A turbulence dissipation model for particle laden flow

A turbulence dissipation model for particle laden flow
of 10
All materials on our website are shared by users. If you have any questions about copyright issues, please report us to resolve them. We are always happy to assist you.
Related Documents
  A Turbulence Dissipation Model for ParticleLaden Flow John D. Schwarzkopf, Clayton T. Crowe, and Prashanta Dutta School of Mechanical and Materials Engineering, Washington State University, Pullman, WA 99164  DOI 10.1002/aic.11773 Published online May 7, 2009 in Wiley InterScience (  A dissipation transport equation for the carrier phase turbulence in particle-laden flow is derived from fundamental principles. The equation is obtained by volume aver-aging, which inherently includes the effects of the particle surfaces. Three additionalterms appear that reveal the effect of the particles; these terms are evaluated usingStokes drag law. Two of the terms reduce to zero and only one term remains which isidentified as the production of dissipation due to the particles. The dissipation equationis then applied to cases where particles generate homogeneous turbulence, and experi-mental data are used to evaluate the empirical coefficients. The ratio of the coefficient of the production of dissipation (due to the presence of particles) to the coefficient of the dissipation of dissipation is found to correlate well with the relative Reynoldsnumber. V V C 2009 American Institute of Chemical Engineers AIChE J  , 55: 1416–1425, 2009  Keywords: turbulence, particles, dissipation, volume average Introduction A recent literature review in the area of modeling particle-laden turbulent flows reveals that there is a continuing needto develop a robust model for the effect of the dispersephase on the turbulence of the conveying phase. A shortreview of the modeling status was published by Curtis et al. 1 who pointed out that large industries such as the chemical,pharmaceutical, agricultural and mining industries can bene-fit from an understanding of particle-laden flows. Such abenefit is claimed to affect cost savings and increased pro-ductivity. Curtis et al. also identified several areas of investi-gation that could benefit industry; these include turbulent-gasflow interactions, particle clustering, particle shape, frictioneffects, and particle size distribution. Other applicationswhere the effect of particles on fluid- phase turbulencebecomes important are fluidized beds, chemical reactors,drug delivery systems, pollution control, and the food proc-essing industries, to mention a few.In particle-laden turbulent flow, the mechanisms responsi-ble for turbulence modulation (e.g., the effect of particles oncarrier phase turbulence) are not well understood. 2 As par-ticles are introduced, the statistics of the continuous phaseturbulence are altered. Depending on the particle characteris-tics such as size, density, mass loading and relative velocitydifference, the level of turbulent kinetic energy (TKE) anddissipation changes relative to the corresponding un-ladenflow. Gore and Crowe 3 showed that there is a relationshipbetween turbulent modulation and the ratio of the particlesize to a characteristic length of the most energetic eddy inthe flow. The primary reason for this modulation is attributedto the two-way-coupled kinetic energy and dissipationbetween the continuous and dispersed phases.The modulation of turbulence due to the presence of par-ticles is attributed to the altered dissipation within the con-tinuous phase caused by the work done at the surfaces of theparticles. 4 The modulation of turbulence in particle ladenflows has been demonstrated by extensive experimentationover the last two decades. 5–15 However, a turbulence modelthat adequately predicts these modulations over a wide rangeof data is still lacking.The most robust and widely used model for turbulence insingle phase flows has been the two equation k  - e model. Theequation for turbulence kinetic energy is:  Dk  t   Dt  ¼ ð  P k  Þ t  À e t  þ @ @   x i m þð m T  Þ t  r k  8>:9>; @  k  t  @   x i ! (1) Correspondence concerning this article should be addressed to P. Dutta at or V V C 2009 American Institute of Chemical Engineers 1416 AIChE JournalJune 2009 Vol. 55, No. 6  where k  t  is the time averaged turbulence kinetic energy ð k  t  ¼ u 0 i u 0 i Þ = 2 Þ ; ð  P k  Þ t  is the production of turbulent energy dueto mean (i.e., time averaged) velocity gradients, v is themolecular kinematic viscosity, ( v T  ) t  is the turbulent kinematicviscosity (based on time averaging), e t  is the time averageddissipation and r k  is the effective Schmidt number for turbulent diffusion. The turbulence kinetic energy is affectedby diffusion, the generation due to mean flow velocitygradients and time averaged dissipation. The equation for dissipation is:  D e t   Dt  ¼ C e 1 ð  P e Þ t  e t  k  t  À C e 2 e 2 t  k  t  þ @ @   x i v þð v T  Þ t  r e 8>:9>; @  e t  @   x i ! (2)where (  P e ) t  is the production of dissipation due to mean (i.e.,time averaged) velocity gradients, C e 1 , C e 2 are empiricalconstants and r e is the turbulent Schmidt number for diffusionof dissipation. As with the turbulence kinetic energy, thedissipation is affected by diffusion of dissipation, productionof dissipation and dissipation of dissipation.The development of the equation for dissipation is not asstraight forward as for the turbulence kinetic energy equa-tion. Bernard and Wallace 16 identify the time averaged dissi-pation as: e t   v @  u 0 i @   x  j  @  u 0 i @   x  j  8>>>>:9>>>>; (3)They show the development of an equation for dissipation bytaking the gradient of the momentum equation, multiplying itby twice the kinematic viscosity and by the gradient of thefluctuating velocity and then time averaging the entireequation, which is mathematically represented by: @ @   x  j  ½  NS i  8>>:9>>; Ã 2 v @  u 0 i @   x  j  8>>:9>>; The instantaneous velocity, pressure, and shear stress aredecomposed into the sum of a time averaged and a fluctuatingproperty to obtain:  D e t   Dt  ¼ À 2 v @  u k  @   x  j  @  u 0 i @   x  j  @  u 0 i @   x k  ! À e ik  ð Þ t  @  u i @   x k  À 2 v u 0 k  @  u 0 i @   x  j  ! @  2 u i @   x  j  @   x k  À 2 v @  u 0 i @   x  j  @  d u 0 k  @   x  j  @  u 0 i @   x k  ! À v @ @   x k  u 0 k  @  u 0 i @   x  j  @  u 0 i @   x  j  ! À 2 v q @ @   x i @  u 0 i @   x  j  @   P 0 @   x  j  ! þ v @  2 e t  @   x 2 k  À 2 v 2 @  2 u 0 i @   x  j  @   x k  8>>:9>>; 2 ð 4 Þ where ( e ik  ) t  is the dissipation tensor. A discussion of each of the terms is presented in Bernard and Wallace. 16 They makearguments for grouping terms together and modeling of other terms to yield the equation for dissipation, namely Eq. 2.A typical approach to obtain two-equation models for tur-bulence energy and dissipation in dispersed phase flows is tobegin by adding a source term to the single-phase momen-tum equation to account for the surface effects, namely, @ @  t  q u i ð Þ þ @ @   x  j  q u  j  u i ÀÁ ¼ À @   P @   x i þ l @ @   x  j  @  u i @   x  j  8>>:9>>; þ a d q d s p  f v i À u i ð Þ ð 5 Þ where u i is the instantaneous carrier phase velocity, v i is theinstantaneous dispersed phase velocity, a d and q d are thevolume fraction and material density of the dispersed phase,respectively, s p is the particle response time, and f  is the dragfactor. The derivations then proceed using the same Reynoldsaveraging procedures employed for single phase incompres-sible flows. This additional term is the drag force per unitvolume on the continuous phase. The concept of adding apoint force to represent the effect of a cloud of particles isopen to argument.A test to assess the viability of a turbulence model for dis-perse phase flows is to apply the model to the simplest pos-sible flow configuration. This idealized case would be a uni-form, steady flow through a cloud of particles fixed in posi-tion over a large region of space with no walls (shown inFigure 1). The volume averaged properties of the flow wouldbe homogeneous and steady. In this case the production of turbulence by the particles would be equal to the dissipationbecause there would be no diffusion or production due tomean velocity gradients. Applying the turbulence modelsderived from Eq. 5 to this configuration typically yields azero or negative value for the dissipation. 17 The momentum equation shown in Eq. 5 cannot bederived from fundamental principles; even for very diluteflows, the momentum equations cannot be reduced to Eq. 5.The two valid approaches for developing the momentumequations for dispersed phase flow are volume averaging 18 and ensemble averaging. 19 It has been shown 18 that the addi-tional source term needed in the momentum equations toaccount for the surface effects of particles arises from vol-ume averaging the momentum equations (i.e., a volumelarger than the continuum limit is necessary). The averagevelocities in the volume averaged or ensemble averagedequations do not represent the local (point wise) instantane-ous velocity of a given flow and thereby are not amenable tothe Reynolds averaging procedures used in single phaseflows. In other words, the temporal fluctuations of the aver-aged velocities do not reflect the flow turbulence.Crowe and Gillandt 20 developed an equation for carrier phase turbulent kinetic energy by volume averaging the me-chanical energy equation. When applied to the basic testcase, the equation reduces to the expected result; the rate of  Figure 1. An idealized case used to test two-way coupled turbulence models in particle-ladenflows. For such a case, it is assumed that there are no wall effectsand the particles are stationary; therefore the generationmust balance with the dissipation. AIChE Journal June 2009 Vol. 55, No. 6 Published on behalf of the AIChE DOI 10.1002/aic 1417  turbulence generation by the particles is equal to the rate of dissipation. The turbulence kinetic energy equation devel-oped by Crowe and Gillandt 20 has been used by Lain et al. 21 in bubble flow. The comparison showed that the numericalresults using Crowe and Gillandt’s 20 turbulence kineticenergy equation slightly under-predicted the average velocitybut was an improvement over conventional models. Zhangand Reese 22,23 also performed an extensive study on Croweand Gillandt 20 turbulent kinetic energy equation and foundgood comparison with the data of Tsuji et al. 8 The purpose of this article is to present an approach toobtain a volume averaged dissipation equation for particleladen turbulent flows. By deriving the dissipation equationfrom first principles, it is possible to establish the effects of the dispersed phase on the turbulence dissipation of the car-rier phase. Review of Volume Averaging Concepts In single phase flows, the turbulence equations are devel-oped by Reynolds averaging the Navier- Stokes equationswhich describe the instantaneous properties at a point. Tur-bulence is described as the temporal velocity fluctuationfrom its time averaged value at a point in the flow. In dis-persed phase flows it is not possible to describe the flowproperties at a point without the inclusion of the effect of the neighboring particles (illustrated in Figure 2).Volume averaging and ensemble averaging provide ascheme to include the effects of the dispersed phase withoutthe necessity of including the details of the surface interac-tion. Crowe et al. 18 and Slattery 24 provide a detailed descrip-tion of the volume average concept. The local volume aver-age of a property B is defined as:  B ¼ 1 V  Z  V  c  BdV  (6)where V  is the volume of the mixture and V  c is the volume of the continuous phase in the mixture volume. The phasevolume average of the property B is defined as: h  B i ¼ 1 V  c Z  V  c  BdV  (7)The phase average property is related to the local volumeaveraged property by:  B ¼ a c h  B i (8)where a c is the volume fraction of the continuous phase, oftenreferred to as the ‘‘void fraction.’’ The averaging volume mustbe large enough to maintain a stationary average yet smallcompared to system dimensions to enable the use of differential operators.Aside from temporal averaging, another way of definingturbulence is by the velocity deviation from the volumeaveraged velocity at a point in time, such as: u i ¼ u i h iþ d u i (9)where u i is the instantaneous velocity, h u i i is the phase volumeaveraged velocity as illustrated in Figure 3. The turbulenceenergy is then defined as k  ¼ 1 V  c Z  V  c d u i d u i 2 dV  ¼ d u i d u i 2 () (10)The advantage of using volume averaging is that the effects of the surfaces are easily distinguished from the effects of thefluid. One of the identities introduced is the volume average of the gradient of a property, which brings out the effects of eachparticle surface within the domain. This identity is expressedas: @ @   x  j   B i ð Þ ¼ @   B i @   x  j  À 1 V  Z  S d  B i n  j  dS (11)where the integration is performed over the particle surfaces, S d , inside the control volume.A very important advantage in applying the volume aver-age concept to dispersed phase flows is that jump boundaryconditions and moving meshes are not needed as would bein a point wise flow analysis (such as the RANS equations).In the presence of millions of particles, this approach wouldbecome computationally expensive. Although DNS practicesuse point wise forces to represent particles, the same Figure 2. A qualitative comparison of the volume aver-aging approach and temporal averagingapproach to modeling effects of particles. Unless the particle surfaces are treated as boundary condi-tions, a temporal averaging approach does not include theeffect of neighboring particles at a point in the flow. Figure 3. An illustration of the volume deviation veloc-ity used to define turbulence in a volumeaveraged setting. The instantaneous velocity, at any point in the flow, is thesum of the volume average and the volume deviation veloc-ities at a point in time. 1418 DOI 10.1002/aic Published on behalf of the AIChE June 2009 Vol. 55, No. 6 AIChE Journal  problem is imposed. In addition, the effect of the particlevolume is ignored. An interim solution to this complex prob-lem is volume averaging.The difficulty with the application of volume averaging tomulti-phase turbulence equations is in the comparison toexperiments. Typical experiments are set up for point wisemeasurements, however with newly developed instrumenta-tion such as Particle Image Velocimetry (PIV) there ispotential to perform volume averaged measurements. Derivation of the Dissipation Equation To close the volume averaged turbulence equation set, anequation for the time rate of change of dissipation is needed.The following derivation is analogous to the derivation of the time average dissipation equation, provided by Bernardand Wallace. 16 The definition of volume average dissipationintroduced by Crowe and Gillant 20 is: e ¼ v @  d u i @   x  j  @  d u i @   x  j  () (12)To begin, a spatial gradient of the Navier-Stokes equation istaken. This is multiplied by the volume deviation velocitygradient ( q d u i  /  q  x  j  ) and twice the kinematic viscosity. Finally,the result is volume averaged, which is represented mathema-tically by: @ @   x  j  ½  NS i  8>>:9>>; Ã 2 v @  d u i @   x  j  8>>:9>>; which can also be expressed as:2 v @  d u i @   x  j  @ @   x  j  q @  u i @  t  8>:9>; þ 2 v @  d u i @   x  j  @ @   x  j  q u k  @  u i @   x k  8>:9>; ¼ À 2 v @  d u i @   x  j  @ @   x  j  @   P @   x i þ 2 v @  d u i @   x  j  @  2 s ik  @   x  j  @   x k  ð 13 Þ Decomposing the instantaneous terms in Eq. 13 into volumeaverage and deviation terms and assuming the flow isincompressible, the above equation can be rewritten as:2 v @  d u i @   x  j  @ @   x  j  @  u i h i @  t  8>:9>; þ 2 v @  d u i @   x  j  @ @   x  j  @  d u i @  t  8>:9>; þ 2 v @  d u i @   x  j  @  h u k  i @   x  j  @  h u i i @   x k  þ 2 v h u k  i @  d u i @   x  j  @  2 h u i i @   x  j  @   x k  þ 2 v @  d u i @   x  j  @  h u k  i @   x  j  @  d u i @   x k  þ 2 v h u k  i @  d u i @   x  j  @  2 d u i @   x  j  @   x k  þ 2 v @  d u i @   x  j  @  d u k  @   x  j  @  h u i i @   x k  þ 2 v d u k  @  d u i @   x  j  @  2 h u i i @   x  j  @   x k  þ 2 v @  d u i @   x  j  @  d u k  @   x  j  @  d u i @   x k  þ 2 v d u k  @  d u i @   x  j  @  2 d u i @   x  j  @   x k  ¼ À 2 v q @  d u i @   x  j  @ @   x  j  @  h  P i þ d  P @   x i þ 2 v q @  d u i @   x  j  @  2 @   x  j  @   x k  ðh s ik  i þ ds ik  Þ ð 14 Þ Applying the volume averaging concept to each term in Eq. 14shows (details are shown in Appendix): v @ @  t  a c @  d u i @   x  j  @  d u i @   x  j  ()! þ v @ @   x k  a c h u k  i @  d u i @   x  j  @  d u i @   x  j  ()! ¼ À 2 v a c @  h u k  i @   x  j  @  d u i @   x  j  @  d u i @   x k  () À 2 v a c @  h u i i @   x k  @  d u i @   x  j  @  d u k  @   x  j  () À 2 v a c @  2 h u i i @   x  j  @   x k  d u k  @  d u i @   x  j  () À 2 v a c @  d u i @   x  j  @  d u k  @   x  j  @  d u i @   x k  () À v @ @   x k  a c d u k  @  d u i @   x  j  @  d u i @   x  j  ()! À 2 v q @ @   x i a c @  d u i @   x  j  @  d  P @   x  j  ()! þ v 2 @  2 @   x 2 k  a c @  d u i @   x  j  @  d u i @   x  j  ()! À 2 v 2 a c @  2 d u i @   x  j  @   x k  8>>:9>>; 2 *+ À v 2 V  @ @   x k  Z  S d @  d u i @   x  j  @  d u i @   x  j  n k  dS þ 2 v q V  Z  S d @  d u i @   x  j  @  d  P @   x  j  n i dS À 2 v 2 V  Z  S d @  d u i @   x  j  @ @   x  j  @  d u i @   x k  n k  dS ð 15 Þ By identifying the volume averaged dissipation tensor as e ik  ¼ 2 v @  d u i @   x  j  @  d u k  @   x  j  DE and noting that the volume averagedcontinuity equation for incompressible flow is @  a c @  t  þ @  ð a c h u k  iÞ @   x k  ¼ 0, Eq. 15 can be rewritten in the form: a c  D e  Dt  ¼ À 2 v a c @  h u k  i @   x  j  @  d u i @   x  j  @  d u i @   x k  () À a c e ik  @  h u i i @   x k  À 2 v a c d u k  @  d u i @   x  j  () @  2 h u i i @   x  j  @   x k  À 2 v a c @  d u i @   x  j  @  d u k  @   x  j  @  d u i @   x k  () À v @ @   x k  a c d u k  @  d u i @   x  j  @  d u i @   x  j  ()! À 2 v q @ @   x i a c @  d u i @   x  j  @  d  P @   x  j  ()! þ v @  2 @   x 2 k  a c e ½  À 2 v 2 a c @  2 d u i @   x  j  @   x k  8>>:9>>; 2 *+ À v 2 V  @ @   x k  Z  S d @  d u i @   x  j  @  d u i @   x  j  n k  dS þ 2 v q V  Z  S d @  d u i @   x  j  @  d  P @   x  j  n i dS À v 2 V  Z  S d @ @   x k  @  d u i @   x  j  @  d u i @   x  j  ! n k  dS ð 16 Þ The above equation is the general dissipation equation for two-way coupled particle laden flows. The assumptionsassociated with Eq. 16 are incompressible flow and no masstransfer between the dispersed and continuous phase. If thevoid fraction is unity and no dispersed phase surfaces arepresent, Eq. 16 reduces to the single-phase flow dissipationequation: AIChE Journal June 2009 Vol. 55, No. 6 Published on behalf of the AIChE DOI 10.1002/aic 1419  Production of Dissipation  D e  Dt  ¼ À 2 m @  h u i i @   x k  @  d u  j  @   x k  @  d u  j  @   x i () À e ik  @  h u i i @   x k  À 2 m d u k  @  d u i @   x  j  () @  2 h u i i @   x  j  @   x k  À 2 m @  d u i @   x  j  @  d u k  @   x  j  @  d u i @   x k  () zfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl}|fflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl{  À m @ @   x k  d u k  @  d u i @   x  j  @  d u i @   x  j  ()! |fflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl{zfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl}  À 2 mq @ @   x i @  d u i @   x  j  @  d  P @   x  j  ()! |fflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl{zfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl}  þ m @  2 @   x 2 k  ½ e À  |fflfflfflfflfflfflffl{zfflfflfflfflfflfflffl}  2 m 2 @  2 d u i @   x  j  @   x k  8>>:9>>; 2 *+ |fflfflfflfflfflfflfflfflfflfflfflfflfflfflffl{zfflfflfflfflfflfflfflfflfflfflfflfflfflfflffl}  Transport Pressure Viscous Dissipationof Diffusion of Diffusion of of Dissipation Dissipation Dissipation Dissipation(17)which is the volume average equivalent to time averagedissipation equation presented by Bernard and Wallace. 16 It isnow apparent that the effects of the surfaces of the dispersedphase are associated with the following terms: À v 2 V  @ @   x k  Z  S d @  d u i @   x  j  @  d u i @   x  j  n k  dS þ 2 mq V  Z  S d @  d u i @   x  j  @  d  P @   x  j  n i dS À m 2 V  Z  S d @ @   x k  @  d u i @   x  j  @  d u i @   x  j  ! n k  dS (18)The integrals in Eq. 18 represent the dissipation effects causedby surfaces of the particles. Within these integrals are spatialgradients of volume deviation properties. To evaluate theintegrals, the coupled gradients must be captured. A firstattempt to evaluate these terms is based on the assumption thatthe particles are much smaller than the equivalent Kolmogorovlength scale and that the drag force is given by Stokes draglaw; in addition, the effects of particle rotation are neglected.The particle-fluid relative velocity ( U  i ) can be expressed as theinstantaneous velocity between the particle and the surround-ing fluid as: U  i ¼ u i À m i (19)which is the same as taking a particle at rest in a flow fieldwith velocity U  i . Substituting Eq. 9 into Eq. 19 shows arelationship between the local velocity deviation and therelative velocity in the form: d u i ¼ U  i þ m i À h u i i (20)The spatial velocity gradients shown in Eq. 18 are evaluated atthe surfaces of the particles. Taking a spatial gradient of theabove equation shows: @  d u i @   x  j   S d ¼ @  U  i @   x  j   S d þ @  m i @   x  j   S d À @  h u i i @   x  j   S d (21)where S d represents the surface of the dispersed phaseparticles. If the particle is rigid and rotational effects areneglected, then the velocity of the particle is constant acrossthe particle. Therefore, the last two terms on the right handside of the above equation are zero when evaluated along theparticle surface, reducing Eq. 21 to: @  d u i @   x  j   S d ¼ @  U  i @   x  j   S d (22)The assumption that the particles are much smaller than theequivalent Kolmogorov length scale (i.e., Stokes flow) allowsthe relative velocity gradients to be solved for analytically.The reason for this assumption is to obtain a simplified form of each term in Eq. 18 and then through empiricism extend theseforms to flows containing particles that are larger than theequivalent Kolmogorov length scale. By transforming thegradients and unit normal vectors between Cartesian andspherical polar coordinate systems, the terms in Eq. 18 can bedirectly solved for. Evaluation of the diffusion term shows thatthe integral over the surface of each particle is zero: À m 2 V  @ @   x k  Z  S d @  d u i @   x  j  @  d u i @   x  j  n k  dS ¼ 0 (23)which is primarily because of symmetry. However, this maynot be the case if the particle is larger than the equivalentKolmogorov length scale. Evaluation of the second term inEq. 18 shows:2 mq V  Z  S d @  d u i @   x  j  @  d  P @   x  j  n i dS ¼ 2 mq V  Z  S d @  u r  @  r  @  d  P @  r dS þ 2 mq V  Z  S d 1 r  @  u r  @  h À u h r  ! 1 r  @  d  P @  h dS ð 24 Þ 1420 DOI 10.1002/aic Published on behalf of the AIChE June 2009 Vol. 55, No. 6 AIChE Journal
Related Search
We Need Your Support
Thank you for visiting our website and your interest in our free products and services. We are nonprofit website to share and download documents. To the running of this website, we need your help to support us.

Thanks to everyone for your continued support.

No, Thanks