Numerical simulation and analysis of solid-liquid two-phase threedimensional unsteady flow in centrifugal slurry pump

Based on RNG k-ε turbulence model and sliding grid technique, solid-liquid two-phase three-dimensional(3-D) unsteady turbulence of full passage in slurry pump was simulated by means of Fluent software. The effects of unsteady flow characteristics on solid-liquid two-phase flow and pump performance were researched under design condition. The results show that clocking effect has a significant influence on the flow in pump, and the fluctuation of flow velocity and pressure is obvious, particularly near the volute tongue, at the position of small sections of volute and within diffuser. Clocking effect has a more influence on liquid-phase than on solid-phase, and the wake-jet structure of relative velocity of solid-phase is less obvious than liquid-phase near the volute tongue and the impeller passage outlet. The fluctuation of relative velocity of solid-phase flow is 7.6% smaller than liquid-phase flow at the impeller outlet on circular path. Head and radial forces of the impeller are 8.1% and 85.7% of fluctuation, respectively. The results provide a theoretical basis for further research for turbulence, improving efficient, reducing the hydraulic losses and wear. Finally, field tests were carried out to verify the operation and wear of slurry pump.

Computational Analysis of Centrifugal Pump Delivering Solid-liquid Two-phase Flow during Startup Period

The transient behavior of centrifugal pumps during transient operating periods, such as startup and stopping, has drawn more and more attention recently because of urgent needs in engineering. Up to now, almost all the existing studies on this behavior are limited to using water as working fluid. The study on the transient behavior related to solid-liquid two-phase flow has not been seen yet. In order to explore the transient characteristics of a high specific-speed centrifugal pump during startup period delivering the pure water and solid-liquid two-phase flow, the transient flows inside the pump are numerically simulated using the dynamic mesh method. The variable rotational speed and flow rate with time obtained from experiment are best fitted as the function of time, and are written into computational fluid dynamics （CFD） code-FLUENT by using a user defined function. The predicted heads are compared with experimental results when pumping pure water. The results show that the difference in the transient performance during startup period is very obvious between water and solid-liquid two-phase flow during the later stage of startup process. Moreover, the time for the solid-liquid two-phase flow to achieve a stable condition is longer than that for water. The solid-liquid two-phase flow results in a higher impeller shaft power, a larger dynamic reaction force, a more violent fluctuation in pressure and a reduced stable pressure rise comparing with water. The research may be useful to tmderstanding on the transient behavior of a centrifugal pump under a solid-liquid two-phase flow during startup period.

Numerical simulation of predicting and reducing solid particle erosion of solid-liquid two-phase flow in a choke

Chokes are one of the most important components of downhole flow-control equipment. The particle erosion mathematical model, which considers particle-particle interaction, was established and used to simulate solid particle movement as well as particle erosion characteristics of the solid-liquid two-phase flow in a choke. The corresponding erosion reduction approach by setting ribs on the inner wall of the choke was advanced. This mathematical model includes three parts： the flow field simulation of the continuous carrier fluid by an Eulerian approach, the particle interaction simulation using the discrete particle hard sphere model by a Lagrangian approach and calculation of erosion rate using semiempirical correlations. The results show that particles accumulated in a narrow region from inlet to outlet of the choke and the dominating factor affecting particle motion is the fluid drag force. As a result, the optimization of rib geometrical parameters indicates that good anti-erosion performance can be achieved by four ribs, each of them with a height （H） of 3 mm and a width （B） of 5 mm equaling the interval between ribs （L）.

Numerical Simulation of Erosion-Corrosion in the Liquid-Solid Two-Phase Flow

Erosion-corrosion of liquid-solid two-phase flow occurring in a pipe with sudden expansion in cross-section is numerically simulated in this paper. The global model for erosion-corrosion process includes three main components: the liquid-solid two-phase flow model, erosion model and corrosion model. The Eulerian-Lagrangian approach is used to simulate liquid-solid two-phase flow, while the stochastic trajectory model was adopted to obtain properties of particle phase. Two-way coupling effect between the fluid and the particle phase is considered in the model. The accuracy of the models is tested by the data in the reference. The comparison shows that the model is basically correct and feasible.

Pressure Drop of Liquid–Solid Two-Phase Flow in the Vertical Tube Bundle of a Cold-Model Circulating Fluidized Bed Evaporator

A cold-model vertical multi-tube circulating fluidized bed evaporator was designed and built to conduct a visualization study on the pressure drop of a liquid–solid two-phase flow and the corresponding particle distribution.Water and polyformaldehyde particle(POM)were used as the liquid and solid phases,respectively.The effects of operating parameters such as the amount of added particles,circulating flow rate,and particle size were systematically investigated.The results showed that the addition of the particles increased the pressure drop in the vertical tube bundle.The maximum pressure drop ratios were 18.65%,21.15%,18.00%,and 21.15%within the experimental range of the amount of added particles for POM1,POM2,POM3,and POM4,respectively.The pressure drop ratio basically decreased with the increase in the circulating flow rate but fluctuated with the increase in the amount of added particles and particle size.The difference in pressure drop ratio decreased with the increase in the circulating flow rate.As the amount of added particles increased,the difference in pressure drop ratio fluctuated at low circulating flow rate but basically decreased at high circulating flow rate.The pressure drop in the vertical tube bundle accounted for about 70%of the overall pressure drop in the up-flow heating chamber and was the main component of the overall pressure within the experimental range.Three-dimensional phase diagrams were established to display the variation ranges of the pressure drop and pressure drop ratio in the vertical tube bundle corresponding to the operating parameters.The research results can provide some reference for the application of the fluidized bed heat transfer technology in the industry.

Mechanism from particle compaction to fluidization of liquid–solid two-phase flow

A new model of particle yield stress including cohesive strength is proposed,which considers the friction and cohesive strength between particles.A calculation method for the fluidization process of liquid–solid two-phase flow in compact packing state is given,and the simulation and experimental studies of fluidization process are carried out by taking the sand–water two-phase flow in the jet dredging system as an example,and the calculation method is verified.

SIMULATION OF GAS AND LIQUID TWO-PHASE FLOW THROUGH THE BLAST FURNACE DROPPING ZONE

A three-dimensional mathematical model,based on differential balances of mass and momentum,hasbeen developed to describe the two-phase flow of gas and liquid through the dropping zone of the blast fur-nace.Agreement between observed and calculated values verifies the validity of this model.On the basis of this model,various parameters for the surrounding of the dry zone of Blast FurnaceNo.I-BF of the Beijing Iron and Steel Company have been computed,from which a diagram for demar-cation of fluidization of coke and flooding of slag has been proposed.

Effects of tube cross-sectional shapes on flow pattern, liquid film and heat transfer of n-pentane across tube bundles

The heat transfer of hydrocarbon refrigerant across tube bundles have been widely used in refrigeration.Three-dimensional simulation model using volume of fluid(VOF) was presented to study the effects of tube shapes on flow pattern, film thickness and heat transfer of n-pentane across tube bundles, including circle, ellipse-shaped, egg-shaped and cam-shaped tube bundles. Simulation results agree well with experimental data in the literature. The liquid film thickness of sheet flow and heat transfer for different tube shapes were obtained numerically. The flow pattern transition occurs lower vapor quality for ellipse-shaped tube than other tube shapes. For sheet flow, the liquid film on circle tube and ellipseshaped tube is symmetrically distributed along the circumferential direction. However, the liquid film on egg-shaped tube at circumferential angles(θ) = 15°–60° is thicker than θ = 135°–165°. The liquid film on cam tube at θ = 15°–60° is slightly thinner than θ = 135°–165°. The liquid film thickness varies from thinner to thicker for ellipse-shaped, cam-shaped, egg-shape and circle within θ = 15°–60°. The effect of tube shape is insignificant on thin liquid film thickness. Ellipse-shaped tube has largest heat transfer coefficient for sheet flow. In practical engineering, the tube shape could be designed as ellipse to promote heat transfer.

Experimental Investigation of Vibration Response of A Free-Hanging Flexible Riser Induced by Internal Gas-Liquid Slug Flow

The vibration response of a free-hanging flexible riser induced by internal gas-liquid slug flow was studied experimentally in a small-diameter tube model based on Froude number criterion. The flow regime in a curved riser model and the response displacements of the riser were simultaneously recorded by high speed cameras. The gas superficial velocity ranges from 0.1 m/s to 0.6 m/s while the liquid superficial velocity from 0.06 m/s to 0.3 m/s.Severe slugging type 3, unstable oscillation flow and relatively stable slug flow were observed in the considered flow rates. Severe slugging type 3 characterized by premature gas penetration occurs at relatively low flow rates. Both the cycle time and slug length become shorter as the gas flow rate increases. The pressure at the riser base undergoes a longer period and larger amplitude of fluctuation as compared with the other two flow regimes. Additionally, severe slugging leads to the most vigorous in-plane vibration. However, the responses in the vertical and horizontal directions are not synchronized. The vertical vibration is dominated by the second mode while the horizontal vibration is dominated by the first mode. Similar to the vortex-induced vibration, three branches are identified as initial branch, build-up branch and descending branch for the response versus the mixture velocity of gas-liquid flow.

RESEARCH ON METHOD TO CALCULATE VELOCITIES OF SOLID PHASE AND LIQUID PHASE IN DEBRIS FLOW

Velocities of solid phase and liquid phase in debris flow are one key problem to research on impact and abrasion mechanism of banks and control structures under action of debris flow. Debris flow was simplified as two-phase liquid composed of solid phase with the same diameter particles and liquid phase with the same mechanical features. Assume debris flow was one-dimension two-phase liquid moving to one direction, then general equations of velocities of solid phase and liquid phase were founded in two-phase theory. Methods to calculate average pressures, volume forces and surface forces of debris flow control volume were established. Specially, surface forces were ascertained using Bingham＇s rheology equation of liquid phase and Bagnold＇s testing results about interaction between particles of solid phase. Proportional coefficient of velocities between liquid phase and solid phase was put forward, meanwhile, divergent coefficient between theoretical velocity and real velocity of solid phase was provided too. To state succinctly before, method to calculate velocities of solid phase and liquid phase was obtained through solution to general equations. The method is suitable for both viscous debris flow and thin debris flow. Additionally, velocities every phase can be identified through analyzing deposits in-situ after occurring of debris flow. It is obvious from engineering case the result in the method is consistent to that in real-time field observation.

通道压裂支撑剂缝内分布规律研究

通道压裂是低渗透致密油气藏高效、低成本开发的关键技术,通过采用非连续簇团铺砂的方式,使裂缝中形成具有高导流能力的通道,但目前关于通道压裂的理论研究仍然处于起步阶段.因此,基于计算流体力学建立欧拉-欧拉固液两相流模型,对通道压裂过程中支撑剂的分布状态进行模拟,通过与实验结果进行对比,证明了所建立模型的有效性,并系统研究了不同中顶压裂液(纯压裂液脉冲段)黏度、支撑剂密度、泵注排量对通道压裂通道率的影响.结果表明,中顶压裂液的黏度从1 mPa·s增加到20 mPa·s,通道内平均通道率增加5%;支撑剂密度从1400 kg/m^(3)增加到2000 kg/m^(3)时,缝内通道率减小了7%;排量由3 m^(3)/min增加到7 m^(3)/min时,通道率由28%增加到33.5%后减小到31%.现场应用过程中应使用较高黏度中顶压裂液、较低密度支撑剂和合理的泵注排量以保证裂缝中形成有效支撑通道.

转轮及导叶流域固液两相流研究

为了研究灯泡贯流式机组内流状态和磨损规律基于欧拉-欧拉法中的Particle非均匀相模型,对不同固相直径、浓度、导叶开度下水轮机固液两相流工况进行计算。结果表明,固相高浓度区集中在转轮域和尾水管进口处,且随着固相直径和浓度的增加而增加。随着固相直径和浓度的增加,导叶域表面压力、固相速度、固相浓度分布均增加,导叶背面更易发生磨损。在转轮域,固相高浓度区分布在叶片正面轮毂处和进水边,叶片背面整体固相浓度分布较高,且表面固相速度、浓度分布与固相直径和入口浓度呈正相关。

强迫振动下垂直管道固液两相流数值模拟研究

粗颗粒固液两相流的管道输运适用于深海采矿工程.扬矿管道在流致振动作用下的内部固液两相流的输运机理尚未被完全探究.因此,采用计算流体动力学(CFD)与离散元(DEM)耦合的方法,分析不同粒径、不同振动频率与振幅和不同浓度工况下在强迫振动管道中的粗颗粒动力学特性以及管内流场变化特性.其中,将管道的振动简化为一维径向振动,将实际工况中的柔性管道假定为刚体管道.研究表明,在管道振动过程中,大颗粒相比小颗粒的惯性更大,而流体也需要更大的速度产生更大的曳力推动大颗粒,导致更大的轴向流场速度以及更大的轴向颗粒速度.随着粒径增大,大颗粒对流场的扰动更大,导致流体与壁面间的作用力更大;并且大颗粒与壁面间的碰撞和摩擦作用力更大,因此壁面剪应力增大.同时,大颗粒与流体间摩擦损耗的能量也更大.因此管道需要更大的能量将其输运,导致振动管道内的压降增加.增大管道振动频率与振幅会导致颗粒在截面上的分布更加分散,同时对流场扰动更大,然而对轴向流场速度的影响相对较小.增大进料浓度使颗粒间、颗粒与流场间的作用更加频繁,导致颗粒分布发生变化,并导致更大的轴向流场速度和湍动能.

丁二酸结晶釜搅拌结构数值模拟与分析

基于计算流体动力学(CFD)对丁二酸连续结晶釜内固液两相流场进行模拟,探究不同叶轮结构、叶轮安装高度、釜底形状对结晶釜内固液分散情况的影响。模拟计算结果表明,减小桨叶倾角、增加叶片数量,有助于提升搅拌效果;搅拌功率、叶轮循环效率随桨叶倾角减小而增大。叶轮安装高度过高或过低均会造成颗粒堆积,影响固相悬浮状态;叶轮安装高度为1/3H是较优的选择,其云高、均匀度优于其余安装高度,且搅拌功率相对不高。复曲面釜底能显著改善釜底颗粒堆积情况,相较锥形釜底、W型釜底效果更优且能耗更低。

高压隔膜泵单向阀阀隙流场的冲蚀磨损特性分析

目的探究高压隔膜泵单向阀阀隙流场冲蚀磨损产生的原因及主要影响因素。方法基于固液两相流基本理论和冲蚀模型,考虑颗粒保护效应及磨蚀效应,采用计算流体力学(CFD)方法模拟单向阀阀隙流场的冲蚀磨损行为,探究矿粉颗粒体积分数、颗粒粒径、单向阀半锥角、胶垫突出高度等参数对单向阀冲蚀磨损特性的影响。结果矿粉颗粒紧贴阀芯壁面的剪切运动是造成阀芯发生冲蚀磨损失效的主要原因。当矿粉的体积分数由0.1增大到0.5时,由冲蚀造成的最大冲蚀磨损速率随之减小,由磨蚀造成的平均冲蚀磨损速率随之增大。当矿粉粒径为0.025~0.048 mm时,随着矿粉粒径的增大,平均冲蚀磨损速率随之增大。当矿粉粒径超过0.048 mm时,平均冲蚀磨损速率逐渐减小。当单向阀半锥角由30°增大到45°时,阀隙流场的最大流速由12.23 m/s减小至9.19 m/s,矿粉颗粒对阀芯壁面的最大冲蚀磨损速率减小了41.16%。阀隙流场的最大流速和冲蚀磨损速率随着胶垫突出高度h的增大而增大,同时位置也发生了相应变化。结论矿粉颗粒体积分数的增加会加重粒子对阀芯壁面的损伤程度,随着粒径的增加,泵阀的最大冲蚀磨损速率先增大后减小,增大半锥角可以缓解颗粒对壁面的冲蚀磨损,增大胶垫突出高度会导致冲蚀磨损区域逐渐向胶垫突出位置集中。

考虑载荷模拟作用的高压弯头冲蚀数值仿真

在水力压裂过程中,地面高压管汇在管内复杂固液两相流冲击和管体恶劣载荷的耦合作用下,弯头、三通及接头等薄弱部件长期遭受严重的冲蚀磨损,极易导致管件发生断裂破坏,对现场人员及设备构成严重威胁。开展载荷作用下的高压管汇典型材料冲蚀磨损试验,根据试验结果,基于E/CRC冲蚀模型构建一种考虑应力状态影响的新型冲蚀数学模型,所构建的新模型与冲蚀试验数据之间的准确度可达95%以上。采用计算流体力学离散相模型(CFD-DPM),开展高压管汇件冲蚀性能的三维数值模拟,考察高压弯头在不同压裂工况下的冲蚀磨损程度及空间分布情况。结果表明:在固液两相流冲击下,主要冲蚀区位于靠近弯头出口处的弯头外侧,且管件的最大冲蚀率也位于该处;在弯头内侧二次流涡流的影响下,部分颗粒在流经弯头后会在下游直管内侧积聚,从而在这个区域造成次要冲蚀区;随着流动颗粒斯托克斯系数增加,主要冲蚀区面积增大,次要冲蚀区面积减小;此外,在嵌入新型冲蚀数学模型后,可观察到随着操作压力增大,高压管汇弯头部位的冲蚀磨损率明显增加。

明渠湍流结构对粒子运动跟随性影响综述

近年来大量学者通过室内试验、现场观测以及数值模拟等方法对明渠湍流中粒子的运动规律进行了深入细致的研究,逐步揭示了明渠湍流中粒子运动复杂性的本质和规律,并将成果应用于河流泥沙输移、河流地貌演变以及生态环境保护等多个领域。鉴于明渠湍流具有明显的分区效应,其湍流流速分布、分区结构组成以及相干结构分布特性等对水中粒子的运动过程均会产生显著影响,对水中粒子在明渠湍流结构中的整体运动规律、湍流结构内区以及外区的运动过程进行了总结;重点阐述了近壁区粒子运动规律的反常现象和原因,以及湍流结构中粒径、密度和Stokes数这3个影响粒子运动过程的主要因素。研究成果可为泥沙运动以及生态保护等研究及应用提供参考。

大型浓密机两相流动与沉砂规律数值模拟研究

大型浓密机的复杂结构和系统参数识别是制约认识固液两相流动和沉砂规律的关键问题。本文按照沉砂机制,给出了一套大型浓密机模糊系统运行参数识别方法。建立了车河选矿厂30 m浓密机的数值模型,依次识别出进料流速、进料级配和进料体积分数,通过大量数值模拟指出车河选矿厂30 m大型浓密机进料井特征结构使其自然稀释功能较好,但动能耗散性能较差,进料井结构还存在较大的改进空间,并给出了各粒径颗粒的沉降规律。

旋转水力提升多金属结核运动特性数值模拟

采用CFD-DEM耦合方法对多金属结核提升进行模拟,研究了垂直管道中不同旋转流场旋流比对水力提升多金属结核输运特性的影响。结果表明,随着旋转流场旋流比增大,旋转强度显著增强,流体流速最大值增大,颗粒群轴向平均速度增大。旋转流场的旋转强度明显影响管道内颗粒的速度分布:速度大的颗粒逐步分布在管壁周围,速度较小的颗粒分布在管道中心处。旋转流场可降低颗粒群局部浓度,有利于降低因颗粒滞留效应引起局部浓度升高造成的输送管堵塞风险。

压裂双弯头液固两相流冲蚀影响数值分析

在水力压裂过程中,地面高压管汇受管内携砂压裂液的复杂流动影响,长期承受着严峻的冲蚀破坏。在各类高压管汇构件中,弯管的冲蚀损伤最为严重。为改善压裂双弯头冲蚀磨损状况,采用DPM模型、RNG k-ε湍流模型,综合分析了斯托克斯数(St)、重力方向、粒径及流速对串联双弯头冲蚀磨损的影响。结果表明:冲蚀磨损区域主要由St和重力方向共同决定;St<1时,最大冲蚀率随颗粒尺寸增大呈线性增加,St>1时呈指数增长;St相同时,速度对冲蚀磨损程度的影响远比颗粒尺寸强烈;向下流重力方向下,损伤区域随St增加完全转移至第二弯头的临界粒径显著小于向上流临界粒径;重力方向对同向冲击颗粒的冲蚀损伤虽有增强效应,其对冲蚀磨损程度影响远不及颗粒尺寸因素作用大。