陶瓷微滤膜处理钛白粉水洗液的过程强化研究

本文采用湍流促进器和反冲对陶瓷膜处理钛白粉水洗液的微滤过程进行了强化研究。实验和以上两种方法均不同程度地提高了渗透通量,降低了能耗。考察卫湍流促进器结构参数和反冲持续时间、压力、周期对强化效果的影响,确定了合适的湍流促进器结构参数和反冲条件,并对反冲的重复性进行了实验考察。     

湍流促进器强化陶瓷膜微滤CaSO_4悬浆液的研究

研究了湍流促进器对19通道陶瓷膜微滤CaSO4悬浆液过程的影响,优化湍流促进器的优化设计参数。确定螺旋式湍流促进器的强化效果较好。设置方式为内圈螺间距4 mm,外径3.4 mm和外圈螺间距8 mm,外径3.4 mm的组合式,螺旋湍流促进器的强化效果最佳,膜通量提高23.76%,并有效地改善了膜通道内流体流动状态。     

湍流促进器对液固一体式膜反应器中膜过滤性能影响的研究

以改善液固一体式膜反应器中膜过滤性能为目的,设计了3种外置式湍流促进器进行膜过滤强化实验,考察了湍流促进器的构型、旋转速度等因素对膜通量的影响。结果表明,旋转的湍流促进器可以明显地提高膜通量,其中推进式湍流促进器的强化效果最明显;随着湍流促进器旋转速度的增加,膜通量也相应增加;采用该湍流促进器可以进行高悬浮液质量浓度的膜过滤强化实验。     

陶瓷膜分离CaCO_3悬浆液强化过程的研究

在固定反冲条件下,研究了螺旋型湍流促进器及其螺杆直径、螺间距等参数对19通道无机陶瓷膜分离轻质碳酸钙悬浆液的强化过程,确定了湍流促进器的优化设计参数,并在优化条件下,对操作压力、操作温度、膜面流量和溶液浓度等操作条件进行了研究。     

陶瓷膜过程强化的数学模拟

对 Altmann等人提出的数学模型进行了改进 ,提出了沉积层空隙率随操作参数变化的观点 ,较好地拟合了陶瓷膜非强化过程的实验数据。并在此基础上对湍流促进器强化过程进行了数学模拟 ,反映了操作参数对过滤通量的影响。     

低砷磷生产工艺中分相器的优化技术研究

通过建立计算流体力学模型,采用Fluent软件,选用雷诺应力模型(RSM模型)作为湍流模型对该工艺中的液-液旋流分相器进行流体力学数值模拟,通过数值模拟仿真优化旋流器的各结构参数,同时研究不同操作参数和物性参数对旋流器分离效率的影响,并在此基础上进行结构参数的优化.模拟结果表明,溢流口直径为30 mm,溢流管伸入长度为60 mm,圆柱段长度为80 mm时旋流器分离效率最佳.     

基于BP神经网络的湍流促进器多目标优化

利用CFD软件STAR-CCM+对螺旋缠绕式湍流促进器的8种设计参数进行流场数值计算,以壁面剪应力和轴向压降为指标,比较不同参数的湍流促进器强化效果。建立了基于遗传算法优化的BP神经网络,使用神经网络对不同的设计参数进行流场效果预测,网络拟合精确度达到了0. 99 718。以最小化轴向压降最大化平均壁面剪应力为目标,利用NSGA-Ⅱ算法进行多目标优化,计算出Pareto最优支配前沿,在最优支配前沿中寻找到合适的设计点,并对预测出的优化参数进行建模并模拟验证。结果分析表明,与初始设计参数相比,在中心杆直径选取为10. 8 mm、螺距为6. 5 mm时,流场的轴向压降增加了1. 7%,平均壁面剪应力提高了9. 7%。     

低阻力湍流促进器设计与流动特性分析

设计了一种梯形截面的新型螺旋型湍流促进器,分析了速度、湍动能、湍流耗散率、压力、壁面剪切力等物理量的指标变化以及在流场中的分布状态,结合数值模拟分析法探索螺旋型湍流促进器强化传质过程的作用机理,并与传统半圆形截面螺旋型湍流促进器的流体动力学性能和能耗进行了对比。研究表明,梯形截面螺旋型湍流促进器流场的最大速度为1.44 m/s,湍动能平均值为0.023 K,壁面剪切力平均值为9.55 Pa,轴向压力降与壁面剪切力的比值为165;半圆形截面螺旋型湍流促进器流场的最大速度为1.17 m/s,湍动能平均值为0.02 K,壁面剪切力平均值为7.35 Pa,轴向压力降与壁面剪切力的比值为155;梯形截面的螺旋型湍流促进器流场的流体动力学性能要优于半圆形截面螺旋型湍流促进器,且压力降与壁面剪切力相比增加幅度较小,即相对阻力更小,在满足强化传质要求的同时消耗更少的能量。     

双切向环流气体分布器结构优化的研究

双切向环流气体分布器性能的优劣与导流板和套筒结构的密切相关。优化导流板和套筒结构可强化双切向环流气体分布器的稳流性能,改善塔内流场分布。文中利用CFD软件采用k-ε湍流模型,对分布器内不同环形通道宽度下的流场分布进行了数值模拟。考察了套筒与塔壁的间距L变化对分布器性能的影响,并得出了在既定塔径下分布器性能达到最优时L的尺寸。通过模拟不同导流板数目和结构下塔内的流场分布,考察了分布器性能随导流板数目、轴向及径向倾角的变化趋势。分析得出使分布器压降最小,流场分布最优时挡板的结构参数。为工程设计时预测分布器的速度场及能量耗散提供参考。     

大粗糙度横肋管摩擦阻力与传热特性

在凝结换热实验台上 ,采用恒壁温法和恒热流法对油品在大粗糙度横肋管中的层流与湍流摩擦阻力与传热特性进行了实验研究 .实验过程中Re为 5 0～ 6 2 0 0 ,Pr为 75～ 2 6 0 ,管子粗糙高度为 5mm ,导程为 30mm .实验结果表明 ,由于实验管特殊几何结构 (大粗糙度 )和油品物性参数的相互作用 ,使其表现出与以水或空气为工质的常用强化管不同的流动传热规律 ,并且实验方法对实验结果的影响不大 .根据实验结果 ,提出了层流区和湍流区油品量纲 1摩擦系数及传热系数的关联式 ,并将实验数据与Ravigururajan和Bergles关联式的计算值进行了比较 .研究结果可用于大粗糙度横肋管换热器的设计及运行参数优化 .     

Mass transfer in 3D-printed electrolyzers: The importance of inlet effects

This article investigates the effect of inlet shape, entrance length, and turbulence promoters on mass transfer by using 3D-printed electrolyzers. Our results show that the inlet design can promote turbulence and lead to an earlier transition to turbulent flow. The Reynolds number at which the transition occurs can be predicted by the ratio of the cross-sectional area of the inlet to the cross-sectional area of the electrolyzer channel. A longer entrance length results in more laminar behavior and a later transition to turbulent flow. With an entrance length of 550 mm, the inlet design did no longer affect the mass transfer performance significantly. The addition of gyroid type turbulence promoters resulted in a factor of 2 to 4 increase in mass transfer depending on inlet design, entrance length, and the type of promoter. From one configuration to another, there was a minimal variation in pressure drop (<1600 Pa).     

Mass-transfer conditions at a cathode support plate in an electrochemical cell

The presence of turbulence promoters in an electrochemical cell increases the intensity of local turbulence which enhances the limiting current density and hence the mass-transfer coefficient at the transfer surface. The regularity of their geometrical configuration induces a pseudo-uniformity of the spatial distributions of the local mass-transfer coefficients.

Limiting current data have been obtained at point copper electrodes flush-fitting on a cathode support plate in the presence of rectangular turbulence promoters. The effect of the flow rate of the electrolyte, the height of the promoter and the spacing between the promoters have been studied. The data are best correlated by the following equation: J_D=390Re^−0.87(S/H^−0.15

where S is the promoter spacing (m) and H the promoter height (m).     

Flux Improvement during Cross-flow Microfiltration of Wheat Starch Suspension using Turbulence Promoter

The objective of this study was to investigate the effects of the process variables (transmembrane pressure, flow rate, and concentration) on the permeate flux during the microfiltration of model starch suspensions, and to determine the conditions under which the use of Kenics statics mixer as a turbulence promoter is justified. A response surface methodology was used to examine the influence of the selected operating conditions on starch suspension microfiltration using a single channel ceramic membrane with 200 nm pore size. The experimental results clearly show that the improved performance of starch suspension cross-flow microfiltration can be obtained by using a Kenics static mixer, especially at lower flow rates. Compared to the operation without the turbulence promoter, the average permeate flux improvement during the filtration period ranged from 30% to 230%. As a result of the statistical analysis, the optimal conditions for starch suspension microfiltration were determined and applied to microfiltration of starch industry wastewater.     

Local mass transport effects in the FM01 laboratory electrolyser

A number of patterns of segmented line electrodes have been manufactured using copper printed circuit board technology. These segmented electrodes have been used to investigate local mass transport effects in ICI's FM01-LC parallel plate electrolyser. It is shown that in the absence of a turbulence promoter the current distribution is uneven. Along the direction of electrolyte flow, a tertiary current distribution is observed. In addition, close to the cell entrance, an uneven current distribution occurs perpendicular to the direction of electrolyte flow; this reflects the design of the electrolyte distributor. With a turbulence promoter the current distribution is more even and the entry effects are much reduced. The turbulence promoter can, however, impose its own pattern on the current distribution perpendicular to the flow.     

Experimental Investigation on the Separation of Bentonite using Ceramic Membranes: Effect of Turbulence Promoters

Abstract

The static turbulence promoters presented in this work are designed to enhance filtration within tubular ceramic membranes of 0.5 micron pore size. Permeate flux enhancement still remains a topical problem during tangential crossflow filtration. The decline in flux with time is due to the usual phenomena of concentration polarization and membrane fouling, operating parameters including the system pressures, feed composition, membrane type and configuration, and the hydrodynamics within the membrane module. Solute accumulates on the membrane surface and forms a high concentration gel layer, thus increasing the effective membrane thickness and reduces its hydraulic permeability. Turbulence promoters of varying pitch lengths have been incorporated into the work to ultimately reduce the deposition of bentonite particles on the membrane surface during microfiltration. Yeast suspensions have previously been used as feed suspensions in order to compare the effectiveness of the turbulence promoters with an organic foulant. The objective of this work was to investigate the influence of static promoter geometry on flux sustainability enhancement during bentonite suspension filtration. All experiments have been conducted on a tubular ceramic membrane and the experimental membrane rig as shown in this paper. The effects of feed concentration, feed temperature, system pressures, and crossflow rates on the membrane flux sustainability were investigated. It was found that the promoters greatly improved flux sustainability and membrane efficiency over time and in some cases, a loss of 3% in membrane efficiency was realized with turbulence promoters at higher feed temperatures. The use of the turbulence promoter caused a large scouring of the membrane surface and membrane cleaning was significantly improved compared to the experiments without the promoters.     

A simple device to test biodiesel process intensification

In this paper, we have studied the KOH catalyzed transesterification reaction of vegetable oil with methanol in a tubular reactor filled with small spheres of stainless steel of different sizes. Three different packed bed configurations have been tested corresponding to different fluid dynamic situations. The first configuration corresponds to the tubular reactor filled with spheres of 2.5 mm of diameters; in the second configuration an opportune amount of spheres of 1 mm has been added to the mentioned spheres of 2.5 mm for filling the void volume of the octahedral cavities between the bigger spheres; in the third configuration an opportune amount of spheres of 0.39 mm has been added to spheres of 2.5 mm for filling the void volume of the tetrahedral cavities between the bigger spheres. The three mentioned configurations give place to the formation of micro-channels with an approximated size of respectively 1000 μm, 500 μm and 300 μm. These systems, subjected to fluid dynamic characterization, have shown a very high local turbulence (static mixer), in particular, when a packed bed reactor with dual size packing is used. Then, kinetic transesterification runs have been made by using the three mentioned packed bed reactors and a very high productivity has been obtained as a consequence of the induced local micro-mixing. A simplified kinetic model has been developed, which is able to describe many runs in batch conditions reported by the literature. This model resulted unsuitable to simulate the continuous runs performed in the described packed bed reactors. Our conclusion is that monophasic models, often proposed in the literature, are not able to describe the kinetic behavior of KOH catalysed transesterification in microchannels devices. At last, the described microchannels device represents, as it will be discussed, an ideal connection between a traditional tubular packed bed reactor and the recently appeared microreactors that are very efficient in mass and energy transfer operations for process intensification.     

Characterization of dynamic behaviour of the continuous phase in liquid fluidized bed

The dynamic behaviour of the continuous phase in liquid solid fluidized bed is characterized through velocity measurements by laser anemometry at the top of the bed. The experiments were conducted using glass particles of 2, 4 and 8 mm diameter fluidized by water. The root mean square (RMS) of axial velocity fluctuations presents a maximum value at porosity around 0.7 and increases with particle diameter. When compared to the fixed bed situation, we observe an enhancement of the agitation probably due to the added mass effect which plays the role of a turbulence promoter. The spectra analysis of the velocity time series has revealed a specific spectral dynamic of liquid fluidized bed for the higher frequency range which does neither follow strictly the Kolmogorov law nor a Brownian process power law. A time frequency-scale decomposition combined to an autocorrelation analysis of velocity signal was pertinent to capture the impact of porosity waves and cooperative movements of particles on the liquid phase dynamic, and to characterize these coherent structures by low frequency scales (below 1 Hz). The results compare well with the available data obtained directly from void propagation studies by light transmission techniques. Moreover, the high frequency scales have been found random and linked to the small scale movements of the particles. We have shown, when possible, the similarity of behaviour between the liquid and the dispersed phase dynamics through the comparison of some characteristics.     

DEM simulation of the particle dynamics in two-dimensional spouted beds

A Discrete Element Method (DEM) is used together with the continuum model of turbulent fluids to simulate the periodic spouting of granular solids in a two-dimensional spouted bed. The bed is contained in a rectangular column of 152 mm width and 15 mm depth with a tapered base. Glass beads with a diameter of 2 mm are used as bed material. Simulations using the DEM together with a low Reynolds number k-ε turbulence model for the fluid phase yield predictions of the unstable spout regime, characterized as a periodic upward-moving particle jet. The simulation results compare well to experimental data obtained using a particle image velocimetry (PIV) technique, including fluid flow fields, time-averaged particle velocity profiles, and spout shape. Finally, DEM predictions for distribution of drag and net force on the particles, particle concentration fields, gas velocity and turbulence field are discussed.