# Lecture 3 Fluid Dynamics and Balance Equa6ons for Reac6ng Flows

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1 Lecture 3 Fluid Dynamics and Balance Equa6ons for Reac6ng Flows 3.- 1

2 Basics: equations of continuum mechanics - balance equations for mass and momentum - balance equations for the energy and the chemical species Associated with the release of thermal energy and the increase in temperature is a local decrease in density which in turn affects the momentum balance. Therefore, all these equations are closely coupled to each other. Nevertheless, in deriving these equations we will try to point out under certain assumptions. how they can be simplified and partially uncoupled 3.-2

3 Balance Equations A time-independent control volume V for a balance quality F(t) The scalar product between the surface flux φ f and the normal vector n determines the outflow through the surface A, a source s f the rate of production of F(t) Let us consider a general quality per unit volume f(x, t). Its integral over the finite volume V, with the time-independent boundary A is given by 3.-3

4 The temporal change of F is then due to the following three effects: 1. by the flux φ f across the boundary A. This flux may be due to convection or molecular transport. By integration over the boundary A we obtain the net contribution which is negative, if the normal vector is assumed to direct outwards. 3.-4

5 2. by a local source σ f within the volume. This is an essential production of partial mass by chemical reactions. Integrating the source term over the volume leads to 3. by an external induced source s. Examples are the gravitational force or thermal radiation. Integration of s f over the volume yields 3.-5

6 We therefore have the balance equation Changing the integral over the boundary A into a volume integral using Gauss' theorem and realizing that the balance must be independent of the volume, we obtain the general balance equation in differential form 3.-6

7 Mass Balance Set the partial mass per unit volume ρ i = ρ Y i = f. The partial mass flux across the boundary is ρ i v i = φ f, where v i is called the diffusion velocity. Summation over all components yields the mass flow where v is the mass average velocity. The difference between v i defines the diffusion flux where the sum satisfies 3.-7

8 Setting the chemical source term one obtains the equation for the partial density The summation over i leads to the continuity equation 3.-8

9 Introducing the total derivative of a quantity a combination with the continuity equation yields Then using may also be written 3.-9

10 Momentum Balance Set the momentum per unit volume ρ v = f. The momentum flux is the sum of the convective momentum in flow ρ v v and the stress tensor where I is the unit tensor and τ is the viscous stress tensor. Therefore ρ v v + P = φ f. There is no local source of momentum, but the gravitational force from outside where g denotes the constant of gravity

11 The momentum equation then reads or with for we obtain 3.-11

12 Kinetic Energy Balance The scalar product of the momentum equation with v provides the balance for the kinetic energy where v 2 = v. v

13 Potential Energy Balance The gravitational force may be written as the derivative of the time-independent potential Then with the continuity equation the balance for the potential energy is 3.-13

14 Total and Internal Energy and Enthalpy Balance The first law of thermodynamics states that the total energy must be conserved, such that the local source σ f = 0. We set ρ e = f, where the total energy per unit mass is This defines the internal energy introduced in 3.-14

15 The total energy flux is which defines the total heat flux j q. The externally induced source due to radiation is Then the total energy balance may be used to derive an equation for the internal energy 3.-15

16 Using this may be written with the total derivative With the continuity equation we may substitute to find illustrating the equivalence with the first law introduced in a global thermodynamic balance

17 With the enthalpy h = u + p/ρ the energy balance equation can be formulated for the enthalpy 3.-17

18 Transport Processes In its most general form Newton's law states that the viscous stress tensor is proportional to the symmetric, trace-free part of the velocity gradient Here the suffix sym denotes that only the symmetric part is taken and the second term in the brackets subtracts the trace elements from the tensor. Newton's law thereby defines the dynamic viscosity

19 Similarly Fick's law states that the diffusion flux is proportional to the concentration gradient. Due to thermodiffusion it is also proportional to the temperature gradient. The most general form for multicomponent diffusion is written as For most combustion processes thermodiffusion can safely be neglected. For a binary mixture Fick s law reduces to where is the binary diffusion coefficient

20 For multicomponent mixtures, where one component occurs in large amounts, as for the combustion in air where nitrogen is abundant, all other species may be treated as trace species and with the binary diffusion coefficient with respect to the abundant component may be used as an approximation A generalization for an effective diffusion coefficient D i to be used for the minor species is 3.-20

21 Note that the use of does not satisfy the condition Finally, Fourier's law of thermal conductivity states that the heat flux should be proportional to the negative temperature gradient. The heat flux j q includes the effect of partial enthalpy transport by diffusion and is written which defines the thermal conductivity λ

22 In Fourier s law the Dufour heat flux has been neglected. Transport coefficients for single components can be calculated on the basis of the theory of rarefied gases

23 Different forms of the energy equation We start from the enthalpy equation and neglect in the following the viscous dissipation term and the radiative heat transfer term. Then, differentiating yields where c p is the heat capacity at constant pressure of the mixture

24 We can write the heat flux as If the diffusion flux can be approximated by with an effective diffusion coefficient D i, we introduce the Lewis number and write the last term as This term vanishes if the Lewis numbers of all species can be assumed equal to unity

25 This is an interesting approximation because it leads to the following form of the enthalpy If the p= const as it is approximately the case in all applications except in reciprocating engines, the enthalpy equation would be very much simplified. The assumption Le=1 for all species is not justified in many combustion applications. In fact, deviations from that assumption lead to a number of interesting phenomena that have been studied recently in the context of flame stability and the response of flames to external disturbances. We will address these questions in some of the lectures below

26 Another important form of the energy equation is that in terms of the temperature. With and the total derivative of the enthalpy can be written as 3.-26

27 Then with the enthalpy equation without the second last term yields the temperature equation Here the last term describes the temperature change due to chemical reactions

28 It may be written as where the definition has been used for each reaction. The second term on the right hand side may be neglected, if one assumes that all specific heats c pi are equal. This assumption is very often justified since this term does not contribute as much to the change of temperature as the other terms in the equation, in particular the chemical source term

29 If one also assumes that spatial gradients of c p may be neglected for the same reason, the temperature equation takes the form For a constant pressure it is very similar to the equation for the mass fraction Y i with an equal diffusion coefficient D=λ/ρ/c p for all reactive species and a spatially constant Lewis number may be written as 3.-29

30 Lewis numbers of some reacting species occurring in methane-air flames For Le i =1 the species transport equation and the temperature equation are easily combined to obtain the enthalpy equation. Since the use of and does not require the Le=1 assumption, this formulation is often used when nonunity Lewis number effects are to be analyzed

31 For flame calculations a sufficiently accurate approximation for the transport properties is [Smooke] a constant Prandtl number and constant Lewis numbers

32 A first approximation for other hydrocarbon species can be based on the assumption that the binary diffusion coefficients of species i with respect to nitrogen is approximately proportional to Then the ratio of its Lewis number to that of methane is 3.-32

33 Balance Equations for Element Mass Fractions Summation of the balance equations for the mass fractions according to leads to the balance equations for Z j : Here the summation over the chemical source terms vanishes since the last sum vanishes for each reaction

34 The diffusion term simplifies if one assumes that the diffusion coefficients of all species are equal. If one further more assumes Le i =1 this leads to 3.-34

35 A similar equation may be derived for the mixture fraction Z. Since Z is defined according to as the mass fraction of the fuel stream, it represents the sum of element mass fractions contained in the fuel stream. The mass fraction of the fuel is the sum of the element mass fractions where 3.-35

36 With the mixture fraction may therefore be expressed as a sum of element mass fractions Then, with the assumption of Le i =1, a summation over leads to a balance equation for the mixture fraction 3.-36

37 For a one-step reaction with the reaction rate ω this equation can also be derived using and for Y F and Y O 2 with Le F = L O2 = 1 as 3.-37

38 Dividing the first of these by ν W O and subtracting yields a source-free balance 2 O2 equation for the combination which is a linear function of Z according to This leads again to 3.-38

39 For constant pressure the enthalpy equation has the same form as and a coupling relation between the enthalpy and the mixture fraction may be derived where h 1 is the enthalpy of the fuel stream and h 2 that of the oxidizer stream

40 Similarly, using and the element mass fractions may be expressed in terms of the mixture fraction where Z j,1 and Z j,2 are the element mass fractions in the fuel and oxidizer stream

41 It should be noted that the coupling relations and required a two feed system with equivalent boundary conditions for the enthalpy and the mass fractions

42 A practical example is a single jet as fuel stream with co-flowing air as oxidizer stream into an open atmosphere, such that zero gradient boundary conditions apply everywhere except at the input streams. Once the mixture fraction field has been obtained by numerical solution of the adiabatic flame temperature may be calculated using the methods of lecture 2 as a local function of Z

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