2. Numerical set-up

A critical assessment of the hypothesis of McLaren et al. (Reference McLaren, Kovar, Penn, Müller and Boyce2019) concerning the transition between rising and sinking granular clusters requires quantitative information on the gas flow near a cluster. However, this information is not easily accessible by experiments due to the opaque nature of granular matter. To this end, computational fluid dynamics coupled to a discrete element method (CFD-DEM) was applied to simulate a pseudo-two-dimensional vibro-gas-fluidized bed using cfdemCoupling $^{\circledR}$ (Kloss et al. Reference Kloss, Goniva, Hager, Amberger and Pirker2012). Details on the CFD-DEM model and the implemented equations can be found in Appendix A.

The gas flow field was calculated in cubic volume elements of 5 mm edge length using the built-in finite volume method solver of cfdemCoupling $^{\circledR}$ (Kloss et al. Reference Kloss, Goniva, Hager, Amberger and Pirker2012). The boundary conditions used in the CFD are summarized in table 1. Due to the coarse resolution of the CFD mesh, a full-slip boundary condition was implemented between solid walls and the gas phase (Beetstra, van der Hoef & Kuipers Reference Beetstra, van der Hoef and Kuipers2007; Li et al. Reference Li, Gopalakrishnan, Garg and Shahnam2012; Li, Zhang & Hernández-Jiménez Reference Li, Zhang and Hernández-Jiménez2016). However, the frictional and collisional contacts between the particles and the walls are fully resolved in the DEM. Studies of Zenit, Hunt & Brennen (Reference Zenit, Hunt and Brennen1997) and Berzi & Fraccarollo (Reference Berzi and Fraccarollo2015) have shown that particle collisions in inertia-dominated suspensions cause velocity and pressure fluctuations in the interstitial fluid that affect in turn the prevailing stresses and the effective viscosity of the fluid. In our work, the occurring fluid velocity fluctuations due to particle collisions are expected to be of the order of the magnitude of the peak particle velocities (that are ${\sim }0.1\ {\rm m}\ {\rm s}^{-1}$), however, the interstitial gas velocity is approximately 30 times faster on average. Thus, we expect the drag force to dominate over local fluid forces due the collision-induced velocity fluctuations. As the local void fraction $\epsilon$ is fairly constant throughout the entire particle packing, viscous stresses from local flow compressibility are expected to be small and only shear stresses for the fluid stress tensor were used in (A4). Moreover, in our simulations, the fluid density $\rho _g$ is low compared with the solid density of the particles. Thus, further fluid–particle interaction forces such as the added mass effect are minor and have been neglected (Sommerfeld Reference Sommerfeld2018).

Table 1.

Boundary conditions used in the CFD part.

The numerical set-up of the vibro-gas-fluidized bed resembled the experiments of McLaren et al. (Reference McLaren, Kovar, Penn, Müller and Boyce2019), see figure 1(a). Specifically, a box of width $W = 200\ \text {mm}$ and thickness $T = 10\ \text {mm}$ was filled up to a height of $H=250$ mm with a polydisperse mixture of spherical particles, referred to as the bulk phase. The bulk particles had a density $\rho _b = 6000\ \text {kg}\ \text {m}^{-3}$ and a mean diameter $d_b = 1.16\ \text {mm}$. Polydispersity was introduced to reduce crystallization effects of the packing (Pusey Reference Pusey1987). To this end, 60 mass-% of the bulk particles had the nominal diameter $d_b$ and 20 mass-% were attributed each to a particle size equal to $0.9d_b$ and $1.1d_b$, respectively. Inside the bulk phase, a square cuboid of width $W_c = 30\ \text {mm}$ and depth $T$ was cut out and filled with spherical particles of mean diameter $d_c$ and density $\rho _c$ (referred to as the granular cluster). The cluster particles followed the same polydispersity scheme as the bulk particles. The lower edge of the cluster was 30 mm above the bottom of the bed. Details on the DEM particle properties are found in table 2.

Table 2.

Particle properties used in the DEM part.

In the present study, we reduced the coefficient of restitution $e$ of the particles to 0.3 in order to speed up the simulations. However, a parameter study varying $e$ showed that a variation of $e$ in the range 0.1–0.95 has no significant influence on the evolution of granular bubbles, see Appendix E. At the bottom of the bed, an upwards gas flow with a superficial velocity $U = 1.13\ \text {m}\ \text {s}^{-1}$, density $\rho _g = 1.2\ \text {kg}\ \text {m}^{-3}$ and viscosity $\nu = 1.5\times 10^{-5} \text {m}^{2}\ \text {s}^{-1}$ entered the bed. The value of $U$ was equal to the minimum fluidization velocity of the bulk particles ($U_{mf,b}$), i.e. the velocity at which the drag force balances the weight of the bulk particles in the gravitational field $g = 9.81 \ \text {m}\ \text {s}^{-2}$ (Kunii & Levenspiel Reference Kunii and Levenspiel1991). Fluidization reduced frictional forces between the bulk particles, a key requirement for granular clusters being able to rise/sink. During the simulations, the box was subjected to a vertical, sinusoidal vibration with an amplitude $A = 1\ \text {mm}$ and frequency $f = 10\ \text {Hz}$. Applying vibration aids the creation of a mobilized state of the granular material and reduces the emergence of gas bubbles that otherwise would arise if the particles were fluidized by gas alone (McLaren et al. Reference McLaren, Kovar, Penn, Müller and Boyce2019, Reference McLaren, Metzger, Boyce and Müller2021). This allowed the evolution of the granular clusters to be unimpaired by the presence and motion of large gas bubbles. Importantly, applying only vibration without gas fluidization did not establish any convective flow patterns in the bulk phase and lead to an immobile granular cluster.

3. Experimental set-up

In an effort to validate the regimes found in numerical simulations, additional experiments were performed matching the numerical set-up. To this end, a series of granular clusters was prepared in a pseudo-two-dimensional vibro-gas-fluidized bed made of acrylic glass sheets. The inner dimensions of the bed were $W=200$ mm and $T=10$ mm. Analogue to the procedure described in Metzger et al. (Reference Metzger, McLaren, Pinzello, Conzelmann, Boyce and Müller2022), a granular cluster with $W_c=30$ mm was initialized in a bed of bulk particles, ensuring a configuration as shown in figure 1(a). The height of the granular bed was set to $H=250$ mm. Table 3 lists all combinations of bulk and cluster particles that have been used in the experiments. During the experiments, a shaker (Labworks Inc., ET-139) vertically vibrated the fluidized bed at identical conditions used in the simulations, i.e. $A=1$ mm, $f=10$ Hz and $\varGamma =0.4$. A flow of pressurized air was used to fluidize the granular material at incipient fluidization conditions, i.e. $U/U_{mf,b} = 1$. The gas flow was controlled by a mass flow controller (Bronkhorst AG, F-202AV) and passed through a humidifier before entering the fluidized bed. Humidification of the fluidizing gas mitigated the build-up of electrostatic charges on the granular material. Additionally, the bulk materials were treated with anti-static spray (Electrolube, ASA250). Neither humidification nor anti-static coating led to the formation of liquid bridges such that the granular material maintained its free-flowing properties. The emergence of a granular cluster was recorded with a digital camera (Canon, EOS 77D) at a frame rate of 50 Hz. Each experiment listed in table 3 was repeated three times.

Table 3.

Combination of bulk particles (index $b$) and cluster particles (index $c$) used in the experiments. All experiments were performed with vertical vibration ($A=1$ mm, $f=10$ Hz, $\varGamma =0.4$) and at incipient fluidization ($U/U_{mf,b}=1$). The particles were sieved and the $\pm$ sign indicates the upper and lower bounds of the particle size. The values of $d^{*}=d_c/d_b$, $\Delta \rho ^{*}=(\rho _c-\rho _g)(\rho _b-\rho _g)^{-1}$ and $Re_b=Ud_b/\nu$ were calculated based on the mean particle diameters and the nominal solid densities.

4. Derivation of the analytic gas shift model

First, we evaluate numerically the effect of a granular cluster on the gas flow field. Figures 2(a) and 2(b) display the gas flow in the vicinity and inside a granular cluster for two values of the relative particle diameter

(4.1)\begin{equation} d^{*} = d_c/d_b. \end{equation}

The black curves represent the gas streamlines and the background shows the dimensionless magnitude of the gas velocity $U^{*} = u/U$, where $u$ is the magnitude of the local superficial gas velocity. For $d^{*} = 1.5$, the streamlines concentrate inside the granular bubble and $U^{*}$ is higher in the cluster than in the surrounding bulk phase, i.e. gas flows preferentially through the granular cluster. For $d^{*} = 0.5$ the situation inverts. Such flow characteristics have been expected by Gilbertson & Eames (Reference Gilbertson and Eames2001) and McLaren et al. (Reference McLaren, Kovar, Penn, Müller and Boyce2019) due to an increased/reduced permeability with increasing/reduced particle size (Kozeny Reference Kozeny1927; Carman Reference Carman1937; Ergun Reference Ergun1952). The flow heterogeneity that is caused by the redirection of gas into or around a granular cluster will be referred to as ‘gas shift’ in the following. This gas shift is key to explaining the rising and sinking of granular bubbles and droplets and hence has to be incorporated in any predictive analytical model.

Figure 2.

Heterogeneous gas flow near a square-shaped granular cluster of width $W_c = 30\ \text {mm}$. (a,b) Simulated gas flow with $Re_b = Ud_b/\nu = 88.75$ through a packing with $d^{*} = 1.5$ and 0.5, respectively. The white boxes mark the edge of the granular cluster and the black curves show the gas streamlines. Here, $U^{*}$ is given by the background colour. (c) Decomposition of $U$ into $u_c$ (cluster) and $u_b$ (bulk phase) according to (4.2) and (4.4). (d) The value of $U^{*}$ along the horizontal line through the centre of a granular cluster with, respectively, $d^{*} = 1.5$ (blue) and $d^{*} = 0.5$ (red). Solid lines plot the Eulerian–Lagrangian simulation results; dashed lines plot the solutions of the analytical model.

In order to quantify the gas shift, we derive an analytical model for the gas flow around the granular cluster. For the model we apply a horizontal cut through the centre of the granular cluster that divides the bed into two regions: the cluster of dimensionless width $W^{*} = W_c/W$ and the bulk phase of dimensionless width $(1-W^{*})$, as shown in figure 2(c). The gas that enters the bed is decomposed into two parallel flows through these two regions. Gas is assumed to flow with a uniform dimensionless velocity $U_c^{*} = u_c/U$ and $U_b^{*} = u_b/U$ through the cluster and bulk phase, respectively. Due to its low velocity, the gas flow is assumed to be incompressible and the continuity equation reads

(4.2)\begin{equation} 1 = (1-W^{*} ) U_b^{*}+W^{*} U_c^{*}. \end{equation}

Figures 2(a) and 2(b) show parallel and equally spaced streamlines below and above the granular cluster, i.e. no horizontal pressure gradients exist in these regions. This implies that the gas flow through the cluster is driven by the same vertical pressure drop as the flow through the adjacent bulk phase. Ergun's equation (Ergun Reference Ergun1952) is used to quantify the pressure drop $\Delta p$ across a height $L$ of cluster or bulk phase particles

(4.3)\begin{equation} \frac{\Delta p_i}{L}=\frac{150\mu_g}{d_i^{2}}\frac{(1-\epsilon_i)^{2}}{\epsilon_i^{3}}u_i+\frac{1.75\rho_g}{d_i}\frac{1-\epsilon_i}{\epsilon_i^{3}} u_i^{2}, \end{equation}

where index $i = [b,c]$ denotes the bulk or cluster phase, respectively, and $\mu _g = \nu \rho _g$ is the dynamic gas viscosity. Equating $\Delta p_c/L = \Delta p_b /L$ and rewriting the equation in a non-dimensional form yields a correlation between $U_b^{*}$, $U_c^{*}$, $d^{*}$, the void fraction $\epsilon$ and the Reynolds number of the bulk phase $Re_b = Ud_b/\nu$, see Appendix B for the full derivation. According to our computational simulations, $\epsilon$ is very uniform in the bed ($\epsilon \approx 0.4$) for a large range of $d_c$ and $d_b$ provided that the coefficients of friction of the bulk and cluster particles are identical. Given these boundary conditions, we obtain

(4.4)\begin{equation} 0=\left(U_b^{*}-\frac{U_c^{*}}{d^{*^{2}}}\right)+\frac{Re_b}{k}\left(U_b^{*^{2}}-\frac{U_c^{*^{2}}}{d^{*}} \right), \end{equation}

with $k = 85.7(1-\epsilon ) \approx 51.42$. When $\mu _b$ and $\mu _c$ differ substantially, the assumption of a uniform void fraction $\epsilon$ is no longer satisfied. This case is described in Appendix D. In the following, only cases with identical coefficients of friction are considered. Combining (4.2) and (4.4) allows us to determine $U_c^{*}$ and $U_b^{*}$ as a function of $Re_b$, $d^{*}$ and $W^{*}$. Figure 2(d) compares the values of $U^{*}$ along a horizontal line through the centre of a cluster obtained by the Eulerian–Lagrangian simulation (solid lines) with the analytical model (dashed lines). For both values of $d^{*}$, the analytical model gives an accurate quantitative prediction of the average gas velocity inside the granular cluster and the bulk phase, although not all local effects (e.g. wall effects at $|x/W| = 0.5$ or local depletion/accumulation of gas flow in the bulk phase for $0.075\leqslant |x/W|\leqslant 0.16$ due to the gas shift) are captured in the analytical model. Based on this finding, $U_c^{*}$ can be used as a quantitative measure for the gas shift as $U_c^{*}>1$ indicates an increased gas flow inside the granular cluster compared with the inlet gas velocity $U$. Inversely, $U_c^{*} <1$ denotes a reduced gas flow in the cluster. A further evidence for the validity of the analytical gas shift model is presented in figure 3(a) plotting $U_c^{*}$ vs $d^{*}$. Here, the predictions of the gas shift model agree very well with the results of the Eulerian–Lagrangian simulations ($W^{*} = 0.15$). The analytical model further indicates that $U_c^{*}$ depends on the dimensionless width of the cluster $W^{*}$. An increase in $W^{*}$ yields higher values of $U_c^{*}$ for $d^{*} < 1$ and lower values for $d^{*} > 1$. This is because, for a fixed $W$, an increasing width of the granular cluster reduces the size of the bulk phase from which gas is withdrawn ($d^{*} > 1$) or into which additional gas is shifted ($d^{*} < 1$): thus, $U_c^{*} \rightarrow 1$ for $W^{*} \rightarrow 1$. Inversely, $U_c^{*}$ approaches a finite value for $W^{*}\rightarrow 0$. This solution represents the maximal obtainable gas shift to/from an infinitely small cluster for a given $d^{*}$ and $Re_b$.

Figure 3.

(a) Gas shift ($U^{*}_c$) occurring in granular clusters of particle size $d^{*}$ as predicted by (4.2) and (4.4) for a series of widths $W^{*}$. Triangles ($\vartriangle$) represent the results of the Eulerian–Lagrangian simulations for $U_c^{*}$ with $W^{*} = 0.15$. (b) Neutral buoyancy limits predicted for granular clusters of varying $W^{*}$ (4.2), (4.4) and (5.2) with $\Delta \rho ^{*} = (\rho _c -\rho _g)(\rho _b - \rho _g )^{-1}$. Both panels (a,b) use $Re_b = 88.75$ and ${Ar}_b = 3.40\times 10^{5}$.

5. Derivation of the neutral buoyancy limit

As the analytical model is able to accurately predict the gas shift to/from the granular cluster to the bulk phase, we address next the question of under which circumstances a granular cluster rises or sinks. In our model we use two assumptions: first, the inlet gas velocity $U$ is set to the minimum fluidization velocity of the bulk particles $U_{mf,b }$, i.e. the velocity of the gas flow required to induce a drag force that equals the weight of the particles. Here, $U_{mf,i}$ is determined from a force balance equating the pressure drop across the packing (4.3) with the weight of the packing per cross-sectional area such that

(5.1)\begin{equation} \frac{\Delta p_i}{L} =\frac{150\rho_g\nu}{d_i^{2}}\frac{(1-\epsilon)^{2}}{\epsilon^{3}}U_{mf,i}+ \frac{1.75\rho_g}{d_i}\frac{1-\epsilon}{\epsilon^{3}} U_{mf,i}^{2} = (1-\epsilon)(\rho_i -\rho_g)g, \end{equation}

where $i = [b, c]$ (Kunii & Levenspiel Reference Kunii and Levenspiel1991). Rearranging the right-hand sides and introducing the Reynolds number $Re_{mf,i}=d_i U_{mf,i} \nu ^{-1}$ and the Archimedes number ${Ar}_i = d_i^{3}(\rho _i-\rho _g)(\rho _g\nu ^{2})^{-1}$ yields

(5.2)\begin{equation} \frac{1.75}{\epsilon^{3}}Re_{mf,i}^{2}+ \frac{150(1-\epsilon)}{\epsilon^{3}} Re_{mf,i} = {Ar}_i. \end{equation}

Thus, for constant $\epsilon$ and $\nu$, $Re_{mf,b}$ and $U_{mf,b}$ are only functions of ${Ar}_b$ and $d_b$. Applying this assumption to the bulk particles ($\rho _b = 6000\ \text {kg}\ \text {m}^{-3}$, $d_b = 1.16\ \text {mm}$, $\epsilon = 0.4$) and air ($\rho _g = 1.2\ \text {kg}\ \text {m}^{-3}$, $\nu = 1.5\times 10^{-5}\ \text {m}^{2}\ \text {s}^{-1}$) yields $U = U_{mf,b} = 1.13\ \text {m}\ \text {s}^{-1}$.

Secondly, we assume that the rising/sinking of a cluster is driven by the degree of fluidization of the cluster particles due to the gas flow. This assumption is based on findings by Liu et al. (Reference Liu, Wang, Wu and Jia2010) and Li et al. (Reference Li, Wu, Rehman, Wang, Zhang and Xie2017a,Reference Li, Wu, Zhang and Wangb, Reference Li, Wu, Zhang and Wang2019) who have studied size separation in binary granular materials that have been subjected to combined vibration and fluidizing gas flow. Their research revealed a competition between vibration-induced size separation as well known from the Brazil nut effect (Rosato et al. Reference Rosato, Strandburg, Prinz and Swendsen1987; Knight, Jaeger & Nagel Reference Knight, Jaeger and Nagel1993; Huerta & Ruiz-Suárez Reference Huerta and Ruiz-Suárez2004) and its reverse (Hong, Quinn & Luding Reference Hong, Quinn and Luding2001; Jenkins & Yoon Reference Jenkins and Yoon2002; Trujillo, Alam & Herrmann Reference Trujillo, Alam and Herrmann2003; Breu et al. Reference Breu, Ensner, Kruelle and Rehberg2003; Shinbrot Reference Shinbrot2004; Alam, Trujillo & Herrmann Reference Alam, Trujillo and Herrmann2006) and gas-flow-induced size separation due to differences between the drag and gravitational forces acting on the particles. They found that if the gas velocity $U$ is close to or above the minimum fluidization velocity of a granular material, size separation can be governed by gas flow effects even for strong vibrational accelerations $\varGamma = A(2 {\rm \pi}f)^{2}/g > 1$. Under such boundary conditions, binary granular materials segregate according to their $U_{mf}$ values with the material of lower $U_{mf}$ segregating on top of the material with the higher $U_{mf}$. In our studies, we use $\varGamma = 0.4$ and $U=U_{mf,b}$, i.e. size separation is dominated by gas flow effects. Hence, we hypothesize that a granular bubble rises if the gas flow through the granular bubble gives rise to a drag force that is larger than the particle weight ($u_c > U_{mf,c}$) and the granular droplet sinks for $u_c < U_{mf,c}$; a granular cluster is neutrally buoyant if $u_c = U_{mf,c}$. From the analytical gas shift model we have $u_c = U U_c^{*}$ and $U_{mf,c}$ can be calculated via (5.2). Although vibration may reduce $U_{mf}$ of granular particles for $\varGamma \geqslant 1$ (Gupta & Mujumdar Reference Gupta and Mujumdar1980; Mawatari, Tatemoto & Noda Reference Mawatari, Tatemoto and Noda2003) and $\varGamma < 1$ (McLaren et al. Reference McLaren, Metzger, Boyce and Müller2021), we assumed that vibration does not affect appreciably the neutral buoyancy limit of the granular cluster because the net drag that leads to the rise of a granular bubble is dominated by the effective gas flow. Small fluctuations in the drag force due to vibration are expected to cancel out over a full vibration cycle. However, the dynamics of a granular material in a vibro-gas-fluidized bed might change once the vibrational acceleration exceeds gravity, i.e. for $\varGamma >1$. Hence, to restrict the potential influence of vibration on the emergence of a granular cluster and ensure validity of the previous assumptions, we limit the following derivation to $\varGamma < 1$.

With these two assumptions at hand, the neutral buoyancy limit can be calculated as a function of $d^{*}$, $W^{*}$, $Re_b$ and ${Ar}_b$. Figure 3(b) plots the relative density difference

(5.3)\begin{equation} \Delta\rho^{*} = \left(\rho_c -\rho_g\right)\left(\rho_b - \rho_g \right)^{{-}1} \end{equation}

required to establish a neutrally buoyant granular cluster of width $W^{*}$ as a function of $d^{*}$ at constant $U$ (later referred to as the ‘neutral buoyancy limit’). We observe that $\Delta \rho ^{*}$ decreases monotonically with increasing $d^{*}$. For $d^{*} < 1$, the density of the cluster particles must be larger than the density of the bulk particles to achieve neutral buoyancy, and vice versa for $d^{*} > 1$. The monotonic behaviour is due to the particle size dependence of $U_{mf,c}$. This dependence is depicted for $W^{*} = 1$, i.e. the entire bed is filled with cluster particles and no gas shift occurs ($U_c^{*} = 1$). Here, a constant $U$ leads to $\Delta \rho ^{*} \rightarrow \infty$ (0) when $d^{*} \rightarrow 0$ ($\infty$). For $W^{*} < 1$, the $\Delta \rho ^{*}$-curves increasingly flatten with decreasing $W^{*}$ due to the gas shift to/from the granular cluster. As confirmed in Appendix C, the density of the cluster particles must be equal to the density of the bulk particles to be neutrally buoyant for $W^{*}\rightarrow 0$ (dashed line in figure 3b). To summarize, our model predicts a granular bubble to rise if $\Delta \rho ^{*}$ is below the neutral buoyancy limit for any given ${Ar}_b$, $Re_b$, $W^{*}$ and $d^{*}$, otherwise a granular droplet sinks.

6. Construction of a regime map

Using the present analytical model, we constructed a regime map that predicts the rising or sinking of a granular bubble/droplet of a given size $W^{*}$ (figure 4). In order to test the validity of the regime map, numerical simulations were performed to probe the $\Delta \rho ^{*}$-$d^{*}$ space for a fixed cluster size of $W^{*} = 0.15$, $Re_b = 88.75$ and ${Ar}_b = 3.40\times 10^{5}$. Examples of such simulations are depicted in the time series shown in the figures 5, 8, 9, 10 and 11. The occurring motion patterns of the different granular clusters simulated were classified and marked in the regime map (figure 4). Five different regimes were identified: rising bubbles, rising fingers, disintegrating bubbles, sinking droplets and stagnant cones. The previous experimental study of McLaren et al. (Reference McLaren, Kovar, Penn, Müller and Boyce2019) has identified only the rising bubble and sinking droplet regimes. As can be seen in the regime map, the first four regimes are in agreement with our neutral buoyancy model and their regime boundaries coincide with the neutral buoyancy limit for $W^{*} = 0.15$ and $W^{*} = 0$ (i.e. $\Delta \rho ^{*} = 1$). Moreover, the experiments summarized in table 3 align with this regime map and agree with the numerical findings. As can be seen in figure 4, the existence of all five regimes can be confirmed by experiments. In the following, the characteristics of the different regimes will be discussed.

Figure 4.

Regime map for a granular cluster with $W^{*} = 0.15$, $Re_b = 88.75$ and ${Ar}_b = 3.40\times 10^{5}$. The solid and dashed lines are the neutral buoyancy limits for $W^{*} = 0.15$ and 0, respectively. The following regimes are observed: sinking droplet ($\vartriangle$, blue region), stagnant cone ($\triangledown$, purple region), rising finger ($\triangleright$, red region), rising bubble ($\triangleleft$, yellow region) and disintegrating bubble ($\Diamond$, green region). Coloured symbols are the results of the Eulerian–Lagrangian simulations. The grey filled symbols are results of the experiments listed in table 3. The images show a snapshot of the transformation of an initially square-shaped cluster in the respective regime.

Figure 5.

Time series of a rising bubble as obtained by (a) simulations and (b) experiments (table 3 A). Both rows show a cluster with $d^{*}=2$ and $\Delta \rho ^{*}=0.9$. Time steps of the images are $\Delta t = 0.5$ s for simulations and 1 s for experiments.

6.1. Rising bubble regime

Rising bubbles occur if $\Delta \rho ^{*}$ is below the neutral buoyancy limit of the cluster for $d^{*} \geqslant 1$ or below $\Delta \rho ^{*} = 1$ for $d^{*} < 1$ ($\triangleleft$, yellow region in figure 4). In this region, the cluster particles form a bubble that rises through the bulk phase to the top of the bed, as seen in figure 5. Rising granular bubbles form when the gas velocity in the bubble exceeds the minimum fluidization velocity of the cluster particles and an effective drag pushes the cluster particles upwards.

As can be seen in figure 6(b), the cluster particles within a granular bubble exhibit a circulation flow that resembles vortex structures found in fluid bubbles rising in a denser fluid (Hill & Henrici Reference Hill and Henrici1894; Hadamard Reference Hadamard1911; Rybczynski Reference Rybczynski1911; Batchelor Reference Batchelor2000). Particles from the centre of the bubble move towards its roof, whereas particles close to the side boundaries of the bubble move towards its bottom. At the bubble wake, individual particles detach, forming a tail. The existence of such an internal circulation pattern in granular bubbles points to a fluid-like state of granular matter in and around the bubble. A comparison of the panels of figure 6 reveals that the shape of the bubble and the circulation pattern therein depend on $\Delta \rho ^{*}$. For small values of $\Delta \rho ^{*}$ far away from the neutral buoyancy limit, e.g. $\Delta \rho ^{*}=0.4$ in (c), the bubble is spherical cap-shaped and exhibits a pronounced circulation flow. Increasing $\Delta \rho ^{*}$ to 0.8 (figure 6b) yields a spherical bubble and a circulation pattern which has striking similarities to Hill's spherical vortex (Hill & Henrici Reference Hill and Henrici1894). Increasing $\Delta \rho ^{*}$ further towards the neutral buoyancy limit leads to elongated bubbles with an attenuated inner circulation pattern and a pronounced tail, as can be seen in figure 6(a) and figure 7. This observation raises the question of why a tail is only formed for certain types of granular bubbles. To answer this, we have analysed the number of particles $N_{Tail}$ that are found in the tail after a bubble has reached a height of $y/H = 0.8$ for various combinations of $d^{*}$ and $\Delta \rho ^{*}$. Following Nitsche & Batchelor (Reference Nitsche and Batchelor1997), who have studied the break-up of a falling drop containing suspended particles in a liquid, all particles within a vertical distance of $1.5W_c$ below the topmost cluster particle are considered to be in the bubble. All other particles are regarded as part of the tail. Figure 7(a–d) shows the division of cluster particles into bubble and tail particles for granular bubbles using $d^{*}=1.25$ and $\Delta \rho ^{*}=0.4$, 0.7, 0.85, and 0.93, respectively. Again, the size of the tail increases for increasing $\Delta \rho ^{*}$. Figure 7(e) displays the ratio of $N_{{Tail}}$ to the total number of cluster particles $N$ as a function of $d^{*}$ and $\Delta \rho ^{*}$. It can be seen that, for $d^{*}>1$, $N_{{Tail}}/N$ is close to zero for small values of $\Delta \rho ^{*}$. Once $\Delta \rho ^{*}$ exceeds a certain threshold, the number of particles in the tail increases significantly with increasing cluster particle density. This threshold decreases monotonically from 0.8 for $d^{*}=1.25$ to 0.4 for $d^{*}=2$. Only for $d^{*}=2.75$ the threshold seems to be increasing again. For clusters with $d^{*}\leqslant 1$ no significant tail is formed at all and $N_{{Tail}}/N$ is (close to) zero. A possible explanation for the onset of tailing can be found when inspecting the effective drag acting on the cluster particles. According to Li et al. (Reference Li, Wu, Rehman, Wang, Zhang and Xie2017a), the effective acceleration on a particle in a vibro-gas-fluidized system can be expressed as $\Delta a/g= (|\boldsymbol {F}_{d,c}|-mg)/(mg)= 1-(U/U_{mf,c})^{2}$ provided $\epsilon$ is constant and drag dominates vibration in particle segregation. Imagine a single particle detaches from a granular bubble, leaves the zone of preferential gas flow and disperses in the bulk phase. This particle is only able to rise if the drag on it exceeds gravity, i.e. $\Delta a/g>0$, otherwise it would stay in the tail. Hence the particle would rise if the local superficial gas velocity $u$ exceeds the minimum fluidization velocity $U_{mf,c}$. Since the detached cluster particle is surrounded by bulk particles only, $u$ will be close to the inlet velocity of the fluidized bed $U$. Using this information, one can readily plot the effective drag for various diameters $d^{*}$ (figure 7f). Indeed, the roots of $\Delta a/g=0$ (for a given $d^{*}$) predict well the thresholds for tailing found in figure 7(e). However, simulations with $d^{*}=2.75$ fall outside this trend. This could be explained by the fact that the cluster particles are fairly large compared with the bulk particles and distort the local packing structure changing in turn the gas flow field. Despite the similarities of a granular bubble with sedimenting particle droplets (Nitsche & Batchelor Reference Nitsche and Batchelor1997), a mathematical relation for the rate of particles leaving the bubble has not yet been found.

Figure 6.

Motion of the cluster particles within a rising granular bubble for $\Delta \rho ^{*} = 0.9$ (a), 0.8 (b) and 0.4 (c). Trajectories of 100 particles are shown in a reference frame moving with the centre of mass of the bubble. The colour grading of the trajectories corresponds to the progressing time with dark violet for a bubble at $t(y/H=0.4)$ and bright yellow at $t(y/H=0.8)$. The background shows the location of the cluster particles (grey) when the top of the bubble has reached the height $y/H =0.8$ in the bed. All results were obtained from simulations with $W^{*}=0.15$, $Re_b = 88.75$, ${Ar}_b=3.40\times 10^{5}$ and $d^{*}=1.25$.

Figure 7.

Emergence of a particle tail in the wake of a rising granular bubble. Panels (a–d) show granular bubbles as a function of $\Delta \rho ^{*}$ with $d^{*} = 1.25$, when their roof has reached $y/H = 0.8$. In analogy to Nitsche & Batchelor (Reference Nitsche and Batchelor1997), all particles within a vertical distance of $1.5W_c$ from the topmost particle are considered to be part of the bubble (blue), otherwise the particles are considered to be part of the tail (grey). (e) The number of particles found in the tail $N_{Tail}$ normalized by the number of particles initialized in the bubble $N$. The value of $N_{{Tail}}/N$ depends on $d^{*}$ and $\Delta \rho ^{*}$. All points are obtained from numerical simulations of bubbles at $y/H = 0.8$. The lines are fitted power functions and only guidelines to the eyes. (f) Dependence of the normalized, effective drag of a cluster particle $\Delta a/g$ on $\Delta \rho ^{*}$ for varying $d^{*}$. $\Delta a/g= (|\boldsymbol {F}_{d,c}|-mg)/(mg)= 1-(U/U_{mf,c})^{2}$ for constant $\epsilon$ and $U\geqslant U_{mf,c}$ with $U_{mf,c}$ calculated from (5.2).

Figure 8.

Time series of a rising finger. (a) Euler–Lagrange simulation of a cluster with $d^{*}=1.75$, $\Delta \rho ^{*}=0.9$ and $\Delta t = 2$ s. (b) Experiment (table 3 G) with $d^{*}=1.8$, $\Delta \rho ^{*}=0.9$ and $\Delta t = 8$ s.

6.3. Disintegrating bubble regime

In contrast to the self-stabilized rising fingers, disintegrating bubbles form for $d^{*} < 1$ and $\Delta \rho ^{*}$ between unity and the neutral buoyancy limit ($\Diamond$, green region in figure 4). Here, the cluster can rise as a coherent granular bubble, but particle fluctuations and emerging gas bubbles during its rise induce its disintegration as seen in figure 9. According to our model, the granular bubble particles rise because $\Delta \rho ^{*}$ is below the neutral buoyancy limit. However, the low $U_{mf,c}$ of the cluster particles combined with the low permeability ($d^{*}<1$) of the cluster makes this granular bubble an unstable configuration. In the case that a small void is created in the granular cluster due to the vibrations, gas suddenly flows into this highly permeable region of the cluster and increases the gas velocity. The gas flow inflates the size of the void and pushes the cluster particles upwards into the bulk phase. Repetitions of this process lead to a disintegrating bubble. If the cluster particles are sufficiently small compared with the bulk particles, they disperse in the surrounding bulk phase filling the interstitial voids, as seen in figure 9(b).

Figure 9.

Time series of a disintegrating bubble. (a) Euler–Lagrange simulation of a cluster with $d^{*}=0.5$, $\Delta \rho ^{*}=1.1$ and $\Delta t = 2.4$ s. (b) Experiment (table 3 H) with $d^{*}=0.38$, $\Delta \rho ^{*}=1.11$ and $\Delta t = 6$ s. In the experiment, cluster particles are dark grey, bulk particles are light grey, whereas emerging gas bubbles are black.

6.4. Sinking droplet regime

For values of $\Delta \rho ^{*}$ significantly larger than unity, a granular droplet sinks ($\vartriangle$, blue region in figure 4), as the cluster particles are too heavy to be carried up by the drag exerted by the gas flow. During its descent, the sinking droplet flattens and performs ultimately a binary split (figure 10). The splitting of such a granular droplet is not caused by the cluster's proximity to the bottom of the fluidized bed, but is a property that also exists for larger distances to the confining walls. McLaren et al. (Reference McLaren, Kovar, Penn, Müller and Boyce2019) discovered the splitting of these droplets and a detailed analysis on the mechanism behind the droplet splitting can be found in Metzger et al. (Reference Metzger, McLaren, Pinzello, Conzelmann, Boyce and Müller2022).

Figure 10.

Time series of a sinking droplet. (a) Euler–Lagrange simulation of a cluster with $d^{*}=0.75$, $\Delta \rho ^{*}=2.38$ and $\Delta t = 1$ s. (b) Experiment (table 3 J) with $d^{*}=0.72$, $\Delta \rho ^{*}=2.42$ and $\Delta t = 2$ s.

6.5. Stagnant cone regime

Although the analytical model predicts that all droplets with $d^{*} > 1$ and $\Delta \rho ^{*}>1$ sink, there is a region for $\Delta \rho ^{*}\geqslant 1$ and $d^{*} > 1$, where droplets become stagnant and develop a conical shape, termed the stagnant cone ($\triangledown$, purple region in figure 4). The lower limit of the stagnant cone regime is at $\Delta \rho ^{*} = 1$ and the upper limit increases with increasing $d^{*}$. As the stagnant cone particles are too heavy to be neutrally buoyant ($\Delta \rho ^{*}>1$), the cluster acts as an additional load and inhibits fluidization of the bulk particles underneath the cluster. However, the net gravitational force of the cluster cannot overcome the interparticle friction in this unfluidized bulk region and thus the cluster remains stagnant. The formation of a cone (figure 11) can be explained by small fluctuations in the local gas velocity due to bed vibration. These fluctuations lead to a temporary fluidization of the cluster particles at the top of the cluster, such that they rearrange to an incipient granular finger. However, the fluctuations cannot maintain fluidization conditions for an extended duration of time, i.e. the cluster particles rest on top of the granular cluster. For $\Delta \rho ^{*}\rightarrow 1$, the cone sharpens further until it finally merges into a rising finger for $\Delta \rho ^{*}=1$.

Figure 11.

Time series of a stagnant cone. (a) Euler–Lagrange simulation of a cluster with $d^{*}=1.75$, $\Delta \rho ^{*}=1.2$ and $\Delta t = 4$ s. (b) Experiment (table 3 F) with $d^{*}=1.57$, $\Delta \rho ^{*}=1.16$ and $\Delta t = 60$ s.