乙烯气相聚合流化床反应器内Geldart B类和Geldart D类颗粒流动特性的三维数值模拟

乙烯气相聚合流化床反应器的设计、操作和优化依赖于对聚合物颗粒粒径大小和分布、气泡运动特性及聚合反应状况的准确描述。采用Eulerian-Eulerian 双流体模型和群体平衡模型耦合方法对某乙烯气相聚合中试规模的工业流化床反应器分别处于常规聚合工艺(属Geldart B 类颗粒)和免造粒工艺(属Geldart D 类颗粒)时床体的气固流动特征以及不同颗粒类型对反应器操作状态和颗粒运动特性的影响进行了三维数值模拟研究。与传统聚乙烯生产工艺相比,免造粒工艺时的Geldart D 类聚合物颗粒更易聚集于气体入口处区域,而且会产生明显的旋涡并出现较大的气泡。研究结果可为免造粒聚乙烯生产工艺的工业推广应用提供参考。     

Geldart A类颗粒节涌床气固流动特性的实验及模拟

针对气固节涌床,在实验基础上,基于欧拉?欧拉双流体模型结合颗粒动力学理论,考虑Geldart A类颗粒聚团对气固间曳力的影响,采用修正后的Gidaspow曳力模型对气固节涌床进行数值模拟。结果表明,通过与实验结果及经验公式进行对比,修正的模型可准确合理地模拟流化床内节涌特性。表观气速0.09 m/s≤Ug≤0.39 m/s时,床层内部压力脉动标准偏差随表观气速增加而增加,流型由鼓泡转变为节涌直至节涌程度最大,床内气固流动主要受轴对称栓运动特性影响,床内压降、床层膨胀比、气栓平均上升速度、最大轴对称栓长度随表观气速增加而增加,最大轴对称栓产生位置随表观气速增加而降低;Ug>0.39 m/s后,床内压力脉动标准偏差随表观气速增加而降低,节涌程度降低至向湍动流态化流型转变,床内气固流动主要受壁面栓运动特性影响,增加表观气速,节涌床内压降变化幅度较小,气栓平均上升速度增加幅度加大,床层膨胀比及最大轴对称栓长度降低,最大轴对称栓产生的位置略有升高。     

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.     

纳米颗粒聚团流化特性的数值模拟

基于气固两相流体动力学和流态化理论,建立气体纳米颗粒气固两相双流体模型.模型中采用了Jung&Gidaspow[1]测量的固相应力模量,并应用了王垚,金涌,魏飞[2]提出的聚团曳力系数计算模型.对纳米颗粒聚团的流化过程进行了数值模拟,得到纳米颗粒的流化特性.模拟得出的床层膨胀比与文献中实验的结果较为接近.     

B类颗粒在鼓泡流化床中流动特性的数值模拟

采用欧拉双流体模型对鼓泡流化床中气-固两相流动行为进行数值模拟。模拟结果表明,采用结构曳力模型能够较好地预测B类颗粒在鼓泡流化床中的流动行为。对比初始流态化颗粒浓度图和完全流态化颗粒浓度分布图,可以发现结构曳力模型能够较好地展现鼓泡流化床中气泡的运动特性。当比较不同曳力模型下的模拟结果时,结构曳力模型比传统曳力模型能够更好地预测颗粒的径向分布。     

多段分级转化流化床颗粒浓度的数值模拟

多段分级转化流化床煤气化反应器是由鼓泡射流流化床和快速流化床耦合而成的新型气化炉,采用欧拉双流体模型对其气固两相流动行为进行了数值模拟。模拟结果表明,两种流型的耦合,并非两种流态形式的简单叠加,回料口下段床内轴向浓度呈"C"型分布,上段轴向浓度呈指数分布,与实验结果较接近。同时考察了局部位置的颗粒浓度分布及其随操作条件的变化情况,表明快速床稀相段边壁区域颗粒浓度波动较中心强烈,且对操作条件的变化敏感,回料口附近的偏流现象以及过渡渐缩段的颗粒弹溅现象均与实验观察一致。研究得到的规律可指导多段分级转化流化床的设计和优化。     

35t/h内循环流化床锅炉流动数值模拟

采用基于颗粒动力学理论的欧拉双流体模型,对35t/h内循环流化床锅炉炉膛的气、固流动特性进行了数值模拟。结果表明:炉膛压差的模拟值与实验值吻合较好,说明欧拉双流体模型能够准确地描述炉膛内气、固流动特性;颗粒体积分数和速度分布特性既揭示了内循环流化床中颗粒的内循环流动机理,又为内循环流化床大型化和流动结构优化提供了参考。     

基于颗粒动力学理论的搅拌器中固液流动的数值模拟

在欧拉双流体模型基础上引入颗粒动力学理论(KTGF),对带挡板圆盘涡桨式搅拌器内的固液两相流动进行数值模拟。结果表明,搅拌器底部颗粒温度分布与固相浓度分布趋势吻合,转速低于600 r/min时,槽底会形成明显的颗粒沉积,转速从600 r/min增至1500 r/min,堆积区向轴中心收缩,基于颗粒动力学理论可以合理解释挡板及叶轮转速对固相浓度分布的影响。随叶轮转速增大,搅拌器内固液两相湍流运动加剧,颗粒温度、湍动能及轴向速度增加,颗粒分布更均匀,但达到完全悬浮状态后颗粒温度趋于稳定。搅拌器底部和挡板处颗粒堆积导致了局部颗粒浓度增加及颗粒平均自由行程减少,颗粒温度反而降低;同时挡板布置使搅拌器内形成了双循环回路,加强了流体的湍流程度,增强了湍动能,但导致颗粒在挡板处积聚,不利于固相在挡板处均匀分布。     

柱形流化床传热特性的数值模拟

对Shedid等搭建的圆柱体流化床采用欧拉?欧拉法进行三维数值模拟,考察了颗粒球形度、表观进气速度和床料初始堆积高度对流化床内垂直加热壁面与流动床料之间对流传热特性的影响,采用有效导热系数分别计算气相和固相的对流传热系数。结果表明,随表观进气速度增大,流化床内颗粒物料湍流运动加剧,加热壁面平均温度和流体平均温度下降,壁面流体间传热平均温度差减小,壁面流体间对流传热系数增大;随初始床料高度增加,流化床内颗粒与加热壁面的接触面积增大,导致固相平均对流传热系数增大。     

引入气相对D类颗粒间歇卸料过程特性的影响

通过测量并分析引入气相前后D类颗粒间歇卸料过程中示踪颗粒的流动状态、压力分布和颗粒流率,发现床体内气固两相流动特性不仅随时间变化,还受到气速（正负压差）的影响。据此将卸料过程按时间分为3个阶段：初始蓄压（PS）阶段、稳定卸料（SD）阶段和非满管流（PP）阶段;并给出各卸料阶段不同正、负压差和重力条件下的气固流动特性。在时间较长、流场较为稳定的SD阶段,发现卸料口颗粒阻力是影响颗粒流率的关键参数,通过修正De Jong公式、Beverloo公式,依次建立卸料口颗粒阻力、D类颗粒卸料流率预测模型,与实验值吻合较好,有望为引入气相调控D类颗粒卸料流率的方法提供参考。     

Investigation of Drying Geldart D and B Particles in Different Fluidization Regimes

Drying of nylon (Geldart D) and expanded polystyrene (Geldart B) particles in fixed and fluidized beds were studied experimentally and theoretically. Fluidized bed dryers are sometimes operated at velocities beyond bubbling fluidization to mitigate against de‐fluidization of surface wet particles. It was found that theoretical analysis using three different drying methods could predict the constant‐drying rate at such velocities and also across the entire fluidization regimes (fixed bed, bubbling, slugging and turbulent fluidization) as long as the bed remains completely fluidized. Results also showed that the theoretical predictions were accurate beyond previously reported velocity limits in a laboratory scale dryer. During bubbling fluidization, the cross flow factor method was used effectively to predict the influence of bubble phase on drying rates. In the falling‐rate period, it is demonstrated that the drying behaviour of nylon at different gas velocities can be characterised by a single normalized drying curve.     

液固流化床中铜颗粒流化特性的研究

以球形铜颗粒为原料,水为流化介质,在横截面为50mm×15mm的液固流化床中,考察不同平均粒径铜颗粒的流化特性。并基于Richardson-Zaki的关联式,提出符合本实验条件计算空隙率方程中指数n的关联式。     

A numerical study of fluidization behavior of Geldart A particles using a discrete particle model

This paper reports on a numerical study of fluidization behavior of Geldart A particles by use of a 2D soft-sphere discrete particle model (DPM). Some typical features, including the homogeneous expansion, gross particle circulation in the absence of bubbles, and fast bubbles, can be clearly displayed if the interparticle van der Waals forces are relatively weak. An anisotropy of the velocity fluctuation of particles is found in both the homogeneous fluidization regime and the bubbling regime. The homogeneous fluidization is shown to represent a transition phase resulting from the competition of three kinds of basic interactions: the fluid-particle interaction, the particle-particle collisions (and particle-wall collisions) and the interparticle van der Waals forces. In the bubbling regime, however, the effect of the interparticle van der Waals forces vanishes and the fluid-particle interaction becomes the dominant factor determining the fluidization behavior of Geldart A particles. This is also evidenced by the comparisons of the particulate pressure with other theoretical and experimental results.     

稻草及热解半焦颗粒流化特性

研究了稻草及不同温度热解半焦颗粒在内径100 mm、高1000 mm的有机玻璃流化床中的流化特性. 结果表明,稻草颗粒无法单独流化,而其热解半焦颗粒可单独流化;半焦颗粒的最小流化速度随粒径增大而增大,与床层高度无关,筛分粒径为0.45~0.9, 0.18~0.45, 0.125~0.18 mm的半焦颗粒的最小流化速度分别为0.19, 0.16, 0.14 m/s;300~550℃温度范围内稻草热解半焦颗粒的流化特性无明显区别;半焦与稻草颗粒混合流化时,稻草颗粒不大于20%(w)时床层有较好的流化质量,混合颗粒的最小流化速度都随混合颗粒中稻草含量增大而增大.     

黏性颗粒流态化的气固流动模型研究进展

黏性颗粒间存在较强的范德华力、液体桥力、静电力等黏附力作用,在流态化时易发生聚团现象,影响流化床的正常操作. 连续介质模型、离散颗粒模型和拟颗粒模型用于研究颗粒聚团流态化行为时各有优缺点. 基于欧拉方法的连续介质模型无法具体描述颗粒间的相互作用;采用拉格朗日法则能从颗粒微观受力、颗粒碰撞、聚团流动等多尺度研究黏性颗粒的流态化特性. 但受限于巨大的运算量,离散颗粒模型模拟的颗粒数有限,拟颗粒模型目前仅适合处理纳微尺度问题. 随着高性能计算机的发展和普及,基于拉格朗日法的黏性颗粒流动模型应用前景广阔.     

快速流化床的整体模拟

工业应用中的快速流化床一般不能直接对固相速度进行调控,属于B类操作.本文采用一维双流体模型与存料量方程相结合的方法可以计算B类操作时的上升管内具有浓、稀两相特征的轴向空隙率分布,模拟与实验结果较为吻合.     

Case study: Optimization of an industrial fluidized bed drying process for large Geldart Type D nylon particles

With an aim to conduct performance rating and optimization of an industrial-scale fluidized bed dryer, a decision tree has been devised to aid selection of the most appropriate mathematical model. The operating fluidization regime is first identified and a theoretical criterion using a cross flow factor is used to decide between using the Class 1 model based on plug flow or the Class 3 model based on the Davidson bubble. In this case-study, this approach is applied on an existing multi-stage dryer for large Geldart Type D nylon particles. The optimization study was carried out using the Class 3 model, which applies the two-phase fluidization theory to determine the transport of moisture between the dense and the bubble phases. An iterative numerical solution has been used to reduce computational time by avoiding the need to solve complex coupled heat and mass balance equations. Changes in bubble size and wall effects along the bed height are taken into account to improve model accuracy. The sensitivity of operating conditions (temperature, weir height, fluidization velocity) and recommendations for optimal operation are presented.

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