Modelling lling industrial ustrial multip tiphase hase flows s - - PowerPoint PPT Presentation

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Modelling lling industrial ustrial multip tiphase hase flows s - - PowerPoint PPT Presentation

Jan 16, 2023 163 likes •385 views

Modelling lling industrial ustrial multip tiphase hase flows s with h STAR-CCM+ CM+ Simon mon Lo & Domin minik ik Kubicki icki Cont nten ents ts Valida dati tion on of the e Eu Euleri rian an mul ultipha tiphase se

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SLIDE 1

Modelling lling industrial ustrial multip tiphase hase flows s with h STAR-CCM+ CM+ Simon mon Lo & Domin minik ik Kubicki icki

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SLIDE 2

Cont nten ents ts

Valida dati tion

  • n of the

e Eu Euleri rian an mul ultipha tiphase se (EM EMP) mode del in chemica emical and proce cess s applicat ations ions

– Slurry pipe flows – Stirred vessels

  • Solid-liquid
  • Gas-liquid

Inter erphase phase transf sfer r of chemica emical l species cies in STAR AR-CC CCM+ M+ v7.02 .02 Granular ar flow w mode del in STAR AR-CC CCM+ M+ v7.04 .04

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SLIDE 3

Horizon rizonta tal l slurr rry pipe e flow experi eriments ments

Pip ipe dia iamet meter er (D) D) = 5 51.5 5 – 495mm 5mm Pip ipe le length th (L) L) = 1 10m Slu lurr rry y veloc locit ity y (V) ) = 3 3.0 – 5.4 m/s Ex Exper periment imental al data a from

  • m Ek

Ekamba ambara a et al. l. (200 009) 9) Ind. Eng. Chem

  • em. Res.
  • s. 48, pp.

8159 59-81 8171. 71. Phas ase e 1 – water er Dens nsit ity y = 9 997. 7.6 6 kg/m3 Vis isco cosity sity = 8 8.887e 87e-4 Pas Ph Phase ase 2 – silic ilica part articles icles Dens nsit ity y = 2 2650 50 kg/m3 Dia iamet meter er (d) d) = 9 90 - 480 480m m Volu lume me fraction ction (vf) f) = 0.0918 918 - 0.273 73

Unif iform soli lids s conce centra tratio ion

g L=10m 10m V 1m 1m D Measur asurem ement ent pla lane ne

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SLIDE 4

Liq iquid id veloci locity Inle let Outle let Mid iddle dle Part rticle icle volume lume frac action ion

Sett ettlin ing g of parti ticles les along ng the pipe

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SLIDE 5

Compari parison

  • n with

th measured asured data

d=90 90 m, , vf=0.19 D=103m 103mm, V=3 m/s d=16 165 5 m, , vf=0. 0.189 189 D=51. 51.5mm, V=4. 4.17 17 m/s

Unif iform soli lids s volu lume fracti ction (vf) and nd slurr urry y velo locity city (V)

g L=10m 10m V 1m 1m D Measur asurem ement ent pla lane ne

STAR-CCM+ STAR-CCM+

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SLIDE 6

Compari parison

  • n with

th measured asured data

d=27 270 0 m, , vf=0. 0.2 D=51. 51.5mm, V=5. 5.4 4 m/s d=48 480 0 m, , vf=0. 0.203 203 D=51. 51.5mm, V=3. 3.41 41 m/s d=16 165 5 m, vf=0. 0.091 0918 8 D=51. 51.5mm, V=3. 3.78 78 m/s d=16 165 5 m, vf=0. 0.273 273, D=495m 495mm, V=3. 3.46 6 m/s

STAR-CCM+ STAR-CCM+

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SLIDE 7

Solid lid-li liquid uid stirr irred d vessel sel

Soli lid-liqu iquid id syst stem em 1ft tank k D=H, fla lat base se sin ingle gle 6bla lade de PBT d=0.5T 5T C/H=0.2 0.25, 5, 4 baffles es Liq iquid: id: Water er-sa

  • salt

t solu lutio tion rl=1150 0 kg/m3 =4.5e-3

  • 3 Pas

Soli lid: d: Gla lass s partic ticles es dp=3.0 3.075 75 mm rp=2485 485 kg/m3

g D H C d Measur asurem ement ent lin line for veloci locities ies at h/H=0 =0.2 h r

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SLIDE 8

Compari parison

  • n of verti

tical cal solid id concentratio ntration

0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1 1 2 3 4 5

h/H C/<C>

Experimental Star-CCM+

STAR-CCM+

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SLIDE 9

Comparis parison

  • n of liqui

uid d velociti cities es

  • 0.5
  • 0.4
  • 0.3
  • 0.2
  • 0.1

0.1 0.2 0.3 0.4 0.5 0.5 1

U/Utip r/R

Liquid Velocities

Uz Experimental Uz Star-CCM+ Ur Experimental Ur Star-CCM+ Utheta Experimental STAR-CCM+ STAR-CCM+ STAR-CCM+

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SLIDE 10

Compari parison

  • n of solids

ids velociti cities es

  • 0.5
  • 0.4
  • 0.3
  • 0.2
  • 0.1

0.1 0.2 0.3 0.4 0.5

0.5 1

U/Utip

r/R

Solids Velocities

Uz Experimental Uz Star-CCM+ Ur Experimental Ur Star-CCM+ Utheta Experimental STAR-CCM+ STAR-CCM+ STAR-CCM+

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SLIDE 11

Gas-liq liquid uid stir irred red vessel el - ICI I mix ixer er

Ga Gas-liquid liquid syste stem D=2ft, t, toris isphe pheric rical al base 3 im impell ller ers 4bla lade de PBT up pumpin ing g d=0.5D .5D 2 Rushto hton n turbine ines s d=0.5D 5D C1/D=0.3 =0.3,C ,C2/D=0 2/D=0.64 .64, , C3/D= D=0.9 0.96 6 4 baffle fles, s, N=280 0 rpm 2 gas sparge rgers rs lo located ted between een PBT and lo lower Rushton hton turbine ine Liq iquid: id: Water er Gas: : Air ir, superfi erficial cial gas veloc locity: ity: 0.0184 184-0.2 0.201 01 m/s

g C1 C1 C2 C2 C3 C3 D

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SLIDE 12

Liquid uid veloc

  • city

ity and gas volume ume fracti tion

  • n

Gas super erficial ficial veloc

  • cit

ity 0.201 01 m/s

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SLIDE 13

Gas caviti ties es behind nd imp mpeller eller paddles les

Lower Rusht hton

  • n turbine

ne Upper Rusht hton

  • n turbine

ne PBT PBT Gas super erficial ficial veloc

  • cit

ity 0.201 01 m/s

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SLIDE 14

Effects cts of increasing easing gas injection ection rate

U=0.0184 0184 m/s

Gas super erfi fici cial al veloc locity ty:

U=0.0448 0448 m/s U=0.0835 0835 m/s U=0.1175 1175 m/s U=0.201 201 m/s

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SLIDE 15

Compari parison

  • n of gas holdup

up

0.05 0.1 0.15 0.2 0.25 5 10 15 20 25 30 35 40 45 50 Experimental Star-CCM+ Superficial velocity [m/s] Gas holdup [%]

STAR-CCM+

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SLIDE 16

Int nter erph phase ase transf ansfer er of chemica ical l species cies in n STAR-CCM+ CM+ v7.02

Al Allow w chemica emical l species cies transf nsfer er betw etwee een n phases: es: gas disso solving ving into

  • liqui

uid, d, gas release lease from

  • m liqui

uid. d. Ai Aimed ed for chem emica cal, l, process cess, , oil & gas, water er, , food

  • d...

... Ap Applications ations: : bub ubble ble columns mns in chemica emical l process cess, , aerati tion

  • n tanks

ks in water er treat atme ment, nt, gas release lease in oil & gas riser ers, s, aerati tion

  • n in bio-react

reactor

  • rs...

s...

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SLIDE 17

Oxyge gen n transf nsfer er in n aeration ation tank nk in n water er treatm eatmen ent

Volu lume me fraction ction of a air ir Oxyg ygen n in in a air ir Oxyg ygen n in in w water er

Oxygen level at water r surface face and exit

Water er Air injec jector

  • r
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SLIDE 18

Gr Granular nular flow model el in n STAR AR-CCM+

  • CCM+ v7.04

Kinetic tic theor eory y mode del for r granular r flows. ws. Par Particle cle-pa particle ticle collis isions ions repre resent sented d by a granular r temperature perature equa uati tion

  • n

deri rived ed from

  • m kine

neti tic theor eory. Sui uitable able for dense nse particle cle flows ws suc uch as flui uidi dise sed d beds ds. Ai Aimed ed for chem emica cal, l, process cess, , oil & gas, water er, , food

  • d,

, ceme ment, nt, minera neral, l, pharma rmace ceuti utical, cal, agricultura ultural.. l... Ap Applications ations: : flui uidis dised ed bed d react ctor

  • rs,

s, sand d and slur urry y transp spor

  • rts

ts, solid id handl ndling... ing...

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SLIDE 19

Flui uidised dised be bed

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SLIDE 20

Summa ummary

We will cont ntinue inue to validat ate e the e Eu Eulerian ian mul ultip ipha hase se (EM EMP) model

  • del against

nst indust strial ial applications ations. We will cont ntinue inue to develop elop new w capabi bilities lities in STAR AR-CC CCM+

– Chemical reaction model (v7.04) – More turbulence model options (v7.04) – Multi-particle phases granular model (v7.06) – Coupling with liquid film model (v7.06) – Non-Newtonian model (v7.06)

We will cont ntinue inue to imp mprove e us user r experi perienc ence e of the e mode dels

– Robustness of models – Clear model description in user manual, tutorial examples