聚丙烯/纳米羟基磷灰石复合材料流变性能研究

采用毛细管流变仪对聚丙烯/纳米羟基磷灰石(PP/n HA)复合材料的流变性能进行了研究,并讨论了复合材料的表观黏度、非牛顿指数、黏流活化能与温度、剪切速率、n HA用量之间的关系。结果表明:PP/n HA熔体为假塑性流体,其表观黏度随着n HA用量的增加总体呈上升趋势,但在其用量为1%时达到极小值;非牛顿指数随着温度的提高而增大,随着n HA用量的增加而逐渐减小;黏流活化能则随着剪切速率的增加逐渐降低,随着n HA用量的增加呈上升趋势。     

流体流变性对错位六弯叶桨流场特性的影响

利用计算流体力学(CFD)的方法,以高黏牛顿流体和假塑性非牛顿流体为研究对象,对错位六弯叶桨在层流域的搅拌流场特性进行了研究。结果表明:数值计算得到的功率值与实验测量值吻合较好,搅拌雷诺数对假塑性流体搅拌流场的量纲一速度和切应变速率影响较大,因此提高转速对改变流场的速度及切应变速率分布是一个有效的办法;而流体的流变性只对假塑性流体的量纲一速度有明显影响,对切应变速率影响较小,当流变指数n<0.3时与n基本无关。当流动由层流向过渡流转变时,搅拌桨的流量准数及泵送效率有显著提高;假塑性流体的流变指数降低时,其泵送效率显著下降。研究进一步认识了错位桨在不同流体中的搅拌流场特点,为高黏假塑性流体搅拌桨的设计、应用以及开发新型搅拌桨提供了参考。     

DEDS-12/AP-P4/Na_2CO_3三元复合体系流变行为研究

研究了DEDS-12/AP-P4/Na2CO3三元复合体系(ASP)的流变行为以及盐的加入对其流变行为的影响。结果表明,在所研究的浓度范围内,DEDS-12起到无机电解质的作用,随DEDS-12浓度增加,溶液的表观粘度和剪切应力单调降低,稠度系数k下降,流性指数n增大,复合体系溶液流变行为遵循幂律流型;随体系中AP-P4和Na2CO3浓度的增高,虽然该三元体系的流变行为仍遵循幂律流型,但流性指数n增大,多在0.5以上,即与牛顿流体的差异减小;AP-P4浓度为2000 mg/L,Na2CO3浓度为1%,DEDS-12浓度为0.423 mmol/L,在NaCl浓度为1×104mg/L时,表观粘度上升3.88~8.11倍,随NaCl浓度增大,其流变行为由幂律流型逐渐表现出部分Bingham流体行为。     

剪切稠化流体内气泡上浮运动特性

剪切稠化流体是一种典型的非牛顿流体,研究气泡在其中的运动特性对优化设备结构、提高反应效率具有重要意义。文中采用流体体积(VOF)法,通过改变Gallilei数(Ga)、E?tv?s数(Eo)与流变指数(n),对牛顿流体(n=1)及剪切稠化流体(n>1)内气泡的形状、尾涡、终端速度和气泡周围液相黏度分布的变化进行了深入的数值研究。结果表明:气泡变形程度和尾涡尺寸随着Ga数或Eo数的增大而增加;剪切稠化效应会阻碍尾涡的形成,减小气泡的尾涡尺寸;气泡周围剪切速率的差异会导致气泡上方及尾部产生高黏度区域,该高黏度区域会随剪切稠化效应的增加而增大;气泡终端速度随Ga数的增大或流变指数n,Eo数的减小而增大。     

聚乳酸基注射陶瓷喂料的流变特性

使用聚乳酸、乳酸预聚物为粘结剂体系,与ZrO₂粉末制成注射陶瓷喂料。使用毛细管流变仪对陶瓷喂料的流变特性进行测试,通过线性回归分析,计算出非牛顿指数和粘流活化能。实验表明:在ZrO₂质量分数为83%—85%时,喂料的粘度随着温度的升高以及剪切速率的增大而减小,呈假塑性流体,具有较好的充模性。在四种陶瓷喂料中,3号喂料在170℃和36774Pa剪切应力条件下,其非牛顿指数n和粘流活化能E分别为0.36和41kJ·mo^-1,其综合流变性能最好。     

PP/PEG共混体系熔体流变性能研究

以聚乙二醇(PEG)为抗静电剂,在不同共混比例下与聚丙烯(PP)熔融挤出,用流变仪分析了PP/PEG二元共混体系的流变性能,并深入研究了剪切速率、温度、PEG含量等因素对共混体系熔体流变性能的影响。结果表明:PP/PEG共混体系为典型的假塑性流体;随着PEG含量的增加,非牛顿指数n先增大后减小;黏流活化能随PEG含量的增加而增加;结构黏度指数Δη则随PEG含量的增加先减小后增大,且在PEG含量为6%时达到极小值,此时共混体系的可纺性相对较好。     

剪切变稀流体中液滴运动的研究

采用VOF方法,基于非牛顿流体的流变模型对剪切变稀流体中液滴的运动进行数值模拟。结果发现剪切变稀流体中液滴的上升较稳定,上升速度前期增长较快,后期趋于平缓,轨迹呈直线型;单液滴初始半径r越大,上升过程中产生的形变越明显;溶液的稠度指数k越大,液滴上升的速度v越小;幂律指数n越大,液滴上升的速度v越大,k的作用效果比n效果明显。     

聚丙烯酰胺水溶液的流变特性

通过测定聚丙烯酰胺(PAM)水溶液不同状态下的表观黏度,研究了质量浓度、剪切速率和温度对PAM溶液流变特性的影响。结果表明,在浓度范围1.0～4.0 g/L时,PAM溶液表观黏度随浓度的增加呈线性递增。在浓度范围2.0～4.0 g/L时,PAM溶液表现为假塑性流体特性,其表观黏度随剪切速率的升高而降低,且两者的对数值呈线性关系,非牛顿指数n随稠度系数K的增加而降低;溶液表观黏度随温度的升高而降低,其黏流活化能约为10 kJ/mol。PAM溶液表现为明显的正触变性。     

PET/纳米珍珠粉共混体系的制备及其熔体流变性能的研究

制备了不同纳米珍珠粉(NPP)含量的聚酯(PET)/NPP共混体系,然后通过毛细管流变仪对其流变加工性能进行了详细地讨论。结果表明:PET/NPP共混体系属于切力变稀流体,通过加入NPP可有效降低体系的黏度;共混体系非牛顿指数(n)随NPP添加量的增加呈现先升高后下降的趋势,在1%时出现极大值;共混体系的结构黏度指数(Δη)随NPP添加量的增加呈现先减小后上升的趋势,当NPP的添加量为1%时,共混体系Δη较低,具有较好的可纺性。     

中高黏度超有光PET流变性能研究

用毛细管流变仪研究了特性黏数([η])分别为0.631,0.705,0.808,0.898,0.978 dL/g的超有光聚对苯二甲酸乙二醇酯(PET)的流变性能,并计算得到黏流活化能(Eη)和非牛顿指数(n)。结果表明:不同[η]的超有光PET表观黏度(ηa)均随剪切速率(γ)和温度的升高而降低,且n小于1,均为切力变稀假塑性流体;在相同γ和温度时,[η]为0.705,0.631 dL/g PET的ηa,Eη和n较接近,而[η]为0.808,0.898,0.978 dL/g的PET的ηa,Eη,n变化明显。     

错排降膜阵列气液交叉流界面捕集PM2.5的传质类比模型

根据气溶胶颗粒拟流体性质提出了气液交叉流界面捕集PM2.5的传质类比模型.分析了颗粒Schmidt数及其指数m对气溶胶流体传热传质类比的影响机理.以常用的横掠错排管束对流传热Nu方程为基础,导出了横掠错排降膜阵列PM2.5传质Sherwood数方程,由此建立了以m为模型参数的PM2.5捕集效率预测模型.用横掠20列×90排ø3 mm降膜阵列PM2.5捕集效率实测数据回归获得m值为0.808.在Reynolds数50～650的范围内,模型预测传质Sh与实测值误差在±20%之内.     

Effective diffusivity in a structured packed column: Experimental and Sherwood number correlating study

Mass transfer coefficients along a structured packed column were experimentally determined to obtain a new correlation for dispersed phase Sherwood number based on molecular diffusivity. Then in a comparative investigation, the correlation was re-established based on effective diffusivity. The applied chemical systems were toluene/acetic acid/water (T/A/W) and butyl acetate/acetic acid/water (B/A/W). The effects of droplet size and packing height on experimental Sherwood number were also discussed. It was shown that local Sherwood number could be increased up to 188% with increasing the droplet size from 6 to 9 mm in fixed dispersed phase flow rate. It was also observed that when height of packing increased from 10 to 40 cm, local Sherwood number decreased by almost 48% for constant dispersed phase flow rate. The results have shown that the proposed correlation based on effective diffusivity can estimate the experimental drop Sherwood number with high accuracy (error of less than 5%). Moreover, current research shows that replacing molecular with effective diffusivity in some theoretical models can correct their estimation.     

幂律流体自然对流传质的研究

本文从解扩散微分方程组的角度研究非牛顿流体的传质问题,本构方程使用幂律模型,获得近似解,并利用电化学实验进行模拟和验证.在特定条件下,近似解可回复至牛顿流体的解.     

External mass transfer from/to a single sphere in a nonlinear uniaxial extensional creeping flow

This work systematically simulates the external mass transfer from/to a spherical drop and solid particle suspended in a nonlinear uniaxial extensional creeping flow.The mass transfer problem is governed by three dimensionless parameters:the viscosity ratio(λ),the Peclet number(Pe),and the nonlinear intensity of the flow(E).The existing mass transfer theory,valid for very large Peclet numbers only,is expanded,by numerical simulations,to include a much larger range of Peclet numbers(1 ≤ Pe ≤ 10     

MASS TRANSFER COEFFICIENTS FOR REACTIVE FLUIDS FLOWING IN CONDUITS WITH SEMI-PERMEABLE WALLS

The advancing front theory is an approximate solution for mass transfer into a reactive fluid when the reaction can be assumed to be very fast. The theory has had considerable use in predicting mass transfer characteristics for reactive fluids flowing in conduits. In this paper, the mass transfer coefficient, in the form of the local, fluid-side Sherwood number, is derived for reactive flow in conduits with semi-permeable walls. The local, fluid-side Sherwood number is given as a function of the Graetz number, the wall Sherwood number, and a dimensionless reaction strength parameter. The limiting cases of both the constant wall concentration boundary condition (Sh_w?∞) and the constant wall flux boundary condition (Sh_w?∞)are investigated. Comparisons of the results with the classical Graetz and Leveque theories give conclusions about the accuracy of the advancing front theory for the worst possible case.     

Effect of the viscosity ratio on mass transfer from a fluid sphere at low to very high Peclet numbers

The effect of the viscosity ratio on mass transfer from a fluid sphere is examined in this paper. Numerical solutions of the Navier-Stokes equations off motion and the equations of mass transfer have been obtained for the unsteady state transfer from a fluid sphere moving in an unbounded fluid medium of different viscosity. The effects of the viscosity ratio and the flow on the concentration profiles were investigated for Reynolds number, viscosity ratio and Péclet number ranges of 0?Re?400, 0?κ?1000 and , respectively. The local and average Sherwood numbers are also presented graphically. The steady state results show that the average Sherwood number is increasing as Peclet number increases for a fixed viscosity ratio. However, for a fixed Peclet number, the average Sherwood number is decreasing as the viscosity ratio increases and reaches a limit value corresponding to the average Sherwood number for a solid spherical particle. From the numerical results, a predictive equation for the Sherwood number in terms of the Peclet number, the Reynolds number and the viscosity ratio is derived.     

Countercurrent plug flow mass exchange with internal particle diffusion

The model for countercurrent steady state mass transfer between uniform dispersed phase particles and a continuous phase, both assumed to move in plug flow, with diffusion resistance inside the particles, and film resistance around the particles, is solved analytically for three particle geometries: infinite plates, infinite cylinders and spheres. In the solution, the direct relation between the local continuous phase concentration, and the average dispersed phase concentration is accounted for in the boundary condition. Concentration profiles in the mass exchanger are derived from the analytical solution, as well as asymptotic Sherwood numbers. The analytical solution requires the determination of roots of the characteristic equations, which is cumbersome for spherical particles. Correlations are provided for the asymptotic Sherwood numbers for easy computation. The model can easily be used for the analogous direct heat exchange problem.     

GAS-PHASE CONTROLLED MASS TRANSFER IN A FOAM-BED REACTOR

Gas-phase controlled absorption of ammonia in foams made of solutions of sulphuric acid has been studied experimentally. Effects of gas-phase concentration of ammonia and type of surfactant on the performance of the foam-bed reactor are investigated. Gas-phase controlled absorption from a spherical bubble is anaylzed using the asymptotic value of Sherwood number (Sh = 6·58), for both negligible as well as significant changes in the volume of the bubble. The experimental data are shown to be in good agreement with the single-stage model of the foam-bed reactor using these asymptotic sub-models, as well as the diffusion-in-sphere analysis available in literature. Influence of effective diffusivity on the time dependence of fractional gas absorption has been found to be unimportant for foam columns with large times of contact. The asymptotic sub-models have been compared and use of the rigid-sphere asymptotic sub-model is recommended for foam columns of practical relevence.     

Transient gas–liquid mass transfer model for thin liquid films on structured solid packings

This paper describes a model for gas–liquid mass transfer through thin liquid films present on structured packings for gas–liquid operations under dispersed gas flow regime. The model has been derived for two cases: the absorption (or desorption) of a gaseous component into the liquid film and the transfer of the gaseous component through the liquid film to the packing surface where an infinitely fast reaction takes place. These cases have been solved for three bubble geometries: rectangular, cylindrical, and spherical. For Fourier numbers below 0.3, the model corresponds to Higbie’s penetration theory for both cases. The Sherwood numbers for cylindrical and spherical bubbles are 20% and 35% higher, respectively, than for rectangular bubbles. In case of absorption and Fourier numbers exceeding 3, the effect of bubble geometry becomes more pronounced. The Sherwood numbers for cylindrical and spherical bubbles now are 55% and 100% higher, respectively, than for rectangular bubbles. In case of an infinitely fast reaction at the packing surface, the Sherwood number corresponds to Whitman’s film theory (Sh=1$Sh=1$) for all bubble geometries. In this paper also practical approximations to the derived Sherwood numbers are presented. The approximations for both cases and all bubble geometries describe all the model data within an error of 4%. The application of the model has been demonstrated for three examples: (1) gas–liquid mass transfer for a structured packing; (2) gas–liquid mass transfer in a microchannel operated with annular flow; (3) gas–liquid mass transfer in a microchannel with Taylor flow.     

Laminar flow diffusion of power-law fluids in a tube with arbitrary order heterogeneous and homogeneous reactions

Solutions for isothermal laminar flow diffusion with simultaneous heterogeneous and homogeneous reactions in a tube are extended to the case of non-Newtonian power-law fluids with arbitrary order reactions. Finite-difference methods are employed to yield the solutions. Special emphases are placed on the role of the reaction product characterized by two unique parameters, the diffusivity ratio and the stoichiometric coefficient ratio. Effects of reaction rate kparameters on the unique parameters, the diffusivity ratio and the stoichiometric coefficient ratio. Effects of reaction rate parameters on the system performance are also presented, showing a crossover behavior of the Sherwood number. The results are in good agreement with known solutions for systems of Newtonian fluids with first-order reactions.