The effect of axial impeller geometry on the link between power and flow numbers

Stirred vessels are used to facilitate mixing processes across a wide range of industries. Their performance can often be predicted with certain characteristics of the agitator, like the dimensionless power and flow numbers. Since there exists a large number of agitator designs and geometries, it is desirable to be able to predict these characteristics using models rather than rely on previous experimental data. In this study, we use an angular momentum balance combined with computational fluid dynamics to correlate the power, flow, and mixer geometry across a wide range of down-pumping pitched blade turbine geometries. The models developed from the results allow us to predict the power from the flow (or vice versa) for the geometries investigated. We tested two methods for the measurement of the flow rate and found that the choice of measurement method can affect the relationship between the power, flow, and impeller geometry.     

Reconstruction of large-scale flow structures in a stirred tank from limited sensor data

We combine reduced order modeling and system identification to reconstruct the temporal evolution of large-scale vortical structures behind the blades of a Rushton impeller. We performed direct numerical simulations at Reynolds number 600 and employed proper orthogonal decomposition (POD) to extract the dominant modes and their temporal coefficients. We then applied the identification algorithm, N4SID, to construct an estimator that captures the relation between the velocity signals at sensor points (input) and the POD coefficients (output). We show that the first pair of modes can be very well reconstructed using the velocity time signal from even a single sensor point. A larger number of points improves accuracy and robustness and also leads to better reconstruction for the second pair of POD modes. Application of the estimator derived at Re = 600 to the flows at Re = 500 and 700 shows that it is robust with respect to changes in operating conditions.     

Sag in commercial thermoforming

Our previous analytical solution gives sag advancing implicitly as , or for , sag advances with the cube root of time for a thin wide rectangular Newtonian isothermal sheet. This previous analytical work applies to sheets that are pinned along just two edges, and not all the way around. Corresponding sagometer experimental results confirmed this cube root relation. This work compares the prediction with measured commercial thermoforming behavior on rectangular sheets that are, of course, pinned all the way around. Then sag parallel superposition is used to extend for a sheet pinned all the way around. We evaluate sag parallel superposition using a finite element method (FEM) employing ANSYS Polyflow. The equation assumes sagging sheet cylindricity, and from our FEM we find that this assumption is reliable when . We compare sag measured in commercial thermoforming, using high‐impact polystyrene (HIPS) sheets that are pinned all the way around, by extending with parallel superposition. It is found that the time evolution of the commercial sag follows nearly exactly the same shape as the isothermal prediction. We measure sag runaway, and although the isothermal analysis , predicts the sag runaway time accurately, our isothermal theory overpredicts the amount of sag in the nonisothermal commercial operation by as much as a factor of 14. It is also shown how to use sheet sag measurements from commercial thermoforming to deduce the Newtonian viscosity of a thermoforming resin at a temperature that is above its softening point. © 2013 American Institute of Chemical Engineers AIChE J, 60: 1529–1535, 2014     

多层带式干燥机风速场的CFD模拟及检验

多层带式干燥机箱内风速分布不均匀是导致干燥效率低、干燥不均匀的主要原因。对多层带式干燥机风速场进行了实验研究，建立了多层带式干燥机箱的CFD理论模型，对其风速场进行了数值模拟，并与实验测试结果进行对比，认为用CFD方法模拟多层带式干燥机箱内风速场是可行的。     

Application of direct fluid flow oscillations to improve mixing in microbioreactors

This article describes an active mixing method for a microbioreactor that was designed, simulated, tested, and successfully implemented. By applying a varying pressure to a microchannel looping tangentially into a cylindrical microreactor an oscillating fluid flow was shown to occur. Such an oscillating fluid flow improved mixing, both by diffusion and convection. The oscillating fluid flow has a large impact on the ratio between the diffusion domain and the convection domain. A good match was obtained between experimental mixing results, computational fluid dynamics simulation results and the results of a simplified mixing model thus demonstrating the potential of simulation on improving the design of microreactors. © 2009 American Institute of Chemical Engineers AIChE J, 2009     

一种计算搅拌槽混合时间的新方法

基于对混合时间定义的思考,提出了一种新的定义方法,在湍流流场数值计算的基础上通过求解示踪剂的浓度输运方程,研究了单层涡轮桨搅拌槽内的混合过程。结果表明：搅拌转速和搅拌桨安装位置都影响混合时间的大小,而进料位置对混合时间的影响不大。对于不同的搅拌转速而言,随搅拌转速的增大,相同体积分数对应的混合时间逐渐减小。当搅拌桨安装在槽中间位置时所对应的混合时间最小。利用适宜的尺寸和安装位置的导流筒可有效降低混合时间。     

Characterisation of the mixing of non‐newtonian fluids with a scaba 6SRGT impeller through ert and CFD

An attempt has been made to study the mixing of yield‐pseudoplastic fluids with a Scaba 6SRGT impeller using electrical resistance tomography (ERT) and computational fluid dynamics (CFD). The ERT system with four sensor planes, each containing 16 equispaced stainless steel electrodes, was used to measure the mixing time. The multiple reference frames (MRF) technique and the modified Herschel–Bulkley model were applied to simulate the impeller rotation and the rheological behaviour of the non‐Newtonian fluids, respectively. To validate the model, the CFD results for the power consumption were compared to the experimental data. The validated model was then employed to obtain further information regarding the averaged impeller shear rate, impeller circulation, and pumping capacities. The CFD and ERT data were utilised to investigate the effect of the impeller power, fluid rheology, and impeller size on the mixing time. The mixing time results obtained in this study were in good agreement with those reported in the literature. © 2011 Canadian Society for Chemical Engineering     

电场强化层流搅拌的荧光可视化试验及模拟分析

在层流搅拌中,搅拌桨的周期性扰动使搅拌槽内出现封闭、孤立的环状隔离流场。隔离流场严重阻碍了搅拌介质之间的有效交换,降低了搅拌效率。本文提出外加电场以强化层流搅拌的方案,利用电流体动力学效应改变流场的对称结构,消除混合死区。试验采用平面激光诱导荧光（planner laser induced fluorescence, PLIF）技术实现了搅拌槽内流场结构的实时可视化,并通过自编程程序识别并计算出非混合区域面积百分比。结果表明,随着电场强度的增大,混合效率逐渐提升,当电场强度为1.5kV/cm时混合效率可达98%。研究建立了基于有限元法及浓度扩散模型的混合搅拌模拟平台,探究搅拌槽内部流场结构时空演变规律。通过模拟分析发现,当外加平行板电场强度达到0.5kV/cm以上时,搅拌槽内部出现明显的二次涡流。二次涡流的出现与径向混合相互作用从而不断削弱隔离流场。在电场强度不变的条件下,外加周期性电场可以进一步提高搅拌效率,电场强度1kV/cm条件下的外加周期性电场可以使搅拌效率提升至98%以上。     

Scalar mixing in anisotropic turbulent flow

While turbulent mixing has been studied extensively in homogeneous turbulence, chemical engineering processes where mixing is important are anisotropic. In anisotropic turbulence, the interplay between convection and diffusion is critical. Flow in an infinite channel is utilized here with clouds of scalars released instantaneously at different distances from the wall and at Schmidt numbers between 0.7 and 2400. Qualitative and quantitative measures of mixing efficiency and intensity are defined and the dynamics of mixing are explored. It is found that molecular diffusivity can even hinder mixing in some instances, because it affects the development of the cloud of the released scalars from regions within the viscous wall layer. Another finding is that while one would expect mixing to occur mostly in the space between two points of release, considerable amount of mixing could take place outside of this region and closer to the wall. © 2018 American Institute of Chemical Engineers AIChE J, 64: 2803–2815, 2018     

循环射流混合槽内液液两相混合特性数值模拟

循环射流混合槽作为一种高效的混合装置在化工过程强化处理技术中具有潜在的工业应用前景。由于缺乏对其内多相体系流动和混合行为的研究,制约了循环射流混合反应器的优化设计与工业化应用。本文选取水和二甲基硅油两相体系,采用计算流体力学软件ANSYS Fluent V16.1中Eulerian-Eulerian多相流模型和SST k-?湍流模型,对两种不同加料方式下循环射流混合槽内液液两相射流中心线速度、离析强度、拉伸率等参数进行研究。研究结果表明：分散相浓度（α_d）增大射流卷吸能耗增大,在l/s<0.4内α_d=1.80%和2.86%量纲为1的射流中心线速度衰减趋势与α_d=6.00%相比减弱51%和21%;在低分散相浓度时,量纲为1的射流中心线速度随Re的增大衰减趋势变化小,在l/s<0.24内Re=6346、9519和12692量纲为1的射流中心线速度衰减趋势与Re=3173相比分别减弱2.60%、2.87%和12.69%。离析强度随混合时间的增大而减小,随周向角度增大呈W形变化趋势。在相含率和雷诺数相同时,对称球状较圆柱状加料达到混合时间减少65.5%;不同喷嘴之间的拉伸率随迹线长度的增大而增大,jet1和jet9位置处的拉伸率与其余喷嘴相比较大;相同喷嘴之间拉伸率随Re的增大而增大,Re=6346、9519和12692的拉伸率与Re=3173相比分别提高289%~320%、418%~454%和607%~667%。     

自由基聚合反应器中多尺度流场的模拟进展

自由基聚合过程中,由于混合、传递及聚合反应的相互作用使得反应器内部存在复杂的多尺度流场,例如宏观尺度的速度、浓度、温度分布,介观尺度的液滴粒径分布,微观尺度的聚合反应速率、聚合物分子量和多分散性指数分布。这些复杂的多尺度流场分布使得聚合反应器的模型化研究成为难题。本文较为系统地介绍了自由基聚合反应器中存在的多尺度现象;简述了微观尺度聚合物性质流场分布的模型化与模拟研究方法;从悬浮聚合和乳液聚合两个方面介绍了介观尺度液滴粒径分布的模拟研究进展;从非理想混合的角度阐述了宏观尺度多相流流场分布的研究进展。最后,本文分析了多尺度模型的耦合求解方法。本综述也有本文作者对这个领域的初步观点,可为聚合反应器的设计、优化和放大提供参考。     

Direct numerical simulation of the turbulent flow in a baffled tank driven by a Rushton turbine

We present a direct numerical simulation (DNS) of the turbulent flow in a baffled tank driven by by a Rushton turbine. The DNS is compared to a Large Eddy Simulation (LES), a Reynolds Averaged Navier‐Stokes (RANS) simulation, Laser Doppler Velocimetry data, and Particle Image Velocimetry data from the literature. By Reynolds averaging the DNS‐data, we validate the turbulent viscosity hypothesis by demonstrating strong alignment between the Reynolds stress and the mean strain rate. Although the turbulent viscosity ν_T in the DNS is larger than in the RANS simulation, the turbulent viscosity parameter C_μ = ν_T?/k², is an order of magnitude smaller than the standard 0.09 value of the k‐? model. By filtering the DNS‐data, we show that the Smagorinsky constant C_S is uniformly distributed over the tank with C_S ≈ 0.1. Consequently, the dynamic Smagorisnky model does not improve the accuracy of the LES. © 2012 American Institute of Chemical Engineers AIChE J, 2012     

不同入口结构下行床内气固流动及混合行为的CFD-DEM模拟

采用计算流体力学和离散单元模型（CFD-DEM）耦合一种简单的气固催化反应模型对具有不同入口结构的二维下行床内的气粒流动和混合行为进行全床数值模拟。模拟得到了不同入口结构下行床内的多尺度气固运动状态、全床的固含、速度及反应生成物浓度分布,以及气体和颗粒在下行床内的停留时间分布,发现入口结构对反应器内的流动、混合和气固接触效率起着关键性的作用,入口气体和颗粒的不均匀分布将导致下行床内气体停留时间的宽分布以及气固接触效果的恶劣。     

搅拌槽内混合过程的模拟计算方法

利用CFD软件Fluent,对搅拌槽内的混合过程进行了模拟计算。通过整体监测槽内示踪剂浓度的最大、最小值的来计算混合时间,并定义混合体积描述宏观混合过程。结果表明:桨叶产生的流场分布—平行流与文献的PIV研究监测结果具有良好的一致性;整体监测得到的混合时间之间的差值较小;混合体积曲线能够从宏观的角度来分析搅拌混合过程。     

基于CFD的新型布浆器混合室结构

为了进一步改善新型布浆器的布浆性能,设计了单腔式混合室（混合室Ⅰ）、以两组支管为单位的多腔式混合室（混合室Ⅱ）及以单组支管为单位的多腔式混合室（混合室Ⅲ）,采用计算流体力学（CFD）方法对混合室内的流动特性进行了模拟。结果表明,单腔混合室内,由于平行射流组各股射流间的强烈干涉作用,导致各股射流向混合室中部聚集,造成出口处质量流量分布呈现中间明显高于两侧的状态。在多腔混合室Ⅱ内,每个混合腔内有两组射流,保证了浆料的良好混合,避免了射流在中部聚集的现象。在多腔混合室Ⅲ内,由于每个混合腔内只有一组支管射流,实现了互补混合过程,混合效果明显好于混合室Ⅰ和混合室Ⅱ。从质量流量分布看,混合室Ⅲ的分布曲线比混合室Ⅰ和混合室Ⅱ的更平缓,其最大偏差仅为0.254%,明显小于混合室Ⅰ的0.538%和混合室Ⅱ的0.294%,更接近于理论混合平均值和期望值。     

导风叶片对涡流空气分级机内流场的影响

利用ANSYS-Fluent 17.0软件对有、无导风叶片两种结构的涡流空气分级机内流场进行数值模拟和对比分析,研究了导风叶片对涡流空气分级机内流场的影响。数值模拟结果表明：导风叶片降低了转笼外缘处气流切向速度,从而影响转笼通道内旋涡的分布情况,使有、无导风叶片两种结构的稳定工况不同;导风叶片减小了转笼外缘处气流径向速度的波动和湍流耗散率,此处流场分布相对均匀,有利于提高分级精度;此外,导风叶片在导流过程中,改变了环形区速度场的分布,气流切向速度减小,径向速度增大,径向速度的增大使其分级粒径增大。碳酸钙物料分级实验结果表明：具有导风叶片结构的涡流空气分级机分级粒径较大,分级精度较高;导风叶片处较大的湍流耗散率有助于粉体分散,明显减弱“鱼钩效应”现象。     

用数值模拟方法分析混合和导流筒对搅拌槽中沉淀硫酸钡的影响

1 INTRODUCTION Precipitation of sparingly soluble salts is an im- portant operation widely adopted in the production of functional materials, catalyst, protein, pharmaceutical product and pigment. By precipitation, two aqueous streams containing respective reactants are mixed in a precipitator, and the sparingly soluble salt forms as result of chemical reaction if the concentration of produced salt exceeds its solubility. The quality of the final product obtained by precipitation is strong…     

翼形桨搅拌槽内混合过程的数值模拟

采用FLUENT软件的多重参考系(MRF)及标准k-ε模型,将速度场与浓度场方程分开进行求解,对单层轴流式三叶CBY翼形桨搅拌槽内的混合过程进行了数值模拟,所得的混合时间的模拟结果与实验值相吻合。同时采用数值模拟的方法研究了不同的示踪剂加料点、监测点位置及操作条件对混合时间的影响规律;模拟结果表明,混合过程主要由搅拌槽内的流体流动所控制,混合时间与示踪剂加料点及监测点位置密切相关。上述的研究结果对于工业搅拌反应器的优化具有一定的参考意义。