Capillary Extrusion and Swell of a HDPE Melt Exhibiting Slip
|
|
- Oliver Benson
- 6 years ago
- Views:
Transcription
1 Capillary Extrusion and Swell of a HDPE Melt Exhibiting Slip MAHMOUD ANSARI Department of Chemical and Biological Engineering, The University of British Columbia, Vancouver, BC, V6T 1Z3, Canada EVAN MITSOULIS School of Mining Engineering and Metallurgy, National Technical University of Athens, Zografou, , Athens, Greece SAVVAS G. HATZIKIRIAKOS Department of Chemical and Biological Engineering, The University of British Columbia, Vancouver, BC, V6T 1Z3, Canada Received: November 8, 2011 Accepted: April 27, 2012 ABSTRACT: The extrudate (die) swell of a high-density polyethylene (HDPE) melt was studied both experimentally and numerically under slip conditions. The excess pressure drop due to entry (entrance pressure drop), the effect of pressure and temperature on viscosity, and the slip effects on the capillary data analysis have been examined. Using a series of capillary dies having different diameters, D, and length-to-diameter L/D ratios, a full rheological characterization has been carried out and the experimental data have been fitted both with a viscous model (Carreau Yasuda) and a viscoelastic one (the Kaye-Bernstein, Kearsley, Zapas/Papanastasiou, Scriven, Macosko or K-BKZ/PSM model). Particular emphasis has been placed on the effects of wall slip (significant for HDPE). It was found that viscous modeling underestimates the pressures drops (especially at Correspondence to: Savvas G. Hatzikiriakos; savvas. hatzi@ubc.ca. Contract grant sponsor: Natural Sciences and Engineering Research Council (NSERC) of Canada. Contract grant sponsor: National Technical University of Athens (NTUA), Athens, Grrece. Advances in Polymer Technology, Vol. 32, No. S1, E369 E385 (2013) C 2012 Wiley Periodicals, Inc.
2 the higher apparent shear rates and L/D ratios) and predicts virtually no extrudate swell. On the other hand, the viscoelastic simulations were capable of reproducing the experimental data well, and this was particularly true for the pressure drop. The prediction of viscoelastic extrudate swell presented a problem, since the simulations grossly overpredict it due to the highly elastic nature of the melt. This occurs despite the presence of severe slip at the wall, which brings the swell down considerably. At this point it is not clear whether this is due to the viscoelastic model used or other phenomena, such as sagging and/or cooling, when simply extruding in the atmosphere. C 2012 Wiley Periodicals, Inc. Adv Polym Techn 32: E369 E385, 2013; View this article online at wileyonlinelibrary.com. DOI /adv KEY WORDS: Capillary flow, Extrudate swell, HDPE, K-BKZ model, Slip Introduction Capillary rheometry is extensively used in both industry and academia to assess the rheological and processing behavior of polymer melts at high shear rates before testing their processability in full industrial scale. 1 One important aspect of material performance in processing is extrudate (die) swell. 2 4 This is the phenomenon of increasing area or diameter of the extrudate as it comes out from the die, whereupon it suddenly encounters a dramatically different type of flow, i.e., from a constrained flow within the die walls with no-slip or partial slip to a shear-free flow without walls outside the die. As a result of this change in boundary conditions, the polymer swells, sometimes dramatically. 2 The degree of swelling heavily depends on its past deformation history (memory effects), geometric characteristics of the die, and viscoelastic properties. 2 Extrudate swell was designated as a benchmark problem in rheology in the early 1970s. 2 The Newtonian problem was solved first by Tanner, 5 where it was established that Newtonian fluids swell about 13% when exiting from a tube die and 19% when exiting from a slit die, in agreement with experiments. 6 Since then, the majority of efforts have been directed toward the swelling of polymer solutions and melts, where substantial swelling was found experimentally and predicted numerically by a number of viscoelastic constitutive equations, such as the Oldroyd-B model, 7,8 the Phan-Thien/Tanner model, 9,10 and the integral K-BKZ model. 11,12 From the point of view of polymer solutions, success has been quite recently achieved by correctly predicting the extrudate swell of highly elastic Boger fluids with the K-BKZ model. 13 For polymer melts, the first successful simulations of extrudate swell for the highly elastic IUPAC LDPE melt were obtained by Luo and Tanner 11 with the K-BKZ model and verified and extended by Barakos and Mitsoulis 14 and Sun et al.. 15 Meanwhile, the other important polyethylene melt, namely high-density polyethylene (HDPE), was also studied experimentally and computationally 12,20 22 with mixed results. Namely, experiments by Orbey and Dealy 16 from annular dies were simulated with the K-BKZ model by Luo and Mitsoulis 12 and captured the major trends dictated by the die design and the viscoelastic nature of the HDPE melt; other experiments by Park et al. 17 were simulated by Kiriakidis and Mitsoulis 20 but for low apparent shear rates, where the swelling was moderate; and still other experiments by Koopmans 18,19 were simulated by Goublomme et al., 21 and Goublomme and Crochet 22 and showed that various integral models of the K-BKZ type had different degrees of success in predicting the swelling of HDPE, in most cases highly overestimating the experimental values. It is important to note that the situation for HDPE melts is somewhat different from other polymer melts. It is known that HDPE shows significant slip at the wall This greatly alters the deformation history, and if such effects are not taken into account, there is no hope that any constitutive equation would be able to correctly predict the magnitude of extrudate swell. The main objective of the study is to measure and predict the extrudate swell of a HDPE melt that exhibits significant slip effects. It is our goal to demonstrate that such slip effects have to be seriously considered before any reliable predictions E370 Advances in Polymer Technology DOI /adv
3 FIGURE 1. The experimental setup and method used for extrudate swell measurements. Die dimensions (D = 0.79 mm, L /D = 16), T = 190 C, γ A = 100 s 1. can be made on macroscopic quantities related to processing of polymers; in this case extrudate swell is the macroscopic quantity which is significant in processes such as extrusion, wire coating, and blow molding, among others. Experimental MATERIALS A HDPE melt was used in this work carefully selected to address the effects of slip on extrudate swell. This particular HDPE (m-hdpe) has a molecular weight of about 229,800 g/mol and a polydispersity index of Its rheological behavior has been studied previously by Ansari et al. 26 RHEOLOGICAL TESTING As discussed above, the rheology of this resin was studied by Ansari et al. 26 The master curves of its linear viscoelastic moduli are also reported here along with predictions of the K-BKZ constitutive equation for several rheological properties at the reference temperature of 190 C. An Instron capillary rheometer (constant piston speed) was used to determine the extrudate swell and the slip behavior of this polymer. The viscosity as a function of the wall shear stress, σ W,and apparent shear rate, γ A = 32Q/π D 3, where Q is the volumetric flow rate and D is the capillary diameter, is also studied as part of the slip study. Three series of dies having various diameters (D = 0.079, 0.122, and cm) and length-to-diameters ratios (L/D = 5, 16, and 33) were used (in total nine dies) to directly determine the viscosity and the slip behavior through the well-known Mooney analysis at 190 C. 27 The extrudate swell measurements were performed by analyzing extrudate images (immediately after die exit) taken with a high-resolution Nikon D-90 camera equipped with a Sigma DG Macro 2.8 lens attached to three Kenko extension tubes, which give 1.5 magnification in macrofocusing mode. A reference tip with known thickness has been used to estimate the extrudate diameters with respect to its size. Such a typical image is depicted in Fig. 1. The reported extrudate swells for each shear rate are the average of analyzing at least five different images. GOVERNING EQUATIONS AND RHEOLOGICAL MODELING We consider the conservation equations of mass, momentum, and energy for incompressible fluids, under nonisothermal, creeping, and steady flow conditions. These are written as 2,28 : ū = 0 (1) 0 = p + τ (2) ρc p ū T = k 2 T + τ : ū (3) where ρ is the density, ū is the velocity vector, p is the pressure, τ is the extra stress tensor, T is the temperature, C p is the heat capacity, and k is the thermal conductivity. The viscous stresses are given for inelastic non- Newtonian incompressible fluids by the relation 2 : τ = η( γ ) γ (4) Advances in Polymer Technology DOI /adv E371
4 where η( γ ) is the apparent non-newtonian viscosity, which is a function of the magnitude γ of the rate-of-strain tensor γ = ū + ū T, which is given by γ = ( 1 1 ( ) ) 1/2 2 II γ = γ : γ 2 where II γ is the second invariant of γ II γ = ( γ : γ ) = i (5) γ ij γ ij (6) To evaluate the role of viscoelasticity in the prediction of die swell, it is instructive to consider first purely viscous models in the simulations. Namely, the Carreau Yasuda model was used to fit the shear viscosity data of the HDPE melt. The Carreau Yasuda model is written as 1 : j η = η 0 [1 + (λ γ ) α ] n 1 α (7) where η 0 is the zero-shear-rate viscosity, λ is a time constant, n is the power law index, and α is the Yasuda exponent (2 for the simple Carreau model). The fitted viscosity of the HDPE melt by Eq. (7) is plotted in Fig. 2, whereas the parameters of the model are listed in Table I. We observe that the HDPE melt is very shear thinning for shear rates above 1s 1 giving a low power law index n = The Carreau Yasuda model fits the data well over the range of experiment results. It should be noted that our recent paper 29 with another HDPE melt having a higher polydispersity index PDI = 42 (herein desig- Shear viscosity, η (Pa.s) Experimental Carreau Yasuda model Shear Rate, γ (s -1 ) FIGURE 2. The shear viscosity of the HDPE melt at 190 C fitted with the Carreau Yasuda model (Eq. (7)) using the parameters listed in Table I. TABLE I Parameters for the HDPE Melt Obeying the Carreau Yasuda Model (Eq. (7)) at 190 C Parameter Value η 0 191,660 Pa s λ s n α natedashdpe-42)hasusedthecrossmodelforits fitting. However, the Carreau Yasuda model gives a better fit to the present data than the Cross model. Viscoelasticity is included in the present work via an appropriate rheological model for the stresses. This is a K-BKZ equation proposed by Papanastasiou et al. 30 and modified by Luo and Tanner. 11 This is written as τ = 1 t 1 θ N a k exp ( t ) t λ k k=1 α (α 3)+β I C 1 +(1 β)i C [C 1 t (t ) + θc t (t )]dt where t is the current time, λ k and a k are the relaxation times and relaxation modulus coefficients, N is the number of relaxation modes, α and β are material constants, and I C, I 1 C are the first invariants of the Cauchy Green tensor C t and its inverse C 1 t,the Finger strain tensor. The material constant θ is given by λ k N 2 = θ N 1 1 θ (8) (9) where N 1 and N 2 are the first and second normal stress differences, respectively. It is noted that θ is not zero for polymer melts, which possess a nonzero second normal stress difference. Its usual range is between 0.1 and 0.2 in accordance with experimental findings. 1,2 As discussed above, experiments were performed in the parallel plate and extensional rheometers for the HDPE melt to rheologically characterize it. Figure 3 shows plots of the master dynamic moduli G and G for HDPE at the reference temperature of 190 C. The model predictions obtained by fitting the experimental data to Eq. (8) with a spectrum of relaxation times, λ k,and coefficients, a k, determined E372 Advances in Polymer Technology DOI /adv
5 Dynamic moduli, G, G (Pa) Frequency, ω (rad/s) Fit G G FIGURE 3. Experimental data (symbols) and model predictions of storage (G ) and loss (G ) moduli for the HDPE melt at 190 C using the relaxation times listed in Table II. TABLE II Relaxation Spectrum and Material Constants for the HDPE Melt Obeying the K-BKZ Model (Eq. (8)) at 190 C (α = , β = 0.6, θ = 0, λ = 96 s, η 0 = 190,425 Pa s) k λ k (s) a k (Pa) , , , , , , , by a nonlinear regression package, 31 are also plotted. The parameters found from the fitting procedure are listed in Table II. The relaxation spectrum is used to find the average relaxation time, λ, and zeroshear-rate viscosity, η 0, according to the following formulas: λ = N k=1 a kλ 2 k N k=1 a kλ k (10) η 0 = N a k λ k (11) k=1 The values of these parameters are λ = 96 s and η 0 = 190,425 Pa s, indicating an elastic melt with a high average relaxation time. It should be noted that the other HDPE-42 used in our recent paper 29 has Shear (elongational) viscosity, η S(E) (Pa. s) η Ε Ν 1 η S Shear (elongational) rate, γ (ε) (s -1 ) FIGURE 4. Experimental data (solid symbols) and model predictions of shear viscosity, η S, first normal stress difference, N 1, and elongational viscosity, η E,for the HDPE melt at 190 C using the K-BKZ model (Eq. (8)) with the parameters listed in Table II. The N 1 data have been obtained from G and G according to Laun s formula (Eq. (12)). a much lower λ = s and a lower η 0 = 140,073 Pa s. From the data on G and G, it is possible to use Laun s formula to obtain data for the first normal stress difference N 1 according to Dealy and Wissbrun 1 : First normal stress difference, N 1 (Pa) ( G N 1 = 2G [1 ) ] (12) G Figure 4 presents plots of a number of calculated and experimental material functions for the HDPE melt at the reference temperature of 190 C. Namely, data for the shear viscosity, η S, the elongational viscosity, η E, and the first normal stress difference, N 1, are plotted as functions of corresponding rates (shear or extensional). The parameter β that controls the calculated elongational viscosity was fitted by using the extensional behavior of the melt, which is essentially equal to 3η +. It can be seen that the overall rheological representation of all material functions is excellent. NONISOTHERMAL MODELING The nonisothermal modeling follows the one given in earlier publications 11,32 34 and will not Advances in Polymer Technology DOI /adv E373
6 be repeated here. Suffice it to say that it employs the Arrhenius temperature shifting function, a T,given by Dealy and Wissbrun 1 and Tanner 2 : a T (T) = η [ ( E 1 = exp η 0 R g T 1 )] T 0 (13) In the above, η 0 is a zero-shear viscosity at T 0, E is the activation energy constant, R g is the ideal gas constant, and T 0 is a reference temperature (in K). The activation energy constant E can be determined from the shift factors obtained by applying the time temperature superposition to get the master curves plotted in Fig. 2. It was found to be 28,840 J/mol, typical for a HDPE resin. In the present work, we have applied the above equation to derive the nonisothermal constitutive equation from the isothermal one. This method is based on the time temperature superposition principle and simply consists of shifting the relaxation times λ k from the temperature history within the material s internal timescale t. 32 The equation used to shift the relaxation times in the material s history is given by 34 λ k (T (t )) = λ k (T 0 )a T (T (t )) (14) where T is the temperature at time t. The viscoelastic stresses calculated by the nonisothermal version of the above constitutive equation (Eq. (8)) enter in the energy equation (Eq. (13)) as a contribution to the viscous dissipation term. The thermal properties of the melt have been gathered from various sources and are given in our recent publication. 29 The values are reproduced in Table III. TABLE III Values of the Various Parameters for the HDPE Melt at 190 C Parameter Value References β p MPa 1 37,38 β sl 18,800 cm/(s MPa b ) This work b 4.0 This work ρ g/cm 3 54 C p J/(g K) 54 k J/(s cm K) 54 E 28,840 J/mol This work R g J/(mol K) 54 T C (463 K) This work The various thermal and flow parameters are combined to give appropriate dimensionless numbers. 35,36 The relevant ones here are the Peclet number, Pe, and the Nahme Griffith number, Na. These are defined as Pe = ρc pur k Na = ηeu2 kr g T0 2 (15) (16) where η = f (U/R) is a nominal viscosity given by the Carreau Yasuda model (Eq. (7)) at a nominal shear rate of U/R and U(= γ A R/4) is the average velocity in the capillary die. The Pe number represents the ratio of heat convection to conduction, and the Na number represents the ratio of viscous dissipation to conduction and indicates the extent of coupling between the momentum and energy equations. A thorough discussion of these effects in nonisothermal polymer melt flow is given by Winter. 35 With the above properties and a die radius R = 0.04 cm, the dimensionless thermal numbers are in the range: 4 < Pe < 814 and < Na < 1, showing a relatively strong convection (Pe 1) and a weak to moderate coupling between momentum and energy equations (Na 1). A value of Na > 1 indicates temperature nonuniformities generated by viscous dissipation and a strong coupling between momentum and energy equations. More details are given in Table IV. PRESSURE-DEPENDENT MODELING Similarly with the time temperature superposition principle where the stresses are calculated at a different temperature using the shift factor a T,the time pressure superposition principle can be used to account for the pressure effect on the stresses. In both cases of viscous or viscoelastic models, the new stresses are calculated using the pressure-shift factor a p. For viscous models, the following Barus equation is used to modify the viscosity 1 : a p η η p0 = exp(β p p) (17) where η is the viscosity at absolute pressure p, η p0 is the viscosity at ambient pressure, and β p is the pressure coefficient. This coefficient has been reported to be GPa 1 for HDPE. 37,38 E374 Advances in Polymer Technology DOI /adv
7 TABLE IV Range of the Dimensionless Parameters in the Flow of HDPE Melt at 190 C (Die Radius R = 0.04 cm) Apparent Shear Peclet Number, Nahme Number, Pressure-Shift Slip Parameter, Rate, γ A (s 1 ) Pe Na Parameter, B p B sl For viscoelastic models, such as the K-BKZ model (Eq. (8)), the pressure-shift factor modifies the relaxation moduli, a k, according to a k (p(t )) = a k (p 0 )a p (p(t )) (18) This is equivalent to multiplying the stresses by a p, according to Eq. (17). It should be noted that a p is an exponential function of β p, which itself may depend on pressure p, as was the case for the low-density polyethylene (LDPE) melt. 26 Since in a flow field negative pressures may appear, especially around singularities as is the case in contraction flows, special care must be taken numerically to handle these functions for negative numbers. Failure to do so leads to nonsensical results and/or to divergence. The pressure dependence of the viscosity gives rise to the dimensionless pressure-shift parameter, B p. This is defined as B p = β p ηu R (19) When B p = 0, we have no pressure dependence of the viscosity. For the present data, we get < B p < , showing a weak dependence of viscosity on pressure in the range of simulations, unlike the LDPE melt. 39 More details are given in Table IV. SLIP-AT-THE-WALL MODELING In the case of slip effects at the wall, the usual noslip velocity at the solid boundaries is replaced by a slip law of the following form 1,23,24 : u sl = β sl σ b w (20) where u sl is the slip velocity, σ w is the shear stress at the die wall, β sl is the slip coefficient, and b is the slip exponent. As it will be shown below, the values found experimentally for this HDPE melt are β sl = mm/s/mpa b and b = 4. It should be noted that due to its high polydispersity, the selected HDPE does not undergo a stick-slip transition, and therefore both the flow curve and slip velocity are continuous functions. In fact, Eq. (20) describes its complete slip behavior from very small to very high shear rates. For narrow molecular weight HDPEs, and some other melts such as polybutadienes, stickslip may occur; in those cases the slip behavior is a double-valued function of shear stress. 25,40,41 In two-dimensional simulations, the above law means that the tangential velocity on the boundary is given by the slip law, while the normal velocity is set to zero, i.e., β sl ( t n : τ) b = ( t ū), n ū = 0 (21) where n is the unit outward normal vector to a surface, t is the tangential unit vector in the direction of flow, and the rest of symbols are defined above. Implementation of slip in similar flow geometries for a polypropylene (PP) melt has been previously carried out by Mitsoulis et al. 42 and in our recent work Ansari et al. 43 The corresponding dimensionless slip coefficient, B sl, is a measure of fluid slip at the wall: B sl = β sl η b U ( ) U b (22) R When B sl = 0, we have no-slip conditions. When B sl 1, we have macroscopically obvious slip. For the present data, we get < B sl < 1, showing a strong slip effect in the range of simulations, again unlike the LDPE melt, which shows no slip. 39 It should be noted that the other HDPE-42 used in our recent paper 29 has similar slip behavior but a higher slip exponent b = Advances in Polymer Technology DOI /adv E375
8 Method of Solution The solution of the above conservation and constitutive equations is carried out with two codes, one for viscous flows (u-v-p-t-h formulation) 44 and one for viscoelastic flows. 33,45 The boundary conditions (BCs) for the problem at hand are well known and can be found in our earlier publication. 33 Briefly, we assume no-slip (or slip, Eq. (21)) and a constant temperature T 0 at the solid walls; at entry, a fully developed velocity profile v z (r) is imposed, corresponding to the flow rate at hand (found numerically for no-slip or slip conditions), and a constant temperature T 0 is assumed; at the outlet, zero surface traction and zero heat flux q are assumed; on the free surface, no penetration and zero heat flux are imposed. The entry length of the domain is L res = 40R, long enough to guarantee fully developed conditions even for viscoelastic runs for the highest apparent shear rate. The extrudate length depended on whether we used viscous or viscoelastic simulations. For the viscous simulations, there are no memory effects and a relatively short extrudate length L ext = 12R suffices. For the viscoelastic simulations, memory effects are important and longer meshes are necessary. We have tried various extrudate lengths L ext ; however no matter how long the domain was, the calculated swell never leveled off due to the strong viscoelastic nature of the melt. Therefore, we have chosen here to report results for L ext = 16R and this issue will be discussed further in the simulations section. Having fixed the model parameters and the problem geometry, the only parameter left to vary was the apparent shear rate in the die ( γ A = 4Q/π R 3 ). Simulations were performed for the whole range of experimental apparent shear rates, namely from 5s 1 to 1000 s 1, where smooth extrudates were obtained. The viscous simulations are extremely fast and are used as a first step to study the whole range of parameter values. The viscoelastic simulations admittedly are harder to do, and they need good initial flow fields to get solutions at elevated apparent shear rates. In our recent work, 43 we explained how it was possible for the first time to do viscoelastic computations up to very high apparent shear rates (1000 s 1 ) with good results. Here, an extra complication arises from the presence of free surface, for which severe underrelaxation (factor ω f = 0.1 down to 0.01) must be used to avoid particle tracking occurring outside the domain. Briefly, the solution strategy starts from the Newtonian solution at the lowest apparent shear rate (0.1 s 1 ) for the base case (β p = a T = β sl = 0). Then at the given apparent shear rate, the viscoelastic model is turned on and the solution is pursued in the given domain until the norm of the error is below Then the free-surface update is turned on, and the u v p T solution is alternated with the h-solution (free surface location) until the maximum free surface change is less than Meeting this criterion gives a very good solution for the problem at hand. Using this solution as an initial guess, the apparent shear rate is then raised slowly to get a new solution at an elevated value. This way it was possible to achieve solutions for as high as 1000 s 1. It must be noted that HDPE is strongly viscoelastic 12 as is LDPE, 33,46 for which it was not possible to reach apparent shear rates greater than 10 s 1 for the extrudate swell problem (without slip). When all effects are present, we follow the same procedure. Now the biggest contribution comes from slip, since temperature dependence and pressure dependence of the viscosity have opposite effects and they are small anyway. With slip present, the simulations are much faster as they require fewer iterations due to the effectively lower flow conditions encountered in the flow field (actual shear rates at the die walls are an order of magnitude less with slip present). Also the swell is reduced compared with the base case, which makes it easier to solve the nonlinear problem. All velocities have been made dimensionless with the average velocity U and the lengths with the die radius R. Then the pressures and stresses are made dimensionless by η 0 U/R. Experimental Results ENTRANCE (END) PRESSURE Figure 5 presents the apparent flow curves of the HDPE for three dies having the same D and different L/D ratios in terms of the apparent shear stress, σ W,A defined as σ W,A p/(4l/d), versus the apparent shear rate, γ A, where p is the pressure drop along the capillary die including the entry. The data do not superpose due to the fact that the end pressure, p end, has not been taken into account. This E376 Advances in Polymer Technology DOI /adv
9 0.60 Apparent wall shear stress, σ w,a (MPa) L/D = 5 L/D = 16 L/D = Apparent shear rate, γ Α (s 1 ) FIGURE 5. The apparent flow curves of the HDPE melt at 190 C as a function of the apparent shear rate for various L /D ratios. Pressure (MPa) γ 1 ( s A ) L / D FIGURE 6. The pressure drop for the capillary extrusion of the HDPE melt at 190 C as a function of L /D for different values of the apparent shear rate (Bagley plot). can be done by constructing the Bagley plot, which is shown in Fig. 6. The pressure drop for the capillary extrusion is plotted as a function of the die length L/D for an extended range of values of the apparent shear rate from 5 s 1 to 1000 s 1.Thedata fall on straight lines (shown in Fig. 6), indicating that the effect of pressure on viscosity is negligible or that both effects of pressure and viscous heating on viscosity are negligible as these effects point to opposite directions. The values of p end are obtained as points of intersections of the fitted straight lines on the vertical pressure axis. Advances in Polymer Technology DOI /adv E377
10 0.30 Wall shear stress, σ w (MPa) L/D =5 L/D = 16 L/D = Apparent shear rate, γ Α (s 1 ) FIGURE 7. The apparent flow curves of the HDPE melt at 190 C as a function of the apparent shear rate for various L /D ratios corrected for the entrance effects. The data superposes well showing that the pressure effect of viscosity is negligible as expected for HDPE melts. FLOW CURVES AND DIAMETER DEPENDENCE Figure 7 depicts flow curves for the HDPE obtained by using capillaries of different diameter and constant ratio L/D = 16 at 190 C. The diameter dependence of the flow curves is clear. This diameter dependence is consistent with the assumption of slip, and the Mooney technique can be used to determine the slip velocity as a function of shear stress. 27 Also on the same plot, the linear viscoelastic (LVE) data are plotted in the form of a flow curve; in other words, the complex modulus, G G 2 + G 2, is plotted as a function of frequency, ω. The failure of the Cox Merz rule is clear, and this is due to the occurrence of slip, also reported by Ansari et al. 26,43 SLIP-CORRECTED FLOW CURVES AND THE SLIP VELOCITY The data plotted in Fig. 8 can be used to construct the Mooney plot to obtain the slip velocity as a function of the wall shear stress. 27 The Mooney technique is defined by the following relationship: γ A = γ A,s + 8u sl D (23) Wall Shear stress, σ w (MPa) Complex modulus, G * (MPa) LVE D = 1.22 mm D = 2.11 mm Apparent shear rate, γ A (s 1 ) or frequency, ω (rad/s) FIGURE 8. Bagley corrected flow curves of the HDPE melt for different diameters at 190 C. The diameter dependence and the significant deviation from the LVE data (failure of the Cox Merz rule) are consistent with the assumption of slip. where γ A,s is the apparent shear rate corrected for slip effects. Figure 9 is the Mooney plot. The slopes of the straight lines fitted to the data are equal to 8u sl according to Eq. (23). These slopes increase with increasing wall shear stress values. The calculated slip velocity function versus the wall shear stress is plotted in Fig. 10. The values E378 Advances in Polymer Technology DOI /adv
11 Apparent shear rate, γ A (s 1 ) σ w (MPa) / D (mm 1 ) FIGURE 9. Mooney plot using the data plotted in Fig. 8. The slopes of the lines are equal to 8u sl for the corresponding value of stress. The slopes increase with increasing shear stress. Slip velocity, u sl (mm/s) u sl (mm/s)= [σ w (MPa)] 4 Mooney, deviation from LVE D = 1.22 mm, deviation from LVE D = 2.11 mm, deviation from LVE Wall shear stress, σ w (MPa) FIGURE 10. The slip velocity as a function of shear stress for the HDPE melt at 190 C. The solid line represents the slip law given by Eq. (20). log(g )/ log(ω) from the flow curve. All data define a single line indicating consistency of the analysis. Equation (20) was fitted to the data, resulting values of β sl = mm/s/mpa b and b = 4. These numbers indicate a strong nonlinear slip law with a very high exponent b. Based on experimental findings, Funatsu and Kajiwara 47 have reported an exponent of 3.65 for their slip model, Hatzikiriakos and Dealy 24 reported exponents of about 3 3.6, whereas Hill et al. 48 have reported an exponent of 6. Obviously, different HDPE melts slip under different nonlinear slip laws. The corrected capillary flow curve for slip effect alongside with the LVE flow curve are presented in Fig. 11. This figure now shows the validity of the Cox Merz rule for the HDPE, as an excellent superposition is obtained. calculated from the slopes of straight lines are shown as Mooney points. In parallel, slip velocities were calculated from the deviation of each flow curve from the curve indicated as LVE by using the following relationship: where n LVE γ A = 4n LVE 3n LVE + 1 ω + 8u sl D (24) is the local slope defined as n LVE EXTRUDATE SWELL Figures 12a and 12b show the extrudate swell as a function of the apparent shear rate and wall shear stress, respectively. Extrudate swell increases exponentially with an increase in both apparent shear rate and wall shear stress. Moreover, extrudate swell increases with a decrease in the die length, which plays the role of dampening the excitation of the Advances in Polymer Technology DOI /adv E379
12 σ w or G* (MPa) Shifted LVE Mooney D = 1.22 mm D = 2.11 mm γ A (s 1 ) or (4n/3n+1)ω LVE (rad/s) FIGURE 11. The slip corrected flow curve of the HDPE at 190 C compared with the LVE data. Good agreement is shown, demonstrating the validity of the Cox-Merz rule. elasticity effects (normal stresses) at the entry to the capillary. This well-known behavior was first successfully simulated for an LDPE melt (the IUPAC LDPE melt A) by Luo and Tanner. 11 D Extrudate swell Extrudate swell L/D = 5 L/D = 16 L/D = 33 L/D = 5 L/D = 16 L/D = Apparent shear rate, γ Α (s 1 ) (a) Numerical Results VISCOUS MODELING It is instructive to perform first calculations with a purely viscous model, so that the effect of viscoelasticity will become evident later. The numerical simulations have been carried out with the finite element method (FEM) as outlined in the Method of Solution section. For the finite element mesh arrangement, we have used our experience with viscous and viscoelastic flows and chosen a grid that progressively adds more elements as one moves from the reservoir toward the singularity at the entrance to the die, while the elements become larger as one moves away from this entry singularity. Again as the die exit is approached, the elements become smaller due to the exit singularity there, after which the elements progressively become larger. A typical finite element grid is shown in Fig. 13 for L/D = 16 (L/R = 32). The domain represents an 18.75:1 abrupt circular contraction with an entrance angle 2α = 180.Thegrid consists of 1584 elements, 3775 nodes, and 10,260 unknown degrees of freedom (d.o.f.), while a four times denser grid is also used, having been created by subdivision of each element into four subelements for Wall shear stress, σ w (MPa) (b) FIGURE 12. (a) The extrudate swell of the HDPE melt at 190 C as a function of the apparent shear rate for three different L /D values. The extrudate swell decreases with increasing die length. (b) The extrudate swell of the HDPE melt at 190 C as a function of the wall shear stress for three different L /D values. The extrudate swell decreases with increasing die length. checking purposes of grid-independent results. This checking consists of reporting the overall pressures in the system from the two meshes and making sure that the differences are less than 1% between the two results. The viscous numerical simulations have been undertaken with the Carreau Yasuda model (Eq. (7)). This constitutive relation is solved together with the conservation equations of mass, momentum, and energy without or with slip at the wall. Namely, we present two sets of simulations, one called the base case of no effects at all (β p = β sl = a T = 0). Then, all E380 Advances in Polymer Technology DOI /adv
13 FIGURE 13. (a) A typical finite element grid for the simulations in an 18.75:1 abrupt circular contraction with L /R = 32 and 2α = 180. The upper grid (M1) consists of 1584 elements and 5101 nodes, whereas the lower grid is created by subdivision of each M1 element into four subelements to form a denser grid for checking the results for grid-independence; (b) detailed grids near the die entry; and (c) detailed grids near the die exit and extrudate region. effects were turned on, referred to in the graphs as slip (because slip is the dominant effect), so that the differences become evident. Figure 14 presents the pressure drops in the capillary obtained from the simulations (lines) together with the experimental data of Fig. 6 (symbols) for different apparent shear rates and L/D ratios (Bagley plot). The base case simulations (continuous lines) overestimate significantly the experimental data. For example, at γ A = 1000 s 1 and L/D = 33, the experimental pressure drop is P = 26 MPa whereas the simulations result in a pressure drop of P = 39 MPa (an error of +50%). On the other hand, the slip simulations (broken lines) underestimate the experimental data. Again, at γ A = 1000 s 1 and L/D = 33, the simulations give 21 MPa (an error of 19%). Obviously, the inclusion of slip brings the simulation predictions closer to the experimental data, although purely viscous simulations do not predict these well. The situation is even worse when extrudate swell is concerned. The viscous simulations (base case)predict swell ratios that hover around zero swell (from a maximum of +2.8% to 1.6%). The slip simulations never predict negative swell, but they are even closer to zero swell (from +1.3% to 0). These very small swell predictions are well known for purely viscous fluids It is therefore, at this point that we turn our attention to the viscoelastic simulations. VISCOELASTIC MODELING Viscoelastic simulations were performed with the K-BKZ model (Eq. (8)) and the data of Table II. First the simulations did not consider the free surface and the extrudate swell, because the problem is much Advances in Polymer Technology DOI /adv E381
14 Pressure (MPa) γ A ( s ) (slip) 11 (slip) 64 (slip) 390 (slip) 1000 (slip) Carreau Yasuda Model L / D FIGURE 14. The pressure drop for the capillary extrusion of the HDPE melt at 190 C as a function of L /D for different values of the apparent shear rate (Bagley plot). Symbols are experimental data, whereas lines are viscous simulation results with the Carreau Yasuda model (Eq. (7)) and the data of Table I. Solid lines are for the base case (β p = β sl = a T = 0), whereas broken lines are for all effects accounted for (slip). The viscous simulations either overpredict (base case) or underpredict (slip) the experimental data. easier to solve. These simulations provide good results for the pressures because the exit flow does not contribute appreciably to the overall pressure drop in the capillary). 1,52 The results from the simulations are depicted in Fig. 15 with all effects accounted for. Now the viscoelastic predictions are much closer to the experimental data, and in some cases the agreement is excellent (in the case of γ A = 64 s 1 ). If we consider again the data at γ A = 1000 s 1 and L/D = 33, the simulations now give 26 MPa vs. 29 MPa found experimentally (with an error of 10%). If we also consider that there may be a ±10% error in the experimental data, the predictions are very good indeed. Therefore, it is safe to say that the viscoelastic simulations with the K-BKZ model and slip at the wall do a good job in predicting the pressure drops in capillary flow of this highly elastic HDPE melt. The situation for the pressure drop when the exit region and extrudate swell are considered is not affected very much. Typically, the difference in the pressure drop was in the second decimal digit for low-to-moderate shear rates. At higher shear rates, as it will be explained below, it was not possible to obtain reliable solutions with extrudate swell present. The simulations with the exit region present and the accompanying phenomenon of extrudate swell showed very similar results with those reported earlier for HDPE melts Namely, the swell was very high even at low shear rates (below 10 s 1 ) and convergence was lost for shear rates above 100 s 1,because the swell had exceeded 300% up to 16R.Points to be noticed are 1. the melt is very elastic due to high relaxation times and tends to recover the shape it possessed in the reservoir (i.e., to reach 10R and higher in the radial direction); 2. longer dies gave smaller swells, as was also found experimentally, because the material had more distance (and hence time) to relax its stresses; 3. in all our viscoelastic simulations, we have always used irreversibility of the damping function, 45 which was found essential in bringing the swell down by Goublomme et al. 22 ; 4. a nonzero second normal stress difference (θ < 0) reduced the swelling somewhat but not the general trends; and E382 Advances in Polymer Technology DOI /adv
15 Pressure (MPa) γ A ( s ) K-BKZ Model L / D FIGURE 15. The pressure drop for the capillary extrusion of the HDPE melt at 190 C as a function of L /D for different values of the apparent shear rate (Bagley plot). Symbols are the experimental data, whereas lines are simulation results with the K-BKZ model (Eq. (8)), the data of Table II, and all effects accounted for (slip). The viscoelastic model predicts well the pressure drops in the capillary. 5. the simulations are carried out in a way that amounts to isothermal swell, meaning that the material will give out all its viscoelastic character as swelling. This is equivalent to an experiment where the melt is extruded in an isothermal oil bath with the same density and temperature as the exiting melt. 19 The experiments here give nonisothermal swell, as the material is extruded freely and downward in the atmosphere. Therefore, cooling and sagging play an important role, which apparently reduces the swelling appreciably. 19 This is not taking into account by the simulations. The least swell obtained from the simulations was for dies without any reservoir present and with a fully developed velocity profile imposed upstream. These conditions give rise to the asymptotic swell, 2,20 where the material does not have to remember its shape in any reservoir that it originated from (its memory has been fully faded). The results for three dies with L/D = 5, 16, and 33 are given in Fig. 16. In all cases the swell is reported at a distance L ext = 16R. The results depend on the L/D ratio only at the higher range of the shear rates. The swell follows an upward trend similar to the experiments, but the numerical values are much higher than the experimental ones. For example, at γ A = 100 s 1 the numerical swell has reached 50%, whereas the experimental values are 22% (see Fig. 1). At even higher shear rates, the differences become even higher, namely at γ A = 1000 s 1 the calculated swell reaches around 80% 90% whereas the experimental values are as Extrudate swell L/D = 5 L/D = 16 L/D = 33 L/D = 5, θ = K BKZ model Apparent shear rate, γ Α (s 1 ) FIGURE 16. Asymptotic extrudate swell of the HDPE melt at 190 C as a function of the apparent shear rate for three different L /D values. Simulation results with the K-BKZ model (Eq. (8)). Symbols are put to show the continuation steps. The extrudate swell decreases slightly with increasing die length at the higher range of apparent shear rates. Swell values are reported at L ext = 16R. low as 28% for the longest die (L/D = 33). A nonzero second normal stress difference N 2 brings the swell down due to hoop stresses. Thus, for θ = 0.25 (N 2 /N 1 = 0.2 from Eq. (9)), the swell is reduced about 2% to 5%. This is in agreement with previous findings. 10,14,22 Again, it should be emphasized that the experimental values refer to nonisothermal swell, where cooling and sagging are very important and help reduce the swelling considerably. 19 Advances in Polymer Technology DOI /adv E383
16 An attempt was made to add gravity to the flow field forces and extend the extrudate length L ext = 100R. Although this brought down the swell considerably for lower shear rates, for γ A > 10 s 1 the elasticity of the melt made the swell take off again to values similar to those shown in Fig. 16. Perhaps other phenomena play a role in nonisothermal swelling (or nonannealed swelling) of this polymer melt. HDPEs are crystalline polymers, and crystallization may play an important role in the swelling behavior. Upon exiting the die, the outside core of the extrudate crystallizes even at temperatures higher than their equilibrium melting point (flow-induced crystallization) 53 and thus prevents the inside part of the melt from swelling (by applying hoop stresses). This is an important aspect not taken into account in the simulations. Thus here, as in earlier works, 22 the correct prediction of the extrudate swell of HDPE melts remains an elusive subject. Conclusions A HDPE has been studied in entry flows through capillary dies with different L/D ratios (5, 16, and 33) with the purpose of predicting the pressure drop in the system and its extrudate swell. The experiments have shown that this particular HDPE slips strongly at the wall. Full rheological characterization was carried out both with a viscous (Carreau Yasuda) and a viscoelastic (K-BKZ) model. All necessary material properties data were collected for the simulations. The viscous simulations showed that when all effects are taken into account the pressure drops are underpredicted, especially for the higher apparent shear rates and L/D ratios. Also, virtually no extrudate swell is predicted, a well-known deficiency of viscous models. The viscoelastic simulations with the K-BKZ/ PSM model showed a good predictive capability of the pressure drops in the system for all cases. However, the swell was overpredicted, despite the fact that slip was included. The general trend of the experimental data that showed an exponential increase of extrudate swell was captured by the model, albeit for the asymptotic swell that does not take into account the presence of the reservoir. An increase in the L/D ratio reduces the swelling, and this was more evident experimentally as a long die gives enough time to the material to forget its elastic stresses (fading memory). References 1. Dealy, J. M.; Wissbrun, K. F. Melt Rheology and Its Role in Plastics Processing Theory and Applications; Van Nostrand Reinhold: New York, Tanner, R. I. Engineering Rheology, 2nd ed.; Oxford University Press: Oxford, UK, Boger, D. V.; Walters, K. Rheological Phenomena in Focus, Rheology Series, Vol. 4.; Elsevier, Amsterdam, Bird, R. B.; Hassager, O.; Armstrong, R. C.; Curtiss, C. F. Dynamics of Polymeric Liquids, Vol. 2: Kinetic Theory; 2nd ed.: Wiley: New York, Tanner, R. I. Appl Polym Symp 1973, 20, Middleman, S.; Gavis, J. Phys Fluids 1961, 4, Crochet, M. J.; Keunings, R. J Non-Newtonian Fluid Mech 1982, 10, Crochet, M. J.; Keunings, R. J Non-Newtonian Fluid Mech 1982, 10, Bush, M. B.; Tanner, R. I.; Phan-Thien, N. J Non-Newtonian Fluid Mech 1985, 18, Sugeng, F.; Phan-Thien, N.; Tanner, R. I. J Rheol 1987, 31, Luo, X.-L.; Tanner, R. I. Int J Num Meth Eng 1988, 25, Luo, X.-L.; Mitsoulis, E. J Rheol 1989, 33, Mitsoulis, E. J Non-Newtonian Fluid Mech 2010, 165, Barakos, G.; Mitsoulis, E. J Rheol 1995, 39, Sun, J.; Phan-Thien, N.; Tanner, R. I. Rheol Acta 1996, 35, Orbey, N.; Dealy, J. M. Polym Eng Sci 1984, 24, Park, H. J.; Kiriakidis, D. G.; Mitsoulis, E.; Lee, K.-J. J Rheol 1992, 36, Koopmans, R. J. Polym Eng Sci 1992, 32, Koopmans, R. J. Polym Eng Sci 1992, 32, Kiriakidis, D. G.; Mitsoulis, E. Adv Polym Technol 1993, 12, Goublomme, A.; Draily, B.; Crochet, M. J. J Non-Newtonian Fluid Mech 1992, 44, Goublomme, A.; Crochet, M. J. J Non-Newtonian Fluid Mech 1993, 47, Hatzikiriakos, S. G.; Dealy, J. M. J Rheol 1991, 35, Hatzikiriakos, S. G.; Dealy, J. M. J Rheol 1992, 36, Hatzikiriakos, S. G.; Dealy, J. M. J Rheol 1992, 36, Ansari, M.; Hatzikiriakos, S. G.; Sukhadia, A. M.; Rohlfing, D. C. Rheol Acta 2011, 50, Mooney, M. J Rheol 1931, 2, Mitsoulis, E.; Hatzikiriakos, S. G. J Non-Newtonian Fluid Mech 2009, 157, Ansari, M.; Hatzikiriakos, S. G.; Mitsoulis, E. J Non- Newtonian Fluid Mech 2012, , Papanastasiou, A. C.; Scriven, L. E.; Macosko, C. W. J Rheol 1983, 27, Kajiwara, T.; Barakos, G.; Mitsoulis, E. Int J Polym Anal Character 1995, 1, Alaie, S. M.; Papanastasiou, T. C. Intern Polym Proc 1993, 8, E384 Advances in Polymer Technology DOI /adv
17 33. Barakos, G.; Mitsoulis, E. J Non-Newtonian Fluid Mech 1996, 62, Beaulne, M.; Mitsoulis, E. J Appl Polym Sci 2007, 105, Winter, H. H. Adv Heat Transfer 1977, 13, Mitsoulis, E.; Wagner, R.; Heng, F. L. Polym Eng Sci 1988, 28, Sedlacek, T.; Zatloukal, M.; Filip, P.; Boltizar, A.; Saha, P. Polym Eng Sci 2004, 44, Carreras,E.S.;ElKissi,N.;Piau,J.M.;Toussaint,F.;Nigen, S. Rheol Acta 2006, 45, Ansari, M.; Zisis, Th.; Hatzikiriakos, S. G.; Mitsoulis, E. Polym Eng Sci, 2012, 52, Lupton, L. M.; Regester, J. W. Polym Eng Sci 1965, 5, Park, H. E.; Lim, S. T.; Smillo, F.; Dealy, J. M. J Rheol 2008, 52, Mitsoulis, E.; Kazatchkov, I. B.; Hatzikiriakos, S. G. Rheol Acta 2005, 44, Ansari, M.; Alabbas, A.; Mitsoulis, E.; Hatzikiriakos, S. G. Int Polym Proc 2010, 25, Hannachi, A.; Mitsoulis, E. Adv Polym Technol 1993, 12, Luo, X.-L.; Mitsoulis, E. Int J Num Meth Fluids 1990, 11, Luo, X.-L.; Mitsoulis, E. Int J Num Meth Fluids 1990, 11, Funatsu, K.; Kajiwara, T. In Encyclopedia of Fluid Mechanics, Vol. 7: Rheology and Non-Newtonian Flows; Ed. Cheremisinoff, N. P., Gulf Publishing Company, Houston, TX, 1988, pp Hill, D. A.; Hasegawa, T.; Denn, M. M. J Rheol 1990, 34, Mitsoulis, E.; Vlachopoulos, J.; Mirza, F. A. Polym Eng Sci 1984, 24, Mitsoulis, E. J Fluids Eng 2007, 129, Mitsoulis, E. J Non-Newtonian Fluid Mech 2007, 141, Mitsoulis, E.; Vlachopoulos, J. J Polym Eng 1985, 5, Sentmanat, M.; Delgadillo, O.; Hatzikiriakos, S. G. Rheol Acta 2010, 49, Tadmor, Z.; Gogos, C. G. Principles of Polymer Processing, SPE Monograph Series; Wiley: New York, Advances in Polymer Technology DOI /adv E385
VISCOELASTIC SIMULATIONS WITH INTEGRAL MODELS AT EXTREMELY HIGH SHEAR RATES
8 th GRACM International Congress on Computational Mechanics Volos, 12 July 15 July 2015 VISCOELASTIC SIMULATIONS WITH INTEGRAL MODELS AT EXTREMELY HIGH SHEAR RATES Evan Mitsoulis School of Mining Engineering
More informationThe Effect of Rheology in Polymer Processing: A Simulation Point of View
ANNUAL TRANSACTIONS OF THE NORDIC RHEOLOGY SOCIETY, VOL. 10, 2002 The Effect of Rheology in Polymer Processing: A Simulation Point of View Evan Mitsoulis School of Mining Engineering and Metallurgy, National
More informationEntry Flow of Polyethylene Melts in Tapered Dies
REGULAR CONTRIBUTED ARTICLES M. Ansari 1, A. Alabbas 1, S. G. Hatzikiriakos 1, E. Mitsoulis 2 * 1 Department of Chemical and Biological Engineering, University of British Columbia, Vancouver, BC, Canada
More informationCONTRIBUTION TO EXTRUDATE SWELL FROM THE VELOCITY FACTOR IN NON- ISOTHERMAL EXTRUSION
Second International Conference on CFD in the Minerals and Process Industries CSIRO, Melbourne, Australia 6-8 December 1999 CONTRIBUTION TO EXTRUDATE SWELL FROM THE VELOCITY FACTOR IN NON- ISOTHERMAL EXTRUSION
More informationMemory Phenomena in Extrudate Swell Simulations for Annular Dies
Memory Phenomena in Extrudate Swell Simulations for Annular Dies X.-L. LUO and E. MITSOULIS, Department of Chemical Engineering, University of Ottawa, Ottawa, Ontario, Canada, KIN 9B4 Synopsis Streamline
More informationTubing Extrusion of a Fluoropolymer Melt
REGULAR CONTRIBUTED ARTICLES E. Mitsoulis 1 *, S. G. Hatzikiriakos 2 1 School of Mining Engineering and Metallurgy, National Technical University of Athens, Athens, Greece 2 Department of Chemical and
More informationTWO-DIMENSIONAL SIMULATIONS OF THE EFFECT OF THE RESERVOIR REGION ON THE PRESSURE OSCILLATIONS OBSERVED IN THE STICK-SLIP INSTABILITY REGIME
1 TWO-DIMENSIONAL SIMULATIONS OF THE EFFECT OF THE RESERVOIR REGION ON THE PRESSURE OSCILLATIONS OBSERVED IN THE STICK-SLIP INSTABILITY REGIME Eleni Taliadorou and Georgios Georgiou * Department of Mathematics
More informationCapillary Flow of Low-Density Polyethylene
Capillary Flow of Low-Density Polyethylene Mahmoud Ansari, 1 Thanasis Zisis, 2 Savvas G. Hatzikiriakos, 1 Evan Mitsoulis 2 1 Department of Chemical and Biological Engineering, The University of British
More informationModelling the Rheology of Semi-Concentrated Polymeric Composites
THALES Project No 1188 Modelling the Rheology of Semi-Concentrated Polymeric Composites Research Team Evan Mitsoulis (PI), Professor, NTUA, Greece Costas Papoulias (Research Student), NTUA, Greece Souzanna
More informationSimulation of pressure drop for combined tapered and nontapered die for polypropylene using ansys Polyflow
IOSR Journal of Polymer and Textile Engineering (IOSR-JPTE) e-issn: 2348-019X, p-issn: 2348-0181, Volume 1, Issue 3 (May-Jun. 2014), PP 22-29 Simulation of pressure drop for combined tapered and nontapered
More informationAN ANALYSIS OF THE EFFECT OF ELONGATIONAL VISCOSITY ONTHEFLOWINAFLATDIE
AN ANALYSIS OF THE EFFECT OF ELONGATIONAL VISCOSITY ONTHEFLOWINAFLATDIE Y. Sun and M. Gupta Mechanical Engineering-Engineering Mechanics Department Michigan Technological University Houghton, MI 49931
More informationTHE 3D VISCOELASTIC SIMULATION OF MULTI-LAYER FLOW INSIDE FILM AND SHEET EXTRUSION DIES
THE 3D VISCOELASTIC SIMULATION OF MULTI-LAYER FLOW INSIDE FILM AND SHEET EXTRUSION DIES Kazuya Yokomizo 1, Makoto Iwamura 2 and Hideki Tomiyama 1 1 The Japan Steel Works, LTD., Hiroshima Research Laboratory,
More information2009 Best Paper Understanding and Quantification of Die Drool Phenomenon During Polypropylene Extrusion Process
2009 Best Paper Understanding and Quantification of Die Drool Phenomenon During Polypropylene Extrusion Process Print (10)» 2010 Best Paper An Engineering Approach to the Correction of Rotational Flow
More informationNon-linear Viscoelasticity FINITE STRAIN EFFECTS IN SOLIDS
FINITE STRAIN EFFECTS IN SOLIDS Consider an elastic solid in shear: Shear Stress σ(γ) = Gγ If we apply a shear in the opposite direction: Shear Stress σ( γ) = Gγ = σ(γ) This means that the shear stress
More informationANALYSIS ON PLANAR ENTRY CONVERGING FLOW OF POLYMER MELTS
Journal of Materials Science and Engineering with Advanced Technology Volume 2, Number 2, 2010, Pages 217-233 ANALYSIS ON PLANAR ENTRY CONVERGING FLOW OF POLYMER MELTS College of Industrial Equipment and
More informationRheological evaluation of melt blown polymer melt
Rheological evaluation of melt blown polymer melt Jiri rabek and Martin Zatloukal Citation: AIP Conf. Proc. 1526, 237 (2013); doi: 10.1063/1.4802618 View online: http://dx.doi.org/10.1063/1.4802618 View
More informationMadrid, 8-9 julio 2013
VI CURSO DE INTRODUCCION A LA REOLOGÍA Madrid, 8-9 julio 2013 NON-LINEAR VISCOELASTICITY Prof. Dr. Críspulo Gallegos Dpto. Ingeniería Química. Universidad de Huelva & Institute of Non-Newtonian Fluid Mechanics
More informationJournal of Non-Newtonian Fluid Mechanics
J. Non-Newtonian Fluid Mech. 157 (2009) 26 33 Contents lists available at ScienceDirect Journal of Non-Newtonian Fluid Mechanics journal homepage: www.elsevier.com/locate/jnnfm Steady flow simulations
More informationViscoelastic Flows in Abrupt Contraction-Expansions
Viscoelastic Flows in Abrupt Contraction-Expansions I. Fluid Rheology extension. In this note (I of IV) we summarize the rheological properties of the test fluid in shear and The viscoelastic fluid consists
More informationAnalysis of Melt Spinning Master-Curves of Low Density Polyethylene
Analysis of Melt Spinning Master-Curves of Low Density Polyethylene Ji-Zhao Liang, 1 Lei Zhong, 1 Kejian Wang 2 1 Research Division of Green Function Materials and Equipment, School of Mechanical and Automotive
More informationExcerpt from the Proceedings of the COMSOL Users Conference 2006 Boston
Using Comsol Multiphysics to Model Viscoelastic Fluid Flow Bruce A. Finlayson, Professor Emeritus Department of Chemical Engineering University of Washington, Seattle, WA 98195-1750 finlayson@cheme.washington.edu
More informationPLEASE SCROLL DOWN FOR ARTICLE
This article was downloaded by: [HEAL-Link Consortium] On: 19 November 2008 Access details: Access Details: [subscription number 772725613] Publisher Taylor & Francis Informa Ltd Registered in England
More informationInvestigation of Polymer Long Chain Branching on Film Blowing Process Stability by using Variational Principle
Investigation of Polymer Long Chain Branching on Film Blowing Process Stability by using Variational Principle ROMAN KOLARIK a,b and MARTIN ZATLOUKAL a,b a Centre of Polymer Systems, University Institute
More informationMeasurement and Prediction of Fluid Viscosities at High Shear Rates
Chapter 5 Measurement and Prediction of Fluid Viscosities at High Shear Rates Jeshwanth K. Rameshwaram and Tien T. Dao Additional information is available at the end of the chapter http://dx.doi.org/10.5772/54282
More informationHEAT TRANSFER OF SIMPLIFIED PHAN-THIEN TANNER FLUIDS IN PIPES AND CHANNELS
HEAT TRANSFER OF SIMPLIFIED PHAN-THIEN TANNER FLUIDS IN PIPES AND CHANNELS Paulo J. Oliveira Departamento de Engenharia Electromecânica, Universidade da Beira Interior Rua Marquês D'Ávila e Bolama, 600
More informationEVALUATION OF NONLINEAR DIFFERENTIAL MODELS FOR THE SIMULATION OF POLYMER MELTS
1 th Fall Rubber Colloquium EVALUATION OF NONLINEAR DIFFERENTIAL MODELS FOR THE SIMULATION OF POLYMER MELTS Jochen Kroll, Stefan Turek, Patrick Westervoß Institute of Applied Mathematics (LS III), TU Dortmund
More informationOn the Computation of Viscosity-Shear Rate Temperature Master Curves for Polymeric Liquids
Morehead Electronic Journal of Applicable Mathematics Issue 1 CHEM-2000-01 Copyright c 2001 On the Computation of Viscosity-Shear Rate Temperature Master Curves for Polymeric Liquids G. T. Helleloid University
More informationRheology and Constitutive Equations. Rheology = Greek verb to flow. Rheology is the study of the flow and deformation of materials.
Rheology and Constitutive Equations Rheology = Greek verb to flow Rheology is the study of the flow and deformation of materials. The focus of rheology is primarily on the study of fundamental, or constitutive,
More informationH. W. Müllner (Sp), J. Eberhardsteiner, Technische Universität Wien (A); W. Fidi, Semperit Technische Produkte Ges.m.b.H. & Co. KG, Wimpassing (A)
Dienstag, 4. Juli 2006 Tuesday, July 4, 2006, 9.30 10.00 h Section A Rheologische Charakterisierung der Strangaufweitung von Kautschukmischungen mittels numerischer Simulationen Rheological Characterisation
More informationPhan-Thien-Tanner Modeling of a Viscoelastic Fluid in the Stick-Slip Scenario. Andrew Griffith
Phan-Thien-Tanner Modeling of a Viscoelastic Fluid in the Stick-Slip Scenario Andrew Griffith Supervisor: Bruce A. Finlayson Department of Chemical Engineering University of Washington March 1, 7 Introduction
More informationMeasuring the rheology of thermoplastic polymer melts
Measuring the rheology of thermoplastic polymer melts Using rotational and capillary rheometry to characterize polymer melts RHEOLOGY AND VISCOSITY Introduction Rheology is the science of studying the
More informationShear rheology of polymer melts
Shear rheology of polymer melts Dino Ferri dino.ferri@versalis.eni.com Politecnico Alessandria di Milano, 14/06/2002 22 nd October 2014 Outline - Review of some basic rheological concepts (simple shear,
More informationDIFFERENCE IN THERMOFORMING PROCESSABILITY OBSERVED FOR THREE HIGH IMPACT POLYSTYRENES
Page 1 of 5 DIFFERENCE IN THERMOFORMING PROCESSABILITY OBSERVED FOR THREE HIGH IMPACT POLYSTYRENES Caroline Woelfle, Kurt Koppi, Stephane Costeux, Todd Hogan, Joe Dooley, Ronald Van Daele, Alexander De
More informationOn Relationship between PVT and Rheological Measurements of Polymer Melts
ANNUAL TRANSACTIONS OF THE NORDIC RHEOLOGY SOCIETY, VOL. 3, 2005 On Relationship between PVT and Rheological Measurements of Polymer Melts Tomas Sedlacek, Peter Filip 2, Peter Saha Polymer Centre, Faculty
More informationMeasuring Slip at a Polymer/Polymer Interface during Three-Layer Flow
Rapid Communication Nihon Reoroji Gakkaishi Vol.41, No.4, 235~239 (Journal of the Society of Rheology, Japan) 2013 The Society of Rheology, Japan Measuring Slip at a Polymer/Polymer Interface during Three-Layer
More informationStress Overshoot of Polymer Solutions at High Rates of Shear
Stress Overshoot of Polymer Solutions at High Rates of Shear K. OSAKI, T. INOUE, T. ISOMURA Institute for Chemical Research, Kyoto University, Uji, Kyoto 611-0011, Japan Received 3 April 2000; revised
More informationModeling of Non Isothermal Film Blowing Process for Non Newtonian Fluids by Using Variational Principles
Modeling of Non Isothermal Film Blowing Process for Non Newtonian Fluids by Using Variational Principles Modified on Friday, 01 May 2015 10:21 PM by mpieler Categorized as: Paper of the Month Modeling
More informationTHE SUBORDINATION OF THE THREE- DIMENSIONAL FLOW INSTALLATION IN THE CONVERGING CHANNEL ON RHEOLOGICAL CHARACTERISTICS OF POLYMER STREAM
International Journal of Civil Engineering and Technology (IJCIET) Volume 9, Issue 13, December 2018, pp. 949-956, Article ID: IJCIET_09_13_095 Available online at http://www.iaeme.com/ijciet/issues.asp?jtype=ijciet&vtype=9&itype=13
More informationCM4655 Polymer Rheology Lab. Torsional Shear Flow: Parallel-plate and Cone-and-plate
CM4655 Polymer heology Lab Torsional Shear Flow: Parallel-plate and Cone-and-plate (Steady and SAOS) Professor Faith A. Morrison Department of Chemical Engineering Michigan Technological University r (-plane
More informationQuasi-1D Modeling of Polymer Melt Die Swell in Short Dies. JAE-HYEUK JEONG and ARKADY I. LEONOV
Quasi-D Modeling of Polymer Melt Die Swell in Short Dies JAE-HYEUK JEONG and ARKADY I. LEONOV Department of Polymer Engineering The University of Aron Aron, Ohio 4435-030 Abstract This paper describes
More informationvs. Chapter 4: Standard Flows Chapter 4: Standard Flows for Rheology shear elongation 2/1/2016 CM4650 Lectures 1-3: Intro, Mathematical Review
CM465 Lectures -3: Intro, Mathematical //6 Chapter 4: Standard Flows CM465 Polymer Rheology Michigan Tech Newtonian fluids: vs. non-newtonian fluids: How can we investigate non-newtonian behavior? CONSTANT
More informationOldroyd Viscoelastic Model Lecture Notes
Oldroyd Viscoelastic Model Lecture Notes Drew Wollman Portland State University Maseeh College of Engineering and Computer Science Department of Mechanical and Materials Engineering ME 510: Non-Newtonian
More informationJournal of Non-Newtonian Fluid Mechanics
Journal of Non-Newtonian Fluid Mechanics 177-178 (2012) 97 108 Contents lists available at SciVerse ScienceDirect Journal of Non-Newtonian Fluid Mechanics journal homepage: http://www.elsevier.com/locate/jnnfm
More informationInfluence of steady shear flow on dynamic viscoelastic properties of un-reinforced and Kevlar, glass fibre reinforced LLDPE
Bull. Mater. Sci., Vol. 27, No. 5, October 2004, pp. 409 415. Indian Academy of Sciences. Influence of steady shear flow on dynamic viscoelastic properties of un-reinforced and Kevlar, glass fibre reinforced
More informationAuthors: Correspondence: ABSTRACT: Keywords:
Implementation of a material model with shear rate and temperature dependent viscosity Authors: Mathias Vingaard, Benny Endelt, Jesper declaville Christiansen Department of Production Aalborg University
More informationLecture 2: Constitutive Relations
Lecture 2: Constitutive Relations E. J. Hinch 1 Introduction This lecture discusses equations of motion for non-newtonian fluids. Any fluid must satisfy conservation of momentum ρ Du = p + σ + ρg (1) Dt
More informationFinal Polymer Processing
030319 Final Polymer Processing I) Blow molding is used to produce plastic bottles and a blow molding machine was seen during the Equistar tour. In blow molding a tubular parison is produced by extrusion
More informationSimulation of Die-swell Flow for Oldroyd-B Model with Feedback Semi-implicit Taylor Galerkin Finite Element Method
KMUTNB Int J Appl Sci Technol, Vol.8, No.1, pp. 55-63, (2015) Simulation of Die-swell Flow for Oldroyd-B Model with Feedback Semi-implicit Taylor Galerkin Finite Element Method Nawalax Thongjub and Vimolrat
More information5 The Oldroyd-B fluid
5 The Oldroyd-B fluid Last time we started from a microscopic dumbbell with a linear entropic spring, and derived the Oldroyd-B equations: A u = u ρ + u u = σ 2 pi + η u + u 3 + u A A u u A = τ Note that
More informationFundamentals of Fluid Dynamics: Elementary Viscous Flow
Fundamentals of Fluid Dynamics: Elementary Viscous Flow Introductory Course on Multiphysics Modelling TOMASZ G. ZIELIŃSKI bluebox.ippt.pan.pl/ tzielins/ Institute of Fundamental Technological Research
More informationTubeless Siphon and Die Swell Demonstration
Tubeless Siphon and Die Swell Demonstration Christopher W. MacMinn & Gareth H. McKinley September 26, 2004 Hatsopoulos Microfluids Laboratory, Department of Mechanical Engineering Massachusetts Institute
More informationCHAPTER 3. CONVENTIONAL RHEOMETRY: STATE-OF-THE-ART. briefly introduces conventional rheometers. In sections 3.2 and 3.
30 CHAPTER 3. CONVENTIONAL RHEOMETRY: STATE-OF-THE-ART This chapter reviews literature on conventional rheometries. Section 3.1 briefly introduces conventional rheometers. In sections 3.2 and 3.3, viscometers
More informationAn Adjustable Gap In-Line Rheometer
An Adjustable Gap In-Line Rheometer By D. M. Kalyon, H. Gokturk and I. Boz Highly Filled Materials Institute Hoboken, NJ 07030 Introduction The rheological behavior of polymer melts, and structured fluids
More informationRolling of bread dough: Experiments and simulations
food and bioproducts processing 8 7 (2 0 0 9) 124 138 Contents lists available at ScienceDirect Food and Bioproducts Processing journal homepage: www.elsevier.com/locate/fbp Rolling of bread dough: Experiments
More informationModeling of Anisotropic Polymers during Extrusion
Modeling of Anisotropic Polymers during Extrusion Modified on Friday, 01 May 2015 10:38 PM by mpieler Categorized as: Paper of the Month Modeling of Anisotropic Polymers during Extrusion Arash Ahmadzadegan,
More informationMechanical Properties of Polymers. Scope. MSE 383, Unit 3-1. Joshua U. Otaigbe Iowa State University Materials Science & Engineering Dept.
Mechanical Properties of Polymers Scope MSE 383, Unit 3-1 Joshua U. Otaigbe Iowa State University Materials Science & Engineering Dept. Structure - mechanical properties relations Time-dependent mechanical
More informationRheology of cellulose solutions. Puu Cellulose Chemistry Michael Hummel
Rheology of cellulose solutions Puu-23.6080 - Cellulose Chemistry Michael Hummel Contents Steady shear tests Viscous flow behavior and viscosity Newton s law Shear thinning (and critical concentration)
More informationCENG 501 Examination Problem: Estimation of Viscosity with a Falling - Cylinder Viscometer
CENG 501 Examination Problem: Estimation of Viscosity with a Falling - Cylinder Viscometer You are assigned to design a fallingcylinder viscometer to measure the viscosity of Newtonian liquids. A schematic
More informationRHEOLOGY Principles, Measurements, and Applications. Christopher W. Macosko
RHEOLOGY Principles, Measurements, and Applications I -56081-5'79~5 1994 VCH Publishers. Inc. New York Part I. CONSTITUTIVE RELATIONS 1 1 l Elastic Solid 5 1.1 Introduction 5 1.2 The Stress Tensor 8 1.2.1
More informationCorrections to flow data in polymer melts
Corrections to flow data in polymer melts Narongrit Sombatsompop Polymer PROcessing and Flow (P-PROF) Materials Technology, School of Energy & Materials King Mongkut s University of Technology Thonburi
More informationDetermining the Processability of Multilayer Coextruded Structures
Determining the Processability of Multilayer Coextruded Structures Joseph Dooley The Dow Chemical Company, Midland, MI ABSTRACT Multilayer coextrusion is a process in which two or more polymers are extruded
More informationRheological Properties of ABS at Low Shear Rates: Effects of Phase Heterogeneity
Malaysian Polymer Journal, Vol 4, No, p9-36, 9 Available online at wwwfkkksautmmy/mpj Rheological Properties of ABS at Low Shear Rates: Effects of Phase Heterogeneity Asif Ali Qaiser *, Yasir Qayyum and
More informationMultilayer Rheology Effects in Coextruded Structure Design
2008 Best Paper Multilayer Rheology Effects in Coextruded Structure Design Print (10)» Best Papers» 2009 Best Paper Understanding and Quantification of Die Drool Phenomenon During Polypropylene Extrusion
More informationModeling the Rheology and Orientation Distribution of Short Glass Fibers Suspended in Polymeric Fluids: Simple Shear Flow
Modeling the Rheology and Orientation Distribution of Short Glass Fibers Suspended in Polymeric Fluids: Simple Shear Flow Aaron P.R. berle, Donald G. Baird, and Peter Wapperom* Departments of Chemical
More informationPolymer rheology at high shear rate for microinjection moulding
Polymer rheology at high shear rate for microinjection moulding Cheima Mnekbi, Michel Vincent, Jean-François Agassant To cite this version: Cheima Mnekbi, Michel Vincent, Jean-François Agassant. Polymer
More informationPressure Drop Separation during Aqueous Polymer Flow in Porous Media
Pressure Drop Separation during Aqueous Polymer Flow in Porous Media D.C. Raharja 1*, R.E. Hincapie 1, M. Be 1, C.L. Gaol 1, L. Ganzer 1 1 Department of Reservoir Engineering, Clausthal University of Technology
More informationAuthor's personal copy
Computers & Fluids 57 (2012) 195 207 Contents lists available at SciVerse ScienceDirect Computers & Fluids journal homepage: www.elsevier.com/locate/compfluid A study of various factors affecting Newtonian
More informationQuasi-Three-Dimensional Simulation of Viscoelastic Flow through a Straight Channel with a Square Cross Section
Article Nihon Reoroji Gakkaishi Vol.34, No.2, 105~113 (Journal of the Society of Rheology, Jaan) 2006 The Society of Rheology, Jaan Quasi-Three-Dimensional Simulation of Viscoelastic Flow through a Straight
More informationLinear viscoelastic behavior
Harvard-MIT Division of Health Sciences and Technology HST.523J: Cell-Matrix Mechanics Prof. Ioannis Yannas Linear viscoelastic behavior 1. The constitutive equation depends on load history. 2. Diagnostic
More informationON THE ROLE OF EXTENSIONAL RHEOLOGY, ELASTICITY AND DEBORAH NUMBER ON NECK-IN PHENOMENON DURING FLAT FILM PRODUCTION
ON THE ROLE OF EXTENSIONAL RHEOLOGY, ELASTICITY AND DEBORAH NUMBER ON NECK-IN PHENOMENON DURING FLAT FILM PRODUCTION Martin Zatloukal 1, Tomas Barborik 1 and Costas Tzoganakis 2 1 Polymer Centre, Faculty
More informationChapter 1 Introduction
Chapter 1 Introduction This thesis is concerned with the behaviour of polymers in flow. Both polymers in solutions and polymer melts will be discussed. The field of research that studies the flow behaviour
More informationChapter 6 Molten State
Chapter 6 Molten State Rheology ( 流變學 ) study of flow and deformation of (liquid) fluids constitutive (stress-strain) relation of fluids shear flow shear rate ~ dγ/dt ~ velocity gradient dv 1 = dx 1 /dt
More informationStability analysis of a three-layer film casting process
Korea-Australia Rheology Journal Vol. 19, No. 1, March 2007 pp. 27-33 Stability analysis of a three-layer film casting process Joo Sung ee 1, Dong Myeong Shin, Hyun Wook Jung* and Jae Chun Hyun Department
More informationPolymer Rheology. P Sunthar. Department of Chemical Engineering Indian Institute of Technology, Bombay Mumbai , India
Polymer Rheology P Sunthar Department of Chemical Engineering Indian Institute of Technology, Bombay Mumbai 400076, India P.Sunthar@iitb.ac.in 05 Jan 2010 Introduction Phenomenology Modelling Outline of
More informationHow to measure the shear viscosity properly?
testxpo Fachmesse für Prüftechnik 10.-13.10.2016 How to measure the shear viscosity properly? M p v Rotation Capillary Torsten Remmler, Malvern Instruments Outline How is the Shear Viscosity defined? Principle
More information2D TIME AVERAGED FLOW MAPPING OF DIE ENTRY IN FLOW OF HIGHLY CONCENTRATED SHEAR-THINNING AND SHEAR-THICKENING SUSPENSIONS
2D TIME AVERAGED FLOW MAPPING OF DIE ENTRY IN FLOW OF HIGHLY CONCENTRATED SHEAR-THINNING AND SHEAR-THICKENING SUSPENSIONS Boris Ouriev (Ur ev) Bühler AG, Uzwil, CH-9244, Switzerland, e-mail: boris.ouriev@buhlergroup.com
More informationWall-Slip of Highly Filled Powder Injection Molding Compounds: Effect of Flow Channel Geometry and Roughness
Wall-Slip of Highly Filled Powder Injection Molding Compounds: Effect of Flow Channel Geometry and Roughness Berenika Hausnerovaa,b, Daniel Sanetrnika,b, Gordana Paravanovab a Dept. of Production Engineering,
More informationCPGAN # 006. The Basics of Filament Stretching Rheometry
Introduction Measurement of the elongational behavior of fluids is important both for basic research purposes and in industrial applications, since many complex flows contain strong extensional components,
More informationSolvent casting flow from slot die
Korea-Australia Rheology Journal, 27(4), 325-329 (November 2015) DOI: 10.1007/s13367-015-0032-x www.springer.com/13367 Short Communication Semi Lee and Jaewook Nam* School of Chemical Engineering, Sungkyunkwan
More informationCONVERGING FLOW ON-LINE RHEOMETRY FOR AN ENGINEERING EXTENSIONAL VISCOSITY OF UPVC.
CONVERGING FLOW ON-LINE RHEOMETRY FOR AN ENGINEERING EXTENSIONAL VISCOSITY OF UPVC. H. J. Ettinger, J. F. T. Pittman*, J. Sienz Centre for Polymer Processing Simulation and Design, C2EC, School of Engineering,
More informationCessation of Couette and Poiseuille flows of a Bingham plastic and finite stopping times
J. Non-Newtonian Fluid Mech. 29 2005) 7 27 Cessation of Couette and Poiseuille flows of a Bingham plastic and finite stopping times Maria Chatzimina a, Georgios C. Georgiou a,, Ioannis Argyropaidas b,
More informationPerformance evaluation of different model mixers by numerical simulation
Journal of Food Engineering 71 (2005) 295 303 www.elsevier.com/locate/jfoodeng Performance evaluation of different model mixers by numerical simulation Chenxu Yu, Sundaram Gunasekaran * Food and Bioprocess
More informationOn the performance of enhanced constitutive models for polymer melts in a cross-slot flow
J. Non-Newtonian Fluid Mech. 82 (1999) 387±427 On the performance of enhanced constitutive models for polymer melts in a cross-slot flow Gerrit W.M. Peters *, Jeroen F.M. Schoonen, Frank P.T. Baaijens,
More informationFlow Induced Molecular Weight Fractionation during Capillary Flow of Linear Polymer Melt
Flow Induced Molecular Weight Fractionation during Capillary Flow of Linear Polymer Melt JAN MUSIL a,b and MARTIN ZATLOUKAL a,b a Centre of Polymer Systems, University Institute Tomas Bata University in
More informationOn the effects of Non-Newtonian fluids above the ribbing instability
On the effects of Non-Newtonian fluids above the ribbing instability L. Pauchard, F. Varela LÓpez*, M. Rosen*, C. Allain, P. Perrot** and M. Rabaud Laboratoire FAST, Bât. 502, Campus Universitaire, 91405
More informationNon-linear and time-dependent material models in Mentat & MARC. Tutorial with Background and Exercises
Non-linear and time-dependent material models in Mentat & MARC Tutorial with Background and Exercises Eindhoven University of Technology Department of Mechanical Engineering Piet Schreurs July 7, 2009
More informationChapter 1. Continuum mechanics review. 1.1 Definitions and nomenclature
Chapter 1 Continuum mechanics review We will assume some familiarity with continuum mechanics as discussed in the context of an introductory geodynamics course; a good reference for such problems is Turcotte
More information3D CFD ANALYSIS OF HEAT TRANSFER IN A SCRAPED SURFACE HEAT EXCHANGER FOR BINGHAM FLUIDS
3D CFD ANALYSIS OF HEAT TRANSFER IN A SCRAPED SURFACE HEAT EXCHANGER FOR BINGHAM FLUIDS Ali S.* and Baccar M. *Author for correspondence Department of Mechanical Engineering, National Engineering School
More informationIndex. Boundary integral method, 27 Boundary location method, 255 Brinkman number, 14, 158
Index ABFIND,275 Adaptive control, 304, 312 Adaptive process model, 315 Air drag, 221 Alternating Direction Implicit (ADI) technique, 30 Axisymmetric flow, 48 die entry, 58 Boundary integral method, 27
More informationApplication Of Optimal Homotopy Asymptotic Method For Non- Newtonian Fluid Flow In A Vertical Annulus
Application Of Optimal Homotopy Asymptotic Method For Non- Newtonian Fluid Flow In A Vertical Annulus T.S.L Radhika, Aditya Vikram Singh Abstract In this paper, the flow of an incompressible non Newtonian
More informationFAILURE AND RECOVERY OF ENTANGLED POLYMER MELTS IN ELONGATIONAL FLOW
FAILURE AND RECOVERY OF ENTANGLED POLYMER MELTS IN ELONGATIONAL FLOW Yogesh M. Joshi and Morton M. Denn Benjamin Levich Institute for Physico-Chemical Hydrodynamics and Department of Chemical Engineering
More informationARTICLE IN PRESS. J. Non-Newtonian Fluid Mech. 154 (2008) Contents lists available at ScienceDirect. Journal of Non-Newtonian Fluid Mechanics
J. Non-Newtonian Fluid Mech. 154 (2008) 77 88 Contents lists available at ScienceDirect Journal of Non-Newtonian Fluid Mechanics journal homepage: www.elsevier.com/locate/jnnfm Numerical simulation of
More informationOn the congruence of some network and pom-pom models
Korea-Australia Rheology Journal Vol 8, No, March 2006 pp 9-4 On the congruence of some network and pom-pom models Roger I Tanner* School of Aerospace, Mechanical and Mechatronic Engineering, University
More informationFor an imposed stress history consisting of a rapidly applied step-function jump in
Problem 2 (20 points) MASSACHUSETTS INSTITUTE OF TECHNOLOGY DEPARTMENT OF MECHANICAL ENGINEERING CAMBRIDGE, MASSACHUSETTS 0239 2.002 MECHANICS AND MATERIALS II SOLUTION for QUIZ NO. October 5, 2003 For
More informationCompressible viscous flow in slits with slip at the wall
Compressible viscous flow in slits with slip at the wall Georgios C. Georgiou Department of Mathematics and Statistics, University of Cyprus, Kallipoleos 75, F!O. Box 537, Nicosia, Cyprus Marcel J. Crochet
More informationEFFECT OF TYPICAL MELT TEMPERATURE NON-UNIFORMITY ON FLOW DISTRIBUTION IN FLAT DIES
EFFEC OF YPICAL MEL EMPERAURE NON-UNIFORMIY ON FLOW DISRIBUION IN FLA DIES Olivier Catherine, Cloeren Incorporated, Orange, X Abstract In this study, the influence of non-uniform incoming melt temperature
More informationRheometry. II.1 Introduction
II Rheometry II.1 Introduction Structured materials are generally composed of microstructures dispersed in a homogeneous phase [30]. These materials usually have a yield stress, i.e. a threshold stress
More informationA numerical method for steady and nonisothermal viscoelastic fluid flow for high Deborah and Péclet numbers
A numerical method for steady and nonisothermal viscoelastic fluid flow for high Deborah and Péclet numbers Peter Wapperom Martien A. Hulsen (corresponding author) Jaap P.P.M. van der Zanden Delft University
More informationA Phenomenological Model for Linear Viscoelasticity of Monodisperse Linear Polymers
Macromolecular Research, Vol. 10, No. 5, pp 266-272 (2002) A Phenomenological Model for Linear Viscoelasticity of Monodisperse Linear Polymers Kwang Soo Cho*, Woo Sik Kim, Dong-ho Lee, Lee Soon Park, Kyung
More informationViscoelasticity, Creep and Oscillation Experiment. Basic Seminar Applied Rheology
Viscoelasticity, Creep and Oscillation Experiment Basic Seminar Applied Rheology Overview Repetition of some basic terms Viscoelastic behavior Experimental approach to viscoelasticity Creep- and recovery
More information