# Prediction of Pollutant Emissions from Bluff-Body Stabilised Nonpremixed Flames

Authors: Nelu Munteanu; Shokri M. Amzaini
Journal: Journal of Combustion
 (2018)

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## Abstract

Construction of a stable flame is one of the critical design requirements in developing practical combustion systems. Flames stabilised by a bluff-body are extensively used in certain types of combustors. The design promotes mixing of cold reactants and hot products on the flame surface to improve the flame stability. In this study, bluff-body stabilised methane-hydrogen flames are computed using the steady laminar flamelet combustion method in conjunction with the Reynolds-averaged Navier-Stokes (RANS) approach. These flames are known as Sandia jet flames and have different jet mean velocities. The turbulence is modelled using the standardk-ϵ model and the chemical kinetics are modelled using the GRI-mechanism with 325 chemical reactions and 53 species. The computed mean reactive scalars of interest are compared with the experimental measurements at different axial locations in the flame. The computed values are in reasonably good agreement with the experimental data. Although some underpredictions are observed mainly for NO and CO at downstream locations in the flame, these results are consistent with earlier reported studies using more complex combustion models. The reason for these discrepancies is that the flamelet model is not adequate to capture the finite-rate chemistry effects and shear turbulence specifically, for species with a slow time scale such as nitrogen oxides.


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## Body

## 1. Introduction

Combustion of fossil fuels has a severe impact on the environment and humankind. Environmental and health-related issues such as global warming, acid rain, and ocean acidification will continue to be at the forefront for years to come [1, 2]. The primary products generated from combustion are carbon dioxide (CO2) and water (H2O) among other primary pollutants such as nitrogen oxides (NOx), sulphur oxides (SOx), carbon monoxide (CO), unburned hydrocarbons (UHC), and particle matter (PM). For instance, an increase in CO2 concentration would trap the heat in the atmosphere, and as a result, an increase in average global temperature is observed [3]. Nitrogen oxides and sulphur oxides react with water in the atmosphere and fall as acid rains causing a severe health and economic losses [2]. Subsequently, environmental regulations become stricter to minimise these pollutants. However, statics show that the contribution of renewable energy such as the wind, solar, and hydro is less than 8.4% according to the European Commission statistics in 2008 [4]. Therefore, replacing fossil fuels with another source of renewable energy especially for high energy density application such as the aviation sector is unlikely to be soon. Thus, engineers and scientists are required to develop cleaner combustion systems that meet the environmental legislation demands and at the same time maintain high efficiency.Mixing the reactants is crucial in sustaining combustion. For instance, if the mixture is inhomogeneous, some regions will have a higher equivalence ratio creating pockets with elevated temperature, which lead to NOx formation [5]. Furthermore, the stability of lean premixed flames can reduce the efficiency and the lifetime of the combustion device [6]. Construction of a stable flame is one of the critical design requirements in developing practical combustion systems [7, 8]. Flames stabilised by a bluff-body are extensively used in certain types of combustors. The design promotes mixing of cold reactants and hot products on the flame surface and improves the flame stability.The primary challenge in turbulent combustion modelling is to find a physically and chemically meaningful closure for the mean reaction rate,ω˙α~, which appears in the species transport equation. This term is nonlinear and evaluating it from the mean temperature and species concentration is known to be inappropriate [10]. RANS-Flamelet-based methods are widely used in industry and research for both premixed [11–14] and nonpremixed combustion [11, 15, 16]. Despite its limitation, the method is capable of predicting the interaction between turbulence and chemical reaction. Hence, the aim of this work is to predict pollutants from nonpremixed flames stabilised by a bluff-body. These flames were investigated in previous experimental studies [17, 18].The outline of this paper is as follows. In Section2, the flamelet method for nonpremixed flames with its assumptions and limitations is discussed. In Section 3, the chosen test flames are presented. The computational details are discussed in Section 4. The outcome of this study is discussed in Section 5. Finally, the summary and conclusion of this study are discussed in the last section.


## 2. Flamelet Model Formulation

The fundamental principle of the flamelet-based methods is to presume the turbulent flame structure as a collection of laminar flamelets that are locally one-dimensional [11]. This assumption is satisfactory when the flame characteristic turbulence scales are much larger compared with the flame scales, and consequently, turbulence eddies do not penetrate and disturb the flame structure. The deviation from the flamelet regime and the relation between these scales is given by Damköhler number, which is defined as Da=τt/τc. τt and τc denote the turbulent and chemical time scale, respectively. These laminar flames are usually characterised using a passive scalar mixture fraction (z), which measures the ratio between fuel and oxidiser. The values of mixture fraction are set to be 1 in the fuel and 0 in the oxidiser.In the steady laminar flamelet method, the mean scalars of interest are parametrised using the mixture fraction,z, and the scalar dissipation rate (χ) which is broadly defined as the rate at which turbulence-generated fluctuations in the mixture fraction are dissipated. Scalar dissipation can disturb the structure of the laminar flamelet by stretching the reaction zone. It is to be noted that, at low strain rate values, the structure of the laminar flamelet resembles the equilibrium state, and at high values, flame extinction takes place. The computational tool used in this study solves the scalar dissipation rate with an initial value that is specified to be 0.2 and continuously increases until the maximum scalar dissipation rate is reached, or the flame has extinguished. The scalar dissipation rate, χ, is defined as(1)χ=2D∂z∂xi2,where D is the diffusion coefficient. The scalar dissipation χ varies along the axis of the flamelet. The stretch effects and quenching at stoichiometry are accounted by χst [19]. For a counter-flow flame, the flamelet strain rate, as, is related to the scalar dissipation at the location wherez is stoichiometric by(2)χst=as-2erfc-12zst2π,where χst is the stoichiometric scalar dissipation rate at the stoichiometric mixture fraction, zst. as is the strain rate, and erfc-1 is the inverse complementary error function.In the tabulated approach, a set of one-dimensional instantaneous species mass fractionYαz,χst (4) and the instantaneous temperature Tz,χst (7) with different values of χst are solved with detailed reaction mechanisms to account for nonequilibrium and finite-rate chemistry effects [11]. These scalars are tabulated as a function of mixture fraction and dissipation rate as follows:(3)ϕ=ϕZ,χ.The instantaneous transport equation of species concentration is expressed as(4)ρ∂Yα∂t-12ρχ∂2Yα∂z2-ω˙α=0.The first term in (4) denotes the unsteady changes of species mass fraction, Yα. The second term represents the diffusion of species, Yα. The third term represents the instantaneous reaction rate and is given by (5)ω˙k=kfk∏α=1nρYαWαναk′-kbk∏α=1nρYαWαναk′′.kfk and kbk represent the forward and backward reaction rate coefficients, respectively. Wα is the molecular weight of species α. ναk′ and ναk′′ are the forward and backward stoichiometric coefficient, respectively. The forward and backward reaction rate coefficients are given by Arrhenius law: k=ATnexp⁡-Ea/RT,where A, Ea denote the preexponential factor and the activation energy, respectively. The instantaneous chemical reaction of species, α, in mass basis can be expressed as(6)ω˙α=Wα∑k=1nω˙kναk′′-ναk′.The instantaneous transport equation of temperature is written as(7)ρ∂T∂t-12ρχ∂2T∂z2+1cP∂cP∂z∂T∂z+1cp∑α=1nhαω˙α=0.The first term of (7) denotes the variation of the temperature, with time. The second term represents the diffusion of temperature, whereT and cP represent the temperature and the specific isobaric and heat capacity, respectively. The third term represents the contribution from the production of species α. hα denote the specific enthalpy of species α.The Favre-averaged mean scalars of interest are then obtained using a Joint Probability Density Function ofz and χst as follows:(8)ρ-ϕ~=∫0∞∫01ρϕz,χstp~z,χstⅆzⅆχst,where p~z,χst is the probability density function ofz and χst and is given by p~z,χst=p~zp~χst.p~z is closed using a presumed shape with a Beta function as follows [20]:(9)p~z=Cza-11-zb-1,whereC denotes the inverse of the normalisation factor and is given by C=1/βa,b.a andb denote the parameters of Beta function and are given by a=z~(v-1) and b=1-z~v-1.  v is the variance parameter given by v=z~1-z~/z′′2~. The normalisation factor is given by βa,b=∫01za-11-zb-1ⅆz.  p~χst is given by a Dirac-delta as follows [20]:(10)p~χst=δχst-χ~st.The mean mixture fraction,z~, is obtained from the following transport equation:(11)∂ρ-z~∂t+∂∂xiρ-u~iz~=∂∂xiρD∂z∂xi--ρ-ui′′z′′~.The turbulent scalar flux is closed using the classical gradient assumption and is given by ρ-ui′′z′′~=-μt/Sct(∂z~/∂xi). μt denotes the viscosity and Sct denotes the turbulent Schmidt number. The turbulent viscosity is closed by μt=ρ-Cμk2~/ε~.The mean mixture fraction variance is obtained from the following transport equation:(12)∂ρ-z′′2~∂t+∂∂xiρ-ui~z′′2~=∂∂xiρD∂z′′2∂xi--ρui′′z′′2--2ρui′′z′′-∂z~∂xi-2ρD∂z′′∂xi∂z′′∂xi-.The terms on the L.H.S denote the time variation and convection of z′′2~. The terms into the brackets on the R.H.S account for the molecular diffusion and turbulent scalar transport. The second term represents the production of z′′, where the unknown ρui′′z′′- is modelled using the gradient assumption. The third term on the R.H.S represents the dissipation rate and is given by(13)2ρD∂z′′∂xi∂z′′∂xi-=χ~=Cχz′′2~τt=Cχε~k~z′′2,~k~ and ε~represent the mean kinetic energy and its dissipation rate, respectively. Cχ is a constant given by Cχ= 2 [21]. Two transport equations for the mean k~,ε~ are solved and written as(14)∂∂tρ-k~+∂∂xiρ-u~ik~=∂∂xiμ+μtσk~∂k~∂xi+ρ-τij∂u~j∂xi-ρ-ε~,and(15)∂∂tρ-ε~+∂∂xiρ-u~iε~=∂∂xiμ+μtσε~∂ε~∂xi+Cε~1ε~kρ-τij∂u~j∂xi-Cε~2ρ-ε~2k~.The standard model constants [22, 23] are Cμ=0.09,σk=1.0,σε=1.30, Cε1=1.44, and Cε2=1.92.


## 3. Test Flames

The test flames chosen to test the flamelet method are the nonpremixed bluff-body flames described in [17, 18]. The burner consists of a centre jet with a diameter of 3.6 mm and a bluff-body with a diameter of 50 mm, showed in Figure 1. The burner is surrounded by a co-flow tunnel with the following dimensions DCO=305x 305 mm. The main jet contains a (50/50% by volume) mixture of methane and hydrogen with an initial temperature of 293K. Three flames were considered in the experiment and are labelled as B3F3A, B3F3B, and B3F3C with different jet velocities of 118, 178, and 217 m/s, respectively. The Reynolds number Rej, which is defined based on the main jet bulk velocity Uj and integral length scale Dj, is 15800, 23900, and 28700, respectively. The B4F3A flame, which has the lowest jet velocity, is considered to test flamelet method. The characteristics of the selected flame are summarised in Table 1. The major and minor species concentrations are measured using Raman/ Rayleigh/ LIF technique at different radial and axial locations in the flame [24]. To minimise the heat losses, the bluff-body is coated with a ceramic layer. The bluff-body creates a recirculation zone to substantially improve the flame stability over an extensively range of co-flow and jet conditions [8, 25]. These flames have been used to validate different combustion models such as conditional moment closure (CMC) [26], probability density function (PDF) [27], and flamelet [28].Table 1
Characteristics of the flame B4F3A.
Flame Mixture D J / D B [mm] U J / U C O [m/s] R e J T[K] ϕ  B4F3A CH4/H2(1:1) 3.6/50 118/40 15800 298 0.05Figure 1
Schematic diagram of the flame B4F3A.


## 4. Computational Details

The computational tool used in this study is the commercial software Star CCM+. The tool solves the steady Favre-averaged transport equations forz~ and z′′2~ in (11) and (12) along with their appropriate closures on the physical grid. The turbulence is modelled using the standard k-epsilon model (14) and (15). The PDF is obtained by presuming a β-function (9). The chemical kinetics are modelled using the GRI-mechanism with 325 chemical reactions and 53 species.The computational domain consists of 2D axisymmetric with 1000 mm in the axial direction and 153 mm in the radial direction as shown in Figure2. The polygonal mesh type was selected to construct the physical grid with 37143 cells. The cells size is refined near to the fuel port to capture the finite-rate chemistry effects as shown in Figure 3. The smallest cell before the refinement has a size of approximately 0.5 mm.Figure 2
Computational domain dimension.Figure 3
Computational domain grid point.In the flamelet method in Figure4, a library is constructed by solving the instantaneous Yαz,χst and Tz,χst as a function of mixture fraction and the stoichiometric dissipation rate. 100 grid points are specified for the mixture fraction and 14 different values of χst are specified to account for the stretch effects and quenching at the stoichiometry. The nonlinear differential steady governing equations for the complex flow fields are discretised using a mixed finite element method, which employs stabilisation techniques to address issues with the pressure-velocity coupling and the nonlinear convection terms. The mean quantities are obtained from the integral equation (8). 2200 iterations are specified to ensure the solution is converged as shown in Figure 5 along with the residuals.Figure 4
Presumed PDF flamelet computational steps [9].Figure 5
Residual plot.


## 5. Results and Discussion

The computed mean quantities are compared to the experimental measurements [17, 18] at three axial locations x/D =0.26, 0.60, 0.90, and 1.30, in the flame B4F3A, and will be discussed in this section.The recirculation zone and the shear flow created by the bluff-body are well captured in the simulation as shown in Figure6.Figure 6
The recirculation zone of the flame B4F3A.The mean passive scalar, the mixture fraction,z~, and its variance, z′′2~, are solved to obtain the PDF. Figure 7 shows the computed radial variation of z~ at different axial locations in the flame. Also, the contours are shown for the visual inspection. The computed values are in excellent agreement with the measurements at all three axial locations. It should be noted that the mean quantities are linked to the instantaneous values through the PDF and hence this accuracy will improve the prediction of the mean values.Figure 7
Contours of the mean mixture fraction for flame B4F3A and comparison to the experimental results at three axial locations.The radial variations of the mean temperature are compared to the experimental measurements and are shown in Figure8. The contours show that the flame is well developed with a maximum temperature of 2019K. This temperature is typical for this type of reactants. Despite some minor discrepancies, the computed values using the flamelet method are in good agreement with the experimental data at all axial locations. Identical levels of agreement are also observed for the major species mass fraction such as YCH4, YCO2, and YH2O which are not reported in this study.Figure 8
Contour of the mean temperature for flame B4F3A and comparison to the experimental results at three axial locations.The computed mean values of the minor species CO and NO are compared to the experimental data and are shown in Figures9 and 10. The flamelet method has captured the typical radial profile of these species. The comparison of CO is in good agreement upstream near the fuel port. As for the axial locations x/D = 0.60 and x/D = 0.90, some discrepancies are explicitly noticed, at radial locationsr/D > 12. This behaviour can be attributed to the effect of turbulence and require further investigations. The agreement with experimental measurements is highly overpredicted at axial locations greater than 1.3.Figure 9
Contour of the mean carbon monoxide mass fraction for flame B4F3A and comparison to the experimental results at three axial locations.Figure 10
Contour of the mean nitrogen oxide mass fraction for flame B4F3A and comparison to the experimental results at three axial locations.The mass fractions of NO are underpredicted at all axial locations in the flame. Predicting pollutants with slow time scale such as NO from combustion systems is a challenge for turbulent combustion modelling. These results are consistent with earlier reported studies using more complex combustion models. The reason for these discrepancies is that the flamelet model is not adequate to capture the finite-rate chemistry effects and shear turbulence specifically, for species with a slow time scale such as nitrogen oxides. Similar behaviour is noted at axial location greater than x/D = 1.3.


## 6. Summary and Conclusions

The overall aim of this study is to predict pollutants using the flamelet method from nonpremixed flames stabilised by a bluff-body and to compare the results with the experimental measurements, precisely, to predict pollutants with slow time scale such as CO and NO. The flamelet method is a well-established method, and it has been used in previous studies to compute nonpremixed and premixed flames in RANS and LES paradigms. The B4F3A flame, which has the lowest jet velocity, is considered to test RANS-Flamelet method. The main jet contains a (50/50% by volume) mixture of methane and hydrogen with an initial temperature of 293K. The turbulence is modelled using the standardk-ϵ model. The chemical kinetics are modelled using the GRI-mechanism, which includes the formation of CO and NO. This mechanism consists of 325 chemical reactions and 53 species. The PDF is obtained by presuming a β-function. The computed values are observed to be in reasonably good agreement with the experimental data. Although some underpredictions are observed mainly for NO and CO at downstream locations in the flame, these results are consistent with earlier reported studies using more complex combustion models. The reason for these discrepancies is that the flamelet model is not adequate to capture the finite-rate chemistry effects and shear turbulence specifically, for species with a slow time scale such as nitrogen oxides.



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