**Hailin Yang ^{1}, Jianzhong Lin This email address is being protected from spambots. You need JavaScript enabled to view it.^{1}, Tatleung Chan^{2}**

^{1 }Department of Mechanics, State Key Laboratory of Fluid Power and Mechatronic Systems, Zhejiang University, 310027 Hangzhou, China^{2 }Department of Mechanical Engineering, The Hong Kong Polytechnic University, Hung Hom, Kowloon, Hong Kong

Received:
November 4, 2019

Revised:
January 9, 2020

Accepted:
February 24, 2020

* ***Copyright **The Author(s). This is an open access article distributed under the terms of the Creative Commons Attribution License (CC BY 4.0), which permits unrestricted use, distribution, and reproduction in any medium, provided the original author and source are cited.

Download Citation: ||https://doi.org/10.4209/aaqr.2019.11.0556

Cite this article:

Yang, H., Lin, J. and Chan, T. (2020). Effect of Fluctuating Aerosol Concentrations on the Aerosol Distributions in a Turbulent Jet. *Aerosol Air Qual. Res.* 20: 1629–1639. https://doi.org/10.4209/aaqr.2019.11.0556

**HIGHLIGHTS**

- Aerosol fluctuating coagulation resulting from the fluctuating concentrations is modeled.
- The model is applied to an aerosol particle laden jet flow first.
- Fluctuating aerosol concentration intensifies the aerosol coagulation.
- Fluctuating aerosol coagulation effect comes into play at
*x/D*= 5 and cannot be neglected.

**ABSTRACT**

We apply the Reynolds averaging method to derive the averaged particle general dynamic equation (APGDE), which models the effect of fluctuations in aerosol concentrations on coagulation, referred to as the fluctuating coagulation term (FCT), based on the turbulent kinetic energy. The APGDE is numerically solved using the Taylor-series expansion method of moments for a turbulent jet; the equation is then validated by comparing some of the results with experimental values. Obtaining the distribution and evolution of the aerosol particle number concentration, mass concentration, mean diameter and geometric standard deviation both when the FCT is incorporated and when it is excluded, we find that the contribution of fluctuating concentrations to the coagulation becomes a factor when* x/D* = 5 and reaches a stable state when *x/D* = 20. When the FCT is considered, the number concentration, mean diameter and geometric standard deviation are clearly lower, larger and greater, respectively. The fluctuating concentrations intensify the coagulation, reduce the number concentration and increase the mean diameter. Therefore, such fluctuations in a turbulent jet cannot be neglected.

Keywords:
Aerosol particles; Fluctuating aerosol concentration; Fluctuating coagulation; Aerosol distribution; Turbulent jet.

**INTRODUCTION**

Air quality is related to the amount of aerosols in the atmosphere. To understand the number and distribution of aerosols requires understanding the generation and motion and dynamics of aerosols. So the solution to the aerosol particle general dynamic equation (PGDE) is required. PGDE proposed by Smoluchowski is a fundamental equation describing the evolution of aerosol particle distribution, and made up of unsteady, convective, diffusion and source terms. The source terms are contributed by many physical and chemical processes including aerosol particle coagulation, growth, nucleation, condensation and so on (Lesniewski and Friedlander, 1998; Zhou and Chan, 2011; Chan *et al.*, 2018). In the aerosol flow, the turbulent motion is more common (Zhu *et al.*, 2018). The effect of turbulence on the source terms has been investigated extensively.

Reade and Collins (2000) simulated the fluid flow and particle motion using direct numerical simulation method and statistical method, respectively, and showed that, in general, the degree of particle preferential concentration increases with increasing Reynolds number. Zajchik and Solov’Ev (2002) investigated the particle collision and coagulation due to Brownian and turbulent effect, and found that the coagulation kernel varies with increasing particle sizes while passing through a minimum in the region transitioning from the Brownian continual to turbulent mode. Chun *et al.* (2005) solved the equation of aerosol size distribution function to study the clustering of aerosol particles in isotropic turbulence, and showed that clustering of aerosol particles increases the rate of coagulation or coalescence. Das and Garrick (2010) investigated the growth and Brownian coagulation of aerosol particle in the turbulent jet flow calculated by large eddy simulation, and showed that the unresolved small-scale fluctuations can both enhance and restrain particle growth, however, the predominant influence is to reduce particle growth. Gan* et al.* (2010) studied the turbulent coagulation and breakage of particle in the turbulent jet flow, and found that the polydispersity and particle diameter are very large in the shear layers at the upstream and in the core of vortex structures at the downstream. Loeffler *et al.* (2011) used the subgrid-scale modeling of mean concentration coagulation term and obtained the formation and growth of aerosol particle in turbulent jet, they suggested that neglect of the unresolved particle-particle interactions may enhance the particle growth rate with increasing the precursor concentration. Yin and Liu (2014) showed that the interaction of the two jets and turbulence eddy structures rolling up, paring and shedding in flow sharply affects particles’ number concentration. Particle diameter grows quickly at the interfaces of jets. Liu and Chan (2017) combined the Monte Carlo method and PGDE to simulate the complex aerosol dynamics in turbulent flows with considering the turbulent effect on the convective and diffusion terms of the aerosol particle, and it is shown that Reynolds number has significant impact on the aerosol particle coagulation. Rittler *et al.* (2017) simulated the aerosol synthesis from flame spray pyrolysis with considering the turbulent effect on the convective and nucleation terms of the particle, and showed that turbulent mixing leads to a broader size distribution of the primary and aggregate particle diameters.

All the references mentioned above refer to the effect of fluid fluctuation on the aerosol particles in the turbulent flow. However, the concentration fluctuation of aerosol particles also has the effect on the aerosol particle distributions. From a theoretical point of view, the physical quantities of fluid and particle could be written as the sum of mean and fluctuating components. Therefore, the averaged particle general dynamic equation (APGDE) can be derived using Reynolds averaging method, and two new terms appear in the APGDE (Friedlander, 2000). One of those is the contribution to coagulation resulting from the fluctuating concentrations of aerosol particles, referred as the *fluctuating coagulation term* (FCT). The FCT is very complex and used to be neglected because of lacking available theory and model. Lin *et al.* (2016) modeled the FCT and applied it to a turbulent pipe flow. However, the pipe flow is a kind of confined flow with effect of wall. In the present study, therefore, in order to explore the effect of fluctuating concentrations on the aerosol particle coagulation as well as the distribution in the free shear flow, the FCT is analyzed and modeled based on the turbulent kinetic energy in a turbulent jet. Then the APGDE is solved numerically combined with the Reynolds-averaged Navier-Stokes equation and *k*-*ε* equation. The aerosol particle mass concentration, number concentration, mean diameter and geometric standard deviation are simulated numerically.

MATHEMATICAL FORMULATION AND MODELS

MATHEMATICAL FORMULATION AND MODELS

Particle General Dynamic Equation for Turbulent Flows

Particle General Dynamic Equation for Turbulent Flows

Particle General Dynamic Equation for Turbulent Flows

In the present study, we explore the combined effects of convection, diffusion and coagulation on the evolution of aerosol particles. The PGDE which governs the evolution of aerosol particles in the flow is given:

where *n*(*v*, *t*) is the particle size distribution function; ** u** is the fluid velocity vector;

*β*(

*v*

_{1},

*v*) is the coagulation kernel for two particles of volume

*v*and

*v*

_{1};

*D*is the particle diffusion coefficient and can be given by:

where *T* is the temperature; *k _{B}* is the Boltzmann constant;

*μ*is the dynamic viscosity of fluid;

*d*is the particle diameter and

_{p}*Kn*is the Knudsen number (the ratio of gas molecular mean free path to the particle radius).

To obtain the PGDE in turbulent flow, the fluid velocity and particle size distribution function are decomposed into the mean and fluctuating components:

Substituting Eq. (3) into Eq. (1) and averaging with respect to time, we obtain the averaged particle general dynamic equation:

where the last term on the left-hand side can be changed into the form of turbulent diffusion of the quantity* n̅*:

where *v _{t}* is the turbulent viscosity and can be obtained by solving the equations of turbulent flow.

The third and fourth terms on the right-hand side of Eq. (4) denote the contribution to coagulation resulting from the fluctuating concentrations (the fluctuating coagulation term), which used to be neglected before. Here we make a following assumption based on the relationship between correlation of fluctuating concentration and the mean concentration, mean flow kinetic energy and turbulent kinetic energy as:

where the factor *χ _{t}* is referred to as number concentration fluctuation intensity:

in which *k* is the turbulent kinetic energy; *u**̅ _{i}*

^{2}is the mean flow kinetic energy.

Substituting Eq. (5) and Eq. (6) into Eq. (4), we obtain the APGDE:

**Moment Equation and Moment Method**

**Moment Equation and Moment Method**

Numerical method has to be employed because of the complexity of the PGDE. These methods include the moment method (Yu *et al.*, 2006; Lin *et al.*, 2016; Lai *et al.*, 2018), the sectional method (Chen* et al.*, 2015), the Monte Carlo method (Liu and Chan, 2018) and so on. The moment method is based on the following moment equation:

where *j* represents the order of the moment. Here we focus on the first three orders (*j* = 0, 1, 2). The zeroth moment *m*_{0} and first moment *m*_{1} are proportional to the particle number concentration and total particle mass, respectively. The second moment *m*_{2} corresponds to the mean particle size and polydispersity.

Based on Eq. (9), Eq. (8) can be transformed into an ordinary differential equation with respect to the moment *m _{j}*:

Thus, we have the transport equations of first three moments:

The particle coagulation kernel *β*(*v*_{1}, *v*) should be given in advance before Eq. (11) is solved. Here the Brownian coagulation in free molecule regime is considered for the nanoparticles (Friedlander, 2000):

where *ρ _{p}* is the particle density.

Substituting Eq. (12) into Eq. (11), we can obtain the transport equations which include fractional order and negative order moments and are not closure. To dispose the surplus moments and get closured equations, we use the Taylor-series expansion method of moment (TEMOM) (Yu *et al.*, 2008) to expand *v ^{j}* about

*v*=

*w*(where

*w*=

*m*

_{1}/

*m*

_{0}represent the volume of particle) and remain the first three term of Taylor series. Thus, arbitrary index

*v*can be transformed into

^{j}*v*

^{0},

*v*

^{1},

*v*

^{2}using following expression:

Above expression can be transformed into moment style using Eq. (9):

Substituting Eqs. (9), (12) and (13) into Eq. (11), we get:

Equation of Fluid Flow

Equation of Fluid Flow

Equation of Fluid Flow

The model and equations mentioned above are applied to a turbulent jet flow. The flow is assumed to be incompressible, and the continuity equation and Reynolds-averaged Navier-Stokes equations are:

where* p**̅ *is the mean pressure; *u*** ̅** is the mean fluid velocity;

*ρ*is the fluid density,

*ν*is the fluid kinematic viscosity and

**R**

*is the Reynolds stress:*

_{t}where *u _{i}'* and

*u*represent the fluctuating fluid velocity;

_{j}'*u*

*̅*and

_{i}*u*

*̅*represent the mean fluid velocity;

_{j}*δ*is Kronecker delta. Turbulent viscosity

_{ij}*ν*is given by

_{t}*v*=

_{t}*C*

_{μ}k^{2}/

*ε*, where

*k*and

*ε*are the turbulent kinetic energy and turbulent dissipation rate, respectively. The corresponding equations are (Faghani

*et al.*, 2011; Ghahremanian and Moshfegh, 2014):

The values of the constants appearing in above equations are:

**COMPUTATION SETTINGS**

Turbulent jet flow and coordinate system are shown in Fig. 1 where we extract a wedge domain from the cylinder based on the axisymmetric assumption. The tip of the wedge is the axis of the circular. A single layer of mesh is adopted to discretize the wedge domain, which converts a three-dimensional axisymmetric problem into a two-dimensional problem. The included angle of two lateral sides is less than 5°.

**Fig. 1.** The sketches of turbulent jet and the wedge-shaped computational domain.

The turbulent jet flow laden with aerosol particles is simulated numerically under different conditions as shown in Table 1. The initial values of *j*^{th} moment and initial particle diameter are denoted by *m _{j}*

_{0}(

*j*= 0, 1, 2) and

*d*

_{p}_{0}, respectively. Computations are performed in OpenFOAM-5 using finite volume method. The pressure and mean velocity are coupled by the OpenFOAM PIMPLE algorithm. The Gauss limited linear difference scheme is adopted for the convective term in Eqs. (14), (16), (18) and (19).

**VALIDATIONS**

**Fluid Mean Velocity**

**Fluid Mean Velocity**

The turbulent jet flow of pure fluid is simulated first as a validation. The self-similarity of velocity profile in the fully developed zone far from the nozzle is a kind of properties of the turbulent jet flow (Pope, 2000). The self-preservation of the mean stream-wise velocity is shown in Fig. 2 where vertical coordinate is normalized by *U _{cl}* (the mean velocity at center line) and horizontal coordinate is the radial location scaled by jet spreading half width

*y*/

*y*

_{1/2}(the radial coordinate where

*U*= 1/2

*U*in jet). We can see that there exists self-similarity of velocity profile at different stream-wise locations.

_{cl}**Fig. 2.** The self-similarity curve of the mean stream-wise velocity.

**Turbulent Kinetic Energy of Fluid**

**Turbulent Kinetic Energy of Fluid**

Another validation we concerned is the turbulent kinetic energy as shown in Fig. 3 where the numerical results of pure fluid are plotted in solid-scatter line and experimental results (Hussein* et al.*, 1994) measured with flying hot-wire (FHW) and burst-mode laser Doppler anemometer (LDA) also are given. It can be seen that the numerical results are in good agreement with the experimental data.

**Fig. 3.** Comparison of turbulent kinetic energy for the numerical and experimental results.

**Geometric Mean Diameter of Particle**

**Geometric Mean Diameter of Particle**

Geometric mean diameter as a function of total volume concentration in *x⁄D* = 60 is shown in Fig. 4 where the experimental results (Chowdhury *et al.*, 2017) are also given. We can see that two results are basically consistent.

**Fig. 4.** Geometric mean diameter as a function of total volume concentration in *x⁄D* = 60 (*Re* = 10,000).

**RESULTS AND DISCUSSIONS**

**Particle Number Concentration**

**Particle Number Concentration**

In order to compare the numerical results with the experimental ones, the total number concentration of particles as a function of total volume concentration in *x*⁄*D* = 60 is shown in Fig. 5 where both numerical and experimental results (Chowdhury *et al.*, 2017) are given. It can be seen that the total number concentration decreases with increasing the total volume concentration, which is reasonable because of particle coagulation.

**Fig. 5.** Total number concentration as a function of total volume concentration in *x*⁄*D* = 60 (*Re* = 10,000).

Fig. 6 shows the distribution of particle number concentration *m*_{0}/*m*_{00} in the flow. We can see that the large values of *m*_{0}/*m*_{00} occur in the area close to jet exit and center line, and the values decrease gradually along the flow and transverse directions.

**Fig. 6.** The contour of *m*_{0}/*m*_{00} (*m*_{0} = 9.75 × 10^{−10}, *Re* = 10,000).

Fig. 7 shows the variation of particle number concentration *m*_{0}/*m*_{00} along the axial direction. Particle number concentration decreases rapidly along the axial direction because of flow convection, particle diffusion and coagulation, and the dilution of particulate jet flow with the ambient fluid. Comparing the cases with different initial mass concentration, it can be seen that higher initial mass concentration *m*_{10} causes more frequent particle coagulation so that the number concentration is reduced faster along the axial direction. Comparing the cases with and without considering the FCT, we can see that the number concentration decreases with a same rate near the exit of the jet (*x*/*D* < 5) for both cases because the fluctuating concentration has an insignificant effect on the particle coagulation in this region. As the flow develops downstream, the difference in number concentration between the two cases is obvious, i.e., the number concentration with considering the FCT is less than that without considering the FCT because fluctuating concentration causes more frequent particle coagulation.

**Fig. 7.** Variation of particle number concentration (*Re* = 10,000).

Variations of particle number concentration along the radial direction at different axial locations are plotted in Fig. 8 where the curves are totally different from those in Fig. 7. Particle number concentration decreases from the center of the jet to the outer edge first slowly and then sharply because of the rolling up of the primary vortex in the area near the edge. The region occupied with particles increases along the axial direction due to the influence of the vortices which act to increase the particle diffusion. Particle number concentration decreases in the jet core as the jet is developing. Within the region near the jet nozzle, particle number concentration decreases rapidly due to the coagulation is strong for the small particles. The phenomenon that particle number concentration with considering the FCT is less than that without considering the FCT is more obvious in the area near the center line, which is consistent with the fact that the turbulent kinetic energy is larger in the area near the center line as shown in Fig. 3.

**Fig. 8.** Variation of particle number concentration along the radial direction (*m*_{10} = 9.75 × 10^{−10}, *Re* = 10,000).

**Particle Mass Concentration**

**Particle Mass Concentration**

Distribution of particle mass concentration *m*_{1}/*m*_{10 }in the flow is shown in Fig. 9, and variations of particle mass concentration along axial and lateral directions are shown in Fig. 10. It can be seen that the large values of particle mass concentration occur in the area close to jet exit and center line. The difference for two curves in Fig. 10 is obvious. As the flow is developing, aerosol particles diffuse across the fluid stream while diluting in the jet core, but the total particle mass remains unchanged in the whole flow field. As shown in Fig. 10(a), the particle mass concentration remains unchanged near the jet nozzle, and then decreases first rapidly and then slowly along the axial direction. However, particle mass concentration decreases from the center region to the jet edge with an almost constant rate as shown in Fig. 10(b).

**Fig. 9.** The contour of *m*_{1}/*m*_{10} (*m*_{10} = 9.75 × 10^{−10}, *Re* = 10,000).

**Fig. 10.** Variation of particle mass concentration *m*_{1} along (a) the axial direction and (b) the radial direction.

Particle Size

Particle Size

Particle Size

Aerosol particle coagulation results in the growth of particle size. The geometric average diameter of particle (*d _{p}*)

*can be determined by the geometric average volume:*

_{g}while geometric average volume of particle is given by (Lee *et al.*, 1984):

The second moment *m*_{2} appears in Eq. (21). Fig. 11 shows the distribution of *m*_{2}/*m*_{20} in the flow.

**Fig. 11.** The contour of* m*_{2}/*m*_{20} (*m*_{10} = 9.75 × 10^{−10}, *Re* = 10,000).

Fig. 12 shows that geometric average diameter of particle increases along the axial direction due to particle coagulation. In the cases with higher initial mass concentration, particle diameter increases rapidly because of more frequent particle coagulation. Particle diameter with considering the FCT is larger than that without considering the FCT because fluctuating concentration causes more frequent particle coagulation.

Fig. 13 shows the variations of geometric average diameter of particle along the radial direction at different axial locations. Particle diameter increases slightly from the center of the jet to the outer edge and is reduced to 1 at the outer edge. The largest values of particle size are found on the interface of the jet and the ambient fluid. Particle diameter with considering the FCT is larger than that without considering the FCT, which is more obvious along the radial direction than that along the axial direction as shown in Fig. 12.

**Fig. 12.** Variation of geometric average diameter of particle along the axial direction (*Re* = 10,000).

**Fig. 13.** Variation of geometric average diameter along the radial direction (*m*_{10} = 9.75 × 10^{−10}, *Re* = 10,000).

**Standard Variance of Particle Volume**

**Standard Variance of Particle Volume**

Another important parameter for particle size distribution is the geometric standard deviation *σ _{g}* which is given by (Lee

*et al.*, 1984):

For the Brownian coagulation in the free molecule regime, the geometric standard deviation *σ _{g}* reaches the asymptotic value of

*σ*= 1.355 when the particle system with the log-normal size distribution reaches the self-preserving size spectrum (Lee

_{∞}*et al.*, 1984; Chen

*et al.*, 2014).

The geometric standard deviation of particles along the axial direction is shown in Fig. 14(a). The value of *σ _{g}* grows rapidly near the exit of the jet (

*x*/

*D*< 10), and then tends to the asymptotic value of

*σ*= 1.355. The geometric standard deviation with higher initial mass concentration and with considering the FCT reaches the asymptotic value faster. A magnified diagram is plotted in Fig. 14(b) where the oscillation process of the curve can be seen in the region of

_{∞}*x*/

*D*< 20.

**Fig. 14.** (a) Variation of geometric standard deviation along the axial direction (*Re* = 10,000) and (b) magnified diagram in *x*/*D* < 20.

Fig. 15 shows the variations of geometric standard deviation of particles along the radial direction at different axial locations. The geometric standard deviation almost increases gradually from the center of the jet to the outer edge, and sharply near the outer edge. The highest values of geometric standard deviation are found near the interface of the jet region and the ambient fluid because the large velocity gradient near the interface makes the particles diffuse outwards, resulting in a rapid increase of *σ _{g}*. Besides, the geometric standard deviation with considering the FCT is larger than that without considering the FCT.

**Fig. 15.** Variation of geometric standard deviation along the radial direction (*m*_{10} = 9.75 × 10^{−10}, *Re* = 10,000).

**CONCLUSIONS**

We apply the Reynolds averaging method to derive the averaged particle general dynamic equation (APGDE), which models the effect of fluctuations in aerosol concentrations on coagulation, referred to as the *fluctuating coagulation term* (FCT), based on the turbulent kinetic energy. The APGDE is numerically solved using the Taylor-series expansion method of moments for a turbulent jet; the equation is then validated by comparing some of the results with experimental values. Analyzing the distribution and evolution of the aerosol particle number concentration, mass concentration, mean diameter and geometric standard deviation both when the FCT is incorporated and when it is excluded, we arrive at the following conclusions.

The particle number concentration decreases rapidly along the axial direction, especially with high initial mass concentrations, whereas it decreases from the center to the outer edge, first slowly and then sharply, along the radial direction. The mass concentration remains unchanged near the jet nozzle but then decreases, first rapidly and then slowly, along the axial direction; however, along the radial direction, it decreases from the center to the outer edge at an almost constant rate. The particle diameter increases along the axial direction, and it increases from the center outward before decreasing to 1 at the outer edge along the radial direction. The largest values are found at the interface between the jet and the ambient fluid. The geometric standard deviation grows rapidly near the exit of the jet and then tends to the asymptotic value of 1.355 along the axial direction, increasing gradually at first from the center outward and then sharply near the outer edge.

The contribution of fluctuating concentrations to the coagulation becomes a factor when *x*/*D* = 5 and reaches a stable state when *x*/*D* = 20. As the flow develops downstream, the particle number concentration when incorporating the FCT is clearly lower than when excluding it; this difference becomes more prominent in the area near the center line. Additionally, incorporating the FCT produces a larger particle diameter, which is more obvious along the radial than the axial direction, and a greater geometric standard deviation, which reaches the asymptotic value more quickly. The fluctuating concentrations intensify the coagulation, reduce the number concentration and increase the mean diameter. Thus, such fluctuations in a turbulent jet cannot be neglected.

ACKNOWLEDGMENTS

ACKNOWLEDGMENTS

This work was supported by the Major Program of the National Natural Science Foundation of China with Grant No. 91852102.

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