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Multi-phase Flow in OpenFOAM

Multi-phase flows have wide applications in process, refrigeration, air conditioning, petroleum, oil and gas, food processing, automotive, power generation and metal industries including phenomena like mixing, particle-laden flows, CSTR - Contunuously Stirred Tanks Reactor, Water Gas Shift Reaction (WGSR), fluidized bed, fuel injection in engines, bubble columns, mixer vessels, Lagrangian Particle Tracking (LPT). Some of the general characteristics and categories of multi-phase flow are described below before moving to actual application of OpenFOAM utilities.

In a multiphase flow, the interface between the phases are influenced by motion of fluid. For example, water flowing through packed bed of rocks is a single phase flow. Multiphase flow regimes are typically grouped into five categories: gas-liquid (which are naturally immiscible) flows and (immiscible) liquid-liquid flows, gas-solid flows, liquid-solid flows, three or more phase flows. As can be seen, the immiscibility is a important criteria. In a multi-phase flow, one of the phase is usually continuous and the other phase(s) are dispersed in it.

The adjective "Lagrangian" indicates that it relates to the phenomena of tracking a moving points ("fluid particles") - such as tracking a moving vehicle on a road. On the other hand, the adjective "Eulerian" is used to describe correlations between two fixed points in a fixed frame of reference - such as counting the type of vehicles and their speeds while passing through a fixed point on the road.

Gas-liquid flows are further grouped into many categories depending upon the distribution and shape of gas parcels. Three such types namely bully, slug and annular are described in later paragraphs. Another broad classification of multiphase flows are 'homogeneous' and 'inhomogeneous'. The differences are tabulated below.

Homogeneous Multiphase Flows | Inhomogeneous Multiphase Flows |

All phases move at same velocity, same flow field | Each phase has its own flow field |

There is no velocity 'slip' | There is velocity 'slip' |

There is no interphase mass and momentum transfer | Interphase mass and momentum transfer are considered |

Mixture momentum equation | Momentum equations for each phase |

Mixture continuity equation | Continuity equations for each phase |

Homogeneous pressure field^{*} | Homogeneous pressure field |

Homogeneous turbulence field | Homogeneous or inhomogeneous turbulence field |

The two dominant method of multi-phase simulations are listed below.

There are three different Euler-Euler multiphase models available in most of the general purpose commercial software and OpenFOAM:**VOF Model**: it is a surface-tracking technique designed for two or more immiscible fluids where the position of the interface between the fluids is of interest. In this model, a single set of momentum equations is shared by the fluids, and the volume fraction of each of the fluids in each computational cell is tracked throughout the domain. Example applications of VF are filling and emptying of tanks or bottles, modeling of liquid splashing...**Mixture Model**: the phases are treated as interpenetrating continua and solves momentum equation for the mixture and prescribed relative velocities to describe the dispersed phases (but it can also be used without relative velocities for the dispersed phases to model homogeneous multiphase flow). It is a good substitute for the full Eulerian multiphase model (it can perform a full multiphase simulation while solving a smaller number of variables than the Eulerian approach and it is less computationally expensive compared to the Eulerian approach. In this case the momentum, continuity and energy equations for the mixture, the volume fraction equations for the secondary phases and algebraic expressions for the relative velocities are solved simultaneously. The essential approximation is the local equilibrium assumption which states that the particles are accelerated instantaneously to the terminal velocity. An algebraic formulation is used for the slip velocity which is based on the assumption of reaching to a local equilibrium between the phases over a short spatial length scale.**Eulerian Model**: the phases are treated as interpenetrating continua and a set of momentum and continuity equations for each phase are solved. Then the coupling is achieved through the pressure and interphase exchange coefficients. Application includes simulations of fluidized bed, mixing of immiscible fluids...

ANSYS FLUENT provide a model called "Dense Discrete Phase Model - DDPM" which is a hybrid Euler-Euler and Euler-Lagrange approach. Excerpts from user's manual: "The discrete phase formulation used by ANSYS FLUENT contains the assumption that the second phase is sufficiently dilute that particle-particle interactions and the effects of the particle volume fraction on the gas phase are negligible. In practice, these issues imply that the discrete phase must be present at a fairly low volume fraction, usually less than 10–12%. Note that the mass loading of the discrete phase may greatly exceed 10–12%:"

Phase-coupling mechanisms strongly influences the behavior of the continuous and dispersed phase. There are 3 different types of couplings present in particle-laden fluid flows.- One-way coupling or uncoupled approach: fluid → particles - this is appropriate only with very dilute concentration (< 0.01% volume fraction) of particles and has no significant effect on turbulence. The flow field is calculated assuming no presence of particle - fixed continuous phase flow field (that is before the particles is injected into the flow) and tracked as they injected into the flow. The particles does not interact with any other particles during its track throughout the flow domain.
- Two-way coupling: fluid ↔ particles - this coupling becomes important when the volume fraction of particles is in the range 0.01% - 10% and affects both dissipation and production of TKE. The flow of fluid is necessarily solved along with the movement for Lagrangian particles. This is enabled in ANSYS FLUENT by switching on "Interaction with Continuous Phase" option in the Discrete Phase Model dialog box. To control the frequency at which the particles are tracked and the DPM sources are updated, "Number of Continuous Phase Iterations per DPM Iteration" option exists. Option "Update DPM Sources Every Flow Iteration" is available for unsteady simulations.
- Four-way coupling: fluid ↔ particles + particle collisions: the particle - particle interaction becomes important if volume fraction of particles is > 10%. Note that the mass fraction can be still higher due to large difference in the densities of the solid and gas / liquid.

**Bubbly Flow**: it represents a flow of discrete gaseous or fluid bubbles in a continuous phase.

Gravity, buoyancy, interfacial tension, pipe diameter, friction and pressure define the shape of a flow. The various spatial shapes the flow takes in two- or three-dimensions are often referred to as *flow pattern*. There are many types of flow patterns that could exist in two-phase flow depending on a specific set of flow parameters including diameter and/or pipe inclination. The various flow regimes based on fraction of gas phase in horizontal and vertical pipes are described in following pictures.

There is no unique and uniform procedure to describe and classify flow patterns in two-phase mixtures. Usually flow pattern maps (such Baker's map, Taitel and Duckler map) are used to identify the flow regimes. A flow pattern worth mentioning is "slug flow". Slug literally means 'strike' or 'thump'. In this type of flow, wave of liquids hit the upper section of the pipe with a higher velocity than the average liquid velocity. Thus, pressure fluctuations are a common in such type of flows.

**Bubble Regime**: In this type of flow regime, there is a distribution of secondary phase bubbles throughout the continuous liquid phase. The bubbles may vary widely in size and shape but they are typically nearly spherical and are much smaller than the diameter of the tube itself. The average bubble size increases with increase in the gas flow rate.

**Slug Regime**: Whennthe gas flow rate is increased beyond a certain value, many bubbles collide and coalesce to produce slugs of gas or to form larger bubbles known as slug flow. These bubbles are also known as Taylor bubbles. The gas slugs have spherical noses along the direction of flow and occupy almost the entire cross section of the tube, being separated from the wall by a thin liquid film. [19]. Between slugs of gas there are slugs of
liquid in which there may be small bubbles entrained in the wakes of the gas slugs.

**Churn Regime**: When the velocity of the flow in increased further, the structure of the flow becomes unstable with fluid traveling up and down in an oscillatory and chaotic type but with a net upward flow. The slug flow pattern is destroyed and over most of the cross section there is a churning motion of irregularly shaped portions of gas and liquid.

**Anular Regime**: Further increase in the gas flow rate causes separation of the phases where the liquid flows mainly on the wall of the tube and the gas in the core area. In the annular flow regime the entrained droplets do not coalesce to form larger drops.

**Wispy-Anular Regime**: When the liquid flow rate is increased further, the volume fraction of liquid increases in the gas core where the entrained liquid is present as relatively large drops and the liquid film contains gas bubbles.

Terminologies associated with two-phase (TP) flows are described here.

**Total Mass Flow Rate**, m_{TP}[kg/s]: it is defined as the sum of the mass flow rate of the liquid phase m_{L}and the gas phase m_{G}.**Total Mass Flux**, G_{TP}[kg/m^{2}-s]: it is defined as the sum of the mass flux of the liquid phase G_{L}and the gas phase G_{G}.**Flow Quality**, x [%]: Flow quality is defined as the ratio of gas phase mass flow rate to the total mass flow rate, that is x = m_{G}/ m_{TP}.**Superficial Velocity**, U [m/s]: 'Superficial' velocity is derived based on total cross-section of the pipe even though actual flow may occur only through fractional area of the pipe. Thus, U_{SUP-G}= G_{G}/ ρ_{G}/ A and U_{SUP-L}= G_{L}/ ρ_{L}/ A**Slip Ratio**, S or σ [%]: It is defined as the ratio of the average 'superficial' velocity of the gas phase to the average 'superficial' velocity of the liquid phase. S = (U_{G}/U_{L}). When the slip ratio = 1, both liquid and vapour (gas) phase move at same speed. This assumption leads to a two phase model known as*homogeneous or zero-slip model*.**Void Fraction or Volume Fraction**, α [%]: Void fraction is defined as the ratio of the cross-sectional area occupied by the gas to the total cross-sectional area of the pipe. Since this ratio will vary along the length or flow direction, an integral or sum results in a ratio that gives the volume of space the gas phase occupies in two-phase flow in a pipe. Thus, for a*homogeneous model*:**Volumetric Quality**[%]: The volumetric quality is the ratio of the volumetric flux of a phase to the total volumetric flux.**Mass Quality**,*x*[%]: It is the ratio of the mass flux of a phase 'i' to the total mass flux of all the phases. This is also known as "flow quality" or "dryness fraction" in case of liquid-gas mixtures.**Drift Velocity**, U_{i}[m/s]: The drift velocity of a component is defined as the velocity of that phase in a frame of reference moving at a velocity equal to the total volumetric flux.**Mixture Density**: ρ_{TP}= α × ρ_{G}+ (1 - α) × ρ_{L}**Froude Number**: A measure of wavinesss of the liquid surface --
**Mixture Viscosity**: There are many definitions of mixture viscosity used by various researched to fit the test data.

Nomenclature as per OpenFOAM

**phi [φ]**: generic phase variable, mixture variable in "mixture models"**alpha [α]**: volume fraction of a phase, α = 1 for mixture models**rho**: density of i_{i}[ρ_{i}]^{th}phase**p_rgh**: Modified pressure p^{*}= p - ρ**g**.**x**obtained by removing hydrostatic pressure component from static pressure P = p/ρ**Dispersed phase**: phase with lower volume fraction**Carrier phase**: phase with higher volume fraction**Particulate loading**: The particulate loading is defined as the mass fraction ratio of the dispersed phase to that of the carrier phase

There are two ways of modeling the two-phase friction multiplier.

- The first one is assuming all the flow to be as one out of the two phases present such as all flow as liquid or all flow as gas. The implication here is to use the total mass flux (the sum of the mass fluxes for each phase) instead of the mass flow for each phase. Subscripts 'LO' and GO' indicate liquid only and gas only respectively.
- The second method is to assume as if only one of the phases exist and use the respective mass flux only while calculating the Reynolds number. Therefore in this case, only the respective mass flux is used to calculate the Reynolds number.

Usually liquid two-phase friction multiplier is preferred because the density of liquids do not vary much (and practically remains constant with changes in pressure) in most of the applications as compared to the gas density. The concept of two-phase friction multiplier was introduced by Martinelli and co-researcher who later along with Nelson introduced the concept of using parameter φ

Lockhart and Martinelli also introduced a dimensionless parameter X defined as follows. The two phase friction multiplier φ_{L} is a function of X as per the equation shown. The constants as per Chisholm are also tabulated.

The LM-parameter 'X' relates the single phase pressure drop each for liquid and gas phase as if each fluid is flowing alone in the pipe and therefore respective mass fluxes should be used.

Flow mechanism | Value of C | |

Liquid | Gas | |

Viscous (Laminar) | Viscous (Laminar) | 5 |

Turbulent | Viscous (Laminar) | 10 |

Viscous (Laminar) | Turbulent | 12 |

Turbulent | Turbulent | 20 |

- Inputs: mass flow rates of each phase or mass flow rate of one phase and volume fraction of the other phase, pipe diameter, operating mean pressure and temperature
- Calculate the Reynolds number for each phase assuming as if each fluid is flowing alone in the pipe. Output: Re
_{L}and Re_{G}. Note that the turbulent flows for two-phase flows in pipe starts at Re = 1000. - After viscous-turbulent classification for each phase, calculate dimensionless parameter X that is calculate either of [X
_{TT}X_{TV}X_{VT}X_{VV}].

One of the important effect of presence of gas phase (such as air) in water is decrease in speed of sound in the liquid phase. This reduction in speed of sound will cause shock waves to occur at lower fluid velocities.

This page summarizes the multi-phase cases supplied with OpenFOAM 1606+.

Some of the resource from the web are listed below.- This web page from CHALMERS university is a comprehensive list of article, research report and presentations on OpenFOAM
- This is a wiki page which is an excellent attempt to categorize the documents with ease of search.
- Since this page is intended for multiphase phenomena only, some of the PDF files I read and used to get insight into the available utilities in OpenFOAM are linked below. Note that the documents are still owned by respective authors and is produced here for reference only.

Thus, if both or all the phases are to be modelled as continuous phases, Eulerian approach is used. When a discrete phase (spatially not continuous) is to be modeled, a Lagrangian frame of reference is used in which spherical particles of pre-defined size distribution is dispersed in the continuous phase (the spherical particles may represent parcels of droplets or bubbles). The fluid phase is modeled as a continuum where time-averaged Navier-Stokes equations are solved to get flow field while the discrete phase is solved by tracking a large number of particles (parcels, bubbles, or droplets) through this calculated flow field. Thus, a Lagrangain approach includes and requires:

- calculation of discrete phase trajectory for both steady and unsteady flows
- estimation of effects of turbulence on dispersion of particles due to vortices and eddies present in the continuous phase
- account for heating or cooling of the discrete phase including break-up of droplets in sprays, vaporization and boiling of such droplets
- the volume fraction of discrete phase should be < 10% even though mass fraction can be higher due to higher density of solids as compared to liquids. Thus, this method will not be appropriate for fluidized bed where volume fraction of discrete phase is > 50%. Note that twoPhaseEulerFoam should be used in such applications. The Euler-Lagrangian solver coalChemistryFoam is not related to fluidized beds.

- Vigorous stirring or agitating two or more immiscible liquids results in the dispersion of one phase in the other in the form of small droplets whose size and shape depend on the equipment, the material properties such as density and surface tension and the operating conditions.
- The mixing of two immiscible liquids is called emulsification where a binding agent called emulsifier holds the two phase together and dispersed. Icecream, milk, mayonnaise, sauces are some of the examples of emulsion.
- Prediction of drop size distributions in turbulent liquid-liquid dispersions in static mixers thus becomes one of the most important output of any test set-up or numerical simulation methods.
- Similarly, any phenomena dealing with droplets require a mathematical model to capture break-up, aggregation and coalesce phenomena of the droplets. One such approach is Population Balance Equations (PBE) - particle size distribution by means of a transport equation, similar to k and ε equations.
- Since each phase is a continuum, Euler-Euler multiphase models are used to simulation emulsification process.

**DPMFoam**: Discrete Phase Model - This is another multi-phase solver which includes the effect of the discrete phase particulate volume fraction on the continuous phase. This utility is recommended for dense particle flow simulation. Though there is no strict and standard definition of 'dense' particle-laden flow, a volume fraction of 10% or higher is usually considered 'dense'. The solver uses existing functionality for particle clouds and their collisions, which directly resolves particle-particle interactions. Official description is "Transient solver for the coupled transport of a single __kinematic particle cloud__ including the effect of the volume fraction of particles on the continuous phase".

- Divide the minimum and maximum diameter into discrete intervals: d
_{0}, d_{1}, d_{2}...d_{N}. But how will one know minimum and maximum diameters a-priori? It is an iterative process and one need not know all information well in advance. - From sieve analysis, estimate the mass fractions of particles below d
_{i}where i = 1, 2, 3 ...N. - Plot the graph: M
_{F}(d) vs. d(i). - Plot a horizontal line which crosses vertical axis at 1/e = 0.3679
- The intersection of these two lines is the mean diameter, d
_{M}. - For each discrete interval, calculate spread parameter n
_{i}= ln[0 - ln(M_{F}[d_{i}])] / [ln(d_{i}) - ln(d_{M})] i = 1, 2, 3 ...N. - Calculate the average of n
_{i}, which is the spread parameter to be input in most of the CFD simulation software such as ANSYS FLUENT.

- Reports>Discrete Phase>Sample>Set Up
- Pick appropriate boundary say "inlet" or "outlet", injection setting, then "Compute". Make sure that the chosen boundaries represents all particles that flow into the system or flow out of the system.
- This action will write to disk a file called "inlet.dpm" or "outlet.dpm" depending upon the boundary selected which will record the profile of particles at that boundary.
- To plot histogram, use GUI option: Reports > Discrete Phase > Histogram > Set Up. Select "Read" then pick the file just saved (*.dpm). Select appropriate entry under "Sample", "Variable" and "Weight" tabs. Select "Plot".

Another aspect of a DPM simulation is modeling of "particle-wall interaction". The particle may either reflect after hitting the wall or get captured by the wall (stick to it). To check whether particle - wall collisions is likely to occur or not, the Stokes number gives an indication whether the particles will follow the flow or hit the wall. The Stokes number is defined as the ratio of particle response time (a measure of how fast the particles react to a change in fluid velocity) to a characteristic timescale of the flow (how fast changes in flow occur). The characteristic time scale of the fluid is often taken as the time constant for turbulence defined as the ratio between turbulent kinetic energy (k) and turbulent dissipation rate (ε).

- If the particle response time is << fluid timescale, the Stokes number is << 1, the particles will react instantly to any change in the fluid velocity and hence follow the flow closely.
- If the particle response time is >> the fluid timescale, the Stokes number is >> 1, the particles will be unaffected by changes in the flow.

In ANSYS FLUENT, particle-particle interactions is included in Discrete Element Model using

The term 'cloud' in OpenFOAM represents the overall presence of all particles, whether they're active or not. Since, this is a transient solver, it is based on PIMPLE algorithm. Turbulence models available in this utility are [a] laminar, [b] k-ε RANS and [c] LES as shown in the header file of the source code.

- Gravity - the well-known force present everywhere!
- Buoyancy - force due to density difference of the particle and continuous phase.
- Pressure gradient - the force due to pressure difference along the direction of motion of the particle.
- Intertia: The acceleration or deceleration of the particle in a fluid requires also an accelerating or decelerating of a fluid surrounding the particle (important for liquid-particle flows).
- Added mass (m
_{a}): The term refers to the additional force (F_{A}) required to accelerate the solid body through a fluid. As the body and the fluid cannot occupy the same volume simultaneously, a force is required to displace the fluid. Though this force can be neglected in gas flow, the force can be significant in liquids due to the high density of liquids. By definition, the added mass force is in phase with the acceleration 'a' (no time lag) which can be expressed in terms of a virtual mass. This will lead to Newton’s 2nd law expressed as F_{A}= (m_{P}+ m_{A}) × a. - Slip-shear lift force: particles moving in a shear layer experience a transverse lift force due to the nonuniform relative velocity over the particle and the resulting nonuniform pressure distribution
- Slip-rotation lift force: particles, which are freely rotating in a flow, may also experience a lift force due to their rotation (Magnus force and/or Saffman force)
- Thermophoretic force: a thermal force moves fine particles in the direction of negative temperature gradients (important for gas-particle flows)
- The solidParticleCloud class in OpenFOAM is a class that calculates the movement of particles. In ANSYS FLUENT, time integration of the particle trajectory
equations described below is controlled by following two parameters:
**Maximum number of time steps**: maximum number of time steps (default = 500) used to compute a single particle trajectory via integration of particle Force Balance Equation, it is used to abort trajectory calculations when the particle never exits the flow domain with trajectory fate reported as 'incomplete'. Simulation where trajectories are reported as incomplete within the domain and the particles are not recirculating indefinitely, one need to increase the maximum number of steps (up to a limit of 10^{9}) to get more trajectories.**Length scale/step length factor**: set the time step for integration within each control volume, it is ∝ to the integration time step and is equivalent to the distance that the particle will travel before its motion equations are solved again and its trajectory is updated. A smaller value for the Length Scale increases the accuracy of the trajectory.

Here subscript 'p' denotes 'particle'. Various empirical correlations of drag laws for viscous forces over solid particles are:

- First breakup stage: Deformation and flattening occurs in the range Weber number We ≤ 12.
- Second breakup stage: Bag breakup, Shear breakup, Stretching and thinning breakup, Catastrophic breakup.
- Bag breakup: 12 ≤ We ≤ 100
- Shear breakup: We < 80
- Stretching and thinning breakup: 100 ≤ We ≤ 350
- Catastrophic breakup: We > 350

**MPPICFoam (MultiPhase Particle-In-Cell method):** This is a "Lagrangian solver" having LPT (Lagrangian Particle Tracking) capabilities and can be used for modelling particles in continuum. This method simulates solid phase as parcels and is used to represent **collisions without resolving particle-particle interactions**. *This solver is identical to DPMFoam, but without the collisions between particles.*. Quote from a post by Bruno Santos on cfd-online.com: ||The solvers DPMFoam and MPPICFoam are virtually identical, except that the first one uses "basicKinematicCollidingCloud" as the base cloud type and the second one uses "basicKinematicMPPICCloud"||

The particles are assumed to be rigid, spherical and are thus described by diameter, density, coefficient of restitution (rebound properties) and coefficient of friction (tangential drag during collision). Hence, collisions between particles are modeled using keywords identifying properties of spring, friction slider and dash-pot in appropriate dictionaries.

There are two time-steps involved: fluid flow time steps (the time-steps used for solution of continuous or carrier phase) and particle tracking time steps which decides the time step for particle injection. In ANSYS FLUENT one can performNote: in ANSYS FLUENT, in steady-state discrete phase modeling, particles do not interact with each other and are tracked one at a time in the domain.

In addition to the methods outlined earlier to post-process particle tracks, the "Block Extract" features can be directly applied on the kinematicCloud to extract the particles as shown below. This can be done at each time step or the final time step of the simulation.

$FOAM_UTILITIES/postProcessing/lagrangian/particleTracks/particleTrackProperties

Both the particleTracks and foamToVTK utility will create a folder named VTK in the case directory which will have further sub-level folders. The folder VTK/lagrangian/kinematicCloud will contain a file kinematicCloud_TTT.vtk files where TTT is the time step. For particle tracking visualization, one needs to open this file. Then, to display the particles the user must filter the Lagrangian field with the Glyph filter, subsequently the scalar option should be selected in the scale mode window along with the spheres as glyphs where Gyph type options [Sphere, arrow, cone, box...] are available.

Glyph settings to plot particles as sphere is shown below

The particles coloured by velocity magnitude plotted using VTK files are shown below.

**Lagrangian >> simpleReactingParcelFoam >> verticalChannel **: a steady state Lagrangian - Eulerian solver for chemical reaction, combustion and particle clouds.

Two-phase flows are often broadly categorised by the physical states of the constituent components and by the topology of the interfaces. Thus, a two-phase flow can be classified as gas-solid, gas-liquid, solid-liquid and liquid-liquid in the case of two immiscible liquids . Similarly, a flow can be broadly classified topologically as separated, dispersed or transitional.

The following video is an attempt to model air entrainment using multiphase flow. In the left video, you may notice how spherical bubbles are formed due air entrained by water stream entering into the bottle. The interface of the air bubble and water is sharp. This feature is not as prominent in the simulation primarily due to coarse mesh. Capturing a sharp interface between gas and liquid will require a very fine mesh. Some improvements planned are:

- Make the domain shape and size identical: as of now they are in 2:1 ratio to keep the number of mesh counts low.
- Match the boundary conditions such as velocity and its profile at inlet, turbulence parameters at inlet.

**multiPhase >> interFoam >> ras >> angledDuct** - Flow of water in an empty angled duct: immiscible two phase flow - there are 3 three implementation with LAMINAR, LES and RAS turbulence as tutorial cases. One of the tutorial with RAS implementation is shown below where water enters into the inlet and fills the duct as it moves towards the outlet.

Volume fraction at t = 0:

The animation of change in water volume fraction with time can be downloaded from here.

**multiPhase >> interFoam >> ras >> DTCHull** - Flow over a ship

Volume fraction of water at t = 0:

Geometry and Volume fraction of water at t = 0:

Specification of miscible and immiscible phases:

Volume fraction of miscible phases after 2 [s]:

- It is not possible to raise the temperature of a liquid uniformly where as uniform change in pressure in a liquid can be easily achieved just by controlling the flow passage.
- Cavitation always results in self-destruction downstream the flow, causing large pressure fluctuations. Though vapour formation are also self-destructing as the vapour bubbles move away from the cause, "the surface heat source".
- Bubble formation involves knowledge of Heat Transfer and boundary layer behaviour of the liquid. understanding the Cavitation phenomena does not need any such information.
- Cavitation is almost always detrimental to the surfaces where bubbles collapse. Bubble generation and extinction phenomena in boiling is not so detrimental to the enclosing surfaces.
- Typical location of cavitation is low-pressure (suction side) of the centrifugal pumps. A pump is said to get incipient cavitation if the pressure head generated by the pump reduces by 10% of a "non-cavitating" performance.

Cavitation modeling in ANSYS FLUNET

Basic Mesh: Level-0

Mesh with level-3 refinement near throat

Close-up view of final mesh near throat

This is an Eulerian-Eulerian solver for two (including compressible) fluid phases where one phase is continuous say water and the other phase is dispersed say gas bubbles or solid particles. It may or may not involve heat transfer. Fluidised bed simulations can be performed using this solver. Note that the flow of solids (the particle bed is bubbling) is being modeled here though it is gas assisted and not the granular flow of solid by its own weight.

For two phase flows involving fluids, the thermophysicalProperties are specified by adding suffix after the dictionary 'thermophysicalProperties' such as thermophysicalProperties.air, thermophysicalProperties.water. Special variables for this solver and few settings are described below.- Theta.particles: Granular temperature of solids phase
- alpha.air: Volume fraction of air (fluid) phase
- alpha.particles: Volume fraction of solid phase
- Note that there is a minimum inlet velocity required to ensure fluidization - that is to move the fluid particles from the bed. Hence, chosen inlet velocity should be higher than or equal to minimum fluidization velocity.
- Gravity should be active.

Three or more phases, interface capturing capabilities configured to work with LES and not RANS. Phases can be segregated or dispersed. As per source code: "Solver for a system of many compressible fluid phases including heat-transfer". The application to 2D geometry of a mixing vessel is shown below. This is based on Multiple Reference Frame (MRF) method for sliding interfaces - set by dictionary constant/MRFProperties.

- chemistryProperties - required to include chemical reactions when 'chemistry' is switched on (for example refer to tutorial case reactingTwoPhaseEulerFoam >> RAS >> bubbleColumnEvaporatingReacting),
- environmentalProperties - specifies gravity,
- combustionProperties - to activate combustion models such as PaSR / XiFoam,
- thermophysicalProperties - specifies type of mixtures and its properties, gas phase reaction scheme, presence of inert species,
- phaseProperties - this dictionary file is specific to this solver and is used to describe interaction between the phases,
- MRFProperties - in case geometry is dealing with rotating domains such as mixer vessel.

As in any VOF simulation with mesh non-optimal mesh refinement, the interface between air and water is not as sharp as observed in real-life examples (refer to the bottle filling animation above). The variation of volume fraction of water (alpha) with time is demonstrated in the following animation. Note how water is raised till upper wall. Also note symmetry during initial stage which gets disturbed once water hits the upper wall and starts falling down. During later stage of simulation, there are zone where the volume fraction of water is in the range 0.5 which is not realistic as water and air are assumed to immiscible and the volume fracion has to be either 0 or 1.

Change are required in constant/turbulenceProperties file, 0/ directory, system/fvScheme and system/fvSolution files.

LAMINAR | RANS |

constant/turbulenceProperties file | |

simulationType laminar; | simulationType RAS; RAS { RASModel kEpsilon; turbulence on; printCoeffs on; } |

0/ folder | |

* | Add following file and modify boundary names: epsilon k alphat nut nuTilda |

system/fvScheme | |

divSchemes { div(phi,alpha) Gauss vanLeer; div(phirb,alpha) Gauss linear; div(rhoPhi,U) Gauss upwind; div(rhoPhi,T) Gauss upwind; div(rhoPhi,K) Gauss upwind; div(phi,p) Gauss upwind; div(((rho*nuEff)*dev2(T(grad(U))))) Gauss linear; } |
divSchemes { div(phi,alpha) Gauss vanLeer; div(phirb,alpha) Gauss linear; div(rhoPhi,U) Gauss upwind; div(rhoPhi,T) Gauss upwind; div(rhoPhi,K) Gauss upwind; div(phi,p) Gauss upwind; div(rhoPhi,k) Gauss upwind; div(rhoPhi,epsilon) Gauss upwind; div(((rho*nuEff)*dev2(T(grad(U))))) Gauss linear; } |

system/fvSolution | |

"(T|B).*" { solver smoothSolver; smoother symGaussSeidel; tolerance 1e-08; relTol 0; } |
"(T|k|epsilon|nuTilda|omega|B).*" {solver smoothSolver; smoother symGaussSeidel; tolerance 1e-08; relTol 0; } |

A complete list of tutorial cases related to Lagrangian Particle Tracking (LPT) and multiphase flow is summarized in following tables.

lagrangian | coalChemistryFoam | simplifiedSiwek | |

DPMFoam | Goldschmidt | ||

icoUncoupledKinematicParcelDyMFoam | mixerVesselAMI2D | ||

icoUncoupledKinematicParcelFoam | hopperEmptying | ||

hopperInitialState | |||

MPPICFoam | column | ||

cyclone | |||

Goldschmidt | |||

injectionChannel | |||

reactingParcelFilmFoam | cylinder | ||

hotBoxes | |||

rivuletPanel | |||

splashPanel | |||

reactingParcelFoam | counterFlowFlame2DLTS | ||

filter | |||

parcelInBox | |||

verticalChannel | |||

verticalChannelLTS | |||

simpleReactingParcelFoam | verticalChannel | ||

sprayFoam | aachenBomb | ||

multiphase | cavitatingFoam | LES | throttle |

throttle3D | |||

RAS | throttle | ||

compressibleInterDyMFoam | RAS | sloshingTank2D | |

compressibleInterFoam | laminar | depthCharge2D | |

depthCharge3D | |||

compressibleMultiphaseInterFoam | laminar | damBreak4phase | |

driftFluxFoam | RAS | dahl | |

mixerVessel2D | |||

tank3D | |||

interDyMFoam | laminar | damBreakWithObstacle | |

sloshingCylinder | |||

sloshingTank2D | |||

sloshingTank2D3DoF | |||

sloshingTank3D | |||

sloshingTank3D3DoF | |||

sloshingTank3D6DoF | |||

testTubeMixer | |||

RAS | DTCHull | ||

DTCHullWave | |||

floatingObject | |||

mixerVesselAMI | |||

multiphase | interFoam | laminar | capillaryRise |

damBreak | |||

mixerVessel2D | |||

wave | |||

LES | nozzleFlow2D | ||

RAS | angledDuct | ||

damBreak | |||

damBreakPorousBaffle | |||

DTCHull | |||

waterChannel | |||

weirOverflow | |||

damBreakRAS | |||

interMixingFoam | laminar | damBreak | |

interPhaseChangeDyMFoam | propeller | ||

interPhaseChangeFoam | cavitatingBullet | ||

multiphaseEulerFoam | bubbleColumn | ||

damBreak4phase | |||

damBreak4phaseFine | |||

mixerVessel2D | |||

multiphaseInterDyMFoam | laminar | mixerVesselAMI2D | |

multiphaseInterFoam | laminar | damBreak4phase | |

damBreak4phaseFine | |||

mixerVessel2D | |||

potentialFreeSurfaceDyMFoam | oscillatingBox | ||

potentialFreeSurfaceFoam | oscillatingBox | ||

reactingMultiphaseEulerFoam | laminar | bubbleColumn | |

mixerVessel2D | |||

multiphase | reactingTwoPhaseEulerFoam | laminar | bubbleColumn |

bubbleColumnEvaporating | |||

bubbleColumnEvaporatingDissolving | |||

bubbleColumnIATE | |||

fluidisedBed | |||

injection | |||

mixerVessel2D | |||

steamInjection | |||

LES | bubbleColumn | ||

RAS | bubbleColumn | ||

bubbleColumnEvaporatingReacting | |||

fluidisedBed | |||

LBend | |||

wallBoiling | |||

wallBoilingIATE | |||

twoLiquidMixingFoam | lockExchange | ||

twoPhaseEulerFoam | laminar | bubbleColumn | |

bubbleColumnIATE | |||

fluidisedBed | |||

injection | |||

mixerVessel2D | |||

LES | bubbleColumn | ||

RAS | bubbleColumn | ||

fluidisedBed |

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