机械搅拌用于水处理中混凝过程的研究

以机械搅拌用于水处理中混凝过程为研究对象 ,在 0 .75 m× 0 .75 m× 1 m方形搅拌槽中 ,利用配制的两种污水 ,以 Al2 ( SO4 ) 3· 1 8H2 O为絮凝剂 ,采用三种不同直径的轴流式 CBY型搅拌桨 ,分别得出适用于快速混合过程及絮凝过程的机械搅拌操作参数 :( 1 )对于快速混合过程 ,搅拌桨直径增加 ,絮凝剂混匀所需输入功率增大 ;( 2 )对于三级絮凝过程 ,三级絮凝搅拌桨叶端线速度之比为3∶ 2∶ 1 ,第一级叶端线速度的适宜范围为 :1 .5～ 1 .8m/s;输入功率相同时 ,不同直径搅拌桨的絮凝效果相当 ;对于 CBY型搅拌桨 ,离底距离对絮凝效果影响不大。     

搅拌磨湿法粉碎

<正> 精细的颗粒或颗粒尺寸的窄分布是获取特定产品性能的保证。在此方面,除了结晶过程和沉淀过程之外当首推研磨过程,如用搅拌磨。要在最经济的前提下获得所希望的细度和分布范围,必须掌握诸如应力强度、应力分布、滞留时间分布、研磨介质尺寸、液体粘度和固体含量对研磨结果的影响程度。本文以实例指出了最主要的影响尺寸和其结果。以数学模型进行了研讨并给出了搅拌磨操作方式。例如在相同的能耗下,使用     

搅拌器在工业合成醋酸反应器中的应用

详细分析了工业合成醋酸反应器中的机械搅拌过程,描述了气液分散搅拌过程中搅拌桨叶的选择和计算。对醋酸反应器这样复杂的气-液反应混合过程,必须采用合适的机械搅拌器。目前采用最多的是径向流和轴向流相结合的多层搅拌桨叶组合形式的搅拌器。搅拌桨的计算和设计对保证醋酸反应中充分的气-液分散混合并达到良好的气-液传质过程十分重要。不同大小醋酸反应釜的搅拌器必须根据不同生产处理量和醋酸装置的工艺条件进行设计和选型。     

通气式搅拌槽的传热特性

研究了通式搅拌槽槽壁给热系数（ｈｗ）随通气速率和搅拌转速变化的规律和机理，在搅拌过程中存在一个临界转速，它决定了通气是增大还是减小ｈｗ。通过引入综合反映操作条件对ｈｗ影响的无因次数Ｈｚ，获得了一个偏差较小并且简单实用的ｈｗ半经验关联式。     

搅拌器的选型方法探讨

<正> 搅拌是一种广泛应用的单元操作,它的复杂性在于它的原理要涉及流体力学、传热、传质和化学反应等多种过程。由于搅拌器是输入机械能量的装置,如何正确选用搅拌器就成为广为关注的问题。 本文阐述了搅拌器的分类、型式、适用条件、使用范围、搅拌过程能量分配和选择应用。     

搅拌反应器中颗粒完全离底悬浮的临界转速

一、引言 工业搅拌釜广泛涉及液-固二相甚至气-液-固三相系统的反应过程。大部分反应的相际传递速率,特别是传质速率,决定了过程的总速率。在传质控制的固体颗粒作催化剂的快速反应过程中,催化剂在液相中的分散程度及外部质量传递,将对     

三相床甲醇合成新工艺开发研究

三相床甲醇合成，可提高反应出口气体中的甲醇浓和单程转化率，提高反应选择性与产品质量。是一项正在开发过程中的新工艺。     

混合时间测定方法剖析与过程模拟

用湍流理论和微观混合理论对碘液退色测混合时间方法进行分析，建立了退色过程中宏观混合与微观混合的数学模型，并给出了一种桨叶的模型参数。计算表明，宏观混合时间与整个过程的混合时间的比例，随单位体积功耗的增大而增大。     

陶瓷原料搅拌混合技术

本文论述了搅拌机设计的基本原理，详细分析了搅拌混合过程中各项参数的控制。     

搅拌设备设计的发展与建议

搅拌过程是过程工业常用的单元操作。综述了搅拌设备设计的发展,目前搅拌设备的设计方法可分成依据经典设计手册的设计、专家经验与实验结合的研发性设计、基于CFD的搅拌设备辅助设计三类,并分别进行了分析和论述,强调搅拌设备的优化设计应注重过程工艺特性和设备特性的有效耦合,指出基于计算机网络平台的智能化设计方法是搅拌设备设计的发展方向。     

POWER CONSUMPTION IN MECHANICALLY AGITATED CONTACTORS USING PITCHED BLADED TURBINE IMPELLERS

Power consumption was measured in mechanically agitated contactors of internal diameter 0.3 m, 0.57 m, 1.0 m and 1.5 m. Tap water was used as a liquid in all the experiments. The impeller speed was varied in the range of 0.3-13.33 r/s. Three types of impellers, namely disc turbine (DT), pitched-blade downflow turbine (PTD) and pitched blade upflow turbine (PTU) were employed. The ratio of the impeller diameter to vessel diameter (D/T) and the ratio of impeller blade width to impeller diameter (W/D) were varied over a wide range. The effects of impeller clearance from the tank bottom (C), blade angle (φ), total liquid height (H/T), number of impeller blades (n_b) and blade thickness (t_b) were studied in detail. Power consumption was measured using a torque table

Power number was found to have a strong dependence on the flow pattern generated by the impeller. Unlike, DT and PTU, the power number of PTD was found to increase with a decrease in clearance. The PTD (T/3) was found to have the lowest power number in all the vessels and the power number increased with either a decrease or an increase in the impeller diameter from T/3. The dependence of power number on impeller diameter was found to be more prominent when the D/T ratio was more than 0.3. In general, the power number was found to increase with an increase in blade angle and blade width. The effect of blade width was found to be more prominent in larger diameter vessels. A correlation has been developed for power number in the case of PTD impellers.     

Computational fluid dynamics simulation of hydrodynamics in an uncovered unbaffled tank agitated by pitched blade turbines

Computational fluid dynamics (CFD) simulations were applied for evaluating the hydrodynamics characteristics in an uncovered unbaffled tank agitated by pitched blade turbines. A volume of fluid (VOF) method along with a Reynolds stress model (RSM) was used to capture the gas-liquid interface and the turbulence flow in the tank. The reliability and accuracy of the simulations are verified. The simulation results show that the vortex can be divided into central zone and peripheral zone, and flow field in the tank can be divided into forced vortex flow region and free vortex flow region. With the increase of impeller speed, the vortex becomes deeper, while the critical radius of the two zones keeps almost unchanged. The impeller clearance and the rotational direction have little effect on the vortex shape. The vortex becomes deeper with increasing of the impeller diameter or the blade angles at the same rotational speed. Power number is little influenced by the impeller speed, and decreases by about 30% when impeller diameter varies from 0.25T to 0.5T. When blade angle varies from 30° to 90°, power number increases by about 2.32-times. Power number in uncovered unbaffled tank is much smaller than that in baffled tank, but is very close to that in a covered unbaffled tank. The discrepancy of power number in uncovered unbaffled tank and that in covered unbaffled tank is less than 10%.     

轴流桨搅拌槽三维流场数值模拟

利用k -ε湍流模型预测了搅拌槽在不同操作条件下宏观速度场 ,模型成功预测了搅拌槽内速度分布 ,计算结果与实验结果吻合较好 .模型预测结果表明 ,搅拌槽内宏观流动场受搅拌桨槽径比影响较大 .对单层搅拌桨 -槽体系 ,挡板前后宏观流动场差别很大 ,在挡板以前区域 ,轴向流动较强 ,在整个r -z断面上形成一个整体循环 ;而在挡板后面区域 ,流体在桨叶安装位置高度附近转向轴心流动 ,槽体上半部区域形成二次循环区域 ,且二次循环区域内流体以向下流动为主 .     

Influence of impeller diameter on overall gas dispersion properties in a sparged multi-impeller stirred tank☆

The impeller configuration with a six parabolic blade disk turbine below two down-pumping hydrofoil propellers, identified as PDT + 2CBY, was used in this study. The effect of the impeller diameter D, ranging from 0.30T to 0.40T (T as the tank diameter), on gas dispersion in a stirred tank of 0.48 m diameter was investigated by experimental and CFD simulation methods. Power consumption and total gas holdup were measured for the same impeller configuration PDT + 2CBY with four different D/T. Results show that with D/T increases from 0.30 to 0.40, the relative power demand (RPD) in a gas–liquid system decreases slightly. At low superficial gas velocity V_S of 0.0078 m·s^-1, the gas holdup increases evidently with the increase of D/T. However, at high superficial gas velocity, the systemwith D/T=0.33 gets a good balance between the gas recirculation and liquid shearing rate, which resulted in the highest gas holdup among four different D/T. CFD simulation based on the two-fluid model along with the Population Balance Model (PBM) was used to investigate the effect of impeller diameter on the gas dispersion. The power consumption and total gas holdup predicted by CFD simulation were in reasonable agreement with the experimental data.     

运用粒子图像测速仪研究双层桨搅拌槽内流体流动

The flow fields in a dual Rushton impeller stirred tank with diameter of 0.48 m （T） were measured by using Particle Image Velocimetry （PIV）. Three different size impellers were used in the experiments with diameters of D = 0.33T, 0.40T and 0.50T, respectively. The multi-block and 360° ensemble-averaged approaches were used to measure the radial and axial angle-resolved velocity distributions. Three typical flow patterns, named, merging flow, parallel flow and diverging flow, were obtained by changing the clearance of the bottom impeller above the tank base （C1） and the spacing between the two impellers （C2）. The results show that while C1 is equal to D, the parallel flow occurs as C2≥0.40T, C2≥0.38T and C2≥0.32T and the merging flow occurs as C2≤0.38T, C2≤0.36T and C2≤0.27T for the impellers with diameter of D=0.33T, 0.40T and 0.50T, respectively. When C2 is equal to D, the diverging flow occurs in the value of C1≤0.15T for all three impellers. The flow numbers of these impellers were calculated for the parallel flow. Trailing vortices generated by the lower impeller for the diverging flow were shown by the 10° angle-resolved velocity measurements. The peak value of turbulence kinetic energy （ k/V^2tip = 0.12-0.15 or above） appears along the center of the impeller discharging stream.     

Experimental Study of Influence of the Impeller Spacing on Flow Behaviour of Double‐Impeller Stirred Tank

The flow fields in the stirred tank with three different kinds of combined double‐impeller agitators: disc turbine + disc turbine (DT‐DT, radial impeller), pitched blade turbine + pitched blade turbine (PTD‐PTD, axial impeller) and pitched blade turbine + disc turbine (PTD‐DT), were investigated in detail by using laser Doppler anemometry. The two‐dimensional mean velocity field and the distribution of turbulence intensity were obtained for different impeller spacings. The experimental results show that the impeller spacing has a significant influence on the flow field. To improve flow homogeneity and agitator efficiency, the appropriate impeller spacing should be in the range of 1/2 to 2/3 of the tank diameter.     

EFFECT OF IMPELLER DESIGN ON LIQUID PHASE MIXING IN MECHANICALLY AGITATED REACTORS

Liquid phase mixing time (θ_mix) was measured in mechanically agitated contactors of internal diameter 0.57 m, 1.0 m and 1.5 m. Tap water was used as the liquid phase. The impeller speed was varied in the range of 0.4-9.0 r/s. Three types of impellers, namely disc turbine (DT), pitched blade downflow turbine (PTD) and pitched-blade upflow turbine (PTU) were employed. The ratio of impeller diameter to vessel diameter (D/T) and the ratio of impeller blade width to impeller diameter (W/D) were varied over a wide range. The effects of impeller clearance from the tank bottom (C), the blade angle (φ), the number of blades (n_b), the blade thickness (k) and the total liquid height (H/T) were studied in detail. Mixing time was measured using the conductivity method.

Mixing time was found to have a strong dependance on the flow pattern generated by the impeller. Mixing time was found to decrease by decreasing the impeller clearance in the case of DT and PTU. However in the case of PTD it increases with a decrease in the impeller clearance. Similar trend of the effect of impeller clearance on θ_mix, was observed for all the other PTD impellers with different diameter, number of blades and blade angle (except 60^° and 90^°). All the impeller designs were compared on the basis of power consumption and on this basis optimum design recommendations have been made. For PTD impellers, a correlation has been developed for the dimensionless mixing time.     

IMPELLER CLEARANCE EFFECT ON OFF BOTTOM PARTICLE SUSPENSION IN AGITATED VESSELS

The effect of impeller off bottom clearance on the power input requirement for off bottom solid suspension was examined for 45° pitched blade impellers in flat and round bottom fully baffled agitated vessels. Results showed a similar dependence as obtained for radial flow impellers when similar flow patterns were observed. The dependence appears to be independent of the impeller diameter to tank diameter ratio and vessel shape.     

Influence of Impeller Diameter on Crystal Growth Kinetics of Borax in a Mixed Dual‐Impeller Batch‐Cooling Crystallizer

The influence of impeller diameter on crystal growth kinetics of borax decahydrate in a batch‐cooling crystallizer of non‐standard aspect ratio was evaluated. The dual‐impeller configuration consisted of a pitched‐blade turbine which was mounted below a straight‐blade turbine on a single shaft. Three different impeller‐to‐tank diameter ratios were investigated. In all experiments, mixing was conducted at just‐suspended impeller speed. To examine hydrodynamic conditions, mixing times were measured. The fluid flow pattern and velocity distribution were determined by computational fluid dynamics. Results showed that the smallest but also more regularly shaped crystals were produced in a system with standard diameter impellers. Product yield and power consumption were highest in this case.     

An experimental study of double-to-single-loop transition in stirred vessels

The velocity characteristics of the flows in a fully baffled vessel of diameter T = 290 mm stirred by a Rushton impeller of diameter D = T/3 were investigated by means of laser-Doppler anemometry measurements. The effects of clearance and rotational speed on the flow patterns in the vessel were studied. It was found that at impeller clearances from the bottom of the vessel (C) around 0.2 T the characteristic double-loop flow pattern undergoes a transition to a single-loop one with the impeller stream direction becoming partly axial and being inclined at around 25 to 30° to the horizontal. The impeller stream inclination varied with radial distance from the impeller, as well as with angular position between blades (blade angle). Impeller speed was found to have no effect on the flow pattern or the mean velocities and turbulence levels normalized by V_tip for C/T > 0.20 or C/T ≤ 0.15. The flow structure measured with C = 0.15T is described in detail and the implications of the data for fluid mixing in stirred vessels are discussed.