基于气泡数密度模型的气体穿越液池过程气泡特性数值模拟

采用考虑了气泡破碎和聚并的平均气泡数密度(ABND)输运方程,并与计算流体力学(CFD)中的湍流双流体模型相结合,建立CFD-ABND耦合计算模型。运用该模型对含固体颗粒气体通过冷却管穿越液池过程中液池内的气泡尺寸和气液界面浓度进行数值模拟。定量获得了液池内气泡尺寸和气液界面浓度分布,并分析了气速变化对其影响规律。结果表明:所建立的CFD-ABND模型能够对液池中的气泡尺寸及气液界面浓度分布等气泡特性进行较好预测;在靠近冷却管外壁面附近区域形成较大尺寸气泡和较高气液界面浓度;液池内隔板的存在有助于气液扰动,使液池内总体的气泡尺寸得到有效降低及气液界面浓度得到提升。     

高温气体穿越液池过程气液传热传质数值分析

建立气液二相间动量、热量及质量同时传递数学模型,数值模拟了高温气体穿越液池气液直接接触热质传递规律。模型中考虑了气泡破碎、聚合以及冷却水蒸发等因素的影响。数值模拟获得了液池内气液二相温度变化规律,探讨了液池内表观气速、气泡尺寸以及进入液池气体温度等因素对液池内气液二相温度分布特性的影响。计算结果与实验值吻合较好,验证了模型的可行性。数值模拟结果表明:高温气体在进入液池后,首先经历一个剧烈的气液热质交换过程,存在一个较大的温度梯度变化,而随后气体温度变化趋于平缓;随着液池内表观气速的降低,池内气体温度降低;最大冷却水蒸发速率和最高气体温度均出现在靠近下降管出口的区域。     

气液固三相湍流流动的E/E/L模型与模拟

采用基于双流体模型与粒子分散模型相结合的方法 ,建立了一个用于描述气液固三相湍流流动的Eulerian/Eulerian/Lagrangian模型 (简称E/E/L模型 ) .在Euler坐标系中考虑了气液两相 ,利用双流体模型来表述气液两相的相互关系 ;同时在Lagrange坐标系中考察了颗粒的运动 ,并把颗粒对气液两相的影响耦合于双流体模型中 .以流化床内气液固三相湍流流动为例进行的数值模拟结果与实验结果吻合良好 .所提出的模型及其模拟具有很好的准确性和可靠性 ,为研究气液固三相湍流流动提供了一种新的途径     

循环流化床多组分颗粒气固两相流动模型和数值模拟

基于稠密气体分子运动论和颗粒动力学,考虑多组分颗粒中颗粒组分与颗粒组分、颗粒组分内颗粒之间的相互作用以及气体与颗粒之间的相互作用,提出多组分颗粒非等温颗粒气固两相流动模型.以颗粒压力、径向分布函数、黏度、颗粒碰撞耗散等耦合各颗粒组分间和颗粒间的相间作用.采用大涡模拟方法模拟气相湍流流动.提出了多组分颗粒的径向分布函数计算方法.对循环流化床上升管中双组分颗粒气固两相流动特性进行了数值模拟,模拟结果揭示了上升管中双组分颗粒气固两相流动的环-核流动结构,得到了平均颗粒粒径的轴向和径向分布规律,计算结果与文献中实验结果相吻合.     

气化炉洗涤冷却室液池内分隔板对气液流动特性影响的数值模拟

为了提高气化炉洗涤冷却室内合成气洗涤热质的传质效果,采用数值模拟技术,研究了液池结构及液池内分隔板对气泡特性的影响。以气化炉液池内气液两相流动过程为研究对象,通过气液两相流动数值模拟实验平台,重点研究了分隔板对气泡特性的影响。基于图像处理技术,从数值计算结果中提取液池内气泡湿周信息,揭示了液池内分隔板对气泡湿周特性的影响,探讨了分隔板结构及分布的优化。结果表明:分隔板能有效增大气泡湿周,减小液位波动;其安装位置不宜太高,合理选择板上孔隙的大小及数量有利于优化气泡特性;分隔板交叉布置比平行布置更有利于均匀分布气泡。     

提升管内气固流动特性的离散元模拟

采用离散单元法模型对二维提升管内气固流动特性进行了数值模拟。利用标准k-ε模型模拟气相的湍流流动,考虑了颗粒间的van der Waals力和滚动摩擦的作用。通过对颗粒和气体流动行为的分析,得到了颗粒浓度、速度、温度及气体速度等的分布,研究了表观气速和颗粒循环速率对颗粒流动的影响。结果显示:颗粒在提升管内呈现边壁浓、中心稀的环核流动及上稀下浓的流动结构;气固两相都存在一定程度的返混现象;增加表观气速,使颗粒浓度降低、速度增大,颗粒分布更均匀;增加颗粒循环速率,使颗粒浓度增大,而颗粒速度对颗粒循环速率的变化不敏感,颗粒分布的不均匀性更强。模拟结果与文献中实验定性吻合。     

65 t/h高低差速循环流化床流动特性模拟

对一台65 t/h高低差速循环流化床炉内流动特性进行二维数值模拟。采用基于颗粒动力学理论的欧拉双流体模型来描述气固流动,湍流模型、气固曳力模型和不同粒径颗粒间曳力模型分别采用RNG k-ε per phase模型、Gidaspow模型和Schiller-naumann模型,并应用商业计算流体力学软件Fluent进行数值计算,得到炉内颗粒速度分布、压力分布和颗粒浓度分布,并将压力分布与实测值进行对比。在欧拉双流体模型中分别采用单粒径固相模型和多粒径固相模型,并对模拟结果进行对比分析。结果表明,单粒径固相模型能够较好预测高低差速循环流化床炉内流动特性,为其优化设计、运行及大型化提供了理论依据。     

短接触旋流反应器混合腔内离散颗粒分布特性的模拟

应用DPM模型对新型催化裂化短接触旋流反应器内的颗粒分布特性进行数值模拟,主要考察混合腔内气、固两相速度与浓度分布的基本特征。模拟结果表明:1~30μm粒径颗粒受到重力场和旋流场的作用,在混合腔内沿气流方向旋转扩散,充满整个混合区域且逐渐螺旋下行;而50、70、100μm粒径的颗粒由于粒径相对较大,不易被气流夹带,在混合腔内的流动更为复杂,浓度分布的不均匀度增大。研究结果为新型反应器的设计和优化提供了重要理论依据。     

旋风分离器内气固两相流动特性的模拟研究

通过数值模拟对旋风分离器内的气固两相流动进行研究。采用RSM湍流模型和DPM两相流模型分析旋风分离器内的气固两相流动特性。旋风分离器内的气流切向速度呈中心准强制涡、外侧准自由涡的双涡分布,分界面大约在0.8倍排气管半径处;气流轴向速度呈中心上行、外侧下行的双行流分布,分界面即零速包络面大约与排气管直径一致;小粒径颗粒的运动具有随机性,粒径大于7μm的颗粒可以完全被捕集分离;流动的非轴对称特性和顶灰环对气固分离不利,应给予重视。     

双流化床生物质气化的三维全循环数值模拟

基于多相质点网格方法 (multi-phase particle-in-cell,MP-PIC)对工业尺度的双流化床生物质气化过程进行了三维全循环数值模拟。其中,在拉格朗日框架下求解颗粒团运动,采用大涡模拟法(large-eddy simulation, LES)求解气相湍流,同时考虑复杂的气固耦合以及生物质的热解、气化、均相/异相反应。首先,通过独立性检验确定了计算所需的最佳网格数与计算颗粒数,且模拟结果和实验结果对比良好。其次,揭示了流化床内生物质气化过程中的气固流动特性及气体组分分布规律,研究了床内温度、生物质粒径、曳力模型等因素对产物气体组分分布的影响。结果表明:温度升高,出口处的CO摩尔分数增加,而其余组分都减小;较小生物质粒径的气化效果要优于较大的生物质颗粒粒径;曳力模型对各产物气体组分的摩尔分数几乎无影响。     

电除尘器飞灰粒径表征及细颗粒降温团聚

基于50000m³/h实烧烟气中试系统,采用Mastersizer 2000E激光粒度分析仪和电子低压冲击仪（ELPI）,首次对电除尘器飞灰几何粒径和空气动力学粒径进行全面表征。结果表明,电除尘器入口及各电场的飞灰几何粒度分布均呈双峰分布特征,各电场峰值依次右移,但末级旋转电极电场≤ 1μm的颗粒占比略有升高,电除尘器入口及第1～5电场飞灰几何中位径分别为6.607μm、17.378μm、2.884μm、2.577μm、2.460μm、2.480μm;温度降低,电除尘器入口飞灰几何粒度分布的双峰均右移,颗粒团聚现象明显,80℃、90℃、110℃、130℃、150℃时电除尘器入口飞灰几何中位径分别为13.183μm、10.500μm、10.171μm、6.607μm、7.586μm,从130℃降至90℃,电除尘器入口几何粒径≤ 1μm、≤ 2.5μm、≤ 10μm的飞灰占比分别减少了19.8%、19.2%、12.6%;不同温度时,电除尘器对空气动力学粒径0.03～10μm段颗粒的个数浓度、质量浓度均有较高脱除效率,均在75%以上,最高可达99.9%;温度降低,电除尘器进出口空气动力学粒径不同粒径段颗粒个数浓度和质量浓度均有不同程度降低,从130℃降至90℃、80℃,对应电除尘器入口PM_2.5团聚效率分别为46.76%、60.08%,对应电除尘器出口PM₁₀减排分别为59.80%、91.08%,PM_2.5减排分别为45.94%、76.22%,PM1减排分别为40.40%、62.12%。     

基于群体平衡的汽轮机动叶表面盐析颗粒分布特性

为深入了解汽轮机动叶内盐析颗粒的微观行为,本文以某超临界汽轮机高压级动叶为研究对象,应用计算流体力学与群体平衡模型耦合方法,对汽轮机动叶内盐析颗粒在流场中的分布进行数值模拟研究,获得了盐析颗粒在动叶内的粒径分布及不同负荷时叶片尾缘处盐析颗粒数量密度分布规律。模拟结果表明：在汽轮机动叶吸力面附近的盐析颗粒粒径较压力面附近盐析颗粒粒径小,且叶根处颗粒粒径小于叶顶处;动叶压力面的颗粒数量密度呈前缘点尾缘点处大、中间段小的分布规律,并且盐析颗粒在叶片上的数量密度分布最大值并不出现在组分数及粒径最大处,而是出现在平均粒径为110~150μm的盐析颗粒沉积位置处;当汽轮机30%负荷运行时,粒径40μm盐析颗粒的数量密度是其在汽轮机额定负荷运行时的1.5倍,而粒径140μm盐析颗粒的数量密度仅为汽轮机额定负荷运行时的80%。     

Investigation of pressure drop in a cocurrent downflow three-phase moving bed

Based on a self-established cold-flow experimental device, the pressure drop in a cocurrent downflow three-phase moving bed was investigated under a wide range of gas, liquid, and solid flow rates during dynamic and steady-state operation. The results showed that for the startup of the bed, since the first bed layer packed by fall-falling of particles had lower voidage, it would take at least one bed volume time to make the voidage in the bed reach the steady-state. Under steady-state conditions, the pressure drop increased with the increase of gas and liquid mass flow rates, liquid viscosity, and decreased with the increase of solid flow rate. Furthermore, it was found that the liquid distribution became more uniform due to particle movement. The experimental data obtained in this study was used to develop a correlation to predict the pressure drop in a three-phase moving bed with an average relative error of 9.32%.     

小型气-液-固流化床液相的停留时间分布

采用脉冲示踪技术,研究了3 mm床径的小型气-液-固流化床内液相停留时间分布。以KCl为示踪剂,液相为去离子水,气相为空气,固相为平均粒径0.123~0.222 mm的玻璃微珠和氧化铝颗粒,测量流化床出口液相的电导率,得到其停留时间分布曲线。结果表明,增大表观液速和表观气速,分布曲线变窄,平均停留时间缩短,Peclet数增大;固相的存在使液相的平均停留时间增长。表观液速1.96~15.70 mm×s^-1,表观气速1.18~1.96 mm×s^-1的条件下,流动接近层流;平均停留时间的范围为（19.6±0.34）s~（48.0±0.92）s,建立的Pe经验关联式对实验结果有较好的预测,偏差在±25%以内。研究结果对于小型三相流化床的设计放大具有指导意义。     

环流预汽提组合旋流快分系统粒级效率的三区计算模型

在大型提升管冷模实验装置上,系统地考查了带有环流预汽提的旋流快分(CVQS)系统的气相流场和粒级效率。结果表明,随着旋流快分系统喷出口气速的增加,粒径小于7 μm颗粒的粒级效率的变化较小,7～20 μm颗粒的粒级效率逐渐变小,而超过20 μm颗粒的粒级效率则逐渐增大。根据CVQS快分系统的气固分离原理和结构特点,建立了计算CVQS系统粒级效率的三区模型。计算结果表明,在颗粒粒径大于20 μm时,模型预测的粒级效率与实验值吻合较好,其最大相对偏差不超过6.1%;在颗粒粒径小于20 μm时,模型计算的粒级效率与实验值相差较大,其相对偏差在45.7%～80.3%之间变化,并且随着颗粒粒径的减小,其相对偏差逐渐增加。模型对于主要用于分离20 μm以上颗粒的CVQS系统的工程设计,具有重要参考价值。     

Particle flow behavior in three-phase fluidized beds

Non-uniform flow behavior of fluidized solid particles in three-phase fluidized beds has been analyzed by adopting the stochastic method. More specifically, pressure fluctuation signals from three-phase fluidized beds (0.152 m ID x 2.5 m in height) have been analyzed by resorting to fractal and spectral analysis. Effects of gas flow rate (0.01-0.07 m/s), liquid flow rate (0.06-0.18 m/s) and particle size (0.001-0.006 m) on the characteristics of the Hurst exponent, spectral exponent and Shannon entropy of pressure fluctuations have been investigated. The Hurst exponent and spectral exponent of pressure fluctuations attained their local maxima with the variation of liquid flow rate. The Shannon entropy of pressure fluctuation data, however, attained its local minima with the variation of liquid flow rate. The flow transition of fluidized solid particles was detected conveniently by means of the variations of the Hurst exponent, spectral exponent and Shannon entropy of pressure fluctuations in the beds. The flow behavior resulting from multiphase contact in three-phase fluidized beds appeared to be persistent and can be characterized as a higher order deterministic chaos.     

THE EFFECT OF DISTRIBUTORS ON TWO-PHASE AND THREE-PHASE FLOWS IN VERTICAL COLUMNS

Two-phase air-water and three-phase air-water-solids flows have been investigated in a 0.152 m internal diameter vertical column. Pressure drop across the distributor and average phase hold-up were measured for two-phase and three-phase flows over flow ranges of superficial gas velocity from 0 to 259 m/s and superficial liquid velocity from 0 to 0.0346 m/s. Gas hold-up/pressure-drop ratios were obtained as a function of superficial gas velocity and liquid flow rate. It was found that the bubble cap was better at gas distribution than that of the Koch static mixer in two-phase and three-phase vertical flows. Drift flux to gas hold-up and drift flux to gas flow rate correlations were obtained for two-phase and three-phase vertical flows. Three flow patterns, churn-turbulent, transition and ideal bubble flows, were observed for vertical upflow.     

沉流式滤筒除尘器气固两相流动的数值模拟与分析

为掌握滤筒除尘器内部流动特征 ,应用FLUENT 5 .4 .8软件对DFT3 12型滤筒除尘器内部紊流气固两相流动进行了数值模拟 ,采用k ε紊流模型和壁面函数法模拟气相流动 ,采用双向耦合拉格朗日法追踪颗粒运动轨迹。对连续相速度和压力分布特征以及颗粒相运动轨迹进行了分析 ,得出了不同工况条件下的系统阻力和颗粒沉积量分布规律 ,对比分析了重力、布朗运动和紊流扩散作用对颗粒运动和沉积的影响     

Numerical simulation of microparticles penetration and gas dynamics in an axi-symmetric supersonic nozzle for genetic vaccination

This paper describes two phase (solid particles/gas) flow in a supersonic nozzle that is part of a device for micromolecular vaccine/drug delivery. It accelerates micro solid particles to high speeds sufficient to penetrate the viable epidermis layer to achieve the pharmaceutical effect. Helium is used as the driving gas for the solid particles because of its high compressibility factor. A numerical parametric study was performed for gas pressures ranging between 3 and 6 MPa and gold particles of diameters 1.8 μm and 5 μm. The computed results show that uniform particle velocity was achieved at standoff distance of 2 exit diameters (D_e) downstream of the device exit with particles concentrated on the supersonic core jet. Increasing the helium pressure from 3 to 6 MPa caused an increase in the particle velocity of 24% for particles with a diameter of 1.8 μm and 7% for particles of diameter 5 μm at the standoff distance. Furthermore increased gas pressure has adverse effect on particles concentration. As the inlet pressure increases, the particles are concentrated more at the core of the nozzle. Semi-empirical particle penetration calculation confirms the numerical results that the 5 μm particles penetration distance is 45-135 μm and the 1.8 μm diameter penetration is 35-95 μm beneath the skin. Comparison of different geometries has been done in order to understand each section function and to gain optimum performance.     

Particle Emissions from Chrome Plating

Aerosol particles formed from the bursting of small gas bubbles emitted from the anode and cathode electrodes during electrolytic chrome plating were measured with a laboratory apparatus. The measured aerosol particle emission factors were about 5.15 mg particles/amp-hour or 3.81 mg Cr^{+ 6}/amp hour. The cathode gases generated more particles on a gas volume basis with 20 mg particles/liter hydrogen gas evolved from the cathode compared to 1 mg particles/liter oxygen gas evolved from the anode. With about 35% more cathode hydrogen gas evolved than anode oxygen gas evolved and with the much greater particle emissions caused by the cathode hydrogen on a gas volumetric basis, the aerosol particle emissions from the cathode bubble bursting were about 97% of the total particle mass emissions. The particle size distributions measured from the cathode had a mass median aerodynamic diameter of about 38 μ m whereas the anode mass median particle diameter was about 8 μ m. The anode particle mass size distribution was bimodal with peaks at about 0.6 and 24 μ m diameter. The cathode particle mass size distribution was trimodal with peaks at 2.5, 9, and about 60 μ m diameter.