Mult ltipha hase F Flo low M Models ls i in S n STAR-C -CCM+ - - PowerPoint PPT Presentation

Mult ltipha hase F Flo low M Models ls i in S n STAR-C

• CCM+

Simo mon L n Lo

Gr Granu nula lar f flo low

– Mixing of multiple particle phases – Transport equation for granular temperature

Mult ltipha hase t turbule lenc nce

– RSM

Mult lti-c

• compone

nent nt b boili ling ng

– Binary mixture evaporation

Popula lation b n bala lanc nce

– Adaptive MUSIG

Mult ltipha hase r rhe heolo logy y

– Suspension – Emulsion

Eule lerian M Mult ltipha hase F Flo low M Models ls i in S n STAR-C

• CCM+

DE DEM A Approach – h – M Mixing ng a and nd C Coating ng o

• f P

Particle les

Mult lti-p

• particle

le R Rotary Dr y Drum – m – P Particle le s segregation n

3 3 mm 4 mm 4 mm 5 mm 5 mm 6 mm 6 mm mm Particle le s segregation i n in t n trans nsverse p pla lane ne o

• f d

drum m

EMP A Approach - M h - Mult lti-p

• particle

le R Rotary Dr y Drum m

Average p particle le v velo locity v y vectors i in t n trans nsverse p pla lane ne o

• f d

drum m Poly ly-d

• dispersed p

particle les – – 3 3mm, 4 mm, 4mm, 5 mm, 5mm, 6 mm, 6mm. mm.

Streamwise velocities at x=0 on the transverse plane, rotating speed 11.6rpm

Multi-particle Rotary Drum – P Particle le v velo locity

Circula lating ng F Flu luidized B Bed

6.1 m m Inle Inlet Outle let

αg= 1 1 αs= 0 0.5 .55 ug= 1 13 m/ m/s ug= u us

s = 1

1.3 .3 m/ m/s

Gr Granu nula lar F Flo low M Model l

• Gr

Granu nula lar t temperature t trans nsport mo model l

• Suited f

for f flu luidised b beds, e , especially i lly in b n bubbli ling ng a and nd t turbule lent nt r regime me. .

Circula lating ng F Flu luidized B Bed - R

• Result

lts

Reyno ynold lds S Stress T Turbule lenc nce M Model l

Reyno ynold lds S Stress T Turbule lenc nce M Model l

k-ε RSM

Mult lti-c

• compone

nent nt b boili ling ng mo model l

Evaporation o n of mu mult lti-c

• compone

nent nt f flu luids. . – Applications refinery and distillation processes.

Evaporation o n of a a b bina nary mi y mixture

Evaporation o n of b bina nary mi y mixture: P : Pent ntane ne & & Do Dodecane ne

Heat Heat Ga Gas Li Liqui uid d Te Temperature Vo Void fraction n x P Pent ntane ne x Do Dodecane ne

An E n Eule lerian p n popula lation b n bala lanc nce me metho hod f for p poly ly-d

• disperse

mu mult ltipha hase f flo lows. . Adaptive M MUS USIG M IG Model l

1 2 2 3 3 4 4 5 5 6 6 7 7 8 8 1 2 2 3 3 4 4 5 5 6 6 7 7 8 8 Mass a and nd nu numb mber d dens nsity a y are r redistributed b between ne n neighb hbour g groups so t tha hat e each g h group ha has t the he s same me ma mass b but ne new d diame meters. . d d d d

Adaptive M MUS USIG M IG Model l

Adaptive M MUS USIG - Dr IG - Drople let b breakup t thr hrough a h an o n orifice

Sauter Mean Diameter Breakup Rate (log scale) Turbulent-induced breakup Shear-induced breakup

Suspensions – relative viscosity model Krieger-Dougherty model

Suspensions – Eulerian multiphase

Two-fluid formulation

The momentum equation for phase k is From the suspension balance model Fluid stress is pressure with viscous term and shear particle stress term Particle stress is Morris and Boulay total stress

Suspensions – relative viscosity models Morris and Boulay model Total particle stress is:

web.mit.edu

Suspensions – pipe flow modelling

Modelling results of Hampton et. al NMR suspensions in pipe experiments At volume fraction of particles = 0.3 The Morris and Boulay relative viscosity model is capable of causing particle migration towards the centre of the pipe. When the normal stresses are turned off then no particle migration occurs. Kn = 2

Emulsions Surfactant stabilised emulsions share many properties of suspensions as the fluid particles can be approximated as solid particles.

• As the volume fraction of the

dispersed phase is increased the effect of maximum packing leads to divergent viscosity,

• eventually a phase inversion occurs.

Emulsions Pressure Drop in STAR-CCM+ Modelling the pressure drop in pipes, (experimental data from Dr. Jose Plasencia)

“Pipe flow of water-in-crude oil emulsions: Effective viscosity, inversion point and droplet size distribution” Jose Plasencia, Bjørnar Pettersen and Ole Jørgen Nydala, Journal of Petroleum Science and Engineering Volume 101, January 2013, Pages 35–43

Crude oil A and seawater emulsion in horizontal pipe of diameter 2.21 cm, At a velocity of 0.44 m/s (laminar regime).

Interestingly with models that have no negative normal stresses, Pressure drop is over- estimated