor.
EXAMPLES OF WORKING OF THE INVENTION
The invention is described in the examples given below which is provided only to illustrate the invention and therefore should not be construed to limit the scope of the invention.
Example 1
FIG. 4 shows the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration B (Flame B) of FIG. 3 , wherein methane in the input stream is fed to the burner through the third tube; air in the second tube and precursor and carrier gas in the first tube.
The configuration of input streams (methane, air, carrier gas and precursor) to the burner has a strong influence on the flame characteristics and hence on the particle size. The influence of burner configuration and arrangement of the burner configurations on flame temperature profile is shown in FIG. 4 .
The flames in configuration B ( FIG. 4 ) are shorter flames surrounded by air on both sides and hence, yield a more efficient combustion.
Example 2
FIG. 5 shows the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration C (Flame C) of FIG. 3 , wherein methane in the input stream is fed to the burner through the second tube; air in the third tube and precursor and carrier gas in the first tube.
The configuration of input streams to the burner has a strong influence on the flame characteristics and hence on the particle size. The influence of burner configuration on flame temperature profile is shown in FIG. 5 .
The configuration B (flame B) has methane in the third tube and air in the second tube where as configuration C has methane in the second tube and air in the third tube. This difference in arrangement alters the flame shape and size drastically as seen in the FIGS. 4 and 5 .
The flames in configuration B ( FIG. 4 ) are surrounded by air on both sides and hence, yield a more efficient combustion than those in configuration C.
For this reason, flames in configuration B are shorter than those in configuration C ( FIG. 5 ), with slightly higher temperatures than the latter.
Example 3
FIG. 6 illustrates the comparison of axial temperature profile in a laboratory scale flame reactor determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 6 compares the data determined by the simulation tool with programmed instructions for the axial temperature profile and influence of distance above burner outlet (m) on the mean particle size with that of published experimental data of Johanessen et al (2000).
Further, Table 1 below provides and compares the simulated data determined by the simulation tool with programmed instructions for the axial temperature profile and influence of distance above burner outlet (m) on the mean particle size with that of published experimental data of Johanessen et al (2000).
TABLE 1
Distance above
burner outlet
Temperature (K)
(m)
Experimental
Simulated
0.00
500
500
0.01
1018
1091
0.02
1117
1493
0.03
1342
1672
0.04
1608
1764
0.05
1887
1816
0.06
1842
1796
0.07
1698
1572
0.08
1486
1462
It can be noticed that the data determinations made by the simulation tool of the present invention are relatively close to the experimental measurements and thereby indicating the accuracy of the data determinations made by the simulation tool of the present invention.
Example 4
FIG. 7 illustrates the comparison of alumina aggregate particle sizes determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)). Further, FIG. 7 compares the data determined by the simulation tool with programmed instructions for the various burner configurations and average particle size with that of published experimental data of Johanessen et al (2000).
Further, Table 2 below provides and compares the data determined and provided by simulation tool with programmed instructions i.e. simulated data for the various burner configurations and average particle size with that of published experimental data of Johanessen et al (2000).
TABLE 2
Average particle size (nm)
Configuration
Experimental
Simulated
C1 179
193
C2 188
204
C3 223.
216
C4 176.
203
C5 187.
171
C6 196.
276
B1 115.
109
B2 146.
135
B3 180.
151
B4 106.
140
B5 132.
141
B6 174.
160
It can be noticed that the data determinations made by the tool of the present invention are relatively close to the experimental measurements and thereby indicating the accuracy of the data determined by the simulation tool of the present invention.
Example 5
FIG. 8 illustrates the burner configuration with five concentric tubes for silica nanoparticles synthesis from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
FIG. 8 shows that the simulation tool of the present invention was tested further for production of silica nanoparticles using a burner with five concentric tubes, wherein Ar and TEOS (precursor) was fed through the centre tube of the burner, Ar was fed through the second tube, H 2 was fed through the third tube, O 2 was fed through the fourth tube and air was fed through the fifth tube.
Example 6
FIG. 9 illustrates the effect of TEOS (precursor) concentration on silica particle specific surface area and compares the data determined by the simulation tool of the present invention with the experimental data from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
The burner configuration of FIG. 8 was integrated with the simulation tool of present invention, to determine the specific surface areas of silica particles at different precursor concentrations and compared with published experimental data from Jang et al (2001) in FIG. 9 .
FIG. 9 illustrates the effect of TEOS (precursor) concentration on silica particle specific surface area and compares the data determined by the simulation tool of the present invention with the experimental data from Jang et al (2001). Further, Table 3 below provides and compares the effect of TEOS (precursor) concentration on silica particle specific surface area and the data determined and obtained by the simulation tool i.e. simulated data of the present invention with the experimental data from Jang et al (2001).
TABLE 3
TEOS Concentration
Specific surface area (m 2 /g)
(l/min)
Experimental
Simulated
1.00E−05
240
225
1.00E−04
230
218
1.91E−04
101
94
2.50E−04
68
60
It can be observed that the trend determined by the simulation tool of the present invention is in close agreement with the experimental measurements, further indicating the accuracy of the data determined by the simulation tool of the present invention.
Further, the simulation tool with programmed instructions of the present invention was used to determine the influence of the three burners with varying diameters of the central tube, the annulus and the outer tube, for scale-up of production of nanoparticles. The inner diameter of the central tube (d 1 ) can be in the range 1.5-5.5 mm, the inner diameter of the outer most tube (d 3 ) can range from 5 mm to 25 mm while the inner diameter of the tube in between the central and outer tubes (d 2 ) could be in the range 3 mm-12 mm.
The precursor and fuel flow rates were kept constant and the oxidant flow rate was varied in order to obtain the operating line of particle size versus fuel to oxidant velocity difference with different burner designs.
Few key examples are demonstrated here for the synthesis of titanium dioxide, silica and carbon black. The data determined by the simulation tool of the present invention are compared with published experimental data for validation of the methodology developed in the present invention.
Example 7
FIG. 10 illustrates Titanium dioxide particle diameter as a function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
According to one of the exemplary embodiments of the invention, FIG. 10 illustrates that particle size and specific surface area are key product characteristics during the scale-up of the nanoparticle production. In order to verify and validate the simulation tool of the present invention, the data determined by present invention tool for different burner designs that lead to different production rates were simulated.
These simulation results are compared with published experimental data from Wegner and Pratsinis (2003) in FIG. 10 for scale-up of Titania production.
Further, Table 4 below provides and compares the data determined and obtained by the simulation tool i.e. simulated data for particle size and specific surface areas during the scale-up of the titania nanoparticle production of the present invention with the experimental data from Wegner and Pratsinis (2003).
TABLE 4
Velocity difference
Particle diameter (dp)
Burner
(ΔV = V oxidant − V fuel )
(nm)
Type
(m/s)
Experimental
Simulated
Burner 1
71.9298
1.2366
70.9840
65.2047
2.9032
58.5689
57.3099
3.6559
45.5512
34.2105
7.6344
31.4976
23.9766
11.4516
25.6017
20.7602
15.5914
16.9228
20.1754
19.2473
13.7482
18.421
23.6559
11.7024
Burner 2
0.59140
78.3626
66.0397
1.6129
73.9766
53.7126
4.0860
47.6608
48.6079
6.3979
38.5965
40.1970
8.4409
31.2865
33.7597
10.7527
28.0702
25.4969
16.0215
23.09941
21.3075
22.2580
21.3450
17.9738
27.9570
20.4678
14.6581
Burner 3
0.48387
87.4269
77.6398
0.9140
82.4561
66.0369
1.2903
77.7778
61.6103
1.8280
78.3626
55.5556
2.2580
61.4035
51.0270
It can be observed that the trend determined by the simulation tool of the present invention in scale-up trials for titania particle production is in close agreement with the experimental measurements for scale-up trials of K. Wegner and S. E. Pratsinis, further indicating the accuracy of the data determined by the simulation tool of the present invention.
Example 8
FIG. 11 illustrates Silica particle diameter as function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
According to one of the exemplary embodiments of the invention, FIG. 11 illustrates that particle size and specific surface area are key product characteristics during the scale-up of the nanoparticle production. In order to verify and validate the simulation tool of the present invention, the data determined by present invention tool for different burner designs that lead to different production rates were simulated.
These simulation results are compared with published experimental data from Wegner and Pratsinis (2003) in FIG. 11 for scale-up of Silica particle production.
Further, Table 5 below provides and compares the data determined and obtained by the simulation tool i.e. simulated data for particle size and specific surface areas during the scale-up of the silica nanoparticle production of the present invention with the experimental data from Wegner and Pratsinis (2003).
TABLE 5
Velocity difference
Particle diameter (dp)
Burner
(ΔV = V oxidant − V fuel )
(nm)
Type
(m/s)
Experimental
Simulated
Burner 1
1.8987
53.6873
53.3431
3.3635
42.7729
49.9199
6.4014
26.8437
42.9147
9.4394
19.7640
34.1374
12.4774
16.2242
29.8594
15.5154
15.0442
25.6395
18.5533
13.8643
21.4307
21.5913
13.5693
19.4750
24.5750
13.8643
17.8405
27.6130
12.9794
17.2361
Burner 2
1.3020
61.6519
50.4210
3.0380
46.3127
44.4037
4.9367
30.3835
32.1954
6.7812
23.0088
29.4649
8.5714
17.9941
25.2198
10.4702
15.6342
21.6056
Burner 3
0.2712
84.0708
66.4055
0.8137
71.9764
60.2579
1.3020
61.6519
52.0373
1.7902
57.5221
44.5560
2.2242
51.6224
37.3804
It can be observed that the trend determined by the simulation tool of the present invention in scale-up trials for silica particle production is in close agreement with the experimental measurements for scale-up trials of K. Wegner and S. E. Pratsinis, further indicating the accuracy of the data determined by the simulation tool of the present invention. Further, it is evident that upon maintaining the same outlet conditions, silica particles of same size can be produced irrespective of the size of the burner used
Example 9
FIG. 12 illustrates the influence of the different burner designs on the velocities of the oxidant and the fuel on carbon black particle size.
According to one of the exemplary embodiment of the invention, Acetylene is used both as a precursor and as the fuel while oxygen was used as oxidant in this process. It is partially oxidized and upon using the heat liberated during oxidation, the remaining acetylene cracks into carbon black and hydrogen gas. The influence of the difference in the velocities of the oxidant and the fuel on carbon black particle size is shown in FIG. 12 .
Further, Table 6 below provides the data obtained by the simulation tool i.e. simulated data for determining the influence of the difference in the velocities of the oxidant and the fuel on carbon black particle size.
TABLE 6
Velocity difference
Particle
Burner
(ΔV = V oxidant − V fuel )
diameter (dp)
Type
(m/s)
(nm)
Burner 1
1.8987
53.6873
3.3635
42.7729
6.4014
26.8437
9.4394
19.7640
12.4774
16.2242
15.5154
15.0442
18.5533
13.8643
21.5913
13.5693
24.5750
13.8643
27.6130
12.9794
Burner 2
1.3020
61.6519
3.0380
46.3127
4.9367
30.3835
6.7812
23.0088
8.5714
17.9941
10.4702
15.6342
Burner 3
0.2712
84.0708
0.8137
71.9764
1.3020
61.6519
1.7902
57.5221
2.2242
51.6224
The results indicate the validity of the simulation tool of the present invention for determining the operating line of particle size versus difference in velocities of the oxidant and the fuel.
Since it was possible to reproduce the operating line for different materials with reasonable accuracy, the simulation tool of the present invention can be utilized for detailed process design and process optimization to produce nanoparticles at different levels of production.
The preceding description has been presented with reference to various embodiments of the invention. Persons skilled in the art and technology to which this invention pertains will appreciate that alterations and changes in the described structures and methods of operation can be practiced without meaningfully departing from the principle, spirit and scope of this invention.
ADVANTAGES OF THE INVENTION
Provides a system and method for optimizing and controlling the particle size distribution of nanoparticles.
Provides a system and method for scale-up of production of nanoparticles with desired properties.
Provides cost effective and time saving method and system for optimizing and controlling the particle size distribution and scale-up of production of nanoparticles.
Reduces the number of trials or experiments to be conducted for scale-up, if not avoid them completely.
Provides details about the internal condition of the process equipment and insight into the phenomena that occur during the process.
1.PublishNumber: US-2012009118-A1
2.Date Publish: 20120112
3.Inventor: RUNKANA VENKATARAMANA
BUDDHIRAJU VENKATA SUDHEENDRA
VARMA NADIMPALLI NAGARAVI KUMAR
4.Inventor Harmonized: RUNKANA VENKATARAMANA(IN)
BUDDHIRAJU VENKATA SUDHEENDRA(IN)
VARMA NADIMPALLI NAGARAVI KUMAR(IN)
5.Country: US
6.Claims:
(en)The present invention relates to a system for optimizing and controlling the particle size distribution and scale-up of production of nanoparticle in an aerosol flame reactor. The method provides nanoparticles with desired, optimized and controlled particle size and the specific surface area in aerosol reactors using a simulation tool with programmed instructions. The said simulation tool couples flame dynamics model and particle population balance model.
7.Description:
(en)CROSS REFERENCE TO RELATED APPLICATION[S]
This application claims priority to Indian Patent Application to Runkana, et al., serial number 1984/MUM/2010, filed Jul. 12, 2010, the disclosure of which is hereby incorporated entirely herein by reference.
FIELD OF INVENTION
The present invention relates to a system and a method for optimizing and controlling the particle size distribution and for scale-up of production of nanoparticles in an aerosol flame reactor. More particularly the present invention relates to a system and a method for optimization of mean particle size, specific surface area, and distribution of nanoparticles in aerosol reactors.
BACKGROUND OF THE INVENTION AND PRIOR ART
In the recent years, nanotechnology has gained importance and has become one of the major research focus areas for its fundamental and practical applications. The smaller size of the particles especially less than 100 nm is one of the key parameters that is responsible for various properties such as electronic, electric, optical, magnetic chemical and mechanical properties that makes nanoparticles suitable for several applications in the fields of ceramics, catalysis, coatings, electronics, chemical and mechanical polishing, data storage, fuel cells, etc.
Many commodity and specialty chemicals and materials such as carbon black, titania, silica and zinc oxide are produced in the form of fine particles, which find applications in a wide variety of industrial and domestic products ranging from tyres, printing inks, paints and pigments, plastics, optical fibers, catalysts, pharmaceutical ingredients and cosmetics.
For many practical applications, it is desirable to have particles of small size as well as of narrow size distribution because smaller particles with narrow size distribution result in better properties of finished products. For example, activity of catalysts, hardness and strength of metals, electrical conductivity of ceramics improve as the particle size decreases.
These special properties of the nanoparticles can vary markedly from those of the analogous bulk materials. The physical and chemical properties of the nanomaterials tend to be exceptionally dependent on their size and shape or morphology. As a result, materials scientists are focusing their efforts on developing simple and effective methods for producing nanomaterials with controlled particle size and morphology and hence, improving their properties.
Many techniques and methods have been employed for the synthesis of nanoparticles on the laboratory scale. Some of the well known methods and systems are as follows:
a) Gas phase synthesis process: It is one of the routinely employed techniques used for large scale production of nano powders, as it is a single step process without any moving parts and any extensive solid-liquid separation processes. b) Chemical and mechanical routes such as microemulsion-based synthesis and grinding.
Amongst the above mentioned methods and techniques, flame aerosol synthesis is one of the commonly and widely used technologies for synthesis of fine powders on an industrial scale, as it offers many control parameters like flame temperature, flame structure, stoichiometry, pressure level, residence time distribution, turbulence etc.
The typical method of synthesis of nanoparticles in flame aerosol synthesis is as follows:
a) Injecting the precursor or reactant into the reactor in the form of a vapor or liquid using a carrier gas along with air and fuel. b) Chemical reactions occur in the gas phase in the flame at high temperatures and results in product molecules; c) Growth of the particles by coagulation and/or surface reaction to form product particles due to decrease in the temperature at downstream in the reactor
The temperature decrease at the downstream of the reactor results in the particle growth mainly by coagulation and results in irregularly structured particles and particle distribution.
Further, the powders produced in the aerosol flame reactors have a relatively large particle size and have wide size distribution, with particle size ranging from a few nanometers to micrometers, the said wide particle size distribution is influenced by several factors, namely, burner geometry, nature of flame and its configuration, inlet reactant flow rate and its concentration, and turbulence characteristics, gas and particle velocities, pressure and temperature profiles and residence time distribution inside the reactor.
Yet another challenging task lies in scaling up of the process to produce nanoparticles in large quantities, while at the same time maintaining the particle size in the nanometer range.
Hence, there is a need for controlling the product particle size distribution by manipulating and designing the process input variables.
Further, there is also a need for scaling up the process of synthesis of nanoparticles with desired characteristics.
Some of the prior arts that propose a system, method and scale-up process for synthesis of nano-particles are as follows:
U.S. Pat. No. 5,498,446 (Axelbaum et al) teaches a method and apparatus for reacting sodium vapor with gaseous chlorides in a flame to produce nanoscale particles of un-oxidized metals, composites and ceramics. The flame is operated under conditions which lead to condensation of a NaCl by-product onto the particles. The condensate encapsulates the particles and aids in controlling desired particle size and preventing undesirable agglomeration among the particles during synthesis. Following synthesis, oxidation of the particles is inhibited by the encapsulation and handling character of the products is greatly enhanced. Though the '446 patent discloses a method and apparatus for synthesis of nanoparticles, it does not disclose the means for optimization, and controlled particle size distribution of nanoparticles. Further, '446 patent does not address challenging aspect for the scale-up of production of nanoparticles with the desired particle size.
EP 1122212 (Hendrik et al) teaches a method to control particle characteristics of flame made nanostructured powders and investigated at high production rates addressing the required safety concerns. The influence of increasing the fuel and production rate, burner configuration and total oxidant flow on particle size morphology and composition is presented for synthesis of silica in a commercial oxy-hydrogen burner. Hence, the said patent application discloses a method to control particle characteristics of flame made nanostructured powders experimentally, which is expensive and time consuming.
“Computational fluid-particle dynamics for the flame synthesis of alumina particles” by Johannessen et al (2000) discloses a mathematical model for the dynamics of particle growth during the synthesis of the ultra fine particles in diffusion flame. The said article combines a simple batch model for coagulation and coalescence of aerosol particles along with the computational fluid dynamics model (Fluent) in a decoupled manner to simulate the gas composition, temperature and velocity profiles in a flame reactor and integrate the simple monodisperse population balance (MPB) model along a set of “characteristic trajectories” only and not for the entire flame structure. Further, the said article discloses the computational fluid-particle dynamics for the flame synthesis using specific burner with three concentric quartz tubes. Further, the said article does not determine the particle characteristics throughout the reactor and does not determine the particle characteristics using various burners and does not address the challenging aspect for the scale-up of production of nanoparticles with the desired particle size. Further, the simple kinetics used in the article only applies for a limited range of temperature and particle size.
Thus, in light of the above mentioned prior arts it is evident that there is a need to have a customizable solution for optimizing and controlling the particle size distribution in a continuous process rather than a batch process and scale-up of production of nanoparticle in an aerosol flame reactor.
Further, there is a need to have a customizable solution to optimize and control the particle size distribution and scale-up of production of nanoparticles in aerosol flame reactor in a coupled manner i.e. by solving the particle dynamics equations in each and every cell of the computational domain.
It is also evident that the process equipment design and scale-up, pilot scale studies are tedious and expensive. Hence, there is growing demand to have a customizable solution for synthesis and scale-up of nanoparticles with desired particle size and shape by improving the process design and scale-up which provides the basic process understanding and dynamic behavior of the flame reactor to reduce the efforts on pilot plant studies for the synthesis of any material.
In the present invention we propose a novel approach for optimizing and controlling the particle size distribution and scale-up of production of nanoparticles in aerosol flame reactor to overcome the above mentioned limitations for synthesis of nanoparticles with controlled particle size, shape and particle size distribution.
In order to address the long felt need for such a solution, the present invention provides a system and method for optimizing and controlling the particle size and scale-up of production of nanoparticles in an aerosol flame reactor, described more particularly herein after.
OBJECTS OF THE INVENTION
The principle object of the invention is to provide a system and method for optimizing and controlling the particle size and specific surface area of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide a system and method for scaling up the synthesis of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide cost effective system and method for optimizing and controlling the particle size and specific surface area of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide cost effective method for scaling up synthesis of nanoparticles in an aerosol flame reactor.
Another object of the invention is to provide system and method which optimizes and controls the particle size and specific surface area of nanoparticles in an aerosol flame reactor requiring less experimentation and utilizing less time.
Another object of the invention is to provide a method for scaling up synthesis of nanoparticles in an aerosol flame reactor which requires less experimentation.
Yet another object of the invention is to provide a simulation tool with programmed instructions for production of nanoparticles with controlled properties.
SUMMARY OF THE INVENTION
The present invention discloses a system and method for optimizing and controlling mean particle size and specific surface area and for scale-up of nanoparticle production in an aerosol flame reactor.
A system for optimizing and controlling mean particle size and specific surface area and for scale-up of nanoparticle production in aerosol flame reactor comprising of:
an aerosol flame reactor integrated with process instruments, wherein the said reactor further comprises of
at least one burner; at least one precursor or reactant fed to the said aerosol flame reactor; at least one stream input fed along with at least one precursor or reactant to the said aerosol flame reactor;
a simulation tool with programmed instructions to cause the processor to couple flame dynamics model and particle population balance model in order to optimize and control mean particle size and specific surface area and for scale-up of nanoparticle production in aerosol flame reactor.
A method for optimizing and controlling the mean particle size and specific surface area and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments, wherein the said method comprises the steps of:
a) Determining
i) the operating data for physical process parameters from the said process instruments integrated with aerosol flame reactor; ii) the mixing characteristics of the precursor or reactant at a particular concentration and the stream input fed to the burner of the said aerosol flame reactor with the process instruments; iii) the flame temperature and different species mass-fractions throughout the said reactor using the Flame dynamics model coupled to the simulation tool with programmed instructions; iv) the data for influence of burner configuration and the design of the reactor on the properties of nanoparticles.
b) Feeding the determined data of step i) to the simulation tool with the programmed instructions to obtain the simulated data for optimizing and controlling the mean particle size and specific surface area and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments; c) Implementation of the simulated data obtained from the said simulation tool with programmed instructions for optimizing and controlling the mean particle size and specific surface area and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments; d) Estimating the rate kinetics of the precursor oxidation reaction using the precursor to product conversion kinetics coupled to Particle population balance model of the said simulation tool with programmed instructions; e) Obtaining the output as product particle size and specific surface area of the reactor from the simulation tool with the programmed instructions to optimize and control the particle size distribution and for scale up of nanoparticle production in an aerosol flame reactor integrated with the process instruments.
BRIEF DESCRIPTION OF THE DRAWINGS
The foregoing summary, as well as the following detailed description of preferred embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the invention, there is shown in the drawings, exemplary constructions of the invention; however, the invention is not limited to the specific methods disclosed. In the drawings:
FIG. 1 of the present invention illustrates the structure of the simulation tool with programmed instructions.
FIG. 2 illustrates the typical diffusion flame burner.
FIG. 3 illustrates the typical aerosol flame burner configurations (Source of figure: T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 4 illustrates the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration B (Source for Flame B figure: T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 5 illustrates the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration C (Source for Flame C figure: T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 6 illustrates the comparison of axial temperature profile in a laboratory scale flame reactor determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 7 illustrates the comparison of alumina aggregate particle sizes determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 8 illustrates the burner configuration with five concentric tubes for silica nanoparticles synthesis from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
FIG. 9 illustrates the effect of TEOS (precursor) concentration on silica particle specific surface area and compares the data determined by the simulation tool of the present invention with the experimental data from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
FIG. 10 illustrates Titanium dioxide particle diameter as a function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
FIG. 11 illustrates Silica particle diameter as function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
FIG. 12 illustrates the influence of the different burner designs on the velocities of the oxidant and the fuel on carbon black particle size.
DETAILED DESCRIPTION OF THE INVENTION
Before the present method, and hardware enablement are described, it is to be understood that this invention in not limited to the particular methodologies, and hardware described, as these may vary. It is also to be understood that the terminology used in the description is for the purpose of describing the particular versions or embodiments only, and is not intended to limit the scope of the present invention which will be limited only by the appended claims. The words “comprising,” “having,” “containing,” and “including,” and other forms thereof, are intended to be equivalent in meaning and be open ended in that an item or items following any one of these words is not meant to be an exhaustive listing of such item or items, or meant to be limited to only the listed item or items. The disclosed embodiments are exemplary to the invention, which may be embodied in various forms.
The present invention provides a system for optimizing and controlling particle size distribution and for scale-up of nanoparticle production in an aerosol flame reactor comprising of:
an aerosol flame reactor integrated with process instruments, wherein the said reactor further comprises of
at least one burner; at least one precursor or reactant fed to the said aerosol flame reactor; at least one stream input fed along with at least one precursor or reactant to the said aerosol flame reactor;
a simulation tool with programmed instructions to cause the processor to couple flame dynamics model and particle population balance model in order to optimize and control mean particle size and specific surface area and for scale-up of nanoparticle production in an aerosol flame reactor.
According to one of the embodiments of the present invention, the process instruments comprises of precursor flow rate gauze, precursor pressure gauze, air flow rate gauze, air pressure gauze, fuel flow rate gauze, fuel pressure gauze, carrier gas flow rate gauze, carrier gas pressure gauze and temperature sensors.
The process instruments integrated with the aerosol flame reactor provides the operating data for variables such as precursor flow rate, precursor pressure, air flow rate, air pressure, carrier gas flow rate, carrier gas pressure to the simulation tool with programmed instructions to manage the process.
FIG. 1 of the present invention illustrates the structure of the simulation tool with programmed instructions.
According to one of the embodiments of the present invention, simulation tool with programmed instructions ( 10 ) couples flame dynamics model ( 20 ) and particle population balance model ( 30 ) to optimize and control the mean particle size and specific surface area and for scale-up of the production of nanoparticles with the desired characteristics.
Flame dynamics model ( 20 ) coupled to the simulation tool with programmed instructions determines the flame temperature and different species mass-fractions throughout the reactor and further determines and simulates the physical process parameters such as but not limited to fluid flow rate, heat transfer rate, etc.
Further, the Flame dynamics model ( 20 ) is coupled with fuel combustion kinetics ( 70 ) for managing operating data obtained from the various process instruments of the aerosol flame reactor.
The governing equations for the flame dynamics model are as follows:
The equation of motion according to Bird et al., (2002)
∂
∂
t
(
ρ
u
)
=
-
[
∇
·
ρ
uu
]
-
∇
p
-
[
∇
·
τ
]
-
[
∇
·
τ
(
t
)
]
+
ρ
g
(
1
)
Wherein ρ is gas density (kg/m 3 ), u is velocity (m/s), τ (t) is turbulent momentum flux tensor (kg/s 2 /m), τ is stress tensor (kg/s 2 /m) and g is gravitational acceleration (m/s 2 ).
Further, as per Launder and Spalding (1974), the k-ε model is used for calculating the turbulent kinetic energy, k (m 2 /s 2 ) and its dissipation rate, ε (m 2 /s 3 )
∂
∂
t
(
ρ
k
)
+
∇
·
(
ρ
uk
)
=
∇
·
[
(
μ
+
μ
t
σ
k
)
∇
k
]
+
P
k
-
ρɛ
(
2
)
∂
∂
t
(
ρɛ
)
+
∇
·
(
ρ
u
ɛ
)
=
∇
·
[
(
μ
+
μ
t
σ
k
)
∇
ɛ
]
+
ɛ
k
(
C
ɛ
1
P
k
-
C
ɛ
2
ρɛ
)
(
3
)
where P k is turbulence production due to viscous and buoyancy forces (kg/s 3 ) which is obtained using the following equation:
P
k
=
μ
t
∇
u
·
(
∇
u
+
∇
u
T
)
-
2
3
∇
·
u
(
3
μ
t
∇
·
u
+
ρ
k
)
+
P
kb
(
4
)
where μ t is turbulent viscosity (kg/m/s) given by
ρ
C
μ
k
2
ɛ
and P kb is turbulence production due to buoyancy forces (kg/s 3 ).
The continuity equation for component i as given by (CFX 11.0 User's Manual):
∇·(ρ {right arrow over (v)}Y i )=−∇· {right arrow over (J)} i +R i +S i (5)
where R i is the net rate of production of species i by a chemical reaction, S i is the rate of creation by addition from the dispersed phase, Y i is mass fraction of component i and J i is diffusion flux of species i, which arises due to concentration gradients.
The equation of energy in terms of the specific enthalpy h (J/kg) is given by (CFX 11.0 User's Manual):
∂
∂
t
(
ρ
h
)
+
∇
·
ρ
hu
=
∇
·
(
k
g
∇
T
)
+
∂
p
∂
t
+
u
·
∇
p
+
τ
:
∇
u
+
S
E
(
6
)
where k g is thermal conductivity of the gas (J/m/s/K), S E is source term that denotes the rate of heat liberated due to chemical reaction and heat absorption due to radiation. τ:∇u is always negative and is called the viscous dissipation.
The P-1 radiation model according to Siegel and Howell (1992) is incorporated in the enthalpy balance to account for radiant energy absorption and irradiation. The radiation flux is expressed by expanding the radiation intensity in series of orthogonal harmonics in this model. The radiation flux is then directly incorporated into the enthalpy balance to account for the radiation heat transfer process.
The rate of fuel combustion is calculated using the eddy-dissipation model (EDM) proposed by Magnussen and Hjertager (1976). The chemical reaction is fast relative to the transport processes. The fuel combustion model consists of two rate expressions, Equations 7 and 8 given below. Equation 7 represents the reaction rate R 1 (kmol/m 3 /s) that accounts for the mixing of the reactants in the turbulent eddies.
R
1
=
A
EDM
ɛ
k
min
(
[
I
]
v
I
)
(
7
)
where [I] (kmol/m 3 ) is concentration of the reactant I, v I is the stoichiometric coefficient of component I and A EDM is a numerical constant.
Equation 8 represents the reaction rate R 2 (kmol/m 3 /s) that accounts for the mixing of the hot product gases with the cold reactant gases when heat transport to the unreacted gases is the limiting factor.
R
2
=
A
EDM
B
EDM
ɛ
k
(
∑
P
[
I
]
W
I
∑
P
v
I
W
I
)
(
8
)
where P loops over all product components in the reaction. In Eq. 8, W I (kg/kgmol) is molar mass of the component I and B EDM is a numerical constant. The rate of combustion is determined by the smaller of the two rates R 1 and R 2 .
Particle population balance model ( 30 ) coupled to the simulation tool with programmed instructions determines the properties of evolved particles.
The governing equations for particle population balance model ( 30 ) are as follows:
The rate of change of particle number concentration (N) is given by:
∂
N
∂
t
+
∂
u
j
N
∂
x
j
=
∂
∂
x
j
(
η
∂
N
∂
x
j
)
+
I
-
1
2
β
N
2
(
9
)
where η (m 2 /sec) is diffusion coefficient, β (m 3 /sec) is coagulation rate coefficient and I (#/m 3 -sec) is rate of nucleation (Ji et al., 2007):
I=k n ( S− 1) N n (10)
where k n (#·s −1 ·m 3 ) is nucleation rate constant, S is degree of supersaturation and the exponent N n is taken as 1. The last term on the RHS of Eq. 9 represents the reduction of particle number concentration N by coagulation. The coagulation rate coefficient β is calculated using the Fuchs equation (Fuchs, 1964; Seinfield, 1986).
β
=
8
π
Dr
c
(
r
c
2
r
c
+
2
t
p
+
2
D
cr
c
)
(
11
)
The particle diffusion coefficient D is calculated as given by Johannessen (1999):
D
=
K
b
T
6
π
μ
r
c
[
5
+
4
Kn
+
6
Kn
2
+
18
Kn
3
5
-
Kn
+
(
8
+
π
)
Kn
2
]
(
12
)
where Kn is the Knudsen number (λ/r c ), λ (m) is the gas mean free path and μ (Pa·s) is viscosity of the gas. The total surface area density of the particles A (m 2 /m 3 ) decreases by coalescence but remains unaffected by coagulation.
∂
A
∂
t
+
∂
u
j
A
∂
x
j
=
∂
∂
x
j
(
η
∂
A
∂
x
j
)
+
Ia
p
-
1
τ
f
(
A
-
A
min
)
(
13
)
where a p is the monomer surface area (m 2 ), τ f is characteristic coalescence time (s) and A min is minimal total surface area density, given by:
A min =(π N ) 1/3 (6 V) 2/3 (14)
where V is total particle volume density (m 3 /m 3 ). The characteristic coalescence time τ f depends on temperature, primary particle size, material, sintering mechanism, etc. Particle coalescence occurs due to a combination of mechanisms, namely, surface diffusion, grain boundary diffusion, solid state diffusion and viscous flow.
The characteristic coalescence time τ f of two separate, contacting spherical particles is given by Johannesssen et al. (2000):
τ
f
=
k
0
d
p
m
T
T
0
exp
(
E
A
R
(
1
T
-
1
T
0
)
)
(
15
)
where E A is activation energy, d p is initial diameter of the two primary contacting spherical particles in an aggregate, k 0 is pre-exponential term, T 0 is temperature and R is universal gas constant.
The total particle volume density V (m 3 /m 3 ) increases by nucleation and chemical reaction.
∂
V
∂
t
+
∂
u
j
V
∂
x
j
=
∂
∂
x
j
(
η
∂
V
∂
x
j
)
+
Iv
p
+
S
V
(
16
)
where v p is the monomer volume (m 3 ) and S V is rate of increase of total particle mass per unit volume of the system (kg/m 3 ·s), given by the following equation:
S V =(π/2) AGρ (17)
where G is total growth rate of a particle (m/s). The total growth rate G under the combined control of chemical reaction and mass transfer is calculated as
G
=
G
M
G
C
G
M
+
G
C
(
18
)
where G M is growth rate of a particle under the control of mass transfer (m/s) and G C is growth rate of a particle under the control of chemical reaction kinetics (m/s). The linear growth rate of a particle under the control of mass transfer G M (m/s) is given by:
G
M
=
4
V
mol
D
A
-
O
2
1.013
×
10
5
8.314
T
d
n
Y
A
*
(
S
-
1
)
(
19
)
where V mol is molar volume of the product molecule produced (m 3 /mol): TiO 2 , SiO 2 or Carbon black, D A-O2 is diffusion coefficient of A (product molecule) through O 2 (m 2 /s), S is degree of supersaturation, d n is number-averaged particle size (m), Y* A is mole fraction of A at saturation temperature T. The growth rate of a particle under the control of chemical reaction kinetics, G C is given by the following expression:
G c =k gc ( S− 1) N g (20)
where k gc is particle growth rate constant (m/s). The exponent N g is assumed to be 1. When S≦1, G C is set equal to zero.
Particle population balance model ( 30 ) determines the properties of the evolved particles on the basis of the above discussed equations for particle number concentration, particle volume and particle surface area.
Particle population balance model ( 30 ) is further coupled to precursor to product conversion kinetics ( 80 ) for monitoring and controlling the particle size distribution of nanoparticles and further estimates the rate kinetics of the precursor oxidation reaction.
The combined eddy dissipation-finite rate chemistry model available in CFX 11.0 represents the oxidation of precursor to product molecules. The rate of oxidation is taken as the minimum of the rates obtained using the Arrhenius expression, given below, and the eddy dissipation model (Eqs. 7 and 8).
R
A
=
A
exp
(
-
E
RT
)
C
precursor
C
O
2
(
21
)
where A is pre-exponential factor, E (J/kmol-K) is activation energy, C precursor (kmol/m 3 ) is the concentration of the precursor, C O 2 (kmol/m 3 ) is concentration of oxygen and R (J·kmol −1 ·K −1 ) is the universal gas constant.
In one of the embodiments of the present invention, the simulation tool with programmed instructions is developed on a FORTRAN platform to simulate and determine the physical processes.
Nanoparticles with desired particle size and shape are produced in the aerosol flame reactors on provision of the various optimized operating conditions ( 40 ) such as but not limited to flame temperature, pressure, optimum gas flow rate, and reactant or precursor concentrations.
The values for various optimized operating conditions are provided to the simulation tool with the programmed instructions so as to simulate and determine the influence of these various operating parameters on the particle size and specific surface area of the nanoparticles.
Further, according to another embodiment of the present invention, the geometry and design ( 50 ) of the reactor and burner also influences the particle size, particle size distribution and shape of the nanoparticles. The various sizes of burners, the number of concentric tubes of the burner, the spacing between each tube, diameter of the tubes of the burner are fed to the simulation tool with the programmed instructions so as to simulate and determine the influence of the variable geometry and design of the burner and reactor on the particle size.
Further according to one of the embodiments of the present invention, the burners are designed and configured for various stream inputs to the aerosol flame reactor.
Further according to one of the embodiments of the present invention the burner geometry is designed and implemented in co-ordination with the simulation tool with programmed instructions in terms of number of concentric tubes, diameters of each tube and spacing between each tube.
According to another embodiment of the present invention the various characteristics and properties of the physical constants and materials ( 60 ) are fed to the simulation tool with the programmed instructions so as to simulate and determine the influence of the characteristics and properties of the materials ( 60 ) on the particle size distribution.
The simulation tool with the programmed instructions provides output ( 90 ) as product particle size and specific surface area of the reactor.
FIG. 2 of the present invention illustrates the typical diffusion flame burner, wherein carrier gas along with precursor or reactant is injected through the centre tube; fuel is injected through the second tube and oxidant through the third tube; wherein the diameter of centre tube, second tube and third tube are represented by d 1 , d 2 and d 3 respectively.
According to one of the embodiments of the present invention, the simulation tool with programmed instructions of the present invention determines the influence of the three burners with varying diameters of the central tube, the annulus and the outer tube, for scale-up of production of nanoparticles. The inner diameter of the central tube (d 1 ) can be in the range 1.5-5.5 mm, the inner diameter of the outer most tube (d 3 ) can range from 5 mm to 25 mm while the inner diameter of the tube in between the central and outer tubes (d 2 ) could be in the range 3 mm-12 mm.
FIG. 3 of the present invention illustrates the typical aerosol flame burner configurations according to Johannssen et al., (2000).
According to one of the embodiments, four typical aerosol flame reactor burner configurations are illustrated in FIG. 3 with respect to the various modes of stream inputs.
Flame A illustrates the injection of carrier gas along with precursor and air from the centre tube and fuel through the third tube, whereas no stream input is provided through the second tube.
Flame B illustrates the injection of carrier gas along with precursor from the centre tube and air through the second tube while fuel through the third tube.
Flame C illustrates the injection of carrier gas along with precursor from the centre tube and fuel through the second tube while air through the third tube.
Flame D illustrates the injection of carrier gas along with precursor and fuel from the centre tube and air through the third tube, whereas no stream input is provided through the second tube.
Any of the four typical aerosol flame reactor burner configuration values and geometries as illustrated in FIG. 3 can be fed to the simulation tool with programmed instructions of the present invention to simulate, and determine the influence of the burner configuration and geometries on the particle size distribution in the aerosol flame reactor.
EXAMPLES OF WORKING OF THE INVENTION
The invention is described in the examples given below which is provided only to illustrate the invention and therefore should not be construed to limit the scope of the invention.
Example 1
FIG. 4 shows the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration B (Flame B) of FIG. 3 , wherein methane in the input stream is fed to the burner through the third tube; air in the second tube and precursor and carrier gas in the first tube.
The configuration of input streams (methane, air, carrier gas and precursor) to the burner has a strong influence on the flame characteristics and hence on the particle size. The influence of burner configuration and arrangement of the burner configurations on flame temperature profile is shown in FIG. 4 .
The flames in configuration B ( FIG. 4 ) are shorter flames surrounded by air on both sides and hence, yield a more efficient combustion.
Example 2
FIG. 5 shows the temperature contours and the value of the alumina aggregate particle size inside the flame reactor with burner configuration C (Flame C) of FIG. 3 , wherein methane in the input stream is fed to the burner through the second tube; air in the third tube and precursor and carrier gas in the first tube.
The configuration of input streams to the burner has a strong influence on the flame characteristics and hence on the particle size. The influence of burner configuration on flame temperature profile is shown in FIG. 5 .
The configuration B (flame B) has methane in the third tube and air in the second tube where as configuration C has methane in the second tube and air in the third tube. This difference in arrangement alters the flame shape and size drastically as seen in the FIGS. 4 and 5 .
The flames in configuration B ( FIG. 4 ) are surrounded by air on both sides and hence, yield a more efficient combustion than those in configuration C.
For this reason, flames in configuration B are shorter than those in configuration C ( FIG. 5 ), with slightly higher temperatures than the latter.
Example 3
FIG. 6 illustrates the comparison of axial temperature profile in a laboratory scale flame reactor determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)).
FIG. 6 compares the data determined by the simulation tool with programmed instructions for the axial temperature profile and influence of distance above burner outlet (m) on the mean particle size with that of published experimental data of Johanessen et al (2000).
Further, Table 1 below provides and compares the simulated data determined by the simulation tool with programmed instructions for the axial temperature profile and influence of distance above burner outlet (m) on the mean particle size with that of published experimental data of Johanessen et al (2000).
TABLE 1
Distance above
burner outlet
Temperature (K)
(m)
Experimental
Simulated
0.00
500
500
0.01
1018
1091
0.02
1117
1493
0.03
1342
1672
0.04
1608
1764
0.05
1887
1816
0.06
1842
1796
0.07
1698
1572
0.08
1486
1462
It can be noticed that the data determinations made by the simulation tool of the present invention are relatively close to the experimental measurements and thereby indicating the accuracy of the data determinations made by the simulation tool of the present invention.
Example 4
FIG. 7 illustrates the comparison of alumina aggregate particle sizes determined by simulation tool of the present invention with the experimental data of Johanessen et al (T. Johannessen, S. E. Pratsinis and H. Livbjerg, Computational fluid-particle dynamics for the flame synthesis of alumina particles, Chemical Engineering Science, 55, 177-191 (2000)). Further, FIG. 7 compares the data determined by the simulation tool with programmed instructions for the various burner configurations and average particle size with that of published experimental data of Johanessen et al (2000).
Further, Table 2 below provides and compares the data determined and provided by simulation tool with programmed instructions i.e. simulated data for the various burner configurations and average particle size with that of published experimental data of Johanessen et al (2000).
TABLE 2
Average particle size (nm)
Configuration
Experimental
Simulated
C1 179
193
C2 188
204
C3 223.
216
C4 176.
203
C5 187.
171
C6 196.
276
B1 115.
109
B2 146.
135
B3 180.
151
B4 106.
140
B5 132.
141
B6 174.
160
It can be noticed that the data determinations made by the tool of the present invention are relatively close to the experimental measurements and thereby indicating the accuracy of the data determined by the simulation tool of the present invention.
Example 5
FIG. 8 illustrates the burner configuration with five concentric tubes for silica nanoparticles synthesis from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
FIG. 8 shows that the simulation tool of the present invention was tested further for production of silica nanoparticles using a burner with five concentric tubes, wherein Ar and TEOS (precursor) was fed through the centre tube of the burner, Ar was fed through the second tube, H 2 was fed through the third tube, O 2 was fed through the fourth tube and air was fed through the fifth tube.
Example 6
FIG. 9 illustrates the effect of TEOS (precursor) concentration on silica particle specific surface area and compares the data determined by the simulation tool of the present invention with the experimental data from Jang et al (H. D. Jang, 2001, “Experimental study of synthesis of silica nanoparticles by a bench-scale diffusion flame reactor”, Powder Technol., 119, 102-108).
The burner configuration of FIG. 8 was integrated with the simulation tool of present invention, to determine the specific surface areas of silica particles at different precursor concentrations and compared with published experimental data from Jang et al (2001) in FIG. 9 .
FIG. 9 illustrates the effect of TEOS (precursor) concentration on silica particle specific surface area and compares the data determined by the simulation tool of the present invention with the experimental data from Jang et al (2001). Further, Table 3 below provides and compares the effect of TEOS (precursor) concentration on silica particle specific surface area and the data determined and obtained by the simulation tool i.e. simulated data of the present invention with the experimental data from Jang et al (2001).
TABLE 3
TEOS Concentration
Specific surface area (m 2 /g)
(l/min)
Experimental
Simulated
1.00E−05
240
225
1.00E−04
230
218
1.91E−04
101
94
2.50E−04
68
60
It can be observed that the trend determined by the simulation tool of the present invention is in close agreement with the experimental measurements, further indicating the accuracy of the data determined by the simulation tool of the present invention.
Further, the simulation tool with programmed instructions of the present invention was used to determine the influence of the three burners with varying diameters of the central tube, the annulus and the outer tube, for scale-up of production of nanoparticles. The inner diameter of the central tube (d 1 ) can be in the range 1.5-5.5 mm, the inner diameter of the outer most tube (d 3 ) can range from 5 mm to 25 mm while the inner diameter of the tube in between the central and outer tubes (d 2 ) could be in the range 3 mm-12 mm.
The precursor and fuel flow rates were kept constant and the oxidant flow rate was varied in order to obtain the operating line of particle size versus fuel to oxidant velocity difference with different burner designs.
Few key examples are demonstrated here for the synthesis of titanium dioxide, silica and carbon black. The data determined by the simulation tool of the present invention are compared with published experimental data for validation of the methodology developed in the present invention.
Example 7
FIG. 10 illustrates Titanium dioxide particle diameter as a function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
According to one of the exemplary embodiments of the invention, FIG. 10 illustrates that particle size and specific surface area are key product characteristics during the scale-up of the nanoparticle production. In order to verify and validate the simulation tool of the present invention, the data determined by present invention tool for different burner designs that lead to different production rates were simulated.
These simulation results are compared with published experimental data from Wegner and Pratsinis (2003) in FIG. 10 for scale-up of Titania production.
Further, Table 4 below provides and compares the data determined and obtained by the simulation tool i.e. simulated data for particle size and specific surface areas during the scale-up of the titania nanoparticle production of the present invention with the experimental data from Wegner and Pratsinis (2003).
TABLE 4
Velocity difference
Particle diameter (dp)
Burner
(ΔV = V oxidant − V fuel )
(nm)
Type
(m/s)
Experimental
Simulated
Burner 1
71.9298
1.2366
70.9840
65.2047
2.9032
58.5689
57.3099
3.6559
45.5512
34.2105
7.6344
31.4976
23.9766
11.4516
25.6017
20.7602
15.5914
16.9228
20.1754
19.2473
13.7482
18.421
23.6559
11.7024
Burner 2
0.59140
78.3626
66.0397
1.6129
73.9766
53.7126
4.0860
47.6608
48.6079
6.3979
38.5965
40.1970
8.4409
31.2865
33.7597
10.7527
28.0702
25.4969
16.0215
23.09941
21.3075
22.2580
21.3450
17.9738
27.9570
20.4678
14.6581
Burner 3
0.48387
87.4269
77.6398
0.9140
82.4561
66.0369
1.2903
77.7778
61.6103
1.8280
78.3626
55.5556
2.2580
61.4035
51.0270
It can be observed that the trend determined by the simulation tool of the present invention in scale-up trials for titania particle production is in close agreement with the experimental measurements for scale-up trials of K. Wegner and S. E. Pratsinis, further indicating the accuracy of the data determined by the simulation tool of the present invention.
Example 8
FIG. 11 illustrates Silica particle diameter as function of oxygen and fuel velocity difference with different burner designs and compares the data determined by the simulation tool of the present invention with the experimental data from Wegner and Pratsinis (K. Wegner and S. E. Pratsinis, Scale-up of nanoparticle synthesis in diffusion flame reactors, Chemical Engineering Science, 58(20), 4581-4589 (2003)).
According to one of the exemplary embodiments of the invention, FIG. 11 illustrates that particle size and specific surface area are key product characteristics during the scale-up of the nanoparticle production. In order to verify and validate the simulation tool of the present invention, the data determined by present invention tool for different burner designs that lead to different production rates were simulated.
These simulation results are compared with published experimental data from Wegner and Pratsinis (2003) in FIG. 11 for scale-up of Silica particle production.
Further, Table 5 below provides and compares the data determined and obtained by the simulation tool i.e. simulated data for particle size and specific surface areas during the scale-up of the silica nanoparticle production of the present invention with the experimental data from Wegner and Pratsinis (2003).
TABLE 5
Velocity difference
Particle diameter (dp)
Burner
(ΔV = V oxidant − V fuel )
(nm)
Type
(m/s)
Experimental
Simulated
Burner 1
1.8987
53.6873
53.3431
3.3635
42.7729
49.9199
6.4014
26.8437
42.9147
9.4394
19.7640
34.1374
12.4774
16.2242
29.8594
15.5154
15.0442
25.6395
18.5533
13.8643
21.4307
21.5913
13.5693
19.4750
24.5750
13.8643
17.8405
27.6130
12.9794
17.2361
Burner 2
1.3020
61.6519
50.4210
3.0380
46.3127
44.4037
4.9367
30.3835
32.1954
6.7812
23.0088
29.4649
8.5714
17.9941
25.2198
10.4702
15.6342
21.6056
Burner 3
0.2712
84.0708
66.4055
0.8137
71.9764
60.2579
1.3020
61.6519
52.0373
1.7902
57.5221
44.5560
2.2242
51.6224
37.3804
It can be observed that the trend determined by the simulation tool of the present invention in scale-up trials for silica particle production is in close agreement with the experimental measurements for scale-up trials of K. Wegner and S. E. Pratsinis, further indicating the accuracy of the data determined by the simulation tool of the present invention. Further, it is evident that upon maintaining the same outlet conditions, silica particles of same size can be produced irrespective of the size of the burner used
Example 9
FIG. 12 illustrates the influence of the different burner designs on the velocities of the oxidant and the fuel on carbon black particle size.
According to one of the exemplary embodiment of the invention, Acetylene is used both as a precursor and as the fuel while oxygen was used as oxidant in this process. It is partially oxidized and upon using the heat liberated during oxidation, the remaining acetylene cracks into carbon black and hydrogen gas. The influence of the difference in the velocities of the oxidant and the fuel on carbon black particle size is shown in FIG. 12 .
Further, Table 6 below provides the data obtained by the simulation tool i.e. simulated data for determining the influence of the difference in the velocities of the oxidant and the fuel on carbon black particle size.
TABLE 6
Velocity difference
Particle
Burner
(ΔV = V oxidant − V fuel )
diameter (dp)
Type
(m/s)
(nm)
Burner 1
1.8987
53.6873
3.3635
42.7729
6.4014
26.8437
9.4394
19.7640
12.4774
16.2242
15.5154
15.0442
18.5533
13.8643
21.5913
13.5693
24.5750
13.8643
27.6130
12.9794
Burner 2
1.3020
61.6519
3.0380
46.3127
4.9367
30.3835
6.7812
23.0088
8.5714
17.9941
10.4702
15.6342
Burner 3
0.2712
84.0708
0.8137
71.9764
1.3020
61.6519
1.7902
57.5221
2.2242
51.6224
The results indicate the validity of the simulation tool of the present invention for determining the operating line of particle size versus difference in velocities of the oxidant and the fuel.
Since it was possible to reproduce the operating line for different materials with reasonable accuracy, the simulation tool of the present invention can be utilized for detailed process design and process optimization to produce nanoparticles at different levels of production.
The preceding description has been presented with reference to various embodiments of the invention. Persons skilled in the art and technology to which this invention pertains will appreciate that alterations and changes in the described structures and methods of operation can be practiced without meaningfully departing from the principle, spirit and scope of this invention.
ADVANTAGES OF THE INVENTION
Provides a system and method for optimizing and controlling the particle size distribution of nanoparticles.
Provides a system and method for scale-up of production of nanoparticles with desired properties.
Provides cost effective and time saving method and system for optimizing and controlling the particle size distribution and scale-up of production of nanoparticles.
Reduces the number of trials or experiments to be conducted for scale-up, if not avoid them completely.
Provides details about the internal condition of the process equipment and insight into the phenomena that occur during the process.
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Expert System for Optimizing and Controlling Particle Size Distribution And For Scale-Up Of Nanoparticle Production In An Aerosol Flame Reactor
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