3.1. Emergent interface dynamics and associated wake structures

We begin our discussion by first classifying distinct free-surface/interface features observed in our simulations. Figure 2 shows the state diagram summarising the emergent interface dynamics for several combinations of the submergence depth $h/D$ and the Bond ( $Bo$ ) number. The Reynolds ( $Re$ ) and Weber ( $We$ ) numbers are fixed at $150$ and $1000$ , respectively, for all the cases. At the extreme ends of our $ {Bo}$ range, the liquid–gas interface either develops travelling interfacial waves (low $ {Bo}$ ) or undergoes mild deformation (high $ {Bo}$ and $h/D$ ). For intermediate values of $ {Bo}$ , we observe the entrainment of gas bubbles in the liquid phase. The formation of gas bubbles in the entrainment state occurs via the breakup of the liquid–gas interface, which is driven by the unsteady wake flow. It is evident that a significant portion of our phase space in figure 2 is dominated by the gas entrainment regime. To our knowledge, the systematic mapping and identification of various interface regimes in figure 2 is being reported for the first time. Earlier two-dimensional numerical studies (Reichl et al. Reference Reichl, Hourigan and Thompson2005; Subburaj et al. Reference Subburaj, Khandelwal and Vengadesan2018; Karmakar & Saha Reference Karmakar and Saha2020) involving various cylinder shapes mainly operated within the reduced deformation regime in figure 2.

Figure 2.

Flow disturbances resulting from the rigid cylinder drive the interface dynamics towards one or a combination of the following states: ( $1$ ) interfacial waves, ( $2$ ) gas entrainment and ( $3$ ) reduced deformation. The transition between these emerging states is regulated by the submergence depth $h/D$ and the Bond number $ {Bo}$ . The remaining flow parameters are the Reynolds number $ {Re}=150$ and the Weber number $ {We}=1000$ . Instantaneous flow structures and interface shapes corresponding to various ( $ {Bo}$ , $h/D$ ) combinations highlighted by red squares are shown in figure 3.

Notably, the emergence of interfacial waves without breakup is rarely seen in our parameter space, as it appears within a narrow band of $2 \leqslant h/D \leqslant 2.5$ and $100 \leqslant {Bo} \leqslant 150$ . A gradual reduction in the submergence depth makes the interface more susceptible to flow disturbances in the downstream region. Specifically, for a Bond number of $ {Bo}=100$ , the wave-like interfacial structures begin to break at a critical submergence depth of $h/D=1.75$ , giving rise to a mixed regime characterised by the blend of interfacial waves and gas entrainment (see figure 2). At $ {Bo} =200$ , we observe a sudden transition that eliminates the pure interfacial wave regime. At the same time, the mixed (waves $+$ entrainment) regime also shrinks in the phase space, and the pure gas entrainment regime appears. Subsequently, the gas entrainment regime sustains for $200 \lt {Bo} \lt 2000$ , irrespective of the submergence depth. For $ {Bo} \geqslant 2000$ , the liquid–gas interface starts to stabilise, as indicated by the onset of the reduced deformation regime in figure 2. At $ {Bo}=5000$ , the entrainment of gas bubbles takes place only when the interface is relatively close to the cylinder. The transitions across different regimes in figure 2 are relatively sharp at lower Bond numbers ( $ {Bo}\sim \mathcal {O}{ (100 )}$ ) compared with higher values ( $ {Bo}\sim \mathcal {O}{ (1000 )}$ ).

Having introduced the state diagram in figure 2, we now present snapshots of the liquid–gas interface and vorticity field. Figure 3 illustrates a few such plots representing various interface regimes outlined in figure 2. The ${ ( {Bo}, h/D )}={ (100, 2.5 )}$ combination in figure 3(a $_{1}$ ) corresponds to the interfacial wave regime (see figure 2). As the incoming flow approaches and moves past the cylinder, it deflects the liquid–gas interface, as indicated by the bulging of the interface near the cylinder. However, the shedding of vortices is reminiscent of traditional single-phase flows past a cylinder. Therefore, the nearby interface has little to no influence on the flow separation phenomenon. Subsequently, in the wake region starting five diameters away from the cylinder, vortex pairs detached from unstable shear layers begin to diffuse in the cross-stream direction. This exposes the interface to the suction flow induced by a pair of clockwise (blue) and anticlockwise (red) Strouhal vortices, pulling the interface into the liquid phase. Ultimately, a sawtooth-shaped wavy interface becomes apparent.

Figure 3.

Instantaneous liquid–gas interface and wake structure represented by vorticity ( $\omega$ ) contours ( $-3\leqslant \omega D/U\leqslant 3$ ) across various submergence depth $h/D$ and Bond ( $Bo$ ) number combinations from figure 2. The interface regime associated with each ( $ {Bo}$ , $h/D$ ) combination (see figure 2) is labelled in the lower-left corner. ( a ₂,b ₂,c ₂, $ {d}_{2}$ ) Zoomed-in views of the piecewise continuous representation of liquid–gas interfaces in ( $ {a}_{1}$ ,b ₁,c ₁, $ {d}_{1}$ ). The remaining flow parameters are the Reynolds number $ {Re}=150$ and the Weber number $ {We}=1000$ . Note that Cartesian coordinates are in units of the cylinder diameter $D$ . The width of the red-coloured stripe in (b $_{2}$ ,c ₂,d $_{2}$ ) represents the size of the finest control volume in our quadtree-based simulations.

A magnified view of an interface segment is shown in figure 3(a $_{2}$ ). The penetration depth of the interface tip into the flowing liquid is close to the cylinder radius when measured relative to the undisturbed interface. Moreover, the wavelength of these pointed regions on the wavy interface follows the size of vortex pairs in the streamwise direction, repeating approximately every five diameters in figure 3(a $_{1}$ ). The presence of the liquid–gas interface hinders the vorticity diffusion in far-downstream regions. Over time, clockwise vortices spread out at the top (near the interface) and exhibit a tail-like structure at the bottom. On the other hand, anticlockwise vortices expand in the gap between the tails of two neighbouring vortices (refer to the wake structure between streamwise coordinates $25$ and $50$ in figure 3 a $_{1}$ ). In our discussions, we deliberately refrain from analysing flow structures between streamwise coordinates $50$ and $70$ to avoid potential numerical artifacts stemming from boundary conditions.

Figure 3(b $_{1}$ ) shows an example of the regime consisting of a combination of interfacial waves and gas entrainment. It has the same Bond number, $ {Bo}=100$ , as that in figure 3(a $_{1}$ ), but with a lower submergence depth of $h/D=1.25$ (one-half of the previous case). For the current parameters, the bulging of the liquid–gas interface near the cylinder is more prominent due to the amplification of flow disturbances experienced by the interface (compare figures 3 a $_{1}$ and 3 b $_{1}$ ). Furthermore, the vorticity-driven suction of the interface is also enhanced, resulting in a wavy liquid–gas interface with increased curvature. At the same time, unlike the previous case in figure 3(a $_{1}$ ), the local pointed regions on the wavy interface are unstable and undergo breakup. A close-up view of gas bubbles formed through the breakup process is shown in figure 3(b $_{2}$ ), wherein two different size groups of the entrained gas bubbles are noticeable. Relatively large bubbles have sizes slightly below the cylinder radius. However, for the remaining bubbles, the scale separation between their sizes and the cylinder is more extreme.

Following the birth of gas bubbles, a portion of them is transported away from the interface into the flowing liquid with the help of Strouhal vortices, as seen near the bottom-right corner in figure 3(b $_{1}$ ). Given the size of these bubbles, their buoyancy lacks the necessary strength to assist them in escaping Strouhal vortices. In contrast to interfacial waves observed in figure 3(a $_{1}$ ), the emerging deformation pattern along the liquid–gas interface in figure 3(b $_{1}$ ) is non-uniform. More importantly, we observe entirely different wake structures in figures 3(a $_{1}$ ) and 3(b $_{1}$ ). In the present case, vortices emerging from shear layers quickly approach the interface. For example, in figure 3(b $_{1}$ ), notice the clockwise vortex hitting the interface in the downstream location 10 diameters away from the cylinder. Subsequently, the suction effect resulting from Strouhal vortices bends the interface downward (towards the liquid phase), which in turn pushes Strouhal vortices in the negative $y$ direction, consequently leading to a tilted vortex street (refer to the wake structure between streamwise coordinates $5$ and $30$ in figure 3 b $_{1}$ ). Also, observe the rotation of vortex pairs as they get advected by the background flow in the streamwise direction. Eventually, the strength of Strouhal vortices decays as they travel further downstream, allowing the interface to regain the elevation via buoyancy and surface tension.

The influence of gravity becomes more substantial with a gradual increment in the Bond number. For large enough Bond numbers, the stabilising gravitational force dominates over the suction effect generated by wake vortices, suppressing the interface from distorting in the faraway wake regions and eliminating the emergence of interfacial waves. However, depending on the value of the Bond number, the interface in the immediate vicinity of the cylinder may still deform and eventually break. This leads to the gas entrainment regime indicated in figure 2. Figure 3(c $_{1}$ ) demonstrates one such gas entrainment state for ${ ( {Bo}, h/D )}={ (1000, 2.5 )}$ . The value of $h/D$ is identical to that in figure 3(a $_{1}$ ), but the current $ {Bo}$ is 10 times larger. The stabilisation of the interface is evident in figure 3(c $_{1}$ ), as it retains its original elevation corresponding to $h/D=2.5$ in locations away from the cylinder. On the contrary, flow disturbances prevail near the cylinder and lead to gas entrainment.

In figure 3(c $_{1}$ ), the build-up of the anticlockwise vorticity beneath the curved liquid–gas interface is evident within the gas entrainment zone. The accumulated vorticity near the deformed interface subsequently disperses along the adjacent undisturbed interface in the downstream area. Figure 3(c $_{2}$ ) provides an enlarged view of the entrained bubbles. The multi-scale nature of gas bubbles is apparent, similar to our earlier observation in figure 3(b $_{2}$ ). Remarkably, there are no traces of gas bubbles in the wake region covering the vortex street (see figure 3 c $_{1}$ ). The entrainment process in figure 3(c $_{1}$ ) occurs sufficiently away from wake vortices. Thus, newly formed gas bubbles are able to rise freely with the help of buoyancy and eventually merge with the free surface, resulting in a wake devoid of gas bubbles. Lastly, we observe oblique Strouhal vortices in distant wake locations starting $25$ diameters away from the cylinder (see figure 3 c $_{1}$ ).

Flow features within the gas entrainment regime alter dramatically with the reduction in the submergence depth. One such representative case is demonstrated in figure 3(d $_{1}$ ) for ${ ( {Bo}, h/D )}={ (2000, 1 )}$ . Note that $h/D=1$ is the lowest submergence depth in our parameter space. Unlike the previous gas entrainment example, the shedding of periodic vortices is suppressed, and we no longer observe the von Kármán-like vortex street. Instead, the wake region is dominated by the shear flow, as indicated by the gradually thinning anticlockwise vorticity layer in the liquid phase (see figure 3 d $_{1}$ ). At the cylinder top, the incoming flow within the liquid phase separates from the liquid–gas interface, forming a detached shear layer characterised by anticlockwise vorticity. This layer, in conjunction with the clockwise vorticity layer attached to the cylinder, forms a downward jet-like flow between the cylinder’s top surface and the interface. Simultaneously, the shear layer at the lower surface of the cylinder also aligns itself with the emerging jet-like flow, as visible in figure 3(d $_{1}$ ). The detached anticlockwise vorticity layer near the interface dominates the clockwise vorticity layer at the upper surface of the cylinder, ultimately merging with the shear layer at the bottom of the cylinder in the downstream region. Notably, the lateral extension of the top and bottom shear layers attached to the cylinder spans multiple diameters in the wake region.

At lower submergence depths, the gas entrainment zone relocates closer to the cylinder in the upstream direction (compare figures 3 c $_{1}$ –c $_{2}$ and 3 d $_{1}$ –d $_{2}$ ). In addition, the breakup mechanism leading to the entrainment of gas bubbles also alters significantly with the variation in the submergence depth. A more elaborated discussion on the gas entrainment phenomenon follows later in this section. We point out that Sheridan et al. (Reference Sheridan, Lin and Rockwell1997) also reported the development of a jet-like flow in their experimental work, albeit in a flow set-up with $\ {Re}\sim \mathcal {O}{ (1000 )}$ (see § 1 for a summary of Sheridan et al. (Reference Sheridan, Lin and Rockwell1997)).

The last three snapshots in figure 3 correspond to the highest Bond number value of $ {Bo}=5000$ in our investigation. The interface dynamics and the vortex shedding from shear layers remain decoupled for $h/D=2.5$ in figure 3(e). Unlike $ {Bo}=100$ and $1000$ cases with the same submergence depth (see figure 3 a $_{1}$ ,c $_{1}$ ), the liquid–gas interface does not deform when the liquid moves past the cylinder. We also do not observe any pronounced interfacial perturbations in farther wake regions, which is consistent with the previous $ {Bo}=1000$ case in figure 3(c $_{1}$ ) with a similar $h/D$ value. However, contrary to this $ {Bo}=1000$ example, at $ {Bo}=5000$ we see pairs of alternating Strouhal vortices that are nearly symmetric with respect to the centreline passing through the cylinder, reminiscent of the traditional von Kármán vortex street (see wake structures in figure 3 c $_{1}$ ,e). We suspect that the production of interfacial vorticity near the gas entrainment zone perturbs newly shed Strouhal vortices. In figure 3(c $_{1}$ ), one can notice the interfacial vorticity connecting with the vortex street near the wake location approximately 10 diameters away from the cylinder, followed by the tilting of wake vortices in further downstream locations. Conversely, at $ {Bo}=5000$ , the lack of interface deformation and breakup inhibits the generation of interfacial vorticity, and therefore wake vortices remain undisturbed in figure 3(e).

Upon lowering the submergence depth to $h/D=1.5$ while keeping $ {Bo}$ fixed at $5000$ , the wake structure alters in distant wake locations. The cross-stream diffusion of Strouhal vortices gets hindered by the nearby liquid–gas interface. As a result, the vortex street transitions into a pair of parallel shear layers with opposite vorticity, as evident in figure 3(f). There are also additional subtle changes in the dynamics. First, the liquid–gas interface near the rear part of the cylinder undergoes mild distortion, generating interfacial vorticity in the liquid phase. Second, occasional breakup events occur in the region where the interface is distorted, forming liquid droplets, which then drift inside the gas boundary layer. Notice very small dot-like droplets in figure 3(f) between locations $15$ and $45$ diameters away from the cylinder (readers are advised to magnify the figure in the online version to see this clearly). However, there is no entrainment of gas bubbles. Third, the interaction of clockwise Strouhal vortices with the interface creates localised vorticity concentration spots within the gas boundary layer, giving rise to enhanced velocity gradients, visible as dark-red hot spots in figure 3(f).

We continue our discussion at the same $ {Bo}$ and place the interface at height $h/D=1$ . The resulting interface features for this parameter combination are characterised by the gas entrainment state. Our numerical result in figure 3(g) shows small-scale gas bubbles dispersed in the wake region, and the presence of liquid droplets in the gas boundary layer is also visible. The bubbles and droplets formed via the interface breakup appear to be of similar size. More importantly, the wake structure in the present case modifies dramatically compared with a typical von Kármán wake. Overall, it represents an intermediate state between complete and no vortex shedding cases observed in previous ( $ {Bo}$ , $h/d$ ) combinations, e.g. see figures 3(e) and 3(d $_{1}$ ). It is evident from figure 3(g) that clockwise Strouhal vortices emerging from the top shear layer rapidly vanish in the wake region, leading to a partial vortex shedding state wherein the downstream region contains only anticlockwise Strouhal vortices. As the newly shed anticlockwise Strouhal vortex is advected downstream, it merges with the previously shed vortex, forming a larger circulating region. Prior numerical studies have also reported a qualitatively similar wake state with partial shedding (Reichl et al. Reference Reichl, Hourigan and Thompson2005; Subburaj et al. Reference Subburaj, Khandelwal and Vengadesan2018; Karmakar & Saha Reference Karmakar and Saha2020). As pointed out by Reichl et al. (Reference Reichl, Hourigan and Thompson2005), the weakening or annihilation of clockwise Strouhal vortices is enabled by the nearby opposite interfacial vorticity originating through deformation of the interface. In addition to the present case, clearer evidence showcasing such cross-annihilation of vorticity can be observed in figure 3(d $_{1}$ ), where the clockwise vorticity layer at the top of the cylinder is dominated by the adjacent shear layers with opposite vorticity. In addition to cross-annihilation, the transport of vorticity flux across the liquid–gas interface also contributes to the dissipation of Strouhal vortices residing in the interfacial region (Rood Reference Rood1994; Lundgren & Koumoutsakos Reference Lundgren and Koumoutsakos1999).

3.2. Implications of the liquid–gas interface on hydrodynamic lift

Following our earlier qualitative discussion on interface and wake dynamics, we now focus on quantifying various aspects of flow physics. A key response parameter in fluid–structure interaction problems is the hydrodynamic load exerted by the fluid moving past the body under a given flow condition. We are particularly interested in the hydrodynamic lift force experienced by the cylinder, expressed in its non-dimensional form as $C_{l}=2F_{y}/\rho _{1}U^{2}D$ , where $F_{y}$ represents the vertical hydrodynamic load (excluding buoyancy) exerted on the cylinder. For a stationary cylinder placed deep within a flowing liquid, the lift force follows a cyclic pattern due to the periodic shedding of symmetric vortices, causing the net lift force to vanish over one shedding cycle. However, as shown in figure 3, the presence of a deformable boundary in the form of a liquid–gas interface can significantly alter the flow dynamics, potentially affecting the fluid forces acting on the stationary cylinder. For instance, the biased nature of the lift force signal from our validation study in Appendix A already hints at the influence of the liquid–gas interface.

In figure 4, we present various measurements characterising the lift force signal to systematically illustrate the impact of the liquid–gas interface on hydrodynamic lift. The primary plot in figure 4(a) shows the variation in mean ( $\overline {C}_{l}$ ) and root-mean-square (RMS; $C^{RMS}_{l}$ ) values of the lift signal for different submergence depths $h/D$ at a constant Bond number $ {Bo}=100$ . These $ ( {Bo}, h/D )$ combinations are situated on the extreme left of our state diagram, where the phase space is characterised by the presence of interfacial waves, either with or without gas entrainment (see figure 2). As shown in figure 4(a), the net lift force on the cylinder is marginal since $\overline {C}_{l}$ remains close to zero across all $h/D$ values, similar to the behaviour seen in laminar single-phase flows over a fixed cylinder with $\overline {C}_{l}\rightarrow 0$ . However, the fluctuations around the mean lift force ( $C^{RMS}_{l}$ ) decay as the submergence depth is reduced. Likewise, the non-dimensional frequency $fD/U$ of the fluctuating lift force shows a decreasing trend as the interface gets closer to the cylinder, as plotted in the inset of figure 4(a). Overall, under low- $ {Bo}$ conditions, $C^{RMS}_{l}$ and $fD/U$ show significant differences compared with the single-phase flow observations reported in table 1.

Figure 4.

Effect of the submergence depth $h/D$ and the Bond number ( $Bo$ ) on the hydrodynamic lift force experienced by the cylinder at constant Reynolds ( $Re$ ) and Weber ( $We$ ) numbers of $150$ and $1000$ , respectively. The labels $C_{l}$ , $\overline {C}_{l}$ , $C^{RMS}_{l}$ and $fD/U$ denote the instantaneous non-dimensional lift force, the time-averaged value of $C_{l}$ , the RMS of the $C_{l}$ time series relative to $\overline {C}_{l}$ and the non-dimensional primary frequency of cyclic fluctuations in $C_{l}$ , respectively. The inset in (c) displays the interface shapes at the moment of peak downward lift for $ {Bo}=2000$ and $5000$ with $h/D=1.5$ .

Table 1.

Root-mean-square lift coefficient $C^{RMS}_{l}$ and dimensionless frequency $fD/U$ of the lift force signal in conventional single-phase flow around a stationary circular cylinder at a Reynolds number $ {Re}=150$ .

The decline in $C^{RMS}_{l}$ and $fD/U$ with $h/D$ in figure 4(a) can be explained using the argument put forward by Green & Gerrard (Reference Green and Gerrard1993), which has also been previously employed by Reichl et al. (Reference Reichl, Hourigan and Thompson2005) and Karmakar & Saha (Reference Karmakar and Saha2020). Prior to the shedding of a Strouhal vortex, the tail of the shear layer takes the form of a vorticity blob, which gradually grows as fluid continues to accumulate. Eventually, this blob of vorticity detaches from the shear layer, and a vortex emerges. Green & Gerrard (Reference Green and Gerrard1993) pointed out that the frequency of vortex shedding is linked to the time required for the build-up of the vorticity blob, which is regulated by the flow speed near the back of the cylinder. In figure 3(a $_{1}$ ,b $_{1}$ ), we already noted that the incoming flow pushes the liquid–gas interface away from the cylinder, causing the gap between the cylinder and the interface to expand. This expansion of the gap, which is more pronounced at lower $h/d$ values, relaxes the incoming flow. In other words, the average streamwise velocity within the gap decreases. Such alterations in fluid transport around the cylinder delay the formation of Strouhal vortices and affect their strength, which is reflected through a reduction in $C^{RMS}_{l}$ and $fD/U$ observed in figure 4(a).

Figure 4(b) summarises the lift force statistics for data points along the right edge of the state diagram at $ {Bo}=5000$ (see figure 2). Unlike the previous case at $ {Bo}=100$ , most $ ( {Bo}, h/D )$ combinations in figure 4(b) fall within a regime where interface deformation is minimal. This substantial reduction in deformability alters the lift force characteristics significantly. Firstly, the mean lift force $\overline {C}_{l}$ in figure 4(b) remains non-zero, with $\overline {C}_{l}$ increasing sharply as $h/D$ decreases, leading to a considerable net lift force in the negative $y$ direction. Additionally, $C^{RMS}_{l}$ and $fD/U$ both intensify when transitioning from $ {Bo}=100$ to $ {Bo}=5000$ at a given $h/D$ . In figure 4(b), $C^{RMS}_{l}$ and $fD/U$ increase as the interface height decreases, peaking at $h/d=1.5$ before rapidly declining for $h/D$ values below $1.5$ . Interestingly, this also coincides with the regime transition at $h/D=1.5$ for $ {Bo}=5000$ in figure 2. Overall, $C^{RMS}_{l}$ and $fD/U$ across all submergence depths in figure 4(b) surpass the corresponding values in table 1 for the single-phase configuration. These patterns can be reasoned using our earlier qualitative insights derived from the observations of Green & Gerrard (Reference Green and Gerrard1993). However, here, we adopt a quantitative approach to substantiate the validity of our argument.

Figures 5(a $_{1}$ ) and 5(a $_{2}$ ) present the time series of the average streamwise gap velocity

(3.1) \begin{eqnarray} \frac {U_{g}(t)}{U}{=}\frac {1}{h(t)-D{/}2}\int \limits ^{y{=}h(t)}_{y{=}D/2}\frac {\left .u_{x}(y,t)\right |_{x{=}0}}{U}{\textrm d}y \end{eqnarray}

from our simulations for submergence depths $h/D=1.5$ and $1$ , where $u_{x}$ denotes the $x$ component of the flow field. Both $U_{g}/U$ time series show cyclic fluctuations around mean values of $\overline {U}_{g}/U=1.24$ and $1.14$ for $h/D=1.5$ and $1$ , respectively. In comparison, for single-phase flow with virtual heights (no actual interface) $h/D=1.5$ and $1$ , $\overline {U}_{g}/U$ values are $1.11$ and $1.07$ . This suggests that as $h/D$ decreases, the gap above the cylinder also narrows due to weak deformation of the liquid–gas interface, leading to a significant increase in $\overline {U}_{g}/U$ compared with its single-phase counterpart (approximately $12\,\%$ for $h/D=1.5$ and $7\,\%$ for $h/D=1$ ). This increase amplifies the magnitude $C^{RMS}_{l}$ and frequency $fD/U$ of lift force fluctuations compared with the single-phase flow scenario, as evident from figure 4(b) and table 1. Furthermore, the higher $\overline {U}_{g}/U$ at $h/D=1.5$ compared with $h/D=1$ explains the larger values of $C^{RMS}_{l}$ and $fD/U$ at $h/D=1.5$ . Lastly, upon performing a similar exercise for the combination ${ ( {Bo}, h/D )}={ (100, 1.25 )}$ in figure 4(a), we obtain $\overline {U}_{g}/U=0.96$ , further corroborating our claim surrounding the work of Green & Gerrard (Reference Green and Gerrard1993).

Figure 5.

Temporal evolution of the average streamwise gap velocity $U_{g}/U$ , the non-dimensional lift force $C_{l}$ and the front stagnation angle $\theta$ , which varies clockwise with $\theta =0$ located at the front of the cylinder on the horizontal centreline. Velocity $U_{g}$ is calculated using the velocity profile along the vertical centreline between the top of the cylinder and the liquid–gas interface. In (a), $\overline {U}_{g}$ denotes the temporal mean of $U_{g}$ . The Reynolds and Weber numbers are set to $ {Re}=150$ and $ {We}=1000$ . The remaining parameters are indicated in individual plots.

Following our discussion on lift force fluctuations, we now discuss the origin of the non-zero mean lift force $\overline {C}_{l}$ seen in figure 4(b). In single-phase flows, the incoming fluid halts at the front of the cylinder, creating a stagnation point. Once the system reaches a dynamic steady state through periodic vortex shedding, this stagnation point oscillates slightly. For instance, at $ {Re}=150$ , the stagnation point oscillates ${\approx }1.8^{\circ }$ to either side of the horizontal centreline passing through the cylinder. These oscillations are symmetric, and thus, over one vortex shedding cycle, the combined effect of stagnation pressure and low wake pressure results in a net drag force acting along the positive $x$ direction while $\overline {C}_{l}\rightarrow 0$ . However, this symmetry breaks down when a liquid–gas interface is introduced. Figures 5(b $_{1}$ ) and 5(b $_{2}$ ) show the evolution of the instantaneous lift force ${C}_{l}$ and the stagnation angle $\theta$ for $h/D=1.5$ and $1$ at $ {Bo}=5000$ . Here, the stagnation point no longer oscillates symmetrically but instead concentrates in the upper left quadrant of the cylinder. Consequently, the vertical component of the force from the stagnation pressure does not vanish over one shedding cycle, contributing to a sustained non-zero mean lift force. Essentially, the displacement of the stagnation point due to the liquid–gas interface introduces bias in the lift force signal, making $\overline {C}_{l}$ non-zero. As $h/D$ decreases, the stagnation point shifts further into the upper left quadrant, moving away from the horizontal centreline, which increases $\overline {C}_{l}$ even more (see figures 4 b and 5 b $_{2}$ ).

Figure 4(c) shows the variation in the mean lift force $\overline {C}_{l}$ for multiple Bond numbers and submergence depths. At $h/D=2.5$ , the difference in $\overline {C}_{l}$ across various $ {Bo}$ values is marginal. Notably, they all fall within the reduced deformation regime indicated in figure 2. However, as $h/D$ decreases, the $\overline {C}_{l}$ values for different Bond numbers start to diverge. This branching occurs within the $h/D$ range marked by the red zone in figure 4(c), and it corresponds to the regime transition as $ {Bo}$ varies for a specific $h/D$ (see figure 2). For instance, while switching from $h/D=2.5$ to $2.25$ , $ {Bo}=2000$ transitions from the reduced deformation to the gas entrainment regime, while remaining $ {Bo}$ values still exhibit reduced deformation of the interface (see figure 2). This transition at $h/D=2.25$ is reflected in figure 4(c) by the increased $\overline {C}_{l}$ for $ {Bo}=2000$ compared with other Bond numbers. Similar branching patterns are observed for $h/D=1.75$ and $1.5$ as $ {Bo}=3000$ and $4000$ transition to the gas entrainment state. At $h/D=1.5$ , a significant spread in $\overline {C}_{l}$ is visible, with more deformable interfaces (lower Bond numbers) producing higher lift forces. To understand this, we examine the instantaneous interface shapes for $ {Bo}=2000$ and $5000$ in figure 4(c). It is observed that at $ {Bo}=2000$ , the interface deformation near the back of the cylinder reorients the flow towards the cylinder in the negative $y$ direction, thereby generating a higher downward lift force compared with the weakly deformed interface at $ {Bo}=5000$ . As $h/D$ decreases below $1.5$ , the trend reverses within the blue zone on the left in figure 4(c), where all $ {Bo}$ curves start to converge. Note that for $h/D\lt 1.5$ , all $ {Bo}$ values in figure 4(c) belong to the gas entrainment state. At $h/D=1$ , all $ {Bo}$ points nearly collapse with similar $\overline {C}_{l}$ values, except for $ {Bo}=2000$ , indicating a minimal impact of interface deformability. Overall, the net lift force $\overline {C}_{l}$ (approximately) exhibits a quadratic variation with the submergence depth $h/D$ (see the black curve in figure 4 c).

Previously, we noted that at $ {Bo}=2000$ , vortex shedding ceases when the liquid–gas interface is lowered to the submergence depth $h/D=1$ (see figure 3 d $_{1}$ ). This is also evident through the temporal variation of the lift force in figure 4(d), as cyclic fluctuations in ${C}_{l}$ disappear, and ${C}_{l}$ remains nearly constant over time. However, when $ {Bo}$ is increased to $3000$ , cyclic fluctuations in ${C}_{l}$ reappear, as shown in figure 4(d). This particular combination of $ {Bo}=3000$ and $h/D=1$ exhibits partial vortex shedding similar to that shown in figure 3(g). Another peculiar characteristic of this case is the variability in the peak-to-peak amplitude of the lift force signal over time (see $ {Bo}=3000$ curve in figure 4 d), hinting at the presence of two distinct time scales in the system. The smaller of the two time scales is related to cyclic fluctuations in the lift force, which stems from the periodic shedding of vortices. The second time scale is linked to relatively gradual temporal changes in the peak-to-peak amplitude of lift force cycles. For the physical interpretation of the second time scale, we look at velocity magnitude contours in figure 6(a $_{1}$ ,a $_{2}$ ) corresponding to two different time instances marked by black circles in figure 4(d). As illustrated in figure 6(a $_{1}$ ), the jet emerging through the gap above the cylinder separates from the liquid–gas interface near the back of the cylinder. On the contrary, at a later time in figure 6(a $_{2}$ ), it remains attached to the interface. These temporal changes in the orientation of the jet affect the lift force acting on the cylinder and introduce a new time scale associated with jet oscillations. Such metastable states were initially observed in the experiments by Sheridan, Lin & Rockwell (Reference Sheridan, Lin and Rockwell1995; 1Reference Sheridan, Lin and Rockwell1997), which we introduced earlier in § 1.

Figure 6.

(a $_{1}$ ,a $_{2}$ ) Instantaneous snapshots of velocity magnitude $|\boldsymbol {u}|$ within the liquid phase. Intensified colour indicates heightened velocity, with dark red representing the highest velocity within the domain. (b) Discrete Fourier transform of the lift force signal. The simulation parameters are {Re, We, Bo, $h/D$ } = { $150, 1000, 3000, 1$ }.

To better quantify the metastable dynamics observed at $ {Bo}=3000$ and $h/d=1$ , we analyse the amplitude–frequency spectrum of the lift force signal using the Fourier transform, as shown in figure 6(b). The spectrum reveals a dominant frequency $f_{1}D/U=0.212$ , which is consistent with the frequency range reported for other combinations of $ {Bo}$ and $h/D$ in figure 4(a,b), indicating its connection to the vortex shedding. In the lower-frequency range, there is a notable amplitude peak at $f_{2}D/U=0.0254$ , which likely represents the signature of the metastable jet. Earlier, Sheridan et al. (Reference Sheridan, Lin and Rockwell1995) qualitatively estimated $f_{2}/f_{1}\sim \mathcal {O}{ (10^{-2} )}$ in their experiments at high Reynolds numbers. In contrast, numerical simulations by Reichl et al. (Reference Reichl, Hourigan and Thompson2005) and Colagrossi et al. (Reference Colagrossi, Nikolov, Durante, Marrone and Souto-Iglesias2019), conducted at lower Reynolds numbers and without surface tension, reported $f_{2}/f_{1}\sim \mathcal {O}{ (10^{-1} )}$ . Our simulation, which includes surface tension, also yields $f_{2}/f_{1}\sim \mathcal {O}{ (10^{-1} )}$ , aligning with the findings of Reichl et al. (Reference Reichl, Hourigan and Thompson2005) and Colagrossi et al. (Reference Colagrossi, Nikolov, Durante, Marrone and Souto-Iglesias2019). The parameters $ {Re}$ , $ {Fr}$ and $h/D$ in the present case closely match those in their simulations. To resolve the discrepancy in reported $f_{2}/f_{1}$ values, further work needs to be done in the high-Reynolds-number range, although this is beyond the scope of the present article. We note that although high-Reynolds-number simulations are expensive, experimental set-ups are prone to contamination of the liquid–gas interface, which can dramatically influence the dynamics, as pointed out by Reichl et al. (Reference Reichl, Hourigan and Thompson2005). Recently, Zhao et al. (Reference Zhao, Wang, Zhu, Ping, Bao, Zhou, Cao and Cui2021) performed simulations in the turbulent regime but without considering surface tension.

3.3. Interfacial waves at $ {Bo}=100$

The remainder of our discussion in this article focuses on specific features of the liquid–gas interface observed in our parameter space. In this subsection, we analyse interfacial waves at a fixed Bond number $ {Bo}=100$ for two submergence depths: $h/D=2.5$ and $1.25$ , as marked in figure 2. Apart from the intensity of interfacial disturbances, a notable distinction between these cases is the breakup of the interface, observed only at $h/D=1.25$ (see snapshots in figure 3).

Figure 7 illustrates the colour-coded variation of interface elevation $y/D$ in space and time relative to the unperturbed interface height $h/D$ . Starting at the location $x/D=0$ above the cylinder, the interface undergoes static deformation with relative elevation $(y-h)/D$ approaching the size of the cylinder for both $h/D$ values. As we enter the wake region, beginning around $x/D=5$ , the interface deformation becomes time-dependent regardless of $h/D$ when recorded at a given $x/D$ . However, the temporal deformation pattern varies depending on the value of $h/D$ . For instance, at $x/D=10$ , the interface oscillates on either side of the unperturbed height for $h/D=1.25$ , whereas for $h/D=2.5$ , it always fluctuates above the unperturbed height. The transition from static to time-varying deformation arises due to the influence of periodically shed Strouhal vortices. Further downstream, both cases exhibit interface oscillations below their original elevation $h/D$ , which is indicated by the extended blue region spanning several diameters in figure 7. As Strouhal vortices weaken, the interface attempts to regain the original elevation. However, the recoil from buoyancy and surface tension leads to an overshoot in elevation before reaching the equilibrium, reminiscent of the damped oscillations of a standing gravity or capillary wave (Prosperetti Reference Prosperetti1981). The overshoot is evident through the red-coloured band between $x/D=35$ and $45$ . At any given time, on a length scale approaching the extent of the vortex street (filtering out small-scale features), we can notice one large-scale interfacial wave represented by two peaks situated near $x/D=0$ and $45$ (red zones in figure 7), and a valley in between (blue zone). This is also visible through snapshots in figure 3. As we refine this coarse-grained description by adopting a length scale comparable to or smaller than the cylinder diameter, small-scale deformation waves become apparent, which ride on the large-scale wave.

Figure 7.

Spatio-temporal evolution of interfacial perturbations for submergence depths (a) $h/D=2.5$ and (b) $h/D=1.25$ at a Bond number $ {Bo}=100$ . These ( $ {Bo}$ , $h/D$ ) coordinates belong to the interfacial wave regime, where gas entrainment is observed at $h/D{=}1.25$ and absent at $h/D{=}2.5$ (see figure 2). The Reynolds and Weber numbers are fixed at $ {Re}=150$ and $ {We}=1000$ .

Another interesting point to note from figure 7 is the orientation of the emerging pattern. The orientation of various contour levels corresponding to different elevations provides a measure of the phase speed $c$ . Based on this, the inverse slope of the yellow line in figure 7(a) yields $c=\Delta x/ \Delta t=0.92U$ , indicating a lag between the motion of the bulk liquid and interfacial waves. A similar phase speed is also observed at a lower submergence depth in figure 7(b). However, in the mid-downstream area, high-amplitude deformations with negative relative elevation move at a different phase speed of $c=0.82U$ , as suggested by the magenta line in figure 7(b). From snapshots in figure 3(a,b), we estimate the wavelength of the deformation pattern to be $\lambda \approx 5D$ in both cases.

Following the linear theory of travelling capillary–gravity waves (Lighthill Reference Lighthill1978), the phase speed $c^{r}$ of a capillary–gravity wave relative to still liquid is given by

(3.2) \begin{eqnarray} \left (\frac {c^{r}}{U}\right )^{2}{=}\underbrace {\left (\frac {2\pi }{ {We}}\right )\left (\frac {D}{\lambda }\right )}_{\substack { \text {surface-tension-} \\ \text {driven}}}{+}\underbrace {\left (\frac { {Bo}}{2\pi {We}}\right )\left (\frac {\lambda }{D}\right )}_{\substack { \text {gravity-driven}}}, \end{eqnarray}

where $\lambda$ denotes the wavelength (note that $ {Bo}/ {We}=1/ {Fr}^{2}$ ). Using the phase speed relation (3.2), we derive the minimum phase speed of a realisable capillary–gravity wave relative to still liquid: $c^{r}_{m}/U= (4 {Bo}/ {We}^{2} )^{1/4}$ . Given $ {Bo}=100$ and $ {We}=1000$ , we obtain $c^{r}_{m}=0.14U$ , which is about $1.75$ times the relative phase speed $U-c$ shown by the yellow line in figure 7, potentially hinting at a markedly different nature of the present interfacial waves. The relative phase speed associated with the magenta line in figure 7(b) is above the threshold phase speed $c^{r}_{m}$ , although it occurs far from the region of wave onset. Note that $c^{r}$ and $c^{r}_{m}$ are derived under the assumption that the circular cylinder is absent and are valid solely for sinusoidal waveforms.

We also compare the observed interfacial waves with the classical Kelvin–Helmholtz (KH) instability, neglecting the effects of gravity and surface tension. According to linear theory, the wave propagation speed for KH instability is $c_{\text {KH}}=(\rho _{1}U_{1} +\rho _{2}U_{2})/(\rho _{1}+\rho _{2})$ (Drazin Reference Drazin2002), where the subscripts $1$ and $2$ denote the liquid and gas phases, respectively, as shown in figure 1. By substituting $U_{1}=U$ and $U_{2}=0$ , we find $c_{\text {KH}}=0.99U$ , which reasonably approximates the wave speed corresponding to the yellow line in figure 7. It should be noted that $c_{\text {KH}}$ does not account for the influence of the cylinder on KH instability, and the mixing layer in the interfacial region is absent. A refined version of the KH wave speed, referred to as the Dimotakis speed (Dimotakis Reference Dimotakis1986) and commonly used in previous studies (Orazzo, Coppola & de Luca Reference Orazzo, Coppola and de Luca2011; Hoepffner, Blumenthal & Zaleski Reference Hoepffner, Blumenthal and Zaleski2011; Odier et al. Reference Odier, Balarac, Corre and Moureau2015; Ling et al. Reference Ling, Fuster, Zaleski and Tryggvason2017), is expressed as $c_{\text {Dimotakis}}=(\sqrt {\rho _{1}}U_{1}+\sqrt {\rho _{2}}U_{2})/(\sqrt {\rho _{1}}+\sqrt {\rho _{2}})$ . The estimate $c_{\text {Dimotakis}}=0.9U$ for the present case aligns well with the range of phase speeds indicated by the yellow and magenta lines in figure 7.

To further our analysis, we investigate the temporal variations in the interface height at the streamwise positions $x/D=10$ and $22.5$ . Table 2 reports the dominant frequencies associated with the cyclic fluctuations in interface elevation for submergence depths $h/D=2.5$ and $1.25$ , which align closely with the vortex shedding frequencies. This correspondence suggests that the the emergence of interfacial waves observed in figure 3(a $_{1}$ ,b $_{1}$ ) is indeed driven by periodic shedding of Strouhal vortices. Therefore, we refer to these waves as Strouhal waves.

Table 2.

Dimensionless frequency $fD/U$ corresponding to interface oscillations and vortex shedding in the interfacial wave regime at $ {Re}=150$ , $ {We}=1000$ and $ {Bo}=100$ .

3.4. Gas entrainment at $ {Bo}=1000$

In the present subsection, we focus on the gas entrainment regime observed at $ {Bo}=1000$ in figure 2. Before proceeding, we recommend that readers review the brief note in Appendix B on interface breakup and coalescence dynamics in simulations.

We analyse various statistics related to entrained gas bubbles and liquid droplets formed through bubble collapse, such as their total counts, positions and size distributions. Nevertheless, computing these quantities is not trivial since the liquid–gas interface is captured implicitly with the help of the volume fraction field $C$ . To detect bubbles and droplets, existing algorithms in the literature (Herrmann Reference Herrmann2010; Chan et al. Reference Chan, Johnson, Moin and Urzay2021; Gao et al. Reference Gao, Deane, Liu and Shen2021) scan through the domain and first identify a grid point with $C=0$ (for bubble detection) or $1$ (for droplet detection). They then successively search for neighbouring grid points with the same value of $C$ until the boundary of the bubble or droplet is detected. This completes the detection of one bubble or droplet. To identify remaining bubbles or droplets, the same two steps are repeated in a loop by excluding grid points belonging to already detected bubbles or droplets.

In our two-dimensional simulations, bubble and droplet statistics are gathered in the post-processing stage using a non-iterative detection algorithm implemented within Matlab $^{\circledR }$ . For a given volume fraction field snapshot, Matlab $^{\circledR }$ facilitates the extraction of the coordinates tied to isolines of different contour levels. Using this, we are able to obtain the coordinates of $C=0.5$ isolines in the domain, effectively converting our Eulerian interface representation into an equivalent Lagrangian description. In the resulting family of isolines, one of the isolines corresponds to an open curve representing the primary liquid–gas interface, which we eliminate from our subsequent calculations. The remaining isolines are closed curves representing either bubbles or droplets. To bifurcate them into bubbles and droplets, we examine the value of $C$ at grid cells close to the centroid of each curve. Finally, using the coordinates of individual curves, Matlab $^{\circledR }$ readily provides the area enclosed by them, from which we derive the diameter $d$ of an equivalent circle with the same area, giving us the measure of the size of individual bubbles and droplets. Note that we only focus on the detection of bubbles and droplets; we do not track individual bubbles and droplets as time elapses. Lastly, all the statistics in our subsequent discussion are derived by monitoring bubbles and droplets in a subdomain ranging from $-D$ to $8D$ in the $x$ direction and $-5D$ to $5D$ in the $y$ direction.

We first examine the number of bubbles and droplets at a given time instance, denoted as $\mathcal {N}$ , in the wake region (note that $\mathcal {N}$ does not represent the instantaneous count of freshly formed bubbles or droplets). Two such time series are demonstrated in figure 8(a $_{1}$ ,a $_{2}$ ) for submergence depths $h/D=2.5$ and $1$ . A notable spike in bubble count is observed around $tU/D=25$ and $30$ for $h/D=2.5$ and $1$ , respectively. As the flow around the cylinder develops with time, we see oscillations in the instantaneous bubble count for $h/D=2.5$ . On the other hand, the variation of $\mathcal {N}$ with time remains relatively uniform for $h/D=1$ . These trends can be attributed to corresponding wake states, characterised by periodic and no vortex shedding at $h/D=2.5$ and $1$ , respectively. The average bubble count $\overline {\mathcal {N}}$ amplifies by a factor of ${\approx }4$ when the interface is shifted from $h/D=2.5$ to $1$ , indicating a substantial rise in gas entrainment. Conversely, the droplet production appears to be only marginally affected by the change in $h/D$ , as both cases in figure 8(a $_{1}$ ,a $_{2}$ ) have nearly identical average droplet counts $\overline {\mathcal {N}}$ .

Figure 8.

(a $_{1}$ ,a $_{2}$ ) Temporal variation of the number of bubbles and droplets $\mathcal {N}$ in the wake region. Here $\overline {\mathcal {N}}$ is the temporal mean of $\mathcal {N}$ . (b $_{1}$ ,b $_{2}$ ) Collection of bubble coordinates recorded over the time interval $20\leqslant tU/D \leqslant 100$ . High-density regions with tightly clustered bubble coordinates are marked in red, whereas those with low bubble density are shown in blue. (c $_{1}$ ,c $_{2}$ ) Multi-scale bubble-size distributions resulting from the gas entrainment phenomenon. The black curves with green shaded areas show bubble-size distributions fitted to the histograms. Here $\sum \mathcal {N}$ denotes the total bubble count over the time interval $20\leqslant tU/D\leqslant 100$ , and $d$ is the equivalent bubble diameter, as explained in the main text. The Reynolds and Weber numbers are fixed at $ {Re}=150$ and $ {We}=1000$ . The remaining parameters are indicated in individual plots.

To visualise the gas entrainment process over the time interval $20\leqslant tU/D\leqslant 100$ , we plot the bubble coordinates identified by our detection algorithm and colour-code them based on their clustering in the flow domain (see Eilers & Goeman (Reference Eilers and Goeman2004) for details). The red colour implies dense clusters of bubbles, and vice versa for blue. This provides a spatial distribution of bubbles, analogous to a joint probability distribution in physical space, as shown in figure 8(b $_{1}$ ,b $_{2}$ ) for submergence depths $h/D=2.5$ and $1$ . Interestingly, one can also notice the travel paths of different bubbles through trajectories emerging from coordinates. At $h/D=2.5$ , bubbles are concentrated in a narrow region near the liquid–gas interface. Most gas bubbles are produced where the coordinates are marked in red and yellow in figure 8(b $_{1}$ ). Some newly produced bubbles travel downstream parallel to the interface, while others rise to the interface due to buoyancy and collapse, which is evident through trajectories terminating near the interface. When the submergence depth is reduced to $h/D=1$ , there is a significant spread in bubble distribution in the wake region, spanning about a couple of diameters in the $y$ direction. The area with high bubble density (red-coloured coordinates) expands and shifts its orientation compared to the $h/D=2.5$ case, suggesting a different nature of the interface breakup process, which will be explored further in our subsequent discussion. The merging of gas bubbles with the free surface (i.e. bursting bubbles) still persists at $h/D=1$ , but more bubbles are transported to distant wake regions than at $h/D=2.5$ (mainly during the early stages).

To complete the basic statistical description of the gas entrainment process, we examine the bubble-size distributions shown in figure 8(c $_{1}$ ,c $_{2}$ ) for submergence depths of $h/D=2.5$ and $1$ . These distributions are based on bubbles observed over the time interval $20\leqslant tU/D\leqslant 100$ . The entrainment of gas bubbles begins at $tU/D\approx 4$ and ${\approx }14$ for $h/D=1$ and $2.5$ , respectively. In the initial stages of entrainment, large gas bubbles may form, particularly at lower $h/D$ values, resulting in outliers. To circumvent these anomalies, we begin our observations at $tU/D=20$ for both cases. The size distributions show two preferred bubble sizes for each submergence depth, indicated by two peaks on either side of the equivalent bubble diameter $d/D= 0.05$ in figure 8(c $_{1}$ ,c $_{2}$ ). The upper bound of the bubble-size distribution is $d/D=0.3$ , regardless of $h/D$ . While gas entrainment at $h/D=1$ results in a higher bubble count (see figure 8 a $_{1}$ ,a $_{2}$ ), entrainment at $h/D=2.5$ tends to produce larger bubbles ( $d/D\geqslant 0.1$ ) more frequently. For bubble sizes below $d/D=0.05$ , there is no significant difference in size distributions between $h/D=2.5$ and $1$ .

While the multi-scale nature of the bubble-size distributions in figure 8(c $_{1}$ ,c $_{2}$ ) is intriguing, understanding its origin is equally crucial. To explore this, we examine the breakup dynamics of the liquid–gas interface at different submergence depths. Figure 9 shows the formation of the initial interfacial wave at a submergence depth of $h/D=2.5$ . As the flow around the cylinder develops, it draws the interface towards the cylinder and creates a valley, as seen in figure 9(a). Subsequently, this valley shifts in the downstream direction due to the background flow (see figure 9 b), giving rise to a wave crest in figure 9(c–e). When the wave crest reaches a certain height, it bends downward due to gravity (figure 9 f–h) and eventually impacts the liquid–gas interface. Similar features have been observed in previous two- and three-dimensional numerical studies on deep-water waves (Deike, Popinet & Melville Reference Deike, Popinet and Melville2015; Mostert, Popinet & Deike Reference Mostert, Popinet and Deike2022). Interfacial waves similar to that in figure 9 are named plunging waves.

Figure 9.

Formation of a plunging wave at the onset of gas entrainment. The simulation parameters are {Re, We, Bo, $h/D$ } = { $150, 1000, 1000, 2.5$ }. Note that Cartesian coordinates are in units of the cylinder diameter $D$ .

Figure 10 illustrates the changes in the vertical position of the crest and valley of the plunging wave depicted in figure 9. Just before the wave breaks, its vertical span, from valley to crest, approaches the cylinder’s diameter. Reducing the Bond number to $500$ creates relatively tall plunging waves, and vice versa for a lower Weber number of $700$ . We notice that the formation of similar plunging breakers occurs frequently for the submergence depth of $h/D=2.5$ . Figure 11(a $_{1}$ –a $_{4}$ ) shows one such sequence of a plunging breaker at a later time, leading to the entrainment of a gas bubble. Typically, bubbles entrained by plunging breakers are larger than $d/D=0.05$ , which explains the presence of larger bubbles in the bubble-size distribution for $h/D=2.5$ in figure 8(c $_{1}$ ). Moreover, bubble coalescence also contributes to the appearance of larger bubbles in the size distribution.

Figure 10.

Temporal evolution of the interface position $y_{\text {int}}$ in the vertical direction at the valley ( $\text {min}(y_{\text {int}}-h)$ ) and crest ( $\text {max}(y_{\text {int}}-h)$ ) of a plunging wave for different { $ {Bo}$ , $ {We}$ } combinations. The formation of a plunging wave starts with the appearance of the valley, followed by the development of the crest as the interface rises above the initial height $h$ . The inset shows a plunging wave just before the breaking point for $ {Bo}=500$ and $ {We}=1000$ .

In addition to plunging breakers, we also observe surfing breakers, as shown in figure 11(b $_{1}$ –b $_{4}$ ). Surfing breakers are characterised by a finger-like wavefront gliding along the primary liquid–gas interface with a thin gas layer in between. This gas layer continuously releases air bubbles from its tail due to the movement of the wavefront and bulk liquid, introducing smaller bubbles with sizes $d/D\lt 0.05$ in the bubble-size distribution for $h/D=2.5$ . Additionally, the breakup of larger bubbles due to flow disturbances generates more small bubbles, as seen in figure 11(c $_{1}$ –c $_{4}$ ). Our findings on various breakup mechanisms and their effects on the bubble-size distribution are qualitatively similar to those reported by Chan et al. (Reference Chan, Mirjalili, Jain, Urzay, Mani and Moin2019) for the production of multi-scale gas bubbles in turbulent breaking waves. Finally, the sequences in figure 11(d $_{1}$ –d $_{2}$ ) show how droplets are formed due to the bubble collapse. The formation of such film droplets is also observed in experiments on bursting bubbles (Lhuissier & Villermaux Reference Lhuissier and Villermaux2012; Shaw & Deike Reference Shaw and Deike2024).

Figure 11.

(a_1-4 –c_1-4 ) Various interface breakup mechanisms associated with the production of multi-scale gas bubbles in the gas entrainment regime. (d_1-4 ) Birth of film droplets via the collapse of an entrained gas bubble. The simulation parameters are {Re, We, Bo, $h/D$ } = { $150, 1000, 1000, 2.5$ }.

Contrary to $h/D=2.5$ , the entrainment of gas bubbles at $h/D=1$ is driven by a different mechanism. As shown in figure 12, there is no vortex shedding at $h/D=1$ . Instead, shear layers formed due to the cylinder, although stable, tilt downward in the direction of the jet-like flow coming out of the gap above the cylinder. Subsequently, the flow within the gap drags the interface with it and forms a gas finger shown in figure 12 (also refer to figure 3 d $_{1}$ ,d $_{2}$ with similar dynamics). This gas finger continuously emits bubbles from its end via the interface breakup and creates a train of small bubbles with sizes typically less than $d/D=0.05$ . The train of newly formed bubbles travels along the path indicated by the brown arrows. During their transport, these bubbles frequently coalesce with other bubbles, forming larger ones. Eventually, fairly large bubbles deviate from their initial path and begin to rise vertically, as indicated by the grey arrows. The life cycle of a bubble ends when it collapses at the free surface. Thus, the bubble-size distribution for $h/d=1$ is regulated by the number of coalescence cascades each bubble undergoes. Relatively large bubbles can appear only through coalescence events. On the other hand, some bubbles do not coalesce and remain small. Such small bubbles drift in the background flow. For instance, notice gas bubbles between $x/D=5$ and $7$ in figure 12, which are trapped in the circulation formed by the incoming flow and backflow.

Figure 12.

Instantaneous snapshot of the primary liquid–gas interface, entrained gas bubbles, film droplets and shear layers (vorticity isolines in red and blue) arising from the cylinder. The inset provides a close-up view of the gas finger. The simulation parameters are indicated in the plot.

We note that Colagrossi et al. (Reference Colagrossi, Nikolov, Durante, Marrone and Souto-Iglesias2019) previously reported the entrainment of gas bubbles at $h/D=0.9$ , $ {We}=\infty$ , $ {Fr}=0.55$ and $ {Re}=180$ . However, their work did not provide detailed bubble statistics or explore the entrainment mechanism, as their main objective was a numerical comparison of various flow solvers. To further our analysis of gas entrainment at $h/D=1$ , we also explore a three-dimensional case in § 3.6.

3.5. Influence of $ { We}$ and $Re$ on gas entrainment

In this subsection, we briefly discuss the effects of the Weber ( $We$ ) and Reynolds ( $Re$ ) numbers on gas entrainment, specifically within the ranges $700\leqslant {We}\leqslant 1100$ and $50\leqslant {Re}\leqslant 150$ . In principle, for any fixed value of the Reynolds number, the Weber number can be independently adjusted by modifying the surface tension $\sigma$ , for instance, using surfactants. We use the time-averaged bubble count $\overline {\mathcal {N}}$ and size $\overline {d}/D$ as indicators of gas entrainment intensity. At a Bond number of $ {Bo}=1000$ and a submergence depth of $h/D=2.5$ , decreasing the Weber number gradually reduces the formation of gas bubbles, with $\overline {\mathcal {N}}$ approaching zero (see figure 13 a $_{1}$ ). Meanwhile, the time-averaged bubble size $\overline {d}/D$ fluctuates with $ {We}$ but remains within the $\pm 10\,\%$ bound when measured relative to any fixed $ {We}$ . This indicates that changes in $\overline {\mathcal {N}}$ alone provide a qualitative estimate of the entrained gas volume. Additionally, at $ {We}=700$ , gas bubble production becomes intermittent, resulting in a cylinder wake devoid of gas bubbles ( $\mathcal {N}=0$ ) during specific time intervals. This is evident from the time series in the inset of figure 13(a $_{1}$ ).

Figure 13.

Impact of the Reynolds ( $Re$ ) and Weber ( $We$ ) numbers on the time-averaged bubble count $\overline {\mathcal {N}}$ and size $\overline {d}/D$ in the gas entrainment regime for submergence depths $h/D=2.5$ and $1$ . The Bond number is fixed at $ {Bo}=1000$ . The time averaging is performed over the interval $20\leqslant tU/D\leqslant 100$ . The black vertical bars indicate ${\pm }10\,\%$ variations in $\overline {d}/D$ . Insets in (a ₁,a ₂) and (b ₁) show the time series of the number of bubbles $\mathcal {N}$ in the wake region for $ {We}=700$ and $ {Re}=50$ , respectively. The top inset in (b $_{2}$ ) illustrates an instantaneous snapshot of the primary liquid–gas interface, entrained gas bubbles and shear layers arising from the cylinder at $ {Re}=50$ . The bottom inset in (b $_{2}$ ) provides a zoomed-in view of the gas finger shown in the top inset.

When the submergence depth is reduced to $h/D=1$ in figure 13(a $_{2}$ ), the behaviour of $\overline {\mathcal {N}}$ becomes irregular. For instance, increasing $ {We}$ from $1000$ to $1100$ causes $\overline {\mathcal {N}}$ to drop. However, this reduction is compensated by a corresponding increase in $\overline {d}/D$ . Similarly, a slight rise in $\overline {\mathcal {N}}$ from $ {We}=800$ to $700$ is balanced by a corresponding reduction in $\overline {d}/D$ . Compared to the $h/D=2.5$ case shown in figure 13(a $_{1}$ ), surface tension is less effective in suppressing the wake bubble count at $h/D=1$ . At the same time, $\overline {d}/D$ drops by ${\approx }28\,\%$ when switching from $ {We}=1100$ to $700$ . We hypothesise that a broader range of Weber numbers may need to be explored in figure 13(a $_{2}$ ) to identify a clear trend in the variation of $\overline {\mathcal {N}}$ at $h/D=1$ . This is because the influence of flow disturbances on the free surface is already more pronounced for the small gap ratio of $h/D=1$ compared with the $h/D=2.5$ case shown in figure 13(a $_{1}$ ). As a result, the effect of change in surface tension on $\overline {\mathcal {N}}$ may not be immediately apparent and could lead to a non-monotonic trend with only minor variations in $\overline {\mathcal {N}}$ . Previously, in figure 8(a $_{2}$ ) for $ {We}=1000$ , we noted a spike in the bubble count $\mathcal {N}$ at the start of gas entrainment. Conversely, at $ {We}=700$ , surface tension stabilises the onset of gas entrainment, leading to a smoother start without any notable spike, as indicated by the time series in the inset of figure 13(a $_{2}$ ).

Figure 13(b $_{1}$ ) illustrates the effect $ {Re}$ on gas entrainment with parameters {We, Bo, $h/D$ } = { $1000, 1000, 2.5$ }. The time-averaged bubble count $\overline {\mathcal {N}}$ and size $\overline {d}/D$ show marginal variation in the range $100\leqslant {Re}\leqslant 150$ but drops sharply for $ {Re}\lt 100$ . At the lowest $ {Re}$ of $50$ , several changes in dynamics are observed. First, the entrainment of gas bubbles occurs in a sporadic fashion, as shown in the inset of figure 13(b $_{1}$ ). Second, an instantaneous snapshot of the wake structure in figure 14 reveals the absence of vortex shedding. Third and most importantly, we see the emergence of an interfacial wave in the wake region (see figure 14), differing from the localised deformation seen at higher Reynolds numbers (e.g. see figure 3 c $_{1}$ ). This wave pattern at $ {Re}=50$ is static relative to the background flow, but the wave crest near $x/D=5$ in figure 14 is unstable and undergoes occasional small-scale wave breaking, entraining gas bubbles for short intervals (see inset in figure 13 b $_{1}$ ).

Figure 14.

Instantaneous snapshot of the liquid–gas interface and the vorticity field at $tU/D=200$ for {Re, We, Bo, $h/D$ } = { $50, 1000, 1000, 2.5$ }. Note that Cartesian coordinates are in units of the cylinder diameter $D$ .

To characterise the interfacial wave in figure 14, we again use Lighthill’s linear theory of travelling capillary–gravity waves (Lighthill Reference Lighthill1978) as a reference (equation (3.2)). Given $ {We}= {Bo}=1000$ , the influence of the surface-tension-driven component in (3.2) is negligible. Substituting $c^{r}={-}U$ in (3.2) results in a gravity wave characterised by $\lambda /D=2\pi$ , which aligns with the spacing between the initial two wave crests in figure 14. Moving further from the cylinder, the distance between consecutive wave crests decreases by about $0.5D$ . Similar to our findings, Sheridan et al. (Reference Sheridan, Lin and Rockwell1995; Reference Sheridan, Lin and Rockwell1997) also reported the excitation of stationary interfacial waves caused by the presence of the cylinder in their experiments.

Finally, in figure 13(b $_{2}$ ), we examine a submergence depth of $h/D=1$ . The time-averaged bubble sizes $\overline {d}/D$ are in the similar range as previous combinations of { $ {Re}$ , $ {We}$ , $h/D$ }. For $100\leqslant {Re}\leqslant 150$ , the time-averaged bubble count $\overline {\mathcal {N}}$ almost reaches a plateau. Interestingly, for $ {Re}\lt 100$ , we observe the amplification in $\overline {\mathcal {N}}$ , in contrast to $h/D=2.5$ in figure 13(b $_{1}$ ). To understand this, we recall our discussion on the mechanism responsible for the entrainment of gas bubbles at $h/D=1$ , where it was noted that the production of gas bubbles is driven by the breakup of the gas finger (see figure 12). Lowering the Reynolds number increases the thickness of vorticity layers on the cylinder surface, promoting the formation of a very long gas finger due to shear flow in the gap, as shown in the insets of figure 13(b $_{2}$ ) for $ {Re}=50$ . In this case, the gas finger is as long as the cylinder diameter $D$ . Also, compare the relative sizes of gas fingers and vorticity layers close to the cylinder at $ {Re}=50$ in figure 13(b $_{2}$ ) and at $ {Re}=150$ in figure 12. The tail of the longer gas finger at $ {Re}=50$ is more unstable than the shorter finger at $ {Re}=150$ , leading to more frequent interface breakups. Consequently, this results in more gas bubbles being entrained over time at lower Reynolds numbers.

3.6. Gas entrainment in a three-dimensional flow set-up

In this final subsection, we provide an outlook on bubble production through gas entrainment in a three-dimensional configuration. For the range of Reynolds numbers investigated in this study, the occurrence of three-dimensional flow structures is unlikely (Barkley & Henderson Reference Barkley and Henderson1996; Williamson Reference Williamson1996). However, the role of dimensionality in interfacial phenomena involving topological changes, such as breakup events, cannot be determined a priori. If dimensional effects prevail to a greater extent, they may substantially influence the trends associated with various statistical properties of the entrained gas bubbles. Thus, to build further on our two-dimensional findings in the last two subsections, we demonstrate a three-dimensional case with parameters $ {Re}=150$ , $ {We}=1000$ , $ {Bo}=1000$ and $h/d=1$ . This particular parameter combination represents one of the extreme scenarios since it produces a relatively large quantity of gas bubbles through entrainment, as seen in figures 8 and 13. Notably, for $h/D=2.5$ , entrained gas bubbles penetrate to a shallower depth in the liquid phase compared with $h/D=1$ and instead merge with the free surface relatively quickly (see figure 8 b $_{1}$ ,b $_{2}$ ). Consequently, the impact of dimensionality on gas entrainment is expected to be short-lived for $h/D=2.5$ .

The current version of Basilisk (Reference Popinet2013–2024) does not support the use of the cut-cell module (see § 2) for three-dimensional multi-processor simulations involving immersed boundaries. Thus, we utilise the Computational Air-Sea Tank (CAS-Tank) solver, developed by Yang, Lu & Wang (Reference Yang, Lu and Wang2021), to simulate three-dimensional liquid–gas flow. Similar to the Basilisk library, CAS-Tank employs the VOF method for capturing the liquid–gas interface. Additionally, CAS-Tank incorporates the level-set function to compute geometrical parameters such as interface normal and curvature. The coupling between VOF and level set is achieved using the methodology proposed by Sussman & Puckett (Reference Sussman and Puckett2000). Moreover, the numerical stability of CAS-Tank is enhanced by implementing the mass–momentum consistent scheme introduced by Nangia et al. (Reference Nangia, Griffith, Patankar and Bhalla2019). For those interested in recent studies on free-surface flows using CAS-Tank, we refer the reader to Li, Yang & Zhang (Reference Li, Yang and Zhang2024) and Lu et al. (Reference Lu, Yang, He and Shen2024). Finally, the no-slip boundary condition at the curved liquid–cylinder boundary is enforced using the level-set-based sharp interface representation of the solid cylinder. See Cui et al. (Reference Cui, Yang, Jiang, Huang and Shen2017) for further details.

The size of the computational domain is set to $45D$ , $30D$ and $3D$ in the $x$ (streamwise), $y$ (transverse) and $z$ (spanwise) directions, respectively. The current domain size in the $x$ and $y$ directions yields the same lift force as the previously used larger domain of $80D\times 80D$ in two-dimensional simulations. From figure 12, it is evident that interface breakup and bubble formation occur near the cylinder, while the downstream liquid–gas interface further from the cylinder remains undisturbed. Furthermore, no vortex shedding is observed for the current parameters. Based on these observations from a previous two-dimensional simulation, we employ a combination of uniform and non-uniform Cartesian grids in our three-dimensional simulation. A refined uniform grid with a resolution of $0.025D$ ( $40$ grid cells per $D$ ) is applied within the subdomain extending in the ranges $-1.5\leqslant x/D\leqslant 8.5$ , $-3\leqslant y/D\leqslant 3$ and $-1.5\leqslant z/D\leqslant 1.5$ (the origin is positioned at the cylinder’s centre). Beyond this subdomain, the grid gradually coarsens towards the domain boundaries, reaching a maximum grid size of $0.18D$ at the edges. Using a two-dimensional simulation, it has been verified that further refining the uniform mesh resolution to $0.0166D$ ( $60$ grid cells per $D$ ) does not alter the breakup dynamics or the lift force. Lastly, a periodic boundary condition is applied in the spanwise direction, while the boundary conditions in the remaining directions are consistent with those used in the two-dimensional set-up.

Resolving three-dimensional flow and interface features at a moderate resolution within a small subdomain around the cylinder already leads to a substantial number of grid cells ( $55.728\times 10^{6}$ grid cells in the present case), demanding considerable computational resources. Unlike prior two-dimensional simulations, conducting an extensive parametric study in a three-dimensional set-up is not a viable option. Therefore, as an extension of our two-dimensional observations, we present only one model case where the system’s three-dimensional nature is crucial to interface dynamics.

Figure 15(a) provides an instantaneous snapshot of the vorticity field along with gas bubbles in the wake of the cylinder. Similar to the two-dimensional case shown in figure 12, one can observe tilted vorticity layers emerging from the cylinder’s surface. The vorticity layer formed due to the flow separation at the deformed liquid–gas interface is also visible in figure 15(a). This interfacial vorticity enters the wake region and spreads horizontally, forming what can be described as a vorticity carpet. Additionally, the interfacial vorticity plays a role in the cross-annihilation of the vorticity layer at the top of the cylinder and prevents vortex shedding, which is identical to our observation in figure 3(d $_{1}$ ). Although a similar vorticity annihilation mechanism is also present in figure 12, we have not shown the interfacial vorticity there to maintain a clear visualisation of gas bubbles. The qualitative similarities in flow structures between two- and three-dimensional set-ups are further substantiated by the lift coefficient $C_{l}$ with values of ${-}0.355$ and ${-}0.3452$ for the two- and three-dimensional cases, respectively.

Figure 15.

(a) Volume rendering of the vorticity field surrounding the cylinder and entrained gas bubbles in a three-dimensional flow setting. (b) Production of EGRs by interface breakup and the subsequent fragmentation of EGRs into bubbles in the wake region. The simulation parameters are {Re, We, Bo, $h/D$ } = { $150, 1000, 1000, 1$ }.

In a three-dimensional set-up, liquid flow in the gap above the cylinder generates a gas finger (see figure 15), similar to the two-dimensional result shown in figure 12. However, three-dimensional effects become apparent during the entrainment process. The breakup of the gas finger in figure 15(b $_{1}$ ,b $_{2}$ ) leads to the formation of cylindrical gas rolls (labelled as entrained gas roll(EGR)), unlike the planar bubbles observed in figure 12. The successive breakup of the gas finger creates a train of EGRs, analogous to the train of planar bubbles seen in figure 12. These EGRs subsequently undergo fragmentation due to background flow disturbances. A partially fragmented gas roll, EGR1, is highlighted in figure 15(b $_{1}$ ). Later, in figure 15(b $_{2}$ ), EGR1 undergoes complete fragmentation, leaving no remnants. Simultaneously, the fragmentation of the next gas roll in the sequence begins, as indicated by the partially fragmented EGR2 in figure 15(b $_{2}$ ). The ongoing fragmentation of EGRs results in a swarm of rising bubbles in the wake region. Thus, it is clear that the breakup mechanisms differ significantly between two- and three-dimensional flows.

We also collect bubble statistics using the detection algorithm developed by Herrmann (Reference Herrmann2010). A brief discussion on the implementation of the bubble detection method within the CAS-Tank solver can be found in Appendix C. Figure 16 shows the distribution of entrained rolls and bubbles in the wake. Unlike the two-dimensional result shown in figure 8(b $_{2}$ ), the high-concentration regions in figure 16(a $_{1}$ ) are positioned away from the location where the gas finger breaks. This shift is due to the fragmentation of EGRs into multiple bubbles, which occurs a few diameters away from the gas finger. The spread of entrained bubbles in the $y$ direction in figure 16(a $_{1}$ ), which is about twice the cylinder diameter, remains consistent with the two-dimensional case shown in figure 8(b $_{2}$ ). Observing the bubble distribution from above in figure 16(a $_{2}$ ) reveals a spanwise wave-like periodic pattern of high-concentration regions with a wavelength of ${\approx }D$ . The wavelength of this pattern is linked to how the perturbations at the interface of EGRs develop and the subsequent breakup process. However, further investigation is needed to verify whether the spanwise domain size affects the wavelength. The time-averaged bubble count in the present three-dimensional case is $\mathcal {\overline {N}}=536.07$ , which is higher than the two-dimensional bubble count in figure 8(a $_{2}$ ), as expected. The mean bubble sizes are $\overline {d}/D=0.05$ and $0.059$ for the two- and three-dimensional cases, which are still of the same order. However, gas entrainment in the three-dimensional system yields bubbles with a mean size $18{\,\%}$ larger than that of the two-dimensional counterpart.

Figure 16.

Projection of bubble coordinates onto the (a $_{1}$ ) $xy$ and (a $_{2}$ ) $xz$ planes in a three-dimensional gas entrainment process. Both projections include a collection of bubble coordinates recorded over the time window ${\Delta }tU/D=80$ . High-density regions with tightly clustered bubble coordinates are marked in red, whereas those with low bubble density are shown in blue. (b $_{1}$ ,b $_{2}$ ) Bubble-size ( $d/D$ ) distributions resulting from the gas entrainment phenomenon. Here $\mathcal {N}$ , $\mathcal {P}(d)$ and $a_{N}$ denote the number of bubbles, time-averaged bubble-size density and size of the finest computational cell, respectively. The black curve with green shaded area in (b $_{1}$ ) shows the bubble-size distribution fitted to the histograms. The simulation parameters are {Re, We, Bo, $h/D$ } = { $150, 1000, 1000, 1$ }.

The consequences of distinction in the breakup mechanisms between two- and three-dimensional cases become apparent upon examining corresponding bubble-size distributions shown in figures8(c $_{2}$ ) and 16(b $_{1}$ ). The two-dimensional size distribution (figure 8 c $_{2}$ ) loses its bimodal nature in a three-dimensional setting (figure 16 b $_{1}$ ). In three dimensions, most bubbles do not form directly from the free surface; instead, they result from the breakup of EGRs. Additionally, bubbles in the wake region are more densely packed in three dimensions due to a significantly higher bubble count. This increased density can dampen the subsequent fragmentation of bubbles caused by background flow disturbances, leading to larger bubbles and a modified size distribution compared with the two-dimensional entrainment case.

Building on existing studies of bubble entrainment and multi-phase turbulent flows (Deane & Stokes Reference Deane and Stokes2002; Hendrickson et al. Reference Hendrickson, Weymouth, Yu and Yue2019; Mostert et al. Reference Mostert, Popinet and Deike2022; Di Giorgio, Pirozzoli & Iafrati Reference Di Giorgio, Pirozzoli and Iafrati2022; Roccon, Zonta & Soldati Reference Roccon, Zonta and Soldati2023; Li et al. Reference Li, Yang and Zhang2024), we investigate how the time-averaged bubble-size density

(3.3) \begin{eqnarray} \mathcal {P}(d){=}\displaystyle {\frac {1}{(80D/U)}}\left (\int \limits ^{t{+}80D/U}_{t}\displaystyle {\frac {\mathcal {N}(d,t;b)}{Vb}{\textrm d}t}\right ) \end{eqnarray}

varies with the diameter $d/D$ of the entrained bubbles. Using a bin radius of $b=0.005D$ in (3.3), we compute $\mathcal {P}(d)$ by gathering statistics within a fluid volume $V$ , defined as a cuboid extending in the ranges $0\leqslant x\leqslant 8D$ , $-3D\leqslant y\leqslant h$ and $-1.5D\leqslant z\leqslant 1.5D$ .

Figure 16(b $_{2}$ ) presents the time-averaged bubble-size density, $\mathcal {P}(d)$ , for bubble sizes $d/D$ exceeding the size of the finest grid cell, $a_{N}$ . Previous studies across various turbulent flow scenarios have established that $\mathcal {P}(d)$ typically follows a ${-}10/3$ power law (Dean & Stokes Reference Deane and Stokes2002; Roccon et al. Reference Roccon, Zonta and Soldati2023; Li et al. Reference Li, Yang and Zhang2024). However, in the current case with unsteady laminar flow and ongoing air entertainment, $\mathcal {P}(d)$ declines more rapidly with increasing $d/D$ , as indicated by the ${-}9/2$ power law in figure 16(b $_{2}$ ). Such a deviation from the ${-}10/3$ power law is not unprecedented and was recently observed by Hendrickson et al. (Reference Hendrickson, Weymouth, Yu and Yue2019) in their large-eddy simulation study of the canonical stern geometry. A comprehensive investigation into the scaling behaviour of $\mathcal {P}(d)$ for different combinations of dimensionless parameters in the current set-up is planned for future work.