# Mathematical Models for the Novel Cathode Convexes in a Reduction Cell

Authors: Z. He; T. Xia; W. Xiong; Q. Shen; B. Li
Journal: Journal of Metallurgy
 (2013)

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## Abstract

A less magnitude of liquid aluminum deformation is required to shorten the anode-cathode distance so as to lower the electric energy consumption of the aluminum reduction cell. A mathematical model aimed to describe the electrolyte/aluminum two-phase flow in reduction cells, based on the computational fluid dynamics method, was developed to study the impacts of the cathode convexes on the electrolyte/aluminum interface deformation. The results showed that the magnitude of the two-phase interface deformation was reduced for about 17.2% with the novel cathode convexes; while at the same time, the washout of the melt on the ledge was also enhanced.


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## Body

## 1. Introduction

Aluminum and its aluminum material is the second large metal materials in the world whose consumption is only next to the steel. Aluminum metal was produced by the electrolysis of aluminum oxide dissolved in an aluminum-electrolyte fluoride mixture, which requires large amounts of electrical energy. Therefore, there is an urgent demand to lower energy consumption in the process of aluminum production. To decrease the energy consumption, the anode-cathode-distance (ACD) in reduction cells needs to be cut down [1]. However, due to the electrolyte/aluminum interface instability, the ACD cannot be too small to avoid reduction cell voltage fluctuation which may result in cell failure [2].The instability between the layer of molten aluminum and a slightly lighter electrolyte plays a defining role in the energy saving of aluminum reduction cells. Consequently, many researchers have focused on uncovering the mechanism of this instability. By using particle image velocimetry, Cooksey and Yang [3] experimentally investigated the onflow caused by anode gas and its bubble behavior in a full-scale, three-anode liquid model aluminum reduction cell. Pedchenko et al. [4] proposed a new solution for experimental modeling of the interfacial instability in which a tiny electrode stick was immerged into liquid metal of In-Ga-Sn on substitute of molten aluminum overlaid by electrolyte. Due to the difficulty to experimentally study the complex fluid flow phenomenon including molten aluminum, bath, and bubble agitation in aluminum reduction cells, most researchers focused on numerically modeling the magnetic fluid flow in reduction cells. Based on the nonlinear shallow water model, Kadkhodabeigi [5] built up a two dimensional model to study the electrolyte/aluminum interface instability and this model is superior to the linear model because linear model cannot determine the flow mode of the electrolyte and aluminum. Bojarevics and Pericleous [6] presented a nonlinear cell stability analysis for the 500 kA cell based on the shallow water model and showed the cathode surface unevenness and the presence of the anode bottom channels would sharply affect the cell stability. Li et al. [7] developed an improved finite-element model by building the contact mechanisms between steel bars and cathode blocks to make sure the voltage drops are properly distributed in the metal and the cathode. Based on the commercial package Ansys Li and Zhou [8] investigated the effects of various busbar configuration parameters on the stability of the reduction cell and proposed the improved busbar configuration. Bojarevics and Pericleous [9] proposed a simple shallow water model which allowed account of the channels and the interface stability is tested and compared for the channel effects. In their following studies, Bojarevics and Pericleous [10] extended their model to time dependent case and account for the electrolyte channels. Liu et al. [11] developed a current efficiency predictive model based on multiphase multicomponent flow, which provides a new approach for predicting current efficiency of aluminum reduction cells.What have been discussed above showed that though many works have been done to investigate the electrolyte/aluminum interface instability, neither reduction cells with inert anode [12] nor drained cathode cells [13] can decrease the energy consumption significantly in industrial scale experiment. Recently a new kind of aluminum reduction cell with novel cathodes has been tested industrially and the results showed that its energy consumption decreased for more than 1200 kWh/t-Al when compared with other reduction cells [14]. In the present work, the effects of novel cathode convexes on the interface instability were investigated to provide a theoretical foundation for improving the structure of the novel cathode and energy saving effects.


## 2. Numerical Models

Molten aluminum and electrolyte are treated as incompressible viscous fluid and electromagnetic force is the driving factor for melt to flow. Three dimensional Reynolds Average Navier-Stokes Equation was generally used to solve melt flow. Thek-ε turbulence model coupled with standard wall functions was adopted to account for the turbulence effects and second order discretization on governing equations was employed to improve the accuracy of the solution. Volume of Fluid (VOF) method was used to compute the aluminum/electrolyte two-phase flow field.The control equations of the aluminum/electrolyte flow field include the following.Continuity equation:(1)∂uj-∂xj=0.Momentum equation:(2)ρ∂ui-∂t+ρuj-∂ui-∂xj=-∂p-∂xi+∂∂x(μeff(∂ui-∂xj+∂uj-∂xx))+F,
where ρ is the density, ui- is the time averaged velocity component, p- is the time averaged pressure, μeff is the effective viscosity, and F is the volumetric force, which includes electromagnetic force Fem=J×B and gravity Fg, respectively.k-equation:
(3)∂(ρkui)∂xi=∂∂xj[[μ+μtσk]∂k∂xj]+Gk-ρε.ε-equation:
(4)∂(ρεui)∂xi=∂∂xj[[μ+μtσk]∂ε∂xj]+C1εεkGk-C2ερε2k,
where Gk represents the generation of turbulence kinetic energy due to the mean velocity gradients,
(5)G=μt∂uj∂xi(∂ui∂xj+∂uj∂xi),μeff=μ+μt.μt is turbulent viscosity:
(6)μt=ρCμk2ε.The typical constants of thek-εmodel of Launder and Spalding [15] are: c1ε=1.44, c2ε=1.92, cμ=0.09, σk=1.00, σε = 1.30.Volume fraction equation:(7)∂αq∂t+ui∂αq∂xi=0,∑q=1nαq=1,
where αq is the volume fraction of the qth phase, q=1,2 represent aluminum and electrolyte, respectively.The computational model in the present study is the second benchmark case in [16]; its geometry is shown in Figure 1. The computational parameters are listed in Table 1. In this benchmark case, magnetic field and current density distributions are simple analytical expressions, but their shape and magnitude are typical for real cells. No interanode gaps in the longitudinal direction are used.Table 1
Computational parameters.
Aluminum height
Electrolyte height
ACD
Aluminum density
Electrolyte density
0.2 m
0.18 m
0.045 m
2270 kg/m3
2070 kg/m3Figure 1
Geometry of the reduction cell.Firstly, Laplace equationΔV=0 was solved to get the current density distribution in the reduction cell, where V is the electrical potential. At the top of the cathode block, the current density is specified as the boundary condition: Jz=-5625-2500y2 (A/m2). At the top of anode blocks, zero electrical potential is specified. The electromagnetic force density fields, which drive the molten aluminum and electrolyte flow, are obtained as vector product of electric current density and magnetic field. The three components of the magnetic field inside the bath and the metal can be gotten in [16]. Electromagnetic force distributions in the middle plane of the molten aluminum are shown in Figure 2.Figure 2
Distribution of the horizontal electric-magnetic force in the middle plane of the liquid aluminum.


## 3. Results and Discussion

To validate the present model, the calculated results are compared with those presented in [16], as shown in Figure 3. The interface location is calculated where the volume fraction of the metal and of the bath is 0.5. The results in Figure 3 shows that the predictions of the present model agree well with those in [16] with a deviation not exceeding 5%, which laid the basis of further investigation. The aluminum/electrolyte interface shape is shown in Figure 4. Under the influence of the electromagnetic force which is the results of the horizontal magnetic field and the vertical electric current, molten aluminum was upheaved in the middle part. The peak uplift amplitude is about 2.4 cm and the max downwelling amplitude is about 4 cm, which approximately equal to the fluctuation magnitude in real cells. Current efficiency can be further improved by adequate fine adjustment in real reduction cells.Figure 3
Height of the electrolyte/aluminum interface at the middle line.Figure 4
Shape of the electrolyte/aluminum interface.Figure5 shows the velocity vector distributions in the middle plane of the molten aluminum. Four large vortices are formed in flow field and the size of the left vortex is larger than the right one. The velocity magnitude of the molten aluminum around the left vortex is larger, which makes the washout on the side ledge more severe.Figure 5
Distribution of the horizontal velocity vectors in the middle plane of the liquid aluminum.Interface shape of the reduction cell with cathode convexes is shown in Figure6. Similar to the case without convexes, molten aluminum was upheaved in the middle part, but the upheaval magnitude was weaken evidently when cathode convexes were used in the reduction cell. The peak uplift amplitude is about 1.5 cm and the max downwelling amplitude is about 3.8 cm. The peak uplift and downwelling amplitude are reduced by 37.5% and 5%, respectively, and the fluctuation magnitude is reduced by 17.2%.Figure 6
Shape of the electrolyte/aluminum interface with cathode convexes.With the cathode convexes, the magnitude of the electromagnetic force distributions in the middle plane of the molten aluminum is decreased for about 10%, but the distribution is very similar to what is shown in Figure2 (not shown here). The usage of the cathode convexes brings about the secondary flow of the molten aluminum between the cathode convexes as shown in Figure 7. This secondary flow could also be the reason for weaken interfacial fluctuation magnitude. As a result, the usage of cathode convex makes it possible to further decrease ACD and lower the energy consumption. Figure 8 shows the velocity vector distributions in the middle plane of the molten aluminum when cathode convexes are used. The flow mode of the molten aluminum has been changed greatly when compared with that shown in Figure 5. The washout of the molten aluminum on the side ledge is more serious than that in reduction cells without cathode convexes, which can be also observed in Figure 9. The wall shear stress on the side ledge is obviously larger when cathode convexes are used as shown in Figure 9.Figure 7
Velocity vector distribution at the cross planeZX, with Y=-1 (with convexes).Figure 8
Distribution of the horizontal velocity vectors in the middle plane of the liquid aluminum with cathode convexes.Wall shear stress distributions.
(a)
Without cathode convexes
(b)
With cathode convexesFigure10 compared the interface profile on the longitudinal axis located at the center of the cell with and without convex. It clearly showed the inhibition effects of the cathode convexes on the molten aluminum fluctuation.Figure 10
Height of the electrolyte/aluminum interface at the middle line.


## 4. Conclusions

A steady three-dimensional model of the electrolyte/aluminum two-phase flow in reduction cells was developed in the present study, in which time dependent interface motion is not considered. Based on this model electrolyte/aluminum interface fluctuations in the reduction cell with novel cathode convexes were investigated. The results showed that the model is able to represent the flow mode of the electrolyte/aluminum two-phase flow in reduction cells adequately. The model predicted that the magnitude of the two-phase interface deformation was reduced for about 17.2% with novel cathode convexes; while at the same time, the washout of the melt on the ledge was also enhanced.



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*Source: 196891-2013-03-31.xml*