#### Abstract

The chute aerator of a spillway is a structure in such a sense that air is, in the intense emulsification, entrained into the high-velocity water flow. Correctly predicting the air entrainment and two-phase flow pattern at the aerator would contribute to reliable spillway operation. Based on experimental data, 2D numerical simulations are preformed to predict streamwise air concentrations in the aerated flow, in which a two-fluid model is used. Depending on the air bubble size, relatively good agreement is seen with the experiments in the air cavity zone. The simulations give rise to higher air concentration downstream of the cavity, which is presumably due to underestimation of the interfacial forces in the two-fluid model.

#### 1. Introduction

Spillways are important hydraulic structures for dam safety. If the water flow velocity exceeds, for example, 20 m/s and the cavitation index drops below a certain limit, damage may occur due to cavitation in the chute bottom, which affects the safety of the spillway [1]. Hence, protecting spillways from cavitation damage is a primary goal of engineering design. The use of aerators is probably the only economic countermeasure for the purpose. An aerator entrains air into high-speed flow, alleviates the negative pressure near the chute bottom, and thus avoids the risk of cavitation.

Driven by engineering practice, researchers have investigated aerators both in the laboratory and through prototype observations [2–8]. Kramer and Hager [9] examined, through experiments, flow velocity, air concentration, and air bubble size distributions; they concluded that the bubble rise velocity in chute flows depends on the Froude number. Pfister and Hager [7, 8] analyzed the effects of geometrical parameters on streamwise distributions of air concentration downstream of aerators.

For many years, physical models have been the major tool to study the characteristics of the aerated flow. Computational Fluid Dynamics (CFD) has emerged as an important alternative in multiphase flow modelling. Both methods are undoubtedly complementary to each other. With CFD, it is possible to obtain, in detail, air-water flow fields of the aerated flow so as to understand the effects of governing parameters necessary for a project in question.

The Volume of Fluid (VOF) method is an interface tracking scheme addressing the topological changes of the air-water interface in free-surface flows [10]. To describe its hydraulic performance, the VOF model is often used to simulate the aerated flow of a spillway [11–14].

In an air-water flow, exchange behaviors between the dispersed air phase and continuous water phase affect forces between the phases. Hence, the correct modelling of forces and turbulence is of prime importance for capturing the physics. The two-fluid model differs from the VOF model in such a way that the momentum and continuity equations are solved for each phase. Furthermore, the interaction force between phases, the drag force, the virtual mass force, and the turbulent dispersion force are modelled in the momentum equations.

The two-fluid model was used to simulate the complex hydrodynamics of air-water flow in industrial applications [15–17]. Zhang [18] carried out three-dimensional (3D) modelling with the model. He focused on evaluations of such parameters as the diameter of air bubble, wall function, and interphase exchange models. Zhang et al. [19] performed two-dimensional (2D) simulations using the model, in which the turbulence dispersion force was included in the momentum equations. They concluded that the inclusion of the turbulence dispersion force gave better results of air concentration in the flow, which agreed well with the experimental data [20].

Physical model tests of an aerator were performed at the Laboratory of Hydraulics, Hydrology, and Glaciology (VAW), ETH, Zurich [7, 8]. Based on its configurations, CFD modelling is performed using the two-fluid model. The simulations, time dependent and in 2D, examine the transport of air in the flow. Included in the study are evaluations of air cavity length, air-entrainment rate, and air concentration distributions. The effect of bubble diameter, a dominating factor in the two-fluid model, is also considered on the momentum exchange between air and water. With regard to the experimental results, the purpose of the study is to evaluate the suitability of the two-fluid model in solution of the two-phase flow at the aerator and to learn about the air-water features of the flow.

#### 2. Physical Model

The experimental set of data was obtained from a hydraulic model test of an aerator conducted in a flume 0.3 m wide and 6.0 m long at VAW, ETH, Zurich (Figure 1) [7]. One aerator configuration, without offset but with a deflector, is selected for the numerical modelling (Figure 2). The chute bottom angle is set herein to = 30° with the horizontal plane; the defector angle is = 8.13° with the chute bottom. The chute length upstream of the aerator is 2.0 m. The height of defector () is 0.0133 m. The water depth of the approach flow is = 0.084 m. The approach flow Froude number is defined as = = 7.52, where is the mean approach flow velocity and is the acceleration of gravity.

The air supply to the air cavity below the jet occurs through a lateral duct on each side of the chute; its mass flux is measured with a thermoelectric air flow anemometer. To measure the spatial distribution of air concentration (denoted as ), a dual-tip fiber-optical probe is adopted with a sampling frequency of 1 MHz. Its measurement is based on different refraction indices between the sapphire tip and the surrounding phase. If the tips are in the air phase, the light on the tips is reflected and detected. Otherwise, it is “lost” in the water phase. The value at each point is obtained from a period of typically 20 s. The measurement points have a streamwise spacing of 0.2 m; the interval perpendicular to the chute bottom is 2 to 5 mm.

For the approach flow, the Weber and Reynolds number is defined as We = and Re = , where is the surface tension and is the kinematic water viscosity. If they exceed the minimum values, that is, We = 110 and Re = 1.7 10^{5}, the effects of surface tension and viscous force are negligible [21–25]. In the tests, We = 236 and Re = 1.3 10^{6}, both exceeding the limits.

#### 3. Numerical Model

A numerical model was set up to simulate the water-air flow at the aerator. The computations are based on the two-fluid model in ANASYS 15 [26–28].

##### 3.1. Two-Fluid Model

The two-fluid model is based on the Euler-Euler approach. Both separate and interacting phases are allowed to be modelled. In the model, the continuity and momentum equations are formulated for each phase.

The continuity equation for each phase iswhere subscript and , referring to the air and water phase, is the phase volume fraction, is the phase density, is the phase velocity, and is the time.

The momentum balance equation for each phase is where is the water pressure, is the shear stress, is the interphase force, and is the interfacial force between air and water phase.

depends on water-air friction, pressure, cohesion, and other effects and is written as a simple interaction term of the following form:where = = interphase momentum exchange coefficient between the water and the air phase.

consists of several independent forces:where is the drag force, is the lift force, is the virtual mass force, and is the turbulence dispersion force. In the two-fluid model, the air phase is assumed to form bubbles. The viscous stress creates bubble skin drag; the pressure distribution around the bubble creates form drag. The latter becomes significant when the relative bubble Reynolds number () increases. is written aswhere is the drag coefficient. is obtained fromwhere* D* is the bubble diameter. is based on the Schiller and Naumann model [29]:If bubbles accelerate relative to the water, virtual mass effects occur. is due to the inertia of the water mass encountered by the accelerating bubbles [30], defined asThe virtual mass effect is significant when the secondary-phase density is much smaller than the primary-phase density.

acts as a turbulent diffusion in dispersed flows and is based on de Bertodano [31]:where is the water turbulent kinetic energy per unit of mass and is the turbulence dispersion coefficient.

acts on air bubbles mainly due to velocity gradients in the water flow field. From Drew and Lahey [30], it is written aswhere is the lift coefficient.

##### 3.2. Grid, Boundary Conditions, and Grid Independence

The chute included in the simulations comprised 2.0 and 5.06 m upstream and downstream of the aerator. The upper boundary of the domain is parallel to the chute bottom and at a distance of 1.2 m from it. The height of the transversal groove is = 0.03 m; the duct width is = 0.06 m. The bottom of the duct is open to atmosphere, allowing air to be sucked into the jet cavity.

A quadrilateral mesh is generated in the Gambit software. The geometrical size and numerical grids are shown in Figure 3. The boundary conditions are defined in Figure 4. The upstream boundary consists of both water and air in height. A velocity boundary is set to the water phase below; a pressure inlet (the atmospheric pressure) is given to the air phase above the water. Both the top and the duct bottom are specified as pressure inlet; the downstream boundary is set as pressure outlet. The other boundaries are treated as wall.

**(a) Entire domain**

**(b) Local refinement at the aerator**

Simulations are performed in 2D and time dependently using the software Fluent in ANSYS 15. Zhang [18] compared the Standard and Realizable models for aerated flow. The results have shown that there are small differences between them. However, the Realizable* k** ε* model is more suitable to represent features of turbulent free-surface flow [32]. Hence, it is chosen in the simulations. The parameters chosen for use in the two-fluid model are summarized in Table 1.

To guarantee the numerical quality, a check of grid independence is necessary. Three quadrilateral grids are examined, with the number of cells being about 9900 (coarse), 33000 (medium), and 66000 (fine), respectively. The minimum cell size is 1 mm at the aerator. The variable refers to the position corresponding to = 0.9 in the upper edge of the nappe (Figure 2). For the grid independence check, the values are compared as a function of . The comparison for location = 0.211 m is shown in Figure 5. The results indicate that the medium size grid is sufficient to model the aerator flow.

#### 4. Results and Discussions

The flow field is usually divided into three zones, that is, approach flow zone, air cavity zone, and far-field zone (Figure 2). The latter two zones are divided by the reattachment point (R), defined as the intersection of = 0.9 with the chute bottom. The main issues of concern for modelling, either physical or numerical, include the air demand, cavity length, and air concentration in the cavity zone, at the end of the cavity and in the far field of the jet.

A coordinate system (, ) is defined. The -direction is on the chute bottom, while the -direction, perpendicular to the chute bottom, is on the downstream face of the deflector (Figure 2). Several cross sections, denoted as S1–S7 and all perpendicular to the chute bottom, are used to describe the flow (Table 2). The distance between two neighboring locations is 0.2 m.

##### 4.1. Selection of Bubble Diameter

The air phase exists presumptively in the form of bubbles. The air-water exchange behavior is a dominating issue in modelling aerator flow and is influenced by the bubble dimensions. In the two-fluid model, this behavior is described by :where is the interfacial area, * = *, and is the air kinematic viscosity.

Chanson and Toombes [33] carried out an experiment in an open channel to study air-water flow properties. They indicated that the probability of air bubble chord sizes between 0 and 4 mm in the flow region is more than 65%. Takahashi et al. [34] conducted a study of interactions between free-surface and cavity recirculation in a stepped channel. The results showed that the majority of bubble diameters is below 5 mm. Chen et al. [35] studied bubble diameter distributions in an aerated flow by means of physical model tests. They showed that the bubble sizes are commonly in the range of 0.5–3 mm in the vicinity of the chute bottom and 3–5 mm close to the free surface.

In the VAW laboratory tests, no systematical measurements were made of the air bubble sizes. However, fragmentary tests demonstrated that they were usually below 4 mm. With reference to the abovementioned observations, = 1, 2, 3, and 4 mm are selected to examine their effects on the flow characteristics.

##### 4.2. Cavity Length and Air Demand

When the water flows over the aerator, then the deflector separates the flow from the bottom and a cavity region beneath the nappe of the jet is generated, in which air is sucked in. The cavity length and the air supply are two characteristic parameters of interest. Due to the high velocity and turbulence, a well-defined interface between the air and water does not exist for the lower nappe surface. The cavity length, denoted as* L* (m), refers to the distance from the aerator to the reattachment point on the chute bottom (Figure 2). To describe the air-entrainment capacity of an aerator, an air-entrainment coefficient () is defined as the ratio of air discharge (, m^{3}/s) to water flow discharge (, m^{3}/s).

Other conditions being given, the bubble diameter is a primary parameter in the two-fluid model. In literature review, limited information has been found of its effects on the cavity length and the air demand. Table 3 compares the averaged results of from the experiments and the numerical simulations. The simulated values are in relatively good agreement with the experimental one; the maximal difference is 5% for = 1 mm.

As the black-water core stretches to the end of the cavity, the air supply to the aerator is equal to the air entrained into the flow from the lower nappe surface. Table 4 shows the results corresponding to the different values. With the increase of , the value becomes smaller. = 1 mm gives the largest difference; = 4 mm is closer to the experimental result, with an error of 9%. All the simulations overestimate the air demand. is a parameter that does affect the air entrainment.

##### 4.3. Cavity-Zone Air Concentration

Air is entrained into the water by strong emulsification in the cavity zone, particularly at its end near the reattachment zone. If the aerator geometry is given, the state of air entrainment governs the air capacity of the aerator, which forms an initial condition for the streamwise transport of the air in the water. Figure 6 shows the distributions as a function of for the four locations S1, S2, S3, and S4 (Figure 4). Each diagram compares the distributions between the experiments and the simulations. The values vary from 1 to 4 mm.

**(a) Cross section S1**

**(b) Cross section S2**

**(c) Cross section S3**

**(d) Cross section S4**

For the upper edge of the nappe, the four values lead to almost identical results at S1 and differ however from the experimental result; the range of the so-called black-water zone is underestimated. As the streamwise distance increases from the aerator, the simulated values corresponding to the larger diameters decrease and approach gradually the experimental ones. At S4, the result of = 4 mm is in good agreement with the experimental data.

For the lower edge of the nappe, the numerical and test results are more close to each other along the cavity. Some small differences are seen for = 1 mm in the beginning of the cavity (e.g., at S1) and = 4 mm towards downstream (e.g., at S3 and S4).

##### 4.4. Lower Edge Concentration Similarity

To further examine the air concentration of the lower nappe edge, a characteristic thickness, called the air-entrainment thickness , is usually used to describe its development [20, 36]. For a given cross section, it refers to the difference between = 30% and 60%; that is, . A normalized thickness, , is then defined as . For the four locations, Figure 7 compares the changes of the values as a function of .

**(a) Cross section S1**

**(b) Cross section S2**

**(c) Cross section S3**

**(d) Cross section S4**

Figure 8 is a plot of all the experimental values for the lower edge. The distributions are similar for different locations and can be assembled into the expression suggested by Hager [37]:where , , and are constants, = 1.04, = 0.16, and = 1.87.

##### 4.5. Cavity End

The air content at end of the cavity evolves from the air entrainment along the lower edge of the jet; at the same time, it reflects also the air contribution from the backflow upstream of the reattachment point and its interaction with the jet’s lower edge.

Section S5 is located at the end of the cavity. Figure 9 compares, along the whole cross section, the distributions between the experiments and the modelling. Figure 10 shows the similarity profile of , that is, the change of as a function of .

From the experiments, one can see that the black-water zone becomes small at S5 and is about to disappear downstream of it. The thickness of the black water is relatively well produced; its predicted position is however lower. Again, the high air concentration region close to the chute bottom edge is overestimated in the simulations.

##### 4.6. Far-Field Evolution

It is the aerated air bubbles close to the bottom that protect the chute bottom from cavitation damage. It is therefore of practical significance to examine the streamwise development downstream of the reattachment point . It provides information with respect to the effective length of the chute provided by the aerator in question.

Figure 11 shows the profiles at two typical cross sections (S6 and S7) in the far filed, that is, the change of with . The distributions behave in a similar manner for the examined range. For both the upper edge and lower boundary of the flow, is overestimated; all the simulations lead to a much larger value close to the chute bottom. The average value at each location is well reproduced.

**(a) Cross section S6**

**(b) Cross section S7**

##### 4.7. Discussions

As seen from (11), is a parameter that affects the diffusion between the air and water; the momentum exchange becomes more intense with augment in . In the simulations, is a constant value in the entire computational domain. In actual situations, it may vary in the different flow regions. In the approach flow, with the increase of the surface turbulence, air starts to be entrained from the free surface at a location upstream of the aerator. Compared with the flow in the cavity zone, the turbulence intensity in the flow is low [6]. As a result, the* C* distribution of the approach flow might still be overestimated even with the smallest diameter simulated ( mm).

Previous model tests showed that the roughness of the surface water increases along the cavity zone [9]. This implies that the exchange of momentum between the water and air becomes stronger; a larger bubble diameter should be used to describe the process. This is the reason why good agreement is obtained for the upper edge with mm. For the lower trajectory, the simulations show only small deviations from the experiments. The turbulence intensity is high, but not as high as that for the upper edge. The result is somewhat insensitive to , but smaller values than 4 mm give better results for the majority part of the cavity.

In the far-field zone, the values near the chute bottom are overestimated in the simulations. Kramer and Hager [9] studied the air transport process in chute flows. They pointed out that air detrained after the reattachment point and the interfacial force between bubbles and water dominated the process of detrainment in the zone. This implies that the effects of the interfacial forces are underestimated in the two-fluid model.

#### 5. Conclusions

To model the air-water flow at an aerator is a challenging issue, especially if the water flow velocity is high, which is the case in most spillway installations. Based on the experimental data of ETH, Zurich, numerical simulations are performed to reproduce the characteristics of the aerated flow. The CFD model is the two-fluid model in ANSYS 15; the parameters of interest include air concentration, cavity length, and air-entrainment rate. The bubble diameter affects the momentum exchange between the water and air and a range between 1 and 4 mm is investigated.

In terms of the cavity length, the experiments and CFD give similar results irrespective of the bubble size. The bubble diameter affects the amount of air entrained into the flow; the air flow rate from the 4 mm simulations is close to the measured one. Along the cavity zone, the surface-water roughness increases; a somewhat larger bubble size is suitable to describe the exchange between the two phases. For the lower jet trajectory, the simulated air concentration is relatively nonsensitive to the bubble size. However, sizes smaller than 4 mm lead to results closer to the experiments. The air concentration in the far field is overestimated; the experiments showed lower air contents. The contributing reason is presumably the underestimation of the interfacial forces in the two-fluid model. Besides, the use of a single bubble diameter is not sufficient to represent the complex water-air exchange in the aerator flow but seems to be adequate as a first step.

#### Notations

: | Interfacial area (m^{2}) |

: | Constants (−) |

: | Groove width (m) |

: | Local air concentration (−) |

: | Bubble diameter (mm) |

: | Froude number (−) |

: | Interphase force (N) |

: | Acceleration of gravity (m/s^{2}) |

: | Groove depth (m) |

: | Depth of approach flow (m) |

: | Interphase momentum exchange coefficient (−) |

: | Drag coefficient (−) |

: | Turbulence dispersion coefficient (−) |

: | Lift coefficient (−) |

: | Water turbulent kinetic energy (−) |

: | Cavity length (m) |

: | Interfacial force (N) |

: | Drag force (N) |

: | Lift force (N) |

: | Turbulence dispersion force (N) |

: | Virtual mass force (N) |

, , and : | Constants (−) |

: | Water pressure (N/m^{2}) |

: | Air discharge (m^{3}/s) |

: | Water discharge (m^{3}/s) |

: | Reynolds number (−) |

: | Relative Reynolds number (−) |

: | Deflector height (m) |

: | Time (s) |

: | Approach flow velocity (m/s) |

: | Velocity of phase (m/s) |

: | Velocity of air bubble (m/s) |

: | Velocity of water (m/s) |

: | Weber number (−) |

: | -coordinate (m) |

: | Normalized -coordinate (−) |

: | -coordinate (m) |

: | (m) at = 30% |

: | (m) at = 60% |

: | Chute bottom angle (°) |

: | Air-entrainment coefficient (−) |

: | Deflector angle (°) |

: | Surface tension (N/m) |

: | Volume fraction of phase (−) |

: | Air volume fraction (−) |

: | Density of phase (kg/m^{3}) |

: | Water density (kg/m^{3}) |

: | Air density (kg/m^{3}) |

: | Kinematic water viscosity (m^{2}/s) |

: | Kinematic air viscosity (m^{2}/s) |

: | Shear stress of phase (Pa) |

: | Air-entrainment thickness (m) |

: | Normalized air-entrainment thickness (−). |

#### Competing Interests

No potential conflict of interests was reported by the authors.

#### Acknowledgments

The numerical modelling presented here was carried out as part of a Ph.D. Project “Hydraulic Design of Chute Spillway Aerators,” funded by Swedish Hydropower Centre (SVC). SVC has been established by the Swedish Energy Agency, Energiforsk, and Swedish National Grid together with Luleå University of Technology (LTU), Royal Institute of Technology (KTH), Chalmers University of Technology (CTH), and Uppsala University (UU) (http://www.svc.nu). The authors are indebted to Ms. Sara Sandberg of SVC for project coordinations.