聚合物熔体的非仿射网络结构模型及其数值解

假设聚合物熔体的缠结网络形变是非仿射的，运用瞬态网络结构原理。并利用Liu提出的动态速率方程以及上随体Maxwell本构方程来建立一个适合于振动剪切作用下的聚合物熔全非仿射网络结构模型。利用这一模型来研究振动剪切作用下LDPE和HDPE熔体的流变行为。研究表明，在一种合理的初始简化条件下可以获得模型的数值解。将理论预测值与实验值进行比较后得知二者具有良好的吻合性，从而简化了模型的计算过程。同时，通过比较得知所建立的非仿射网络结构本构方程比仿射网络结构本构方程的精确度要高，而且在振动力场作用下。具有长支链的LDPE熔体有少量的非仿射网络形变，而没有长支链的HDPE熔体则有较多的非仿射网络形变。因此在建立振动力场作用下聚烯烃熔体本构方程时应充分考虑聚合物熔体网络的非仿射形变。     

IUPAC-LDPE的流变性测试实验之间的相对滑动

以IUPAC—LDPE熔体在150℃下详细的流变学表征实验和毛细管挤出实验为基础考察了该熔体在挤出实验中的滑动问题．根据相对滑动特性给出了判断相对滑动存在和计算相对滑动速度的方法．用Wagner模型，PSM模型和Osaki模型计算的表观剪切速率，在10s^-1时的毛细管壁面剪切应力比毛细管挤出实验给出的应力值高出约15％-17％，这个结果意味着IUPAC—LDPE熔体在挤出实验中存在滑动现象．在表观剪切速率为0．1，1．0和10s^-1时，挤出实验条件下的流动与根据在旋转流变仪上测定的流变特性用PSM模型计算的流动相比，它们之间存在的相对滑动速度分别为0．004，0．071和1．343mm／s．用Wagner模型和Osaki模型计算的相对滑动速度与PSM模型的结果相近．     

正弦应变下聚合物熔体的非仿射网络结构模型

在正弦应变作用下，假设聚合物熔体的缠结网络形变是非仿射的，运用瞬态网络结构原理，并对上随机Maxwell本构方程加以改进，从而得到一个于振动剪切作用下的聚合物熔体的非仿射网络结构模型，并且在一种合理的初始简化条件下对模型进行数值分析，将理论预测值得实验值进行比较后得知二具有较好的吻合性，同时，通过比较得知所建立的非仿射网络结构本构方程比仿射网络结构本构方程的精确度要高。     

颗粒材料剪切流动状态转变的环剪试验研究

颗粒材料的剪切流动行为广泛地存在于滑坡、泥石流等自然灾害以及矿物原料传输、泵送等工业过程中.颗粒材料在不同体积分数、剪切速率和应力约束下会表现出不同的流动状态并发生相互转化.对颗粒材料在剪切流动过程中力学特性的研究有助于加深理解其发生不同流动状态的内在机理,为解决相应的颗粒材料问题提供理论依据.为此,本文研制了颗粒材料剪切流动的中型环剪仪,并对颗粒材料在不同法向约束应力和剪切速率下的剪切应力和体积膨胀率进行了测试.结果表明,剪切应力和体积膨胀率均随剪切速率的增大而增大,但增长速率在临界剪切速率处发生转变,使其随剪切速率的平方呈分段式线性增长.通过对颗粒材料在不同剪切速率和惯性数下有效摩擦系数变化趋势的分析,讨论了颗粒材料由慢速流向快速流转化的基本规律,以及在临界剪切速率处发生流动状态转化的内在条件.此外,通过对不同法向应力下临界剪切速率以及快速流动下运动规律的测试,发现临界剪切速率随法向应力的增加而减小,即法向应力可促进颗粒材料由慢速流向快速流的转化,但在快速流动状态下的有效摩擦系数对法向应力不敏感.以上对颗粒材料在不同剪切速率、法向应力下流动状态的环剪试验研究有助于揭示其发生不同流动状态转化的内在机理.      

由Bezier曲线构造的聚合物熔体剪切黏度模型

为提高聚合物熔体剪切黏度模型的描述精度,提出了一个基于二次Bezier 曲线的黏度模型. 模型采用分段函数描述,在对数坐标系中,低剪切速率时的牛顿区和高剪切速率时的幂律区采用线性函数,介于二者之间的过渡区采用二次Bezier 曲线. 通过牛顿区和幂律区的直线延长线构造Bezier 曲线的控制多边形,从而保证三段曲线的光滑过渡. 模型可以明确给出任意温度下低剪切速率时牛顿区的结束点,以及高剪切速率时幂律区的开始点. 拟合算例表明,所提出模型的拟合精度明显高于Cross-Arrhenius 黏度模型.      

MEASURING DEVICE DEVELOPMENT OF POLYMER MELT VISCOUS DISSIPATION AND TEACHING APPLICATION

针对聚合物熔体流动过程中黏性耗散现象的理论教学不足, 在双料筒毛细管流变仪基础上研制了聚合物熔体黏性耗散测量装置并进行实验. 根据绝热边界条件径向温度分布方程, 对实验结果进行理论分析计算. 组织学生学习POLYFLOW 软件, 利用其可视化功能对黏性耗散引起的温度场变化进行数值模拟, 并与理论计算结果对比分析. 通过让学生自己动手, 改变了理论模式教学, 对加深黏性耗散知识的理解起到积极的作用.     

Herschel-Bulkley模型下磁流变减振器旁路泊肃叶流动分析

制备了羰基铁粉(CIP)的质量分数为70%的硅树脂基磁流变胶。用安东帕MCR-301型流变仪对其流变特性进行了测量,并对测试结果进行了Herschel-Bulkley本构模型参数识别。最后对MRG-70在该模型下磁流变减振器旁路中的泊肃叶(Poiseuille)流动展开了分析。试验及分析结果表明,在外加磁场下,Herschel-Bulkley本构模型中非牛顿指数n1。剪切应力随半径的增大而线性增大;当τ_rτ_y形成剪切流,反之则为柱塞流动。在剪切流动区域内,流速随半径增大而非线性降低,剪切速率随半径增大而非线性增大。磁感应强度越大,柱塞流区域越大,柱塞流区域内剪切速率恒为0。体积流量随磁感应强度增强而非线性减小。在0mT～500mT之间体积流量随磁感应强度变化剧烈,进一步增加磁感应强度则变化缓慢。     

基于单个压电振子的湍流边界层主动控制

利用安装在壁面上的单个压电振子周期振荡,采用开环主动控制方案,实现了对平板湍流边界层相干结构猝发的主动控制和壁湍流减阻.根据不同的输入电压幅值和频率,完成了10种工况的实验.在压电振子下游2mm处,用热线风速仪和迷你热线单丝探针,精细测量湍流边界层不同法向位置瞬时流向速度信号的时间序列,分析了在Re_?=2183压电振子振动对湍流边界层平均速度剖面、减阻率和相干结构猝发过程的影响.实验结果表明,施加控制的工况使平均速度剖面对数律层上移,产生减阻效果;压电振子振幅越大,减阻率越高,减阻效果越明显;通过对施加控制前后流向瞬时速度的多尺度湍涡结构脉动动能的尺度分析,当压电振子振动频率与壁湍流能量最大尺度的猝发频率相近时,减阻率达到最大,为25%,说明控制壁湍流能量最大尺度相干结构的猝发是实现壁湍流减阻的关键;通过对比相干结构猝发的流向速度分量条件相位平均波形,发现施加控制的工况中相干结构猝发流向速度分量的波形幅值明显降低,且流向速度在扫掠后期高速阶段迅速衰减,缩短了高速流体的下扫过程,说明压电振子的振动能抑制相干结构的高速流体下扫过程,减弱高速流体与壁面的强烈剪切过程,并使近壁区域相干结构的振幅显著减弱,迁移速度加快,从而减小壁面摩擦阻力.      

HPAM稀溶液在微圆管中流动特性的实验研究

实验研究了部分水解聚丙烯酰胺(HPAM)稀溶液(水溶液)在内径为10.1 ~325 \mu m石英微管中的高剪切速率(1 215 ~23 120 s ^{ -1} )流动. 结果表明, 聚合物溶液在管径小于100 \mu m微管中的流动具有明显的微尺度效应, 实测流速高于由同种溶液在常规管径圆管中的流动规律所预测的流速. 实测流速与预测流速之间的偏离程度与管径和剪切速率有关: 相同剪切速率下, 管径越小, 偏离越明显; 在小管径微管中, 偏离随剪切速率的增加而减小, 而当管径超过30.7 \mu m后, 偏离不再随剪切速率的变化而改变.      

基于ALE描述的压缩流动三维粘弹性数值模拟

塑料熔体压缩流动中在主流动平面及厚度方向均有速度变化,结合了剪切和拉伸两种流动特征。为了准确描述和模拟塑料熔体的压缩流动,本文基于粘弹性及ALE原理建立了熔体三维流动理论模型,构造了有限元求解的变分方程。为了避免整体求解计算量大、稳定性差的缺陷,提出了两重迭代解耦合算法分别求解耦合的连续方程、动量方程、本构方程、能量方程,开发了模拟程序。开展了等厚度板及变厚度板的注压成型实验及相应的数值模拟,结果表明:压缩过程中出现压力变化小于4.57%的平台现象;温度呈指数规律下降;塑料入口、流动末端第一法向应力差比平均值分别高1.73MPa、0.87MPa,变厚度区域第一法向应力差比平均值高1.16MPa。本文提出的理论模型和数值算法能够较好地表征压缩过程中熔体的压力、温度变化、应力演化。     

The rheological characterisation of bread dough using capillary rheometry

An Australian hard wheat flour–water dough has been characterised using parallel plate and capillary rheometers over an extensive range of apparent shear rates (10^− 3–10³ s^− 1) relevant to process conditions. Torsional measurements showed that the shear viscosity of the dough increased with strain to a maximum value and then decreased, suggesting a breakdown of the dough structure. Both torsional and capillary experiments revealed the shear-thinning behaviour of the dough. The wall slip phenomenon in capillary rheometry was investigated and found to be diameter dependent and occurred at a critical shear stress of approximately 5–10 kPa. A two-regime power law behaviour was observed, with the power law index approximately 0.3 in the low shear rate range increasing to 0.67 in the high shear rate range. Pressure fluctuation was observed in the capillary data and increased with shear rate, in particular, at shear rates approaching 10⁴ s^− 1. The results demonstrate that capillary rheometry is a viable means of rheologically testing dough at high shear rates provided pressure fluctuation is carefully monitored and capillary rheometry corrections, including wall slip, are accounted for.     

Unstable capillary flow of reinforced polymer melts

The injection capillary flow of various unfilled and glass fibre or calcium carbonate filled polypropylene and nylon 6.6 melts is studied using either a single capillary of five capillaries in series, separated by small reservoirs. Only unfilled nylon 6.6 yields instability during flow through a single capillary due to mechanochemical degradation in the capillary at extremely high shear rates above 5 × 10⁵ s^?1. It is found that only short glass fibre reinforced polypropylene yields high frequency oscillations in the reservoir pressure and extrudate diameter and has discontinuity in the flow curve when the apparent shear rate is above 4 × 10⁵ s^?1 and the flow is through multiple capillaries. Further increase in the shear rate restores the stable flow. The intensity of the oscillations and the range of shear rate during which unstable flow occurs are increased with increasing melt temperature. The mechanism of this unstable flow is investigated by studying fibre orientation at the capillary entrance and exit using mouldings simulating capillary entry-exit flows.     

Processing the capillary viscometry data of fluids with yield stress

The capillary viscometer is used to measure the shear stress-shear rate relationship of a wide range of purely viscous fluids. It is however not considered as an appropriate instrument for obtaining the yield stress and the post-yield behaviour of fluids that have a yield stress. This is partly because conventional methods of processing the capillary viscometry data of purely viscous fluids cannot be applied to similar data of fluids with yield stress. The unavoidable experimental noise in the capillary data, particularly at low shear rates, also makes it difficult to obtain a reliable estimate of the yield stress from capillary data. In this investigation the problem of converting the capillary viscometry data of yield stress fluids into a shear stress-shear rate curve and a yield stress is formulated as a Volterra integral equation of the first kind. This is an ill-posed problem i.e. noise in the data will be amplified by inappropriate methods of data processing. A method, based on Tikhonov regularisation that takes into account the ill-posed nature of the problem, is then developed to solve this problem for fluids with yield stress. The performance of this method is assessed by applying it to a set of “synthetic” capillary viscometry data with added random noise and to a set of experimental data for a concentrated suspension of TiO₂ taken from the literature. In both cases Tikhonov regularisation was able to extract the complete shear properties of these fluids from capillary viscometry data alone. Received: 22 November 1999/Accepted: 17 December 1999     

Flow instabilities in capillary flow of concentrated suspensions

The development of flow instabilities during the capillary flow of two concentrated suspensions filled with 76.5 and 65.6% by volume solids was investigated. The flow instabilities manifested themselves by the development of concentration gradients as a result of the filtering of the binder, superimposed on the bulk motion of the suspension. The effects of apparent shear rate, capillary diameter and the surface roughness of the particles were investigated. The use of the comparison of the filtration rate with the bulk velocity of the suspension during flow is shown to be promising for the prediction of the apparent shear rate at which filtration-based flow instabilities occur.     

不同剪切率来流作用下柔性圆柱涡激振动数值模拟

采用浸入边界法对细长柔性圆柱在线性剪切流条件下的涡激振动进行三维数值模拟。细长柔性圆柱振动采用三维索模型模拟,其两端铰接,质量比为6,长细比为50,无量纲顶张力为496。来流为线性剪切流,剪切率从0到0.024变化,最大雷诺数为250。研究发现:剪切流作用下柔性立管横流向振动表现为驻波模式,而顺流向振动表现为行波-驻波混合模式。随着剪切率增大,振动频谱呈现多频响应,振动能量逐渐向低频转移。阻力系数平均值随着展向变化,脉动阻力系数和升力系数的均方根值均表现为“双峰”模式。流固能量传递系数沿立管轴向的分布表明,振动激励区集中于高流速区,而振动阻尼区多位于低流速区。剪切率较小时,圆柱的泻涡为平行交叉模式;剪切率较大时,圆柱的泻涡为倾斜泻涡模式,且由于泻涡频率沿立管轴向变化,尾流发生涡裂现象,形成泻涡频率不同的胞格结构。      

Evaluation of high shear viscosity data from jet and concentric cylinder viscometers

Summary This work compares and evaluates viscosity data obtained on similar fluids by two widely accepted high shear techniques. Both the jet and concentric cylinder viscometers are useful high shear methods. The major limitation of the jet viscometer is an inability to distinguish quantitatively between energy losses in laminar flow and those due to capillary geometry and experimental conditions. For example, the jet viscometer gives minima in viscosity-shear rate correlations which are difficult to treat. These minima are not found in concentric cylinder viscometer data for the same and similar fluids. The apparent viscosity increase at high shear in the jet may be due to factors other thanReynold's turbulence, as previously supposed. This effect may be due to molecular relaxation phenomena in certain cases. The jet viscometer might thus be used to evaluate molecular relaxation and/or other phenomena contributing to this effect.For a variety of systems, the concentric cylinder viscometer gives significantly smaller temporary viscosity losses due to shear than do the jet viscometer data. These comparisons are made using the maximum jet shear rate at the capillary wall. The differences are, of course, larger if average shear rates are used to compare the data. It is concluded that the jet viscometer results tend to be erroneous. This is possibly due to capillary end effects or problems with kinetic energy corrections.     

The “Twin capillary” a simple device to separate shear- and slip-flow of fluids

When the flow behaviour of fluids is investigated with capillary-or rotational rheometers, adhesion of the fluid to the wall is normally one of the boundary conditions. For many fluids, especially for suspensions, this assumption is not valid. These fluids tend to slip at the wall. Therefore the normal evaluation of rheometer measurements leads to apparent but not compatible flow functions. The flow behaviour of these fluids can be characterized with two material functions which describe separately slipping in the boundary layer and shearing within the fluid. Only if both functions are known, correct predictions of flow processes are possible. A simple equipment to separate the shear function and the slip function is described.List of symbols Y^* apparent shear rate - Y _w ^* apparent wall shear rate - Y_w wall shear rate corrected with Rabinowitsch and Weissenberg correction - Y_s reduced shear rate (slip corrected) - Y_ws reduced wall shear rate (slip corrected) - * (r) velocity distribution in a capillary - _G slip velocity (at the wall) - * (r) velocity distribution in a capillary (without slip) - shear stress - _w wall shear stress - V_S total volume rate - V_G shear volume rate - V_G slip volume rate - p ₁ pressure in the reservoir channel of the capillary rheometer - p ₀ athmospheric pressure - L capillary length - R capillary radius     

Shear Rate Determination from Pore-Scale Flow Fields

Aqueous solutions with polymer additives often used to improve the macroscopic sweep efficiency in oil recovery typically exhibit non-Newtonian rheology. In order to predict the Darcy-scale effective viscosity \(\mu _{\mathrm{eff}} \) required for practical applications often, semi-empirical correlations such as the Cannella or Blake–Kozeny correlation are employed. These correlations employ an empirical constant (“C-factor”) that varies over three orders of magnitude with explicit dependency on porosity, permeability, fluid rheology and other parameters. The exact reasons for this dependency are not very well understood. The semi-empirical correlations are derived under the assumption that the porous media can be approximated by a capillary bundle for which exact analytical solutions exist. The effective viscosity \(\mu _{\mathrm{eff}} (v_{\mathrm{Darcy}} )\) as a function of flow velocity is then approximated by a cross-sectional average of the local flow field resulting in a linear relationship between shear rate \(\gamma \) and flow velocity. Only with such a linear relationship, the effective viscosity can be expressed as a function of an average flow rate instead of an average shear rate. The local flow field, however, does in general not exhibit such a linear relationship. Particularly for capillary tubes, the velocity is maximum at the center, while the shear rate is maximum at the tube wall indicating that shear rate and flow velocity are rather anti-correlated. The local flow field for a sphere pack is somewhat more compatible with a linear relationship. However, as hydrodynamic flow simulations (using Newtonian fluids for simplicity) performed directly on pore-scale resolved digital images suggest, flow fields for sandstone rock fall between the two limiting cases of capillary tubes and sphere packs and do in general not exhibit a linear relationship between shear rate and flow velocity. This indicates that some of the shortcomings of the semi-empirical correlations originate from the approximation of the shear rate by a linear relationship with the flow velocity which is not very well compatible with flow fields from direct hydrodynamic calculations. The study also indicates that flow fields in 3D rock are not very well represented by capillary tubes.     

Influence of photodegradation and aging on the viscosity of antimisting polymer solutions

The effect of aging and exposure to light on the viscosity of an antimisting polymer solution was investigated in laminar capillary flows. A particular feature of this solution is the abrupt increase in its viscosity that occurs if a critical shear rate is exceeded. Whereas storage in the dark induced only slight modification of the viscous characteristics of the samples, exposure to light was found to increase the value of the critical shear rate, substantially decrease the maximum post-gelation viscosity and reduce the susceptiblity to high-shear mechanical degradation.     

An experimental study of food melt rheology

The shear viscosity of commercial maize grits, potato powder and a low density polyethylene has been measured under a range of extrusion processing conditions using an extruder-fed slit die viscometer and a capillary rheometer. The results show the strong dependence of the viscosity of food melts on the processing history undergone during extrusion. To this end, the shear viscosity data for the food materials have been fitted to relationships including the effects of temperature, shear rate and moisture. The effect of the shear processing history on the viscosity has been represented by a power-law relationship with extruder screw speed.