Printer Friendly
The Free Library
22,728,043 articles and books

Study of mixing efficiency in roll-mills.


The two roll-mill geometry, invented in 1835 by Edwin Chaffee for mixing additives into rubber as well as for manufacturing films and sheets, operates by processing a molten polymer between the rotating rolls (cylinders). The very simple and versatile design of the roll-mills [ILLUSTRATION FOR FIGURE 1 OMITTED] accounts for their wide use in compounding and calendering calendering, a finishing process by which paper, plastics, rubber, or textiles are pressed into sheets and smoothed, glazed, polished, or given a moiré or embossed surface. . The main difference between the roll-mills and the calenders is the ratio between the roll radius and the minimum gap separation between the rolls, which is much higher for calenders (200 to 500) than for the roll-mills (30 to 60).

Most of the hydrodynamic hy·dro·dy·nam·ic   also hy·dro·dy·nam·i·cal
1. Of or relating to hydrodynamics.

2. Of, relating to, or operated by the force of liquid in motion.
 analyses for the two roll-mill flow geometry are extensions of Gaskell's (1) work using the lubrication lubrication, introduction of a substance between the contact surfaces of moving parts to reduce friction and to dissipate heat. A lubricant may be oil, grease, graphite, or any substance—gas, liquid, semisolid, or solid—that permits free action of  approximation (2-6). More recent developments use numerical methods of calculation, particularly the finite element See FEA.  method (7-10). Manas-Zloczower et al. (11) attempted to model the dispersive dispersive /dis·per·sive/ (-per´siv)
1. tending to become dispersed.

2. promoting dispersion.
 mixing process in roll-mills. These authors followed the Takserman-Krozer (12) calculation of the flow field using bipolar coordinates and their own model of agglomerate agglomerate

Large, coarse, angular rock fragments associated with lava flow that are ejected during explosive volcanic eruptions. Although they may appear to resemble sedimentary conglomerates, agglomerates are igneous rocks that consist almost wholly of angular or rounded
 rupture in simple shear Simple shear is a special case of deformation of a fluid where only one component of velocity vectors has a non-zero value:

 flow to predict the dynamics of agglomerate size distribution.

In this paper, we used a fluid dynamics fluid dynamics
n. (used with a sing. verb)
The branch of applied science that is concerned with the movement of gases and liquids.
 analysis package - FIDAP FIDAP Fluid Dynamics Analysis Package (Fluid Dynamics International, Inc.)  - based on the finite element method (13) to calculate the flow patterns in a two roll-mill geometry including the bank region. Dispersive mixing efficiency was analyzed in terms of shear stress shear stress
See shear.

shear stress

A form of stress that subjects an object to which force is applied to skew, tending to cause shear strain.
 distributions and elongational flow components. A frame invariant (programming) invariant - A rule, such as the ordering of an ordered list or heap, that applies throughout the life of a data structure or procedure. Each change to the data structure must maintain the correctness of the invariant.  parameter was proposed to quantify the elongational flow components.


Experimental observations show that the roll-mills lack lateral (axial) motion almost completely. Therefore a 2-D analysis will be sufficient to characterize the flow patterns. The field equations (Eqs 1 and 2) were solved for the isothermal flow Isothermal flow is a model of a fluid flow, which remains in the same temperature. In this model the temperature is constant while the stagnation temperature is changing. The change in stagation temperature occur because the temperature is constant but the velocity increasing.  of a power-law model fluid (Eq 3):

[Mathematical Expression A group of characters or symbols representing a quantity or an operation. See arithmetic expression.  Omitted]

[Mathematical Expression Omitted]

[Mathematical Expression Omitted]

where the power law index, n = 0.22, and the consistency index, m = 9.87 x [10.sup.4] N [multiplied by] [s.sup.0.22]/[m.sup.2], are describing the rheological behavior of a rubber compound with 65 parts SBR SBR - Spectral Band Replication  and 35 parts carbon black.

We used nonslip non·slip  
Designed to prevent or inhibit slipping: a bathtub with a nonslip surface.


designed to prevent slipping:
 boundary conditions on the two roll surfaces (namely a tangential tan·gen·tial   also tan·gen·tal
1. Of, relating to, or moving along or in the direction of a tangent.

2. Merely touching or slightly connected.

 velocity [U.sub.1] on the upper roll surface and a tangential velocity [U.sub.2] on the bottom roll surface). In the bank region, the free surface was calculated from the condition of no normal flow across this surface, i.e.

[Mathematical Expression Omitted]

where [Mathematical Expression Omitted] is the unit vector In mathematics, a unit vector in a normed vector space is a vector (often a spatial vector) whose length, (or magnitude) is 1 (the unit length). A unit vector is often written with a superscribed caret or “hat”, like this  normal to the free surface. For polymer melts of high viscosity and high capillary numbers, the surface tension does not play a significant role in the determination of the free surface (14).

The point of detachment of the polymer from the bottom roll and the corresponding blanket thickness on the upper roll were predicted based on Vlachopoulos's isothermal i·so·ther·mal
Of, relating to, or indicating equal or constant temperatures.

isothermal, isothermic

having the same temperature.
 model for the calendering of power-law fluids (15). For a power index of 0.22, this model predicts a ratio [h.sub.1]/[h.sub.0] of 1.27.

The free surface was determined by first selecting a free surface configuration for a given amount of material and solving the flow problem while keeping the nodes on the free surface fixed in space. With the results obtained for the velocity field, a residue for the boundary condition on the free surface is calculated, and the free surface is modified accordingly. In general, three to five iterations are sufficient to calculate the free surface. Figure 2 presents the results obtained in four successive iterations (after the fourth iteration the global relative error in the velocity field was below 3%). Figure 3 shows the mesh design for the entire flow domain with 1832 quadrilateral quadrilateral

having four sides.
 elements with nine nodal points in each element for a total of 6661 nodal points.

In order to analyze the dispersive mixing efficiency of the flow field, we looked at the elongational flow characteristics and the distribution of shear stresses generated. There are numerous studies reported in the literature that point to the increased efficiency of elongational flows in blending immiscible immiscible /im·mis·ci·ble/ (i-mis´i-b'l) not susceptible to being mixed.

Incapable of being mixed or blended, as oil and water.
 liquids (16-20) or breaking solid agglomerates into a continuous matrix (21,22). Also the magnitude of shear stresses generated is a key factor to be considered in analyzing dispersive mixing efficiency.

In order to quantify the elongational flow components, we propose a frame invariant flow strength parameter, [S.sub.f], defined as

[Mathematical Expression Omitted]

where [Mathematical Expression Omitted] is the rate of deformation tensor tensor, in mathematics, quantity that depends linearly on several vector variables and that varies covariantly with respect to some variables and contravariantly with respect to others when the coordinate axes are rotated (see Cartesian coordinates).  and [Mathematical Expression Omitted] is the Jaumann time derivative of [Mathematical Expression Omitted], (e.g. the time derivative of [Mathematical Expression Omitted] with respect to a frame that rotates with the angular velocity of the fluid element). The flow strength parameter [S.sub.f] has been used in the past to characterize various types of steady flows (23). Its value ranges from 0 for pure rotational flow to infinite for pure elongational flow. For simple shear flow, [S.sub.f] has a value of 1.

The frame invariant flow strength parameter can also be used in constitutive equations describing the rheological behavior of fluids in various flow fields. One example is Larson's model (24), which differentiates between the polymeric fluid response in various strength flow fields:

[Mathematical Expression Omitted]

where the coefficients [[Alpha].sub.1] and [[Alpha].sub.2] depend on the flow strength [S.sub.f], m is a power law index, and [Mathematical Expression Omitted] is the magnitude of [Mathematical Expression Omitted].

For graphical purposes, we normalized the flow strength parameter [S.sub.f] as in Eq 7 below:

[N.sub.s] [equivalent to] [S.sub.f]/1 + [S.sub.f] (7)

where [N.sub.s] ranges from 0 to 1.


Velocity profiles in the nip region between the two rolls and in the bank region are shown in Fig. 4. The boundary conditions used were a rotational speed of 40 cm/s for both rolls and a volume of material on the rolls equal to [1.609V.sub.min], where [V.sub.min] = 2[Pi][Rh.sub.0] is the minimum amount (per unit width) of polymer obtained considering a blanket thickness equal to the minimum gap separation. The development of a vortex in the bank region can be observed. The pressure contours for the same boundary conditions are shown in Fig. 5. The maximum pressure is generated in the nip region at x = -1.05 cm.

We have found that for an amount of material on the rolls exceeding approximately 1.5[V.sub.min], one or more vortices vor·ti·ces  
A plural of vortex.
 are developed in the bank region. Figures 6 and 7 compare the streamline contours for V = 1.194[V.sub.min] [ILLUSTRATION FOR FIGURE 6 OMITTED] and V = 1.609[V.sub.min] [ILLUSTRATION FOR FIGURE 7 OMITTED]. Later on we will show that the presence of vortices in the bank region has no beneficial effect on dispersive mixing efficiency.

Figures 8 and 9 show the distribution plots for the parameter [N.sub.s] and shear stress in the bank and nip regions of the roll-mill (for conditions similar to [ILLUSTRATION FOR FIGURE 4 OMITTED]). A strong (elongational) flow (high values of [N.sub.s]) is characteristic for the converging area to the nip region. This region shows also high shear stresses. In fact, it is the Y-shaped region clearly pictured in Fig. 9 that exhibits good flow characteristics for dispersive mixing (high values for [N.sub.s] and shear stress). The nip region shows overall low mixing capability in spite of the two high shear stress stripes near the roll surfaces. Also, the vortex region, exhibiting more rotational flow and low shear stresses is not effective in mixing. Figures 10 and 11 show the volumetric volumetric /vol·u·met·ric/ (vol?u-met´rik) pertaining to or accompanied by measurement in volumes.

Of or relating to measurement by volume.
 distributions for the parameter [N.sub.s] and shear stress. These Figures indicate a broad distribution of flow regimes for the roll-mills.

We looked at the influence of the friction ratio (ratio of the tangential velocities [U.sub.1]/[U.sub.2] for the two rolls) on the mixing efficiency of the roll-mills. Table 1 gives the average flow field characteristics for three different friction ratios (the average values were obtained by weighing the corresponding parameters for each element by the area of the element itself for the flow domain). The last two columns in the Table were calculated based on the concept of better mixing. In the mixing process, we would like the material to experience both high shear stresses and elongational flow at the same time. Although increasing the friction ratio generates higher shear stresses, the overall mixing performance, as judged from the last two columns in Table 1, is not improved.


In this paper, we presented the results of 2-D, isothermal flow simulations of a power-law model fluid in a two roll-mill geometry with a free surface in the bank region. The flow patterns were obtained by using a fluid dynamics analysis package based on the finite element method. The flow field was characterized for dispersive mixing efficiency in terms of shear stresses generated and a parameter quantifying elongational flow components. This last parameter was defined in a frame invariant manner, which makes it useful for further use in constitutive equations describing the rheological behavior of fluids as a function of the flow [TABULAR DATA FOR TABLE 1 OMITTED] field strength. We found that the converging region rather than the nip region provides better mixing flow characteristics. We also found that the presence of vortices in the bank region is not beneficial for dispersive mixing. The overall mixing performance is not improved by increasing the friction ratio between the two rolls.


The authors would like to acknowledge the use of computing services of the Ohio Supercomputer Center The Ohio Supercomputer Center (OSC) is a high performance computing and networking center headquartered in Columbus, Ohio, United States (OSC-Columbus) with a division in Springfield, Ohio (OSC-Springfield). It was stablished in 1987 by the Ohio Board of Regents. .


1. R. E. Gaskell, J. Appl. Mech., 17, 334 (1950).

2. J. T. Bergen and G. W. Scott, Jr., J. Appl. Mech., 18, 101 (1951).

3. P. R. Paslay, J. Appl. Mech., 24, 602 (1957).

4. J. M. McKelvey, Polymer Processing, Wiley Interscience, New York New York, state, United States
New York, Middle Atlantic state of the United States. It is bordered by Vermont, Massachusetts, Connecticut, and the Atlantic Ocean (E), New Jersey and Pennsylvania (S), Lakes Erie and Ontario and the Canadian province of

5. J. S. Chong, J. Appl. Polym. Sci., 12, 191 (1968).

6. W. W. Alston Jr. and K. N. Astill, J. Appl. Polym. Sci., 17, 3157 (1973).

7. C. Kiparissides and J. Vlachopoulos, Polym. Eng. Sci., 16, 712 (1976).

8. Z. Tadmor and C. G. Gogos, Principles of Polymer Processing, John Wiley, New York (1979).

9. J. F. Agassant and M. Espy, Polym. Eng. Sci., 25, 118 (1985).

10. E. Mitsoulis, J. Vlachopoulos, and F. A. Mirza, Polym. Eng. Sci., 25, 6 (1985).

11. I. Manas-Zloczower, A. Nir, and Z. Tadmor, Polym. Compos com·pos  
Compos mentis; sane: "The well-being of the country, even the survival of the world, depends on the president's being compos" Morton Kondracke.
., 6, 222 (1985).

12. R. Takserman-Krozer, G. Schenkel, and G. Ehrmann, Rheol. Acta., 14, 1066 (1975).

13. FIDAP Package Fluid Dynamics International, Inc., Evanston, Ill.

14. Charles L. Tucker III, Fundamentals of Computer Modeling for Polymer Processing, Oxford University Press, New York (1989).

15. J. Vlachopoulos and A. N. Hrymak, Polym. Eng. Sci., 20, 725 (1980).

16. H. P. Grace, Chem. Eng. Commun., 14, 225 (1982).

17. J. J. Elmendorp, Polym. Eng. Sci., 26, 418 (1986).

18. B. J. Bentley and L. G. Leal LEAL. Loyal; that which belongs to the law. , J. Fluid Mech., 167, 241 (1986).

19. F. D. Rumscheidt and S. G. Mason, J. Coll. Sci., 16, 238 (1961).

20. R. L. Powell and S. G. Mason, AIChE J., 28, 286 (1962).

21. I. Manas-Zloczower and D. L. Feke, Intern. Polym. Proc., II, 1185 (1988).

22. I. Manas-Zloczower and D. L. Feke, Intern. Polym. Proc., IV, 3 (1989).

23. R. G. Larson, Rheol. Acta, 24, 443 (1985).

24. R. G. Larson, Constitutive Equations for Polymer Melts and Solutions, Butterworth Publishers, Massachusetts (1988).
COPYRIGHT 1996 Society of Plastics Engineers, Inc.
No portion of this article can be reproduced without the express written permission from the copyright holder.
Copyright 1996 Gale, Cengage Learning. All rights reserved.

 Reader Opinion




Article Details
Printer friendly Cite/link Email Feedback
Author:Yao, Chih-Hsiang; Manas-Zloczower, Ica
Publication:Polymer Engineering and Science
Date:Feb 15, 1996
Previous Article:Multilayer rheology: a comparison of experimental data with modeling of multilayer shear flow.
Next Article:Experimental responses to step changes in temperature.

Related Articles
Custom mixing directory.
The mixer of the future today with ST rotors.
Review of processing equipment.
Twin roll mixing revolution.
Buhler's new Flaker.
Mixing Efficiency in a Pin Mixing Section for Single-Screw Extruders.
Rebuilding in-house capabilities.
Rebuilding in-house capabilities.
Rebuilding in-house capabilities.
Rebuilding in-house capabilities.

Terms of use | Copyright © 2014 Farlex, Inc. | Feedback | For webmasters