变角度Y型分支管气力输送流量分配特性研究

以压缩空气为输送介质,粒径相同而密度不同的小米和空心玻璃珠为输送物料,在水平变角度Y型分支管气力输送试验台上对气固两相的流量分配特性进行了研究.试验结果表明,在保持发送压力恒定条件下,当两分支管路与主管夹角相同时,流动参数的变化对流量分配特性的影响不大.当两分支管路与主管夹角不同时,随变动支管与主管夹角增大,分配到变动支管内固相流量逐渐减少;同时发现,当表观气速处于高速区时,变动支管与主管夹角是影响固相流量分配的主要因素;而当表观气速处于低速区时,流量分配特性变化较大.最后,通过对比,发现固相密度对流量分配特性影响不大.     

球阀不同开度下自流注水管路流固耦合动力学特性研究

以输流管道、电液球阀等附件组成的自流注水复杂管路系统为研究对象,基于流固耦合理论,利用有限元软件ANSYS建立系统仿真计算模型并研究其动力学特性。由于管路不同位置的动力学特性不同,本文根据所建立的有限元模型计算球阀不同开度对管路同一位置流体的压力和速度的影响,并比较不同位置在球阀固定开度时的流体特性。结果表明:阀前弯头的流体压力随阀门开度的增加而减小,阀后弯头随阀门开度的增加而增大;当阀门开度固定时,管路不同位置的流体压力分别以球阀(固定开度≤50%)、大小头(固定开度为50%)为分界点呈现不同的趋势。根据流固耦合理论计算球阀不同开度下自流注水管路结构的振动情况,结果发现阀门开度为50%时在0.5s比其他开度多出现一次激振,且加速度幅值较其它开度明显增大。     

变开度岩体裂隙多相渗流实验与有效渗透率模型

岩体裂隙的有效渗透率是描述岩体非饱和或多相渗流的关键参数,而裂隙开度是影响有效渗透率的重要因素.通过自主研发的粗糙裂隙多相渗流可视化实验平台,针对天然岩体裂隙复制而成的裂隙模型开展变开度条件下的多相渗流可视化实验,研究开度变化对多相渗流流动结构以及有效渗透率的影响.研究表明:非湿润相流体运动通道,在低流量比条件下呈现出气泡流流动结构,而在高流量比条件下呈现较为稳定的通道流流动结构.随着开度的增加,非湿润相流动通道的分支变少、等效宽度增加,两相流体的有效渗透率均增大,流动结构趋于稳定.可视化结果还阐明了柱塞流流动结构下,两相流体交替占据裂隙空间的竞争机制:当非湿润相流体通道由连续转变为不连续时,裂隙进出口压差显著增加;反之,当该通道由不连续转变为连续时,压差显著减小.最后,基于分形理论以及渗透率统计建模方法,建立了考虑开度效应的岩体裂隙多相渗流有效渗透率理论模型,并通过实验测定的有效渗透率数据验证了该模型的正确性与有效性.     

圆管内粗糙壁面处微细颗粒沉积规律研究

针对固体颗粒在圆管中的沉积问题,本文采用DEM(Discrete-Element Method)描述颗粒与壁面的碰撞特征,采用湍流雷诺应力模型结合拉格朗日随机轨道模型对0.01μm~50μm的微细颗粒在壁面的沉积特性进行了研究。考查了颗粒粒径、重力、壁面位置、雷诺数Re、有效表面能、弹性模量对沉积速率的影响。结果表明:下壁面的沉积速率最大,上壁面的最小;颗粒在下壁面的沉积速率随量纲为一的弛豫时间呈V型曲线变化;当空气平均流速为0.5m/s时,颗粒小于1μm时即可忽略重力的影响,并且随着空气流速的增大,需要考虑颗粒重力的临界直径会逐渐增大;颗粒的粘附/反弹特征对沉积有很大影响,有效表面能越大,沉积速率越大;有效弹性模量越大,沉积速率越小;当颗粒小于10μm时,沉积速率随雷诺数Re的增大而增大;当颗粒大于等于10μm时,沉积速率随雷诺数Re的增大而减小。     

Y型分支管内气固两相流动的数值模拟

本文采用Euler-Lagrange两相流研究方法,固相采用离散相(DPM)模型,对三种不同夹角的Y型分支管内气固两相流动进行了数值模拟.气相湍流采用Realizable k-ε模型,固相的湍流耗散采用随机轨道模型.模拟结果较好地预估了颗粒在分叉处的流动形态、颗粒在分支管内的运动轨迹,以及重新实现颗粒相流场均匀分布所需的距离.同时发现,随机轨道模型较适于评估分支与主管夹角较大情况下,固体颗粒在分叉处的运动.将分支管内固体颗粒质量分配的数值模拟结果与试验结果比较,发现两者较吻合,相对误差较小.     

岩体交叉裂隙水流分配特性研究

岩体交叉裂隙的水流分配特性对揭示水体运移规律、人工疏导地下水、优化水力压裂方案等具有指导作用。文章利用自制裂隙渗流实验装置测试了常见"一进两出""人"字裂隙开度、交叉角度变化时的流量分配特性。利用交叉控制体模型和雷诺输运方程分析了产生流量差异的原因。结果表明,偏流来自惯性力与裂隙壁面法向力作用产生的漩涡;流量分配只受进口和旁路裂隙开度的影响,与交角和水力梯度无关;旁路流量比(旁路流量与进口流量之比)与裂隙开度间存在实验幂次定量关系。     

煤粉挤压流型输送特性

具有高固气比、低流速的挤压流型气固两相输送技术已在高技术领域的工程中得到应用.本文从实验和理论两方面研究了煤粉挤压流型的输送特性.试验的范围是:输送的固气比 m=280-770,空隙率8=0.37-0.58,单位面积管道煤粉输送流量 G_s/A=96-453g/s·cm~2.理论上用剪切应力模型进行分析,得到单位管长的压力降计算式.理论预测与实验结果是一致的.     

串联管道串联阀芯受瞬变压力研究

结合成品油停输再启动特性,建立了成品油控制体运动方程、连续方程,提出了串联阀芯流阻系数模型。通过差分方法对其编程求解,以串联管道串联阀芯为例,得出了串联阀芯受瞬变压力变化规律,探讨了停输再启动输油管路瞬变压力震荡衰减问题。以一个具体的工程实例进行研究,结果表明:串联管道串联阀芯线性关闭较单阀门线性关闭产生的最大瞬变压力由5.6MPa减至4.3MPa,减少了30.23%;管路瞬变压力震荡过程中,随着流体可压缩性的增大,流体的振幅衰减加剧,在43.2s时间内,瞬变压力最大峰值由4.85MPa减至1.28MPa;双阀门停输再启动中延长任一个阀门启闭时间均可使最大瞬变压力减小;对于相同关阀计划,阀芯流量系数越平缓,阀芯受瞬变压力越小。     

水平管内气液两相螺旋流实验研究

为研究水平管内气液两相螺旋流的流动特性,开展了以空气和水为实验介质,含气率为10％～90％,气相折算速度为0.01～3.4m/s,液相折算速度为0.05～2.7m/s的气液两相螺旋流实验.利用高速摄影机记录并参考借鉴相关研究结果分析和划分了不同工况下的流型;给出了水平管内气液两相螺旋流的流型图;研究了不同流速、不同起旋参数对流动特性(压降、流型衰减、螺距、螺旋直径以及流型转换边界等)的影响.实验结论如下:将水平管内气液两相螺旋流的流型划分为螺旋波状分层流、螺旋泡状流、螺旋团状流、螺旋线状流、螺旋轴状流、螺旋弥散流6种;将绘制的流型图与经典Mandhane流型图进行对比,出现了线状流、弥散流和轴状流3种新的流型;泡状流的分布基本不变,层状流的分布发生变化,当气相流速在2m/s以内时是线状流和轴状流,而不是层状流;随着液相流速的提高,管内两相流动的损失逐渐变大,流型的衰减程度变弱,螺旋扭矩逐渐变大,螺旋直径逐渐变小.另外,随着叶轮角度的增大或者随着叶片面积的减小,流型转换边界均向进气量增大的方向推移.而当进气量一定时,随着叶轮角度的增大或者随着叶片面积的减小,同样流型转换边界趋于进水量增大的方向.最后,随着起旋角度的增大或者随着叶片面积的减小,压降均有逐渐变大的趋势.     

层流条件下并列三圆柱涡激振动响应与尾流形态

应用基于嵌入式压强-力迭代的高精度浸入边界法研究等间距并列三圆柱涡激振动。其中,雷诺数Re=100,间距比T/D=2.0～5.0,圆柱质量比m*=2.0,折合流速Ur=2.0～10.0,忽略振动系统的阻尼且三圆柱仅横向振动。研究发现,圆柱的振动响应随折合流速的增加呈现初始响应分支和下端响应分支两种模式;振幅响应出现不连续现象,且随着间距比的增加,该不连续现象对应的折合流速增加;尾流模式与间距比和折合流速密切相关。共发现六种尾流形态,分别为窄宽窄尾流、不规律尾流、反相同步尾流、调制尾流、同相同步尾流和偏斜尾流。总结并绘制了尾流形态在参数空间[Ur,T/D]内的分区图。     

垂直下降管中两相流的流型以及液相粘度对流型的影响

对空气－油在垂直下降管中的流型进行了实验研究，采用的管径为２９ｍｍ，油和空气的折算流速分别达到４ｍ／ｓ和２０ｍ／ｓ，并借助于压降脉动分析和目测观察相结合的方法来进行流型的识别。研究表明，油气两相流的流型不同于低粘液体的两相流流动，通过实验研究并结合前人的研究成果，给出了液相粘度对流型转变的影响趋势。     

固-液两相流黑水管道冲蚀磨损的数值模拟研究

煤气化黑水处理系统管道由于其流体介质高含固体颗粒和腐蚀性介质，且工作在高温、高压差环境中，极易受到冲蚀磨损和腐蚀的耦合作用而失效，影响其服役寿命. 采用计算流体力学(CFD)方法数值模拟研究了煤气化黑水处理系统固-液两相流管道的冲蚀磨损行为和机理，以及流体介质速度和固体颗粒粒径对管道冲蚀磨损的影响规律，并分析了盲通管和涡室结构对弯管冲蚀磨损行为的优化改善效果. 研究结果显示，煤气化黑水处理系统管线的冲蚀高危区主要分布在弯管外拱和变径管等结构突变区域；管道冲蚀磨损行为与其内部流体的运动和颗粒冲击特性有关；管道的冲蚀率均随着流体速度的增加而加剧，而粒径对弯管和变径管冲蚀率的影响并非单调关系，这与颗粒受力作用有关；弯管优化分析显示，涡室结构可以降低弯管的最大冲蚀率，减缓弯管的冲蚀磨损.      

准直管磨料射流中各相介质在管内的流动机理与实验研究

介绍了准直管磨料射流的工作原理和特点,准直管磨料射流在准直管内的流动属于气（汽）、液、固多相混合介质的瞬变流动,分析了磨料在多相流体介质中的受力,推导了多相流体介质在准直管内有阻运动时的磨料运动方程式,提出了各种损失的经验计算方法,研究表明,气（汽）、液流体介质和磨料介质在准直管中的速度和密度是逐渐变化的,在０．４～３ｍ管长范围内磨料速度基本保持不变,短管时采用细磨粒,长管时长采用粗磨粒。     

Experimental investigation on the slip between oil and water in horizontal pipes

This work is devoted to study of the slip phenomenon between phases in water–oil two-phase flow in horizontal pipes. The emphasis is placed on the effects of input fluids flow rates, pipe diameter and viscosities of oil phase on the slip. Experiments were conducted to measure the holdup in two horizontal pipes with 0.05 m diameter and 0.025 m diameter, respectively, using two different viscosities of white oil and tap water as liquid phases. Results showed that the ratios of in situ oil to water velocity at the pipe of small diameter are higher than those at the pipe of big diameter when having same input flow rates. At low input water flow rate, there is a large deviation on the holdup between two flow systems with different oil viscosities and the deviation becomes gradually smaller with further increased input water flow rate.     

含双侧分支受限空间油气爆炸火焰行为与超压特性大涡模拟

为研究含分支结构狭长受限空间油气爆炸特性规律，基于大涡模拟WALE模型和Zimont预混火焰模型，对横截面为100 mm×100 mm的含双侧分支管道受限空间油气泄压爆炸特性进行了数值模拟。通过对火焰形态、火焰传播速度和动态超压3个物理量的对比，验证了所建立模型对于含分支结构受限空间油气爆炸计算的适用性。基于数值模拟结果，对爆炸过程中的流场结构、火焰形态和超压变化规律进行了分析，指出了“浪花状”火焰的形成原因。结果表明:（1）火焰传播进入分支管道前，在主管道和分支管道交界处会产生旋转方向相反的对称涡旋结构，并随着火焰传播不断向分支管道内部发展；（2）当火焰传播进入分支管道后，分支管道内部前期已建立流场决定了火焰的形态，火焰锋面在涡旋结构作用下呈“浪花状”，此后火焰和流场相互影响，流场向湍流转捩，火焰锋面褶皱变形；（3）爆炸超压升压过程可划分为4个阶段，受到火焰锋面面积和分支管道泄压共同作用，表明爆炸流场、火焰行为和动态超压呈现出显著耦合性。     

Multiphase drag reduction: Effect of eliminating slugs

Two-phase pressure drop measurements were taken for air/water mixtures in a 0.052-m diameter horizontal pipe with special focus on the superficial liquid velocity range of 0.03–1.2 m/s at superficial gas velocities of 3.8, 5.2, and 6.6 m/s. It was found that the addition of 400 ppm of sodium dodecyl sulfate (SDS) to the water reduced the pressure drop by 25–40% when compared to equal flow rates without SDS. The pressure drop reduction occurred where the SDS eliminated the occurrence of the intermittent flow present with water. It was also found that the same concentration of SDS had virtually no effect on single phase liquid pressure drop. The pressure drop reduction appears to be due solely to the suppression of intermittent flow patterns.     

Studies on two-phase co-current air/non-Newtonian shear-thinning fluid flows in inclined smooth pipes

In this work, co-current flow characteristics of air/non-Newtonian liquid systems in inclined smooth pipes are studied experimentally and theoretically using transparent tubes of 20, 40 and 60 mm in diameter. Each tube includes two 10 m long pipe branches connected by a U-bend that is capable of being inclined to any angle, from a completely horizontal to a fully vertical position. The flow rate of each phase is varied over a wide range. The studied flow phenomena are bubbly flow, stratified flow, plug flow, slug flow, churn flow and annular flow. These are observed and recorded by a high-speed camera over a wide range of operating conditions. The effects of the liquid phase properties, the inclination angle and the pipe diameter on two-phase flow characteristics are systematically studied. The Heywood–Charles model for horizontal flow was modified to accommodate stratified flow in inclined pipes, taking into account the average void fraction and pressure drop of the mixture flow of a gas/non-Newtonian liquid. The pressure drop gradient model of Taitel and Barnea for a gas/Newtonian liquid slug flow was extended to include liquids possessing shear-thinning flow behaviour in inclined pipes. The comparison of the predicted values with the experimental data shows that the models presented here provide a reasonable estimate of the average void fraction and the corresponding pressure drop for the mixture flow of a gas/non-Newtonian liquid.     

Heat Transfer and Gas Flow through Feed Stream within Horizontal Pipe

In the feeding process, the feed stream forms a moving packed bed of particle from the feedstock in the feed channel. When the feeding is at emergency interruption especially in the case of flooding and uncontrollable discharge, the hot gases from reactor would infiltrate into the feed stream. The high heat penetration into feed stream would affect the feeder performance. In this paper, transient thermal response of feed stream within horizontal pipe is described mathematically with a gas flow and heat transfer model. Influences of varied factors on the thermal penetration into feed stream are examined for different conditions. The temperature of the packed-bed particles and the gas velocity distribution curves are obtained for the feeding service at interruption and at normal operating conditions. The numerical results show that the thermal penetration to the packed-bed particles by the seepage flow fluid is high only in the position near the gas entrance. The thermal penetration depth tends to increase with the seepage flow velocity and decrease with feeding rate. There is no appreciable thermal penetration in the feed stream when the feeding service is at normal running. The operating conditions and the porosity of solid bed have importance effects on the gas velocity and temperature field in the thermal penetration zone. A test system is set up to determine the transient thermal response experimentally for the packed bed of particles within a horizontal pipe. The model results are found to compare favorably with the experimental data.     

An experimental study on developing air-water two-phase flow along a large vertical pipe: effect of air injection method

The flow structure in a developing air-water two-phase flow was investigated experimentally along a large vertical pipe (inner diameter, D_h: 0.48 m, ratio of length of flow path L to D_h: about 4.2). Two air injection methods (porous sinter injection and nozzle injection) were adopted to realize an extremely different flow structure in the developing region. The flow rate condition in the test section was as follows: superficial air velocity: 0.02–0.87 m/s (at atmospheric pressure) and superficial water velocity: 0.01–0.2 0.01–0.2 m/s, which covers the range of bubbly to slug flow in a small-scale pipe (D_h about 0.05 m).

No air slugs occupying the flow path were recognized in this experiment regardless of the air injection methods even under the condition where slug flow is realized in the small-scale pipe. In the lower half of the test section, the axial distribution of sectional differential pressure and the radial distribution of local void fraction showed peculiar distributions depending on the air injection methods. However, in the upper half of the test section, the effects of the air injection methods are small in respect of the shapes of the differential pressure distribution and the phase distribution. The comparison of sectional void fraction near the top of the test section with Kataoka's correlation indicated that the distribution parameter of the drift-flux model should be modeled including the effect of D_h and the bubble size distribution is affected by the air injection methods. The bubble size distribution is considered to be affected also by L/D_h based on comparison of results with Hills' correlation.     

The onset of gas entrainment from a flowing stratified gas–liquid regime in dual discharging branches: Part II: Critical conditions at low to moderate branch Froude numbers

This is the second of a two part investigation. Experiments were performed in a 50.8 mm diameter horizontal pipe with three 6.35 mm diameter branches located at the test section mid-span. The inlet length was 1.8 m, and three branch orientations were tested at 0° (side), 45° (inclined), and 90° (bottom) from horizontal. Water and air, operating at 206 kPa, were used and both fluids flowed co-currently within the inlet in the smooth-stratified regime. The inlet superficial velocity of the liquid phase ranged between 0.04 and 0.15 m/s while in the gas phase values of 0.3, 0.4, and 1 m/s were tested. Three different dual discharge combinations were tested and included side-inclined, side-bottom, and inclined-bottom. The tested branch flow Froude numbers were limited between low to moderate values which ranged between 1 and 23. Extensive experimental data are reported for the critical conditions at the onset of gas entrainment during dual discharge. A novel map was developed for the inclined-bottom branch configuration showing the relationship between the inlet superficial liquid velocity and branch Froude numbers. This map was used to quantify the three observed modes of gas entrainment during dual discharge. These modes were classified as onset of gas entrainment in the inclined branch only, in the bottom branch only, or both the inclined and bottom branches simultaneously. The critical height at the onset of gas entrainment results are compared to published models and data sets and poor agreement was found with studies conducted in stratified gas–liquid reservoirs.