Reacti ting ng flow modeling ng and applica cati tions ns in - - PowerPoint PPT Presentation

Yongzhe gzhe Zhang, ng, CD CD-adapco pco

Reacti ting ng flow modeling ng and applica cati tions ns in STAR-CCM+

Bet etter er flow and mixing ng accurac racy Results lts in bett etter er predic iction ion with th PVM combus bustion tion model dels ~32.7 .7 million ion cells ls Δt = 1x10-6 s

LES: : Scaled d Combust ustor

LES Flare: : Impr mproved d predi dicti ction n of combus usti tion n effici ciency ncy

PVM model el ~15 million lion cells ls Δt = 5x10-5 5 s

A Validation of Flare Combustion Efficiency Predictions from Large Eddy

• Simulations. Anchal Jatale, Philip J.

Smith, Jeremy N. Thornock, Sean T Smith, Michal Hradisky. University of

• Utah. Combustion and Flame.

More Large ge Eddy y Simulatio mulation n (LES) ES)

– Better prediction of instantaneous flow characteristics and turbulence structures – Computationally expensive

Include ude Detailed d Chemi mistr try

– Better prediction of autoignition and emissions (CO/NOx)

– Models

• Complex chemistry model
• Tabulated Chemistry model

Applicat ication ion trend

Complex Chemistry Model

CCM CCM Chemistry mistry reducti ction : Offli line (DRG) Turbule lence ce- chemi mistry stry Interactio ction Effici icient t ODE solve ver Computa tati tional Cost Storage/Re /Retrie trieva val l Sch cheme me(IS ISAT AT) Eddy y Dissip ipati tion Conce cept (EDC) Load bala lancin cing for parall llel l compu mputi ting Analyti lytica cal l Jacob cobia ian Equil ilib ibriu ium m Time Scale le (Init itia iali liza zati tion)

Transport equation of chemical species Nonlinear, stiff ordinary differential equations (ODEs)

Equi quili libri brium um Time e Scale e Model (EqTS TSM)‏

Motiva vati tion

– A better initial condition can greatly accelerate DARS-CFD

Model

– The model assumes the species composition to relax towards the local chemical equilibrium at a characteristic time scale determined based on the local flow and chemistry time scales – Quickly provides an reasonable initial condition to DARS-CFD – Results similar to PPDF equilibrium, but more flexible:

• no stream limitation/no precomputed table needed/easier to set up

– Can be used as a standalone model to obtain a quick approximate solution

Motiva vati tion

– Detailed chemistry is important to predict autoignition and emissions (CO/NOx) – Computationally expensive to include a full set of species

Tabulated d Detailed d Chemi mistr stry y for turb rbul ulent nt combustion ustion

– Precompute chemistry table and retrieve during CFD computation

• Can use large mechanism

– Dimension reduction to chemistry – Consider turbulence-chemistry interactions.

Existi ting ng models

– PPDF with equilibrium – PPDF with laminar flamelets – PVM (Progress variable model) – FGM (Flamelet Generated Manifold)

Tabula ulated ed Chemis mistr try y Model

Simi milar r to the existi sting ng PVM model:

– A tabulated detailed chemistry model – A progress variable is used to bridge the CFD side and the table

Impr mproveme ment nts s comp mpared d to the exist sting ng PVM model

– Table is from flamelet manifold

• A turbulent flame is an ensemble of laminar flamelets

– Option of using progress variable variance

• Presumed Beta PDF in progress variable space

– Option of considering heat loss ratio – Flexible progress variable definition

• Chemical enthalpy

– Sum over all species

• Species weights

– Defaults: YCO+YCO2

FGM combus bustion tion model

FGM table le genera eratio tion in DARS-BASI ASIC

9

• Generated table can be directly loaded into STAR-CCM+ for

further construction

A A glass ss furna nace ce simul mulati tion n using ng FGM model

• Furnace

ce dimen mensio sions: s: 3.8m m x 0.88m m x 0.955m, m, fuel l inle let t diamet meter: : 1.2cm cm

• Natural

l gas s at 283 K at Fuel l Inlet

• 10 % exce

cess ss air at 1373 K at Air Inlet

• Compariso

ison with experime iment t at four measu surin ing poin ints; ts; x= 0.6m, , x = 0.9m, , x =1.2m m and x = 1.8m

• Illustrati

stration of approxima ximate te regio ion of NOx formati tion (light t blue), , mixin ing & combusti stion (red)

Boundar ndary y Condi diti tions ns

Quantity Fuel Inlet Air Inlet Glass Wall Chamber Walls Velocity (m/s) 125.0 10.0

• Temperature

(K) 283.0 1373.0

• Heat Flux

(kW/m2)

• 90.0

2.0

Validation tion with h IFRF F glass s furnace nace

Heat loss effect is important

13

Latest t model l additions tions (v 9.04 04-10.0 0.04)

Includ lude e det etailed ed chemist mistry y with an affor

• rdabl

able e computation putational al cost

– Equilibrium Time Scale – Flamelet Generated Manifold (FGM)

Cope e with h more e comple plex conf nfigurat igurations ions

– Inert stream – Reacting channels

Expand nd appli licati cation

• n coverages

erages

– Polymerization – Surface chemistry with multiple sites and open sites

Reacti cting Channel

Reacti tion n models s in STAR-CCM+

Reactio ction Models ls Multi ti-co compo mponent t Gas Lagrangia ian Multi tiphase se Eule leria ian Multi tiphase se Multi ti-co compo mponent t Liquid id Non-Premixe Premixed Combust stio ion Premixe mixed Combusti stion Parti tiall lly-Pre Premixe mixed Combust stio ion Emissio ssion Models s (Soot/ t/NO NOx/CO) x/CO) Eddy y Conta tact ct Model l (ECM) Polyme ymeriza izati tion Parti ticle cle Reactio ction Coal l combu mbusti stion Interphase se Reactio ction Surfa face ce Chemistry mistry

Combu bustion stion models ls for r multi ti-co compo ponent ent gas

Premixe mixed Combustio stion Emissio ssion Multi ti-compo component t Gas Combustio stion Presu sume med PDF (PPDF DF) Progre ress ss Variabl iable Model l (PVM) Turbule lent t Flame me Speed Closu sure (TFC) PCFM PTFC Premixe mixed Eddy- Breaku kup (PEBU BU) Coherent t Flame me Model l (CFM) Premixe mixed PVM (PPVM) VM) Eddy-Bre Breaku kup (EBU) U) Non-Pre Premixe mixed Combustio stion Parti tiall lly-Pre Premixe mixed Combustio stion Dars-CFD FD Dars-CFD FD Dars-CFD FD Eddy-Bre Breaku kup (EBU) U) Flamel melet Genera rate ted Manif ifold ld (FGM) SOOT NOx CO CO

16

Develo elopment ent objectiv ectives es

Meet et all aspects ects of requi uirement rements s from

• m our clients

nts

– Wider er applic icatio tion coverage rage – Ac Accuracy racy – Effic icie iency cy – Robu bustn tness ess – Ease e of use – New mode del l develo lopme ment – Imp mprovem ement ents to existin isting g models dels

17

Latest t model l additions tions (v 9.04 04-10.0 0.04) 4)

Includ lude e det etailed ed chemist mistry y with an affor

• rdabl

able e computation putational al cost

– Equilibrium Time Scale – Flamelet Generated Manifold (FGM)

Cope e with h more e comple plex conf nfigurat igurations ions

– Inert stream – Reacting channels

Expand nd appli licati cation

• n coverages

erages

– Polymerization – Surface chemistry with multiple sites and open sites

Inert t stream eam for r PPDF combu mbust stion ion model el

Motiva vati tion

– To reduce the PPDF table size for complex configurations where one stream, or part of the stream, is inert (negligible reactivity and sole effect is for dilution)

Inert t str tream m treatm tment nt

– Only consider its dilution effects to the reacting mixture – Compared to take it as active

• Smaller table size
• Faster table generation
• Faster interpolation

Inert t strea tream m model

– A transport equation for the mixture fraction solved for inert stream – Species mass fractions from reacting and inert streams – Temperature from local total enthalpy and mean species

Reacti cting ng Channel nel Co-Si Simu mulation ation

Applic ication ation

– Process heaters – Cracking furnaces – Steam reformers

Modeling eling Challen llenges es

– Firebox side has multiple burners – Process side has many tubes – Full 3-D modeling is computationally intensive

Perform

• rmanc

ance e Considerat ideration ions

– Uniform heat distribution – Emissions – Conversion rate

Modelin eling of Proces ess side

Comput mputationally expe pensi sive Comput mputationally less s expensi sive

3-D vs 1-D

Gas-Pha Phase: e: [ FireB eBox Side] e]

– 3-D, turbulent flow – Combustion models – Heat transfer

Reacti ting g Chann nnel: el: [Proc

• ces

ess Side] de]

– 1-D Plug Flow Reactor (PFR) – Inlet composition, temperature – Process-side reactions – No meshing, solving with STAR-CCM+

Couplin ling

– Temperature is provided to the process side – Heat flux is returned back to firebox side

Reacti cting ng Channel nel Co-Si Simu mulation ation

Burner er Proces ess Side Side An elega gant nt way to fully ly couple le Firebo rebox side e and Proces ess side

Output put from

• m Co-simul

simulation ation : Process ess Side

Axial l distr trib ibution ution of Temperature, erature, Heat t Flux, , and Species ies convers ersions ions

CH4 Mass Fraction H2 Mass Fraction

Polymeri ymeriza zation tion

Expand and our applica cati tion n coverage age Polym ymeriza rizati tion

• n Process

cess

– monomers are linked by chemical reactions to form long chains – starts with mixing a Monomer (M) and an Initiator (I) in a Solvent (S) – Steps involved: initiation/propagation/transfer/branching/termination – Final product is polymers of varying lengths and structure.

Polym ymerizati zation

• n Moment

nt Model for free radical cal polym ymerizati tion

– Scalar Transport Equations for Moments are solved in STAR-CCM+: live/dead polymers – source terms of the above moment transport equations depend on the sub processes of polymerization. – Provide: total polymer concentrations, NACL/NAMW, WACL/WAMW, polydispersity index

Industri ustrial-Sca Scale Stirred d Tank k Reactor – Styrene ne Polym ymerization zation

• Steady (Implicit Unsteady)
• K-Epsilon Turbulence
• Realizable K-Epsilon Two-Layer
• Two -Layer All Y+ Wall Treatment
• Multi-Component Liquid
• Polymerization
• Segregated Flow
• Segregated Fluid Enthalpy
• Three Dimensional
• MRF, RBM

Polyd ydisp ispersit sity index

Multi tiple ple sites s for surface ce chemi mistr try Chemical vapor deposition (CVD) reactor

Open sites es for r surface ce chemi emistr stry

Adsorption ption reacti tion n descr cripti tion

– Atomic Site

• AsH3(g)+Ga(s)->AsH3(s)+Ga(b)

– Open Site

• O(s)+AsH3(g)->AsH3(s)

Open sites s treatm tment nt

– Considered as a species – Contains no element (empty) – Named as OPEN in the CHEMKIN kinetics input file

Applications ications

Large ge Eddy Simul mulation ation (LES) S) with h det etailed ed chemist mistry

– Gas turbine combustors – Burners, Furnaces and Incinerators – Fires

High h speed ed flows ws

– Scramjet – Rocket engine nozzles

Multipha phase se react ctions ions

– Coal reactors: Pulverized/Fluidized bed – Surface chemistry (SCR/CVD)

Optimiz mizations tions

– Chemistry – Combustor design

Applications ications

Large ge Eddy Simul mulation ation (LES) S) with h det etailed ed chemist mistry

– Gas turbine combustors – Burners, Furnaces and Incinerators – Fires

High h speed ed flows ws

– Scramjet – Rocket engine nozzles

Multipha phase se react ctions ions

– Coal reactors: Pulverized/Fluidized bed – Surface chemistry (SCR/CVD)

Optimiz mizations tions

– Chemistry – Combustor design

Emissions Fuel Flexibility, Flame Stability Thermo-acoustic Instability Mechanical Durability Cost

• UHC
• Soot
• Nox
• CO
• Flame shape
• Flame location
• Flash-back/ blow-off
• Gaseous/liquid Fuels
• Liner temperature
• Component temperature

System Level Combustion Chemistry Heat Transfer Fluid Dynamics Unit Level

• Flow and mixing
• Swirlers
• Bluff bodies
• Fuel formulation
• Operating conditions
• Chemical kinetics
• Thermodynamics
• Conduction
• Convection
• Radiation

Combus ustion

• n Systems

ems

Droplet Evaporation

– Quasi-steady – User defined

Droplet Break-up

– Primary atomization

• Linear Instability Sheet Atomization (LISA)

– Secondary break-up

• Kelvin Helmholtz-Rayleigh Taylor (KHRT)
• Taylor Analogy (TAB)
• Stochastic Break-up (SSD)

Droplet Wall-impingement

– Bai-Gosman – Satoh

Collision Detection Model

– No Time Counter (NTC) – O’Rourke

Two-way Coupling

Turbulence Dispersion

– Random Walk Technique

Liquid Droplet Combustion

Perform

• rmanc

ance Impr provements nts: : Large ge Cases (LES) S)

• Flow Solver improvements in v9.04

Case 1 Case 2 Case 1 Case 2

• Combustion solver improvements in

v9.02 (40-50% speedup)

• Flow and Lagrangian solver

improvements in v9.04 (20-25% speedup from v9.02)

Run RANS S first st before attemptin pting LES. Need good qu quali lity ty mesh for LES. . Keep p a mesh size that gives s a cut-off wa waven venumbe ber within in the inertial tial subran ange. Use bounde ded d central al differencin cing (BCD) ) with appr propriat priate blendin ding facto tor for LES runs. The coupl pling ing frequ quency cy for Lagran angian ian (in the case of spray combust stio ion) ) and radiat iation ion can be adjusted d for faster run times. s.

– Lagrangian update can be done once every time-step – Dynamic load balancing for Lagrangian spray helps with speed up

Set-up p of monitors s for means and va varian iance in LES.

• S. Start sampli

ling after 4-5 5 flow times. s.

Best t Practi ctice ces s and Sugge gest stions ns

Fuel/Ai Air Ports ts

Fuel el Po Ports ts Air

Bad surface mesh Fuel ports not adequately resolved Good surface mesh Fuel ports well resolved Recommended to have at least 2 prism layer cells and a total of 8 cells across the ports.

In case of swirlers, and other narrow passageways, need to make sure there are adequate cells and good prism layers to get the right velocity profile. Pipes and tubes that are common in process heaters are required to be meshed in such a way that their curvature is retained.

Tubes s and other curved d surface ces

Volume umetr tric c Refine neme ment nt

Fuel el Air Air Fuel el

Use volume control blending with a blending factor of 0.5 to obtain smooth transition between

• verlapping volumetric controls.

Note: blending factor has little or no effect on core mesh if the volumetric control is far away from the surface boundaries.

Table Based d Refine neme ment nt

Fiel eld func nction

• n used

ed for deter ermin mining new mesh sh size ze

($MixtureFraction0 > 0.5)? 2e-4 :(($MixtureFraction0 > 0.3) ? 5e-4 : (($MixtureFraction0 > 0.1)? 0.0025 :0))

Other r criterio rions ns for mesh refine neme ment nt

• Temperature, temperature gradient
• Velocity, velocity gradient
• Species concentrations, their gradients

Applications ications

Large ge Eddy Simul mulation ation (LES) S) with h det etailed ed chemist mistry

– Gas turbine combustors – Burners, Furnaces and Incinerators – Fires

High h speed ed flows ws

– Scramjet – Rocket engine nozzles

Multipha phase se react ctions ions

– Coal reactors: Pulverized/Fluidized bed – Surface chemistry (SCR/CVD)

Optimiz mizations tions

– Chemistry – Combustor design

Densit ity-base ased d Solver er

– Coupled, implicit formulation with AMG acceleration – TVD reconstruction

• AUSM+ or Roe inviscid flux schemes
• MUSCL + Venkata limiter

Real gas models els

– Redlich Kwong – Soave-Redlich Kwong – Modified Soave-Redlich Kwong – Peng Robinson

High Speed Reacting Flows

Advanc vanced ed Initi tializ alizat ation ion

– Grid sequencing option – Fully implicit newton-type solution algorithm – Controllable number of coarse levels

Conti tinuity uity Conver ergen gence e Acceler elerat ator

• r (CCA)

– Used for high speed flows where convergence for mass flow is slow – Solves pressure correction equation using density based Riemann Flux discretization – Overall and individual cell mass imbalances are minimized at each iteration – Option available for Coupled Implicit Solver.

Advanced Initialization and Convergence Control

Global al Chemis mistr try

– Single or multi-step – Variants of eddy break-up model

• Standard
• Hybrid
• Combined time-scale
• Kinetics only

Tabul ulat ated d Chemis mistr try Det etailed ailed Chemis mistr try

– DARS-CFD stiff chemistry solver – Use Equilibrium Time-Scale approximation for initial guess – Then switch to finite rate chemistry

• Laminar flame concept
• Eddy dissipation concept

Combus usti tion n Modeling ng in High gh Speed Flows ws

Coupled Implicit, Axisymmetric Steady, SST K-Omega turbulence Detailed chemistry: 11 species DARS-CFD Approximation options:

– In-situ Adaptive Tabulation

• Populates source terms as the

simulation progresses for subsequent look-up

• Speeds computational time once the

table is populated

– Equilibrium Time-Scale

• Quick approximate solution for

detailed chemistry calculations

• Assumes chemical composition

relaxes to local equilibrium composition at time-scale determined by flow and chemistry

Reacti ting ng Nozzl zle Flow

Supersonic Combustion

• H2 Fueled

led NASA SA SCHOLA OLA direct rect-conn

• nnect

ect Scramje amjet t engine ne

• Valid

idate against experime iment nt and NASA SA VULCA CAN N code de Mesh: h: 1.4M Hex-dominant 10 Prism Layers Solver: er: Density based solver Steady,k-w SST, AUSM+FVS Non-adiabatic PPDF

Supersonic Combustion (2)

Yongzhe Zhang, Ivana Veljkovic, Nolan Halliday and Rajesh Rawat, "Numerical Simulation of a Scramjet Using a Storage/Retrieval Chemistry Scheme", AIAA 2014, Washington DC

Applications ications

Large ge Eddy Simul mulation ation (LES) S) with h det etailed ed chemist mistry

– Gas turbine combustors – Burners, Furnaces and Incinerators – Fires

High h speed ed flows ws

– Scramjet – Rocket engine nozzles

Multipha phase se react ctions ions

– Coal reactors: Pulverized/Fluidized bed – Surface chemistry (SCR/CVD)

Optimiz mizations tions

– Chemistry – Combustor design

Coal l combus ustors

• rs

– Pulverized – Fluidized bed

Simulation lation mot

• tiv

ivations ations

– Particle nozzle design – Stability – Combustion efficiency – New combustion technologies for low NOx/SOx

Simulati lation

• n approac

aches es

– Lagrangian particle – Eulerian Multiphase (EMP) – Discrete Element Method (DEM) particle

Coal-fired d boilers s and gasifiers

Gas phase

– Solves transport equations for mass/momentum/energy and species

Pa Partic icle le Momen entu tum Transfer er

– Solves equation of motion for parcels of dispersed phase – Surface and body forces can be included – Turbulent dispersion model available

Two-Way Coupling ling

– Particle Mass Transfer

• Drying of coal
• Release of coal volatiles
• Oxidation of char

– Particle Heat Transfer

• Heat up of particles
• Radiative transfer in the presence of particles

Lagrangi ngian Approach ch

Heterogeneous s Reactio tions s for Partic ticle les

– Raw Coal Devolatilization

• Two-step devolatilization
• User-defined devolatilization

– Char Oxidation char reaction with O2, H2O and CO2 considers gas phase diffusion and heterogeneous reaction

• First-order char oxidation
• Half-order char oxidation
• User-defined char oxidation

– SO2 reactions

NOx

– Thermal NOx – 3 step Zeldovich – Prompt NOx – global chemistry – Fuel NOx – source of nitrogen from volatiles and char

Gas phase reactio tions

– Global chemistry

Chemi mica cal reacti tions ns

Coal Combust ustion n Valida dati tion

Model el Select ection ion:

– Coal particles

• Moisture evaporation
• Raw coal de-volatilization
• Char oxidation
• Fuel NOx + Thermal Nox
• Particle radiation

– Gas Phase

• 4 step global kinetics
• Radiation

– Participating Media Weighted Sum of Gray Gases Quantity Measured Predicted Dimension T 1353 1347 Kelvins Oxygen 3.0 3.08

• Vol. %, dry

CO2 15.6 15.43 Vol.%, dry Burnout 99.4 100.0 Weight %

Mathematical Modeling of a 2.4 MW Swirling Pulverized Coal Flame

• Combust. Sci. and Tech, 1997, Vol 122, pp. 131-182

Centerli rline ne Temp mperat rature ure

Selecti ctive Catalyt ytic c Reacti tions: ns: Surface ce Chemi mistr try

poro rous us medium ium

• Spray dynamics

mics

• Gas

s chem emist stry & surface ce chem emist stry in the e cata talyst st

• Turbul

ulen ence ce mixing & heat trans nsfer er

• Main

n challenges/o enges/object ectives s in SCR design: n: Mini nimum mum dosing, ng, maximum ximum NOx reduc uction

• n, preven

ention

• n of NH3 slip

Global al Chemistr istry

– One or two step reactions – Computationally fast – Might need tuning of kinetic parameters

Det etailed ailed Chemis istr try with h porous us media ia

– DARS-CFD solver for stiff equations – Computationally expensive – Spatially more accurate

SCR Catalyt ytic c Chemi mist stry

Resul ults ts – NOx x Reducti ction n Compa mparison son

Two wo-Step Model Detailed d Surface Chemi mist stry

Applica cati tion n Example ple: : SCR modelling ng

• Lagrangian droplets are injected into the hot exhaust flow
• The liquid droplets and gas exhaust pass through a mixing vane
• Some of the droplets impinge on the vane and form a film which boils
• The mixture of exhaust gases and boiled vapour move into the catalyst

Applications ications

Large ge Eddy Simul mulation ation (LES) S) with h det etailed ed chemist mistry

– Gas turbine combustors – Burners, Furnaces and Incinerators – Fires

High h speed ed flows ws

– Scramjet – Rocket engine nozzles

Multipha phase se react ctions ions

– Coal reactors: Pulverized/Fluidized bed – Surface chemistry (SCR/CVD)

Optimiz mizations tions

– Chemistry – Combustor design

Opti timiza zati tion n of Gas Turbine ne using ng STAR-CCM+ M+ and Optimate+

• Match flame length and shape with experiments,
• Minimize NOx and CO emissions,
• Minimize pressure drop,
• Maximize combustion efficiency,
• Maximize homogeneity at combustor exit

Geometry Optimization or Operating Condition Optimization

Hybrid id

– Blend of search strategies

Adapti tive

– Adapts to design space

Effic icien ient

– Set-up very easy – Solution found in

Robust

– Global and local optimization at the same time

Easy to use

– One parameter: Number of runs

SHER ERPA Opti timiza mizati tion n Algorithm thm

Generic ric Combus ustor

• r for Optimizati

tion

Combus ustor

• r Type

e – Annular lar

– Optimize geometry based on performance objectives

Pa Paramet eteriz erized ed design ign features tures

– Swirler twist angle – Liner hole radius – Hollow cone injector’s

• Inner and outer cone angle

Pa Parame meter Ranges

Swirler geomet metry y for Min (16°), , Baseline (45°), , Max (93°) Hole radius s for liner: : Min=1mm, =1mm, Baseline=2mm, =2mm, Max=2.9 =2.9 mm Inner cone angle: : 0 to 45 degrees.

• s. Outer cone angle:

: 45 to 120 degrees

Pa Pareto Opti timiza zati tion n – Resul ults ts

1.100E-08 1.300E-08 1.500E-08 1.700E-08 1.900E-08 2.100E-08 2.300E-08 2.500E-08 2.700E-08 8.450E-07 8.650E-07 8.850E-07 9.050E-07 9.250E-07 9.450E-07

Tot

• tal NOx at Outlet

et (kg/s) s) Object ective e 1 - Tot

• tal CO at outlet (kg/s)

s)

'Pa Pareto

• Front'

nt' & Baseline line

1.100E-08 1.120E-08 1.140E-08 1.160E-08 1.180E-08 1.200E-08 1.220E-08 8.400E-07 8.500E-07 8.600E-07 8.700E-07 8.800E-07

'Pareto

• Fron
• nt'

Rank 1 Baseline line

Opti timiza mizati tion n Resul sult

Case Baseline line (Rank k – 40) 40) Rank – 1

Twist st angle gle (°) 45 45 51 51 Liner er Hole Radius us (mm) 2 1 Inne ner Cone e Angle e (°) 10 10 37 37 Outer er Cone ne Angle e (°) 90 90 61 61 Cone ne Angle e (°) 80 80 24 24 Volume ume aver eraged ged T (K) 1000. 0.7 969.5 Tot

• tal CO (kg/s)

/s) 9.441E-07 07 8.613 13E-07 07 Tot

• tal NOx (kg/s

/s) 2.697E 7E-08 08 1. 1.126E 6E-08 08 Perfor

• rma

manc nce

• 2.00

00

• 1.

1.33 33

8.8% 58.2 .2%

New models ls added to (v 9.04-10.04)

– Include detailed chemistry with an affordable computational cost

• Equilibrium Time Scale
• Flamelet Generated Manifold (FGM)

– Cope with more complex configurations

• Inert stream
• Reacting channels

– Expand application coverages

• Polymerization
• Surface chemistry with multiple sites and open sites

Appl plic icati ations

• ns

– Large Eddy Simulation (LES) with detailed chemistry – High speed flows – Multiphase reactions – Optimizations

Summa mmary

Thank nk you for r your r attent ention! ion!