Research Article  Open Access
Effect of Dynamic Center Region on the Flow and Mixing Efficiency in a New TriScrew Extruder Using 3D Finite Element Modeling
Abstract
Threedimensional finite element modeling of polymer melt flowing in a new corotating triscrew extruder was established with mesh superposition technique. Based on the particle tracking technology, three typical particle trajectories in the triscrew extruder were calculated using a 4thorderRungeKutta method to study the dynamic motions of the particles. Then the flow visualizations in the local center region were carried out. Moreover, the dispersive, distributive and stretching mixing efficiencies of the triscrew and twinscrew extruders were compared, respectively. The results show that when the particles move from one screw to another, there are great abrupt changes in the velocities and displacements, which induce the abrupt change in the stress magnitude. Most of particles, which are initially distributed in the inlet plane of the center region, fast flow out the outlet and don’t pass through any screw. This special phenomenon induces a series of new characteristics in the residence time distribution (RTD), flow number, segregation scale and time averaged efficiency. In comparison with the twinscrew extruder, the triscrew extruder has better mixing efficiency.
1. Introduction
Screw extruders are mostly used as pumping and mixing devices in polymer processing such as injection or blow molding. Their mixing efficiency and uniformity significantly affect the properties of the final product, energy consumption and costs. With the development of polymer industry, it is necessary to devise a new type of extrusion equipment with high output and better mixing efficiency. Based on the traditional singleand twinscrew extruders, a new type of triangle arranged triscrew extruder (hereinafter referred to as triscrew extruder) is put forward, which has three intermeshing regions and one dynamic center region [1]. Recently, the triscrew extruder has been paid more and more attention due to its high mixing ability and output. However, as a new mixing setup for polymer processing, the complex modeling and computational simulation of the triscrew extruder still remain very challenging, especially for the special dynamic center region with period changes of areas and geometric shapes. The mixing efficiency of the triscrew extruder depends on its flow profiles, especially axial flow. The dynamic and period changes of areas and geometric shapes of the center region cause the local variations in the axial flow, which can affect the local and overall mixing efficiencies of the triscrew extruder.
With the recent advances in computational fluid dynamics, it is possible to evaluate the flow in complex mixing geometries such as the twin screw and triscrew extruders using finite element method (FEM). In particular, there are studies about the flowing and mixing mechanisms in the single and twin screw extruders with 2D and 3D models [2–9]. In some way, the triscrew extruder is similar in simulation methods to the twinscrew extruder. However, the studies of flow and mixing in the triscrew extruders are more complex than the twinscrew extruder due to their complex geometric modeling such as three intermeshing regions and one center region. In particular, the center regions have dynamically periodic areas with the three screw rotations, which give rise to great effects on the flow and mixing of triscrew extruders. Hu and Chen [10] obtained the 3D isothermal flow rule in kneading blocks of the triscrew extruder with FEM based on the CFD package, Polyflow. The mixing index and cumulative residence time distribution (RTD) in the triscrew and twinscrew extruders were also investigated and compared. In addition, Jiang and Zhu [11] employed the simulation and experiments to verify the stronger conveying capacity in the triscrew extruder. The high shear frequency of material in the triscrew extruder was also found. In our previous researches, a quasithreedimensional modeling polymer melts flowing in a convey element of the triscrew extruders were established using FEM. The flow characteristics and mean mixing evaluations in the triscrew extruder were analyzed and compared with a twinscrew extruder [12]. Moreover, the temperature distributions, energy consumption, and capacity ratio in a triscrew extruder at different screw geometric parameters and operational conditions were studied [13]. In particular, the 2D finite element modeling was used to study the effect of the dynamic center region on the flow and mixing mechanism of the triscrew extruder. Based on the particle tracking technology, the nonlinear dynamics of a typical particle motions in the center region and the mixing process in the triscrew extruder were analyzed with Fast Fourier transform (FFT) spectrums and Poincaré maps [14]. However, no information was presented on the effect of the dynamic center region on the mixing evaluations in the triscrew extruder using threedimensional modeling.
In this work, three dimensional flow and mixing characteristics of the conveying element in a novel intermeshing corotating triscrew extruder were calculated using FEM with mesh superposition technique and CarreauYasuda viscous model. Firstly, the flow patterns in the triscrew extruder, especially in the center region were analyzed. Based on the velocity fields, the typical three singleparticle trajectories were tracked using a 4thorderRungeKutta method to analyze the dynamic motions of material in the triscrew extruder. Then, the flow visualizations in the special center region were carried out with particle trajectories technology. Moreover, the dispersive, distributive, and stretching mixing efficiencies in the triscrew extruder were calculated and compared with those in the twinscrew extruder. It should be noted that the center region has fast axial velocities, which gives rise to a series of new phenomenon in the RTD, flow numbers and segregation scale, and time averaged efficiency distributions. The aim of this work is to further understand the mixing mechanism and the special contributions of the center region to the entire triscrew extruder of axial flow and mixing efficiency with threedimensional modeling.
2. Modeling and Methods
2.1. Geometry and Meshing
The triscrew extruder investigated in this study has three screws, which array in a triangle and all clockwise rotation. In order to avoid screw interfere with one another, the numbers of screw flights must be odd, as shown in Figure 1(a). The geometric parameters of the triscrew extruder are depicted in Table 1. The 3D geometric modeling of the triscrew extruder is established with AutoCAD software. The finite element (FE) models are established using Gambit software with the mesh superposition technique (MST) without remeshing for the periodical geometric change. The screw elements and barrel are meshed individually. The barrel is meshed with quadrilateral element and the screws are meshed with the combination of quadrilateral and triangular elements, as shown in Figures 2(a) and 2(b).

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In order to catch the small velocity changes in the small clearances and near the walls, two boundary layer grids are employed in the FE model, as shown in Figure 2(d). At the same time, the refined grids are used in the special center region to catch the circumfluence phenomenon [13]. There are 41,997 elements and 11,166 nodes in the FE model of the triscrew extruder, respectively. The simulations are carried out using a commercial CFD package, Polyflow. In this work, the comparisons of mixing efficiencies in the triscrew and twinscrew extruder are employed to better understand the mixing mechanism in the triscrew extruder. Therefore, the sizes of geometrical configurations and grid densities of the screws in the triscrew are the same as the twinscrew extruder.
In order to check the convergence to obtain the validity of the gridindependent results for the triscrew extruders, the refined mesh FE model is used to the refined mesh FE model of the triscrew extruder were used to compare with the initial FE model. It can be found that the velocity magnitude curves of two kinds of meshes are almost overlapping. So the initial mesh is enough to insure the validity for the simulations.
2.2. Mathematical Models and Material
In this work, based on the quasisteady assumption, the 3D flow conditions are considered. The governing equations of nonNewtonian flow in the triscrew extruder with nonslip conditions are described as follows [15].
The form of the continuity and momentum equations can be expressed as where the velocity vector, is the polymer density, is the external body force per unit mass; is the stress tensor and can be expressed as where is the isotropic pressure, is the unit matrix, is the extra stress tensor and can be defined as where is the viscosity function of the local shear rate () and is the rateofdeformation tensor and is given as
In this study, a kind of reinforced plastics, LLDPE/SBS blending melt, is used in the triscrew extruder. This blending consists of linear low density polyethylene (LLDPE) and styrene block copolymers (SBS), in which the mass ratio of the LLDPE and SBS is 50 : 50. Due to the low shear rate in the experiment, it is appropriate to use the CarreauYasuda model to describe the rheological behavior of the blending as follows [16]: where is infinite shear viscosity, is a modelspecific relaxation time, and . is the second invariant of the rate of deformation tensor and is the powerlaw index, which is a property of a given material. The simulation parameters of the blending melts at 160°C are described in Table 2.

During the numerical calculations, the minielement and linear interpolations are used in the velocity and pressure calculations, respectively. The robust Picard iterative method is employed in the viscosity calculation due to the powerlaw index less than 0.75. The convergence criterion is set to in all the simulations. The rotational speeds of three screws are 40 rpm.
2.3. Mixing Efficiency Evaluating Models
The residence time distributions are obtained with the particle tracking technique by launching virtual particles into the flow fields obtained from time dependent simulation. The motions of massless particles are dominated only by the velocity field. The trajectory path followed by a particle is obtained by the following equation: where and are the positions of a particle at time and , respectively; is the velocity vector of the particle. The fourth order RungeKutta method is used to track the particle trajectories in the triscrew extruder.
Residence time is an important parameter to evaluate the distributive mixing of screw extruders, which is evaluated by the residence time distribution (RTD) function, and cumulative RTD function, . The cumulative RTD is defined as [17] where is the concentration of the trajectories at the exit section. is the time step. In order to accurately calculate the particle trajectories, a small iterative time step s corresponding to 6° of screw rotation is employed.
Initially, a large number of particles is distributed in some position of the flow domain. After running of the screws, the initial material particles disperse and gradually go to even distributions. The segregation scale is a measure of the size of the regions of homogenous concentration. It decreases when mixing improves and is defined as [15] where is a correlation coefficient for the concentration, and it gives the probability of finding a pair of random points with a relative distance and with the same concentration.
In order to evaluate the elongation flow mixing efficiency of the inside the screw extruders, the flow number is employed and defined as [18] where is the rate of deformation tensor and is the norm of the vorticity tensor. The fluid in screw extruder will be in the rotational and simple shear conditions with and , respectively, whereas the is 1.0 meaning the irrotational flow, such as pure elongational flow.
The instantaneous efficiency of stretching flow is defined as a local instantaneous efficiency of mixing given by where is the rate of strain tensor. The instantaneous efficiency can be thought of as the fraction of the energy dissipated locally that is used to stretch a fluid element at a given instant in a purely viscous fluid.
The timeaveraged efficiency is used to describe the stretching mixing efficiency and can be defined as [19] where is the instantaneous efficiency [19]. The typical timeaveraged efficiency will decrease with the increase of the mixing time.
3. Results and Discussion
3.1. Flow Patterns
The triscrew extruder in the center region has periodic geometrical configurations with screws rotation. In the present study, the mesh superposition technique (MST) is used to model triscrew extruders without calling upon remeshing. The axial velocity distributions in the triscrew extruder at crosssection with different time are described in Figure 2. It can be seen from Figure 2(a) that the positive axial velocity in the center region is obviously bigger than that in other regions when the area of the center region has maximal area ( s). It shows a better pumping ability in the center region. Therefore, the residence time for the material experienced in the center region is shorter than that in other regions. Whereas the center region has minimal area at crosssection in Figure 2(b) ( s), the values of axial velocities in the center region present negative, which reveal the backflow phenomenon in the center region. The velocity vector profiles in the center region are shown in Figures 2(c) and 2(d). Whenever the center region has biggest or smallest area, the vertex phenomenon induced by the drag effect of three screws always exists in the center region. It should be noted that the vertex phenomenon still appears in the minimal center region, which is different from what the literature reported [11]. According to the flow number distributions, the vertex flow in the center region presents rotating flow with little flow number.
3.2. Single Particle Trajectory Behaviors
To understand the flowing and mixing mechanisms in the complex triscrew extruder, three typical particles moving through one screw, three screws, and the center region with different residence time are selected to study their dynamic motions. Based on the particle tracking analysis, some periodical behaviors such as displacements, velocities, stretching rates, and stress magnitudes are calculated, respectively, as shown in Figures 3~5. The dynamic analysis of them may provide useful information about the process inside the triscrew extruder.
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Figure 3 shows the periodical behaviors of Particle 1 in the triscrew extruder, which is a typical motion moving through the three screws and only can be found in triscrew extruder. As can be seen from Figure 4(a), the particle moving through three screws has great transverse and axial displacements with resident time of 15 s. In Figure 3(a), each period presents this particle moving one whole turn through three screws. Each peak of the location corresponds to go through the intermeshing regions. When the particle passes through the three intermeshing regions, the motion of this particle gives rise to abrupt changes of the velocities, as shown in Figure 3(b). In comparison with velocities, the axial velocity of this particle is much less than the transverse velocity. This particle seldom presents backflow motions (negative axial velocity). on the other hand, the abrupt changes of the displacements and velocities result in the rise of stretching rates and stress magnitudes, as shown in Figures 3(c) and 3(d), respectively. The stress magnitude history in Figure 3(d) shows that this particle undergoes continuous and high stress magnitudes in the intermeshing regions, which is useful to increase the stress and stretching rates induced mixing.
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Figure 4 shows the periodical behaviors of Particle 2 in the triscrew extruder. After quickly moving 32 mm along the axial direction, this particle begins to move though only one screws during 5 s~20 s. The transverse displacements and velocities show regular periodical motions and no abrupt changes presents in the transverse displacement and velocity curves during moving around one screw, as shown in Figures 4(a) and 4(b). This is similar to singlescrew extruder. Correspondingly, the stretching rates and stress magnitudes undergoing by the Particle 2 are relatively small during 5 s~20 s, as shown in Figures 4(c) and 4(d). When the displacements and velocities of this particle have abrupt changes, such as moving from one screw to another during 0 s~5 s, this particle undergoes great stretching rates and stress magnitudes. By comparison, the stress magnitude of Particle 2 moving through one screw is less than those of Particle 1 obviously, and there are only little peak values of stress magnitudes, as shown in the Figure 4(d). Therefore, the abrupt changes of displacements and velocities can give rise to the increase of stress magnitudes likely due to the chaotic motion, which is helpful to enhance the mixing efficiency.
To understand the special motions of materials in the center region, Particle 3, only moving in the center region, is selected, as shown in Figure 5. This particle in Figure 5(a) moves in the triscrew extruder with residence time of only 2.5 s and little transverse displacements. However, the abrupt changes of displacements and velocities induced by the rotating screw flights result in the big values of stretching rates and stress magnitudes in the center region, as shown in Figures 5(c) and 5(d). In particular, the stress magnitudes of Particle 3 are even higher than those of Particle 1 and Particle 2, which is useful to enhance the stress and stretching induced mixing. So, the material particles in the center region have better stress induced mixing, although some vertex phenomenon existing in the center region.
3.3. Flow Visualization with Particle Trajectories
In order to investigate the convey performance of the polymer melts in the center region, 2000 particles are injected in the center region of inlet plane at s (0 revolution), as shown in Figure 6(a). With the increase of mixing time, most of particles quickly move from inlet to outlet along the center region. When s (0.83 revolutions), the first string “beads” of polymer melt arrive at the outlet plane. If the particles at inlet section are injected continuously, the consecutive strings of “beads” of polymer will come into being due to the periodic area changes of the center region. This numerical phenomenon shows a good agreement with the experiment results in Figure 6(b) by Jiang and Zhu [11]. Especially, a series of new characteristics distributed in the many mixing evaluation parameters such as dispersive and distributive mixing, are induced by this special phenomenon in the center region and will be discussed in the following sections. Please note that because the feeding position is not in the center region of triscrew extruder, there is only little material entering into the center region and directly flow out the outlet without passing through any one screw.
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3.4. Dispersive Mixing Efficiency
The elongational flow is known to be more effective than the simple shear flow for the dispersive mixing efficiency [20]. To understand the dispersive mixing mechanism in the triscrew extruder, the comparisons of the probability of flow numbers in the twinscrew and triscrew extruders are shown in Figure 7. When the flow numbers are between 0 and 0.6, the twinscrew extruder has bigger probability than the triscrew extruder to obtain high flow numbers. This is because the center region has strong pumping capacity, in which the material quickly flow out the exit with little flow numbers. However, when the flow numbers are between 0.6 and 1, the triscrew extruder has a higher probability than the twinscrew extruder to obtain great flow numbers. In addition, the maximal flow number distributions show that the triscrew extruder has bigger probability than the twinscrew extruder to obtain maximal flow numbers. In summary, most of polymer melts in the triscrew extruder have great maximal flow numbers, except for the center region. This is an advantage of the triscrew extruder in the elongational mixing ability.
The stress magnitudes are important parameters to evaluate the dispersive mixing induced by stress for the triscrew extruder. Figure 8 describes the comparison of mean stress magnitude values along axial distances between the triscrew and twinscrew extruders. From Figure 8, it is clear that the polymer melts undergo higher stress magnitudes in the triscrew extruder than in the twinscrew extruder. Therefore, the stress induced dispersive mixing efficiency is higher in the triscrew extruder than the twinscrew extruder. In addition, please note that with the increase of the axial distances, the differences of the stress values between the triscrew and twinscrew extruder increase. This is mainly because the part of polymer initial in the center region stays in the center region and has great axial velocities, which result in relative short time of experience stress effect. After 2.5 s (1.67 revolutions), those polymer particles (only staying in the center region) have flowed out the exit, and the rest of the particles move through the three screws or from center region into other regions with relatively long residence time and big stress magnitudes. So, the stress magnitudes in the entire triscrew extruder increase gradually along the axial distances.
3.5. Distributive Mixing Efficiency
The analysis of residence time distributions (RTD) has proved to be a useful tool to understand the distributive mixing efficiency in the mixer. The cumulative RTD and RTD are shown in Figures 9(a) and 9(b), respectively. From Figure 9(a), it can be seen that the starting point of the cumulative RTD in the triscrew extruder is about 1.25 s and that in the twinscrew extruder is about 2.5 s. At the same time, there is a platform with the slope of about zero in the cumulative RTD in Figure 9(a). It results in the two peaks in the RTD of the triscrew extruder, as shown in Figure 9(b), which is different from the twinscrew extruder in the RTD. This is mainly because the polymer melt in the center region has bigger axial velocities than these in other regions in the triscrew extruder. At 1.25 s (0.83 revolutions), the first string “beads” of polymer begins to flow out the outlet. So, the starting point of the cumulative RTD in the triscrew extruder is about 1.25 s. During 1.25 s~2.5 s, the particles initial distributed in the center region has been moved out the exit, so the platform appears in the cumulative RTD in Figure 9(a) and the first peak of polymer appears in the RTD in Figure 9(b).
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In addition, the residence time in the triscrew extruder ranges for 1.3 s~30 s, and that in the twinscrew extruder ranges for 2.5 s~24 s. It indicates that the twinscrew extruder has better selfcleanup ability than the triscrew extruder. on the other hand, the width of the RTD in the triscrew extruder is larger than that of the twin screw extruder, so the triscrew extruder has better axial distributive mixing efficiency than the twinscrew extruder.
Distributive mixing also can be evaluated by means of the segregation scale. The comparison of segregation scales between the triscrew and twinscrew extruder are shown in Figure 10. It can be seen that the two kinds of extruders show a rapid drop during 10 s due to the big segregated area. However, it is noted that there is an obvious increase of the segregation scales in the triscrew extruder during 0.9 s~1.7 s due to the fast axial velocities of polymer in the center region. After 10 s, the segregation scale of the triscrew extruder fluctuates smaller than that of twinscrew extruder. At the same time, the values of segregation scale in the triscrew extruder are less than in the twinscrew extruder, because the center region is continually varied from big to small and disturbs the streamline. It indicates that the triscrew extruder has better distributive mixing efficiency than the twinscrew extruder.
In order to study the local dispersive mixing efficiency in the triscrew extruder, 2000 particles are injected in the center region (mid), at screw channel region (bellow) and near the screw edge (tip), respectively. Figure 11 shows the cluster distribution index distributions initial in above three regions in the triscrew extruder. During 0~2.2 s, the value of cluster distribution index initial in the center region is smaller than in other regions. It implies that the better mixing efficiency in the center region. This is because the particles in the center region have great axial velocities and undergo the periodic effect of shearingsqueezingstretching by the three screws. After 5.6 s (3.7 revolutions), the cluster distribution index initial near the screw edge is smaller, followed by initial in the screw channel and the center region. However, it is noted that from our previous study [14], the 2D results of the cluster distribution index distributions show that the center region has minimal values of cluster distribution index than the other regions at crosssection. This difference between the 2D and 3D simulations of the cluster distribution index is because that the center region has better pumping ability, when the particles get to the outlet plane with short period of time, their movements are equivalent to close to the wall for the cluster distribution index with 3D simulation.
3.6. Stretching Efficiency
The mean timeaveraged efficiencies along the axial distances for the triscrew and twinscrew extruder are described in Figure 12. It is shown that the quick rise in the timeaveraged efficiency at the initial axial positions because the initial martial is prone to stretch due to its very small area. As the axial distances increase, the timeaveraged efficiencies of the two types of screw extruders decrease and level off at a value above zero, because the stretching area of material increase. It is necessary for an effective mixer with positive value of timeaveraged efficiency, indicating the strong reorientation effect. By comparison, it is found that the values of triscrew extruder are bigger than those of twinscrew extruder, which indicates that the triscrew extruder has more efficient stretching mixing than the twinscrew extruder. It is noted that with increase of axial distances, the difference between the triscrew and twinscrew extruder of the mean timeaveraged efficiency also increase because the particles initial in the center region have been moved out the outlet in the triscrew extruder.
4. Conclusions
(1)The special center region of the triscrew extruder has better pumping ability. Most of the particles initially distributed in the inlet plane of the center region quickly flow out the exit with the shape of consecutive strings “beads” and do not pass through any one screw. This special phenomenon gives rise to a series of new characteristics in the RTD, flow numbers and segregation scale, and time averaged efficiency. When the polymer particles initially in the center region have flow out the exit, the differences of the flow numbers, segregation scale and time averaged efficiency between the twinscrew and triscrew extruders increase. In particular, there are two peaks of the RTD curve in the triscrew extruder. (2)When the particles move from one screw to another, there are abrupt changes of velocities and displacements, which results in the increase of the stretching rates and stress magnitudes. Because the triscrew extruder has one more screw than the twinscrew, the particles in the triscrew extruder have high probabilities to move from one screw to another. This helps us to further understand the mixing mechanism in the triscrew, twinscrew and singlescrew extruders. In addition, the stress magnitudes of the particle only moving in the center region are even higher than those of the particle moving around three screws. This is beneficial to the stretching rates and stress induced mixing in the center region, although some vertex phenomenon existing in the center region.(3)For the local mixing, the cluster distribution index in the center region is higher than that in the screw channel, implying the poor mixing efficiency in the center region due to the fast axial velocities. In practice, we can use the combined screw elements (such as conveying elements and kneading elements) to reduce the axial flow velocity and increase the material residence time in the center region to further improve the overall mixing efficiency of the triscrew extruders.(4)Overall, the dispersive mixing efficiency evaluations such as flow number and stress magnitudes in the entire triscrew extruder are bigger than those in the twinscrew extruder. For the distributive mixing efficiency, the width of the RTD and in the values of segregation scale in the triscrew extruder is larger than that in the twin screw extruder. For the stretch mixing efficiency, the triscrew extruder has bigger mean logarithm of the area stretch than the twinscrew extruder. Therefore, the triscrew extruder has better distributive, dispersive, and stretching mixing efficiencies than the twinscrew extruder on the overall mixing efficiency.(5)It is noted that in this paper, the conveying element configurations of the twinscrew and triscrew extruders were only employed. Furthermore, we will further discuss the combined screw elements of the twin screw and triscrew extruders, such as conveying and kneading combined elements, to prove the advantage for the triscrew extruder.
Acknowledgments
This research project was funded by the National Natural Science Foundation of China (no. 50903042 and no. 51303075), Program for Liaoning Excellent Talents in the University (no. LJQ2013041), and the Science Foundation of Liaoning Educational Committee of China (no. L2010249 and L2010247).
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Copyright
Copyright © 2013 X. Z. Zhu et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.