转盘边缘黏性薄液膜不同破碎模式临界转变特性

液膜在离心粒化器边缘的破碎模式直接决定了雾化后的液滴形态和尺寸分布,是影响物料品质的关键因素。针对转盘粒化器,提出临界转变系数表征液膜由膜状向纤维状破碎的转变条件,并拓展至其他破碎模式,建立了滴状向纤维状、完全纤维状及纤维状向膜状破碎转变的临界关系。结果表明,转盘表面润湿性对于液膜呈滴状以及滴状向纤维状模式转变影响显著,未完全润湿导致临界流量存在一定的随机性,转盘直径与临界流量间无明确规律;而完全纤维状以及膜状时,大直径转盘临界流量明显升高。转速、流量、密度及黏度的提高,破碎模式趋向于膜状;而增大表面张力,即使对于较大流量和转速,液膜也能维持纤维状或滴状模式。调整转盘直径将引起表面张力与离心力同时变化,若未打破平衡,其破碎模式不会改变。研究结果为转盘粒化器的设计与优化提供了可借鉴的理论与应用基础。     

转盘离心雾化高黏非牛顿流体薄液膜纤维化特性

高黏性流体经转盘离心雾化以液滴形式进入气相可显著改善气液相间接触,其纤维化特性直接决定了雾化液滴的尺寸,是影响物料品质的关键因素。针对转盘离心雾化器,对非牛顿黏性液膜失稳纤维化过程的物理机制进行了分析,分析了高黏度流体,仅考虑黏性作用时,黏性力对纤维间距的贡献,建立了黏性力与表面张力耦合作用下液膜破碎的纤维间距预测模型,探讨了液膜纤维化的一般规律。结果表明,黏性对液膜的失稳纤维化起抑制作用,黏度提高,纤维数量减小,纤维间距增大。纤维数量与转盘边缘液膜线速度相关。进入完全纤维状模式后,纤维数量趋于稳定,提高转速引起纤维数量稳定的流量范围缩小,不利于雾化,可采用低转速、大直径转盘改善雾化效果。非牛顿高黏流体液膜破碎后的纤维数量与Weber数、等效Reynolds数和流变指数直接相关。研究结果对高黏流体的转盘离心雾化系统设计与优化提供了可借鉴的理论与应用基础。     

转盘离心雾化高黏非牛顿流体薄液膜纤维化特性

高黏性流体经转盘离心雾化以液滴形式进入气相可显著改善气液相间接触,其纤维化特性直接决定了雾化液滴的尺寸,是影响物料品质的关键因素。针对转盘离心雾化器,对非牛顿黏性液膜失稳纤维化过程的物理机制进行了分析,分析了高黏度流体,仅考虑黏性作用时,黏性力对纤维间距的贡献,建立了黏性力与表面张力耦合作用下液膜破碎的纤维间距预测模型,探讨了液膜纤维化的一般规律。结果表明,黏性对液膜的失稳纤维化起抑制作用,黏度提高,纤维数量减小,纤维间距增大。纤维数量与转盘边缘液膜线速度相关。进入完全纤维状模式后,纤维数量趋于稳定,提高转速引起纤维数量稳定的流量范围缩小,不利于雾化,可采用低转速、大直径转盘改善雾化效果。非牛顿高黏流体液膜破碎后的纤维数量与Weber数、等效Reynolds数和流变指数直接相关。研究结果对高黏流体的转盘离心雾化系统设计与优化提供了可借鉴的理论与应用基础。     

基于滴膜共存理论热虹吸管冷凝段传热模型

引入滴膜共存冷凝传热理论分析管内存在滴状冷凝的热虹吸管冷凝段传热,将热虹吸管冷凝段传热表示为滴状区和膜状区传热之和建立传热模型。滴状区,以Rose冷凝传热模型计算单个液滴的传热,基于随机分形理论建立了液滴的空间和尺度分布函数,进而求解整个滴状区的热通量。膜状区,根据Nusselt竖壁层流膜状凝结理论进行热通量的计算。通过沟流级别计算滴状区和膜状区的面积比率,从而建立滴膜共存冷凝传热模型。传热模型计算结果与实验结果较为吻合,能够反应热管冷凝段传热本质。     

滴状冷凝强化含不凝气的蒸气冷凝传热机制

为了深入考察滴状冷凝强化混合蒸气冷凝传热传质过程的作用机制，在竖直表面上设计了完全滴状（DWC）、没有液滴向下脱落运动的条形分割滴膜共存（DFC）和膜状（FWC）3种冷凝形态的实验表面。对纯蒸气及含不凝气蒸气的冷凝传热过程进行了分析和实验研究，结果表明纯蒸气滴状冷凝与滴膜共存冷凝传热特性相近；而对含不凝气的冷凝，滴膜共存表面与膜状冷凝表面的传热特性相近；不凝气摩尔分数分别为0.9%、4.8%时，滴状冷凝较其他两种形态下的冷凝传热系数提高了30%～80%。其主要原因是由于混合蒸气冷凝传热阻力主要由气相边界层控制，滴膜共存冷凝并没有使气相的扩散传质过程得到强化，而完全滴状冷凝与设计的滴膜共存冷凝的区别在于后者仅存在小液滴的合并运动而没有大液滴向下脱落和对表面冲刷过程。根据二者实验结果的分析，认为滴状冷凝的大液滴脱落运动是影响气相传质的主要因素，大液滴脱落过程对气相边界层的扰动和剪切作用强化了气液界面传热传质特性。     

表面分割方式对滴膜共存冷凝传热特性的实验研究

实验研究了滴膜面积比为1：1且滴状区域采用较厚的有机涂层时，垂直管外滴膜共存表面的滴膜区域分割方式对冷凝传热特性的影响。结果表明，在表面分割方式一定时，滴膜共存表面的冷凝传热性能随着表面分割数的增加而增加，但总仍是介于全部表面为滴状冷凝和全表面为膜状冷凝型态之间的传热特性。分析表面分割数分别为2和4的滴膜共存表面的传热结果，发现凝液环的缓冲作用对于滴膜共存表面的冷凝强化传热具有重要作用。滴膜共存表面上滴状冷凝区面积对其下游膜状冷凝传热的影响不仅与滴膜区域的面积比有关，而且实验操作条件也有一定的控制作用，且两者之间存在最佳匹配值，即此时的强化传热效果最好。     

滴状冷凝强化传热管制备及性能研究

采用涂覆-热处理法制备了二甲基硅油膜、硅橡胶膜、纳米白炭黑-硅橡胶膜滴状冷凝强化传热管。研究了二甲基硅油、107硅橡胶、纳米Si O2在铸膜液中浓度对热通量、总传热系数、冷凝传热系数及表面传热温差等的影响,并用傅里叶红外光谱和接触角对本实验所制备的传热管表面进行了分析。结果表明:实验所制得的4种类型的传热管均可以实现滴状冷凝现象;与相应的膜状冷凝相比,纳米白炭黑-硅橡胶膜的冷凝传热系数提高了3.1~3.3倍,传热效果最好;二甲基硅油膜强化传热管的传热效果次之,与相应的膜状冷凝相比,其冷凝传热系数提高了1.9~2.1倍;两种膜的表面温差分别约为相应膜状冷凝的1.3~1.4倍和1.2~1.3倍。     

水平降膜管外液膜厚度分布

研究了液膜流动破裂的基础机理,构建了考虑表面张力、重力、惯性力及剪切应力等因素的液膜动力模型,采用边界层积分法,引入含有三次项剪切力项的速度分布函数,推导二维稳态水平管外环向液膜的厚度方程.通过数值方法求解该厚度方程,得到水平管外环向液膜厚度的分布规律.结果表明,随环向角度增大,环向液膜厚度先减小后增大,最薄液膜位置角在环向90?之后,且流量、剪切应力系数与管径等因素不改变环向液膜厚度的分布趋势,改变了环向最薄液膜位置角.最薄液膜位置角随流量增大、剪切应力系数减小及管径减小而增大.表面张力是影响环向液膜稳定性不可忽略的因素.     

表面自由能差对乙醇-水混合蒸气冷凝传热特征的影响

实验研究了常压下不同浓度的乙醇-水混合蒸气的冷凝传热过程.发现在不同的乙醇含量和过冷度条件下,冷凝形态呈现膜状、过渡态和滴状的变化.相应传热系数也发生变化.基于该冷凝过程实质为薄液膜表面上的冷凝过程,以及蒸气冷凝传热系数随表面自由能差渐进变化的机理,首先确定了其表面自由能差为液-液表面自由能差,并以此解释了乙醇-水混合蒸气冷凝过程传热特性的变化规律.研究表明,随着冷凝液与薄液膜二者的表面自由能差的增大,冷凝传热系数逐渐增大,并且冷凝形态发生变化,当表面自由能差小于(14±1)mJ·m-2时为膜状冷凝,大于(21±1)mJ·m-2时为滴状冷凝,介于二者之间时为过渡状态.     

转盘离心粒化中丝状成粒特性

针对转盘离心粒化工艺,以水为工质开展可视化实验。采用高速摄影仪对液膜波动、液丝断裂等粒化过程进行了捕捉,并利用MATLAB自编程序对获得的图像进行了处理。分析了离心粒化过程中液丝形成过程以及液丝断裂形成液滴的过程。研究了运行工况对液丝、液滴形成机制的影响。讨论了液丝形成对液滴形成的影响并获得了Weber数、Reynolds数对粒化效果的影响程度。结果表明,表面不稳定波是形成液丝的主要因素,且液丝在Rayleigh不稳定性的作用下断裂形成液滴。升高转速或者减小流量有利于获得均匀的小液滴。Weber数对液丝、液滴形成具有显著影响;Reynolds数仅对液丝数目有显著影响。     

High speed imaging of drop formation from low viscosity liquids and polymer melts in spinning disk atomization

An investigation of drop formation in a recently developed spinning disk atomization (SDA) technique is presented. In‐situ observations of drop formation at the disk rim, using a high speed imaging installation, are made. Atomizations covering two orders of magnitude in flow rate show that ligaments can also form at low flow rates. Sequences of pictures indicate that drops undergo a rotary motion as they detach from a ligament. In the direct drop regime, oscillating motions dominate. The effect of teeth shape at the disk rim on the resulting drops is compared. The effect on drop size and size distribution is found to decrease with increasing rotation rate and corresponding images are studied. Experiments with liquid viscosities ranging from 1 to 120 mPas reveal a fundamental difference in drop breakup, but a negligible change in drop size. Likewise, only a small effect of liquid density is detected. The surface tension's influence on the liquid spreading at the disk rim is described and the subsequent drop formation is qualitatively analyzed.     

Spray characteristics of a swirl atomiser in trigger sprayers using water–ethanol mixtures

Pressure swirl atomisers are widely used in both industry and daily life. It is critical to understand the spray transient behaviour for better design of these systems. This paper presents an experimental study of conical liquid sheets breakup from a swirl atomiser nozzle in trigger sprayers. Spray and atomisation characteristics were measured and analysed. Water–ethanol mixtures were used to simulate different fluids on the breakup and atomisation quality of the spray development process with a wide range of surface tension while maintaining relatively small changes in fluid viscosity and density. The spray images were taken by a high speed digital camera and post‐processed to analyse the global spray structure, spray cone angle, and breakup length. The droplet size and its distribution were measured using a laser diffraction technique. It was observed that the surface waves grow rapidly on the cone‐shaped liquid sheets and breakup into liquid ligaments and droplets during the initial stage of fluid dispensing. Then the spray transitions into the developed stage. Near the end of the dispensing process, the liquid cone collapses with poor atomisation (large droplets) due to momentum loss. The comparison between different fluids showed that the spray cone angle and liquid breakup length decreased with the increase of ethanol percentage ratio. The percentiles parameters, Sauter mean diameter (SMD) and particle size distribution were measured and compared for different locations. High surface tension fluids produce larger droplets than lower surface tension fluids, which have the same trend as the percentiles parameters and SMD. Results also show that droplet size and its distribution depend on the location of the measurement. Generally speaking, smaller droplet size is found for a location away from the nozzle axis in the vertical direction. In the horizontal direction, larger droplet sizes are found for a location closer to the nozzle exit. © 2013 Canadian Society for Chemical Engineering     

Asymmetric breakup of a droplet in an axisymmetric extensional flow

The asymmetric breakups of a droplet in an axisymmetric cross-like microfluidic device are investigated by using a three-dimensional volume of fluid(VOF) multiphase numerical model. Two kinds of asymmetries(droplet location deviation from the symmetric geometry center and different flow rates at two symmetric outlets) generate asymmetric flow fields near the droplet, which results in the asymmetric breakup of the latter. Four typical breakup regimes(no breakup, one-side breakup, retraction breakup and direct breakup) have been observed.Two regime maps are plotted to describe the transition from one regime to another for the two types of different asymmetries, respectively. A power law model, which is based on the three critical factors(the capillary number,the asymmetry of flow fields and the initial volume ratio), is employed to predict the volume ratio of the two unequal daughter droplets generated in the direct breakup. The influences of capillary numbers and the asymmetries have been studied systematically in this paper. The larger the asymmetry is, the bigger the oneside breakup zone is. The larger the capillary number is, the more possible the breakup is in the direct breakup zone. When the radius of the initial droplet is 20 μm, the critical capillary numbers are 0.122, 0.128, 0.145,0.165, 0.192 and 0.226 for flow asymmetry factor AS= 0.05, 0.1, 0.2, 0.3, 0.4 and 0.5, respectively, in the flow system whose asymmetry is generated by location deviations. In the flow system whose asymmetry is generated by two different flow rates at two outlets, the critical capillary numbers are 0.121, 0.133, 0.145, 0.156 and 0.167 for AS= 1/21, 3/23, 1/5, 7/27 and 9/29, respectively.     

Jet breakup and droplet formation in near-critical regime of carbon dioxide-dichloromethane system

The jet breakup and droplet formation mechanism of a liquid in the near-critical conditions of a solvent-antisolvent system is examined with high-speed visualization experiments and simulated using a front tracking/finite volume method. The size of droplets formed under varying system pressure at various jet breakup regimes is measured with a Global Sizing Velocimetry, using the shadow sizing method. A stainless steel nozzle with 0.25 mm I.D and 1.6 mm O.D was used in this study. Experiments were performed at fixed temperature of 35 °C and system pressure in the range from 61 to 76 bar in the near-critical regime of the DCM-CO₂. At the near mixture critical regime for DCM-CO₂ mixture, the miscibility between the two fluid phases increases and the interfacial tension diminishes. This phase behavior has important applications in particle formation using gas antisolvent (GAS) and supercritical antisolvent (SAS) processes. The jet breakup and droplet formation in the near-critical regime is strongly dependent on the changes in interface tension and velocity of the liquid phase. An understanding of the droplet formation and jet breakup behavior of DCM-CO₂ in this regime is useful in experimental design for particle fabrication using SAS method.     

Mean Droplet Size and Local Velocity in Horizontal Isothermal Free Jets of Air and Water,respectively, Viscous Liquid in Quiescent Ambient Air

Measurements using two‐dimensional Phase Doppler Anemometry as well as high speed cinematography in free jets at several nozzle exit pressures and mass flow rates, show that the Sauter mean droplet diameter decreases with increasing air and liquid‐phase mass flow ratio due to the increase of the air stream impact on the liquid phase. This leads to substantial liquid fragmentation, respectively primary droplet breakup, and hence, satellite droplet formation with small sizes. This trend is also significant in the case of a liquid viscosity higher than that of water. The increased liquid viscosity stabilizes the droplet formation and breakup by reducing the rate of surface perturbations and consequently droplet distortions, ultimately also leading, in total, to the formation of smaller droplets. The droplet velocity decreases with the nozzle downstream distance, basically due to the continual air entrainment and due to the collisions between the droplets. The droplet collisions may induce further liquid fragmentation and, hence, formation of a number of relatively smaller droplets respectively secondary breakup, or may induce agglomeration to comparatively larger liquid fragments that may rain out of the free jet.     

匀强电场作用下分散相液滴的变形和破裂

基于Cahn-Hilliard方程的相场方法,建立了在匀强电场作用下液滴的变形和破裂行为模型。从微观角度研究分散相液滴变形过程中电荷密度、电场强度和电场力的分布规律以及流场和电场分布,探讨了微观液滴变形机理;采用数值模拟方法研究了电场强度、液滴直径和界面张力对液滴变形的影响,结果表明电场强度越强,液滴直径越大,界面张力越小,液滴变形量越大;分析了液滴的两种主要破裂方式,其破裂主要取决于连续相和分散相物性条件,为电破乳技术提供了理论基础。     

电场作用下液滴的变形及库仑分裂模式

基于高速成像技术,本文对电场作用下甲醇液滴的显微形貌特征进行了可视化研究,精确捕捉了两相流体系中不同生长阶段的荷电液滴基于时间分辨特性的变形及库仑分裂演变行为,得到不同工况下荷电液滴的变形分裂过程及行为演化细节。基于液滴所受库仑力和介电泳力与周围流域的耦合作用,揭示了电场作用下不同生长阶段的液滴库仑分裂形成机理。结果表明,电场强度和液滴粒径是决定液滴变形及库仑分裂模式的主要因素,荷电液滴的变形及库仑分裂模式可以分为推压变形、顶部破碎、顶部-边端破碎、伞状破碎。结合量纲为1参数对液滴的变形及破碎特征进行了定量分析,随着电场强度的增大及液滴粒径的减小,液滴变形及顶部破碎的程度更加剧烈,液滴临界伞状破碎长度减小。     

Analysis of liquid distribution in non-uniformly packed trickle bed with single phase flow

The distribution of liquid flow rate is measured in a rectangular bed non-uniformly packed with different particles. The effects of particle properties (size and wettability), liquid properties (viscosity and surface tension) and packed structure on the liquid flow rate distribution are examined. The liquid trickle flow is strongly affected by the capillary force. An experimental equation expressing the liquid flow distribution at the interface between different particles is derived by means of the capillary number.A percolation model combined with the above experimental equation is developed to simulate the liquid flow distribution in the trickle bed. For the trickle flow of liquid droplet, the gravitational and capillary forces are considered to work on the liquid droplet, and the driving force for stochastic liquid flow is assumed to be the potential of the local liquid holdup. Besides a dropping flow in the vertical direction, a permeation flow in the horizontal direction is supposed. The results calculated by the percolation model are in good agreement with the experimental data for various packed systems.