提升管-下行床耦合反应器内颗粒混合行为

引　言循环流化床中气固两相的流动有两种不同的方式 :提升管中为气固并流上行的逆重力场运动 ,下行床中为气固并流下行的顺重力场运动 .其差异表现为提升管内颗粒浓度、速度以及气体速度在径向上严重的不均匀 ,颗粒浓度概率密度分布以及速度的瞬时信号都表明了颗粒团 -空穴两相结构的存在[1] ,一些研究[2 ,3] 还发现提升管中颗粒的停留时间分布 (ＲＴＤ)曲线存在较大的拖尾甚至出现双峰 ,研究者认为提升管内存在弥散颗粒和颗粒团两种不同的混合机理 ;下行床则比提升管大大改善 ,气固速度、颗粒浓度沿径向分布要均匀得多 ,颗粒的ＲＴＤ曲线…     

流动方向对循环流化床中颗粒混合行为的影响

对循环流化床提升管及下行床两种不同气固流动方式对颗粒混合行为的影响进行了较为深入的对比分析，发现在影响循环流化床颗粒混合的众多因素（如操作条件、床层直径、颗粒性质及床层内构件等）中，气固流动方向是影响颗粒轴向混合的最主要因素．当气固流动为顺重力场时（下行床），颗粒的轴向混合很小，流型接近平推流；当气固流动为逆重力场的提升管时，轴向颗粒混合将成倍增大，颗粒流动远离平推流流动．分析表明，下行床中颗粒混合仅为单一的弥散颗粒扩散，而提升管中则存在着两种颗粒混合机制：弥散颗粒扩散及颗粒团扩散．弥散颗粒的扩散基本以平推流的形式通过循环流化床，提升管中大量的颗粒轴向返混归因于颗粒团的严重返混并由此形成了提升管中颗粒停留时间的双峰分布．     

逆向气体射流对下行床颗粒混合的影响

下行床入口结构的研究一直被人们所重视。今在内径为0．192m的下行床中颗粒达到均匀分布的部位，沿床四周均布了三个45度方向逆流场气体射流入口，在此处设立气体入口可以使颗粒分散与气固快速接触不再同时进行。采用磷光颗粒示踪技术对下行床有逆流场射流气体存在时颗粒的轴径向混合行为进行了研究。这种逆流场射流气体对下行床颗粒的轴向混合行为无明显影响，在各操作条件下下行床内颗粒均能以接近平推流的方式运动；但该射流气体可以大大加强颗粒的径向混合，有利于气固接触，在下行床颗粒径向混合越差的操作条件下，射流气体对颗粒径向混合的影响效果越明显，下行床的这种入口结构具有良好的应用前景。     

气固超短接触反应系统中颗粒轴向及径向混合行为研究

气固超短接触反应系统中颗粒轴向及径向混合行为研究魏飞，陈卫，金涌，俞芷青（清华大学化工系，北京１０００８４）关键词：气固超短接触反应器，磷光示踪，颗粒混合１前言气－固并流下行循环流化床反应器是一种新型气固超短接触反应器￣［１］，与传统的提升管反应器相...     

双颗粒提升管中细颗粒的混合行为研究(Ⅱ)──弥散颗粒的轴径向混合行为

利用磷光颗粒示踪技术，使用点源示踪的方法在不同的径向位置测得反映颗粒径向扩散行为的停留时间分布曲线，并对弥散细颗粒的径向混合行为进行了分析．提出二维扩散模型描述所测量的停留时间分布曲线特征．实验发现弥散细颗粒的径向扩散Peclet数随粗颗粒加入量的增加而增加，随细颗粒浓度的增大而增大，而几乎不随气速变化．给出了一个与实验数据吻合较好并可适用于单颗粒提升管的关联式．     

双颗粒提升管中细颗粒的混合行为研究(Ⅱ)──弥散颗粒的轴径向混合行为

利用磷光颗粒示踪技术,使用点源示踪的方法在不同的径向位置测得反映颗粒径向扩散行为的停留时间分布曲线,并对弥散细颗粒的径向混合行为进行了分析．提出二维扩散模型描述所测量的停留时间分布曲线特征．实验发现弥散细颗粒的径向扩散Peclet数随粗颗粒加入量的增加而增加,随细颗粒浓度的增大而增大,而几乎不随气速变化．给出了一个与实验数据吻合较好并可适用于单颗粒提升管的关联式．     

气固下行流化床反应器 Ⅲ气、固混合

与气固并流上行提升管反应器相比，气固并流下行管反应器的轴向气固返混明显降低，而径向气固混和仍然相当大，因而有利于提高气固快速反应的转化率及选择性。本文在分析下行流化床反应器内气、固混合机理的基础上，比较了有关气、固混合的研究方法及结果，并比较了提升管和下行管的不同混合现象，旨在促进对这一课题更加深入系统地研究，以适应循环床下行管反应器设计、放大和模型化的迫切要求。     

内构件对于提升管中颗粒混合行为的影响

对加设了钝体式内构件的提升管内颗粒的轴径向混合为进行了研究。研究结果表明，内构件的存在并不能明显减少提升管内颗粒的轴向返混，这与提升管内稳定的微观两相结构密切相关，但颗粒的径向混合能力却可大大加强，而且在越高的气速和固含条件下，这种加强作用越明显，其原因是内构件的存在加强了边壁区颗粒的脉动，有利于破坏提升管边壁区的颗粒浓环，促进颗粒的径向交换与混合。     

下行床入口段流体力学及混合行为

针对工业快速反应对气固进料混合过程的特殊需求,在内径140mm,高4.7m的并流下行循环流化床中,采用双光路光纤密度测量技术及磷光颗粒示踪技术,对两种不同的气固并流下行床分布器结构的流动及颗粒混合行为进行了研究．分别考察了人口段颗粒浓度径向分布沿轴向的变化规律及颗粒轴径向混合行为．实验结果表明,下行床入口段颗粒浓度随轴向位置的变化可划分为分布器影响区及湍流控制区．分布器结构对入口段颗粒密度分布有较大影响,利用侧向喷嘴并降低入口处颗粒的射流可以获得较好的径向均布效果．侧向喷嘴的分布器结构更有利于颗粒的径向混合．还考察了入口结构对颗粒混合的影响因素,给出了对Pe_a及Pe_r的关联式．     

快速流化床中颗粒浓度及颗粒速度的径向分布

本文在φ140mm的气固并流下行快速流化床中,研究了颗粒浓度及颗粒速度的径向分布随操作气速、颗粒循环速率以及床层轴向位置的变化规律。并探讨了颗粒质量通量的径向分布及颗粒流动的均匀性,表明在相同操作条件下,下行快速流化床中气固流动远比上行快速流化床均匀。     

Axial and lateral dispersion of fine particles in a binary-solid riser

Axial and lateral mixing of fine particles in a binary-solid riser have been investigated using a phosphor tracer method. The measured bimodal residence time distribution (RTD) demonstrated two types of axial dispersions of the fines: the dispersion of discrete particles and that of clusters. A proposed one-dimensional, bimodal dispersion model describes the bimodal RTDs very well. The axial Peclet number of the fines is not sensitive to the fraction of coarse particles, gas velocity and solids circulation rate. Lateral solids dispersion was determined by measuring the solids RTD at different radii using a point source tracer injection. A two-dimensional dispersion model describes the measured RTDs satisfactorily. Lateral solids mixing decreased as coarse particles were added into the riser. Correlations of the axial and lateral Peclet numbers obtained fit the experimental data well.     

Residence time distributions with a radiotracer in a hydrotreating pilot plant: Upflow versus downflow operation

The objective of the present work is to determine the influence of the two-phase flow direction in hydrotreating bench scale plants on the axial dispersion of the liquid phase. Residence time distribution experiments under ambient conditions in cocurrent upflow and in cocurrent downflow are carried out in a catalytic hydrotreating bench scale plant, which contains a thermowell. Particles that are representative of a commercial catalyst are used. The fluids and flow rates are chosen in order to simulate deep desulfurization conditions of a straight-run gas oil. In order to determine the axial dispersion only within the bed of particles, a radioactive tracer is used.The hydrodynamic parameters are identified using an axial dynamic piston dispersion model. The liquid axial dispersion is found to be significantly higher in the downflow mode than in the upflow mode. The values of the upflow liquid saturation are in a good agreement with the values found in the literature whereas the downflow liquid saturation is lower.Simulations with a multiphase model indicate that the difference of the axial dispersion might have a significant influence on the hydrodesulfurization performances.     

Residence time distribution and hold-up in a cocurrent upflow packed bed reactor at elevated pressure

The residence time distribution in liquid phase was measured in a cocurrent upflow packed bed reactor for the system methanol-hydrogen at low Reynolds numbers and at elevated pressure. The plug flow with axial dispersion model was used to describe mixing in the system. The imperfect pulse method was used to measure the system response to a tracer pulse input. The parameters were calculated using the weighted moments method. The influence of the weighting factor was investigated. The experimental and theoretical outputs, as calculated by convolution, agreed very well. Different types of correlations were used for the Bodenstein number and liquid hold-up. From these correlations, the optimal one was selected for each parameter. A comparison was made between the ordinary moments and the weighted moments methods which led to the conclusion that the latter method is superior with respect to the accuracy of the estimated parameters and therefore strongly recommended.     

Liquid phase mixing in turbulent bed contactor

Axial mixing of the liquid phase in turbulent bed contactor (TBC) is studied through residence time distribution (RTD) experiments over a large range of variables such as flow rate of gas and liquid phases, static bed heights, diameter and density of particles and number of stages in presence of downcomer using air water system. Since all the liquid exits only through the downcomer, it enables the correct estimation of exit concentration of the tracer. The experimental RTD curves are satisfactorily compared with the axial dispersion model. The Peclet numbers evaluated by axial dispersion model and the Peclet numbers reported in the literature are used to propose a unified correlation in terms of operating and geometric parameters. Correlation is also developed for predicting the axial dispersion coefficient. It was observed in the present study that almost plug flow conditions can be achieved in multistage TBC.     

Solids mixing in a fluidized bed riser

The solids mixing in a riser with a height of 10 m and 0.186 m inner diameter was investigated by using pneumatic phosphor tracer technique. Considering the shielding effect of the bed material on the light emitted from the phosphor tracer particle, a modified method for the phosphor tracer measurement is proposed. And then the curves of particle residence time distribution were obtained. The experimental results show that the particle diffusion mechanism can be explained by the dispersions of dispersed particles and particle clusters in the axial direction, and as well the core-annulus nonuniform distribution of the solids fraction in the radial direction of the riser. Moreover, based on the experimental results, a two-dimensional dispersion model was established to predict the solids axial and radial diffusion. Furthermore, the effects of superficial gas velocity and solids circulating flux on the axial and radial Peclet number of the particles were discussed; two empirical correlation formulas about the axial and the radial Peclet numbers were given; the calculated values agree well with the experimental results.     

Mixing behavior of wide-size-distribution particles in a FCC riser

A comparison study on the axial and lateral mixing of wide-size-distribution (WSD) particles with normal-size-distribution (NSD) FCC particles is presented. The fines smaller than 20 μm contribute 24.5% in volume in the WSD particles. Phosphor tracer method is used. The axial backmixing of the WSD is slightly lower than the NSD. However, the lateral solids Peclet number increases linearly with the increase of the content of fines smaller than 20 μm because of the serious agglomeration of the fines, which leads to very poor lateral mixing for the WSD particles. And the solids lateral mixing for the WSD particles decreases significantly with increasing solids fraction. These results show that the particle size and the particle-size-distribution is a very important factor that controls the lateral solids mixing and hence the heat and mass transfer in lateral direction, which should be taken into full consideration in the riser reactor. And the NSD may be a good particle size distribution for the FCC riser, the lateral solids mixing of which is satisfactory in the reactor.     

Radioisotope tracer study in trickle bed reactors

The residence time distribution (RTD) of liquid phase in trickle bed reactors has been measured for air‐water system using radioisotope tracer technique. Experiments were carried out in a glass column of internal diameter of 0.152 m packed with glass beads and actual catalyst particles of two different shapes. From the measured RTD curves, mean residence time of liquid was calculated and used to estimate liquid holdup. The axial dispersion model was used to simulate the experimental data and estimate mixing index, ie. Peclet number. The effect of liquid and gas flow rates on total liquid holdup and Peclet number has been investigated. Results of the study indicated that shape of the packing has significant effect on holdup and axial dispersion. Bodenstein number has been correlated to Reynolds number, Galileo number, shape and size of the packing.     

Dimensional Analysis of Particle and Liquid Dispersion in Draining Foam

A dimensionless correlation for the axial dispersion of particles and liquid tracer in draining foam has been developed that expresses the dimensionless dispersion as a function of Peclet and Stokes numbers. The correlation is fitted to the data of Lee et al., Coll. and Surf. A. 263 , 320‐329 (2005). The value of the axial dispersion coefficient is independent of the self‐dispersivity. It is seen that Saffman, J. Fluid. Mech. 6 , 321‐349 (1959) model for the dispersion coefficient in solid porous media only provides order of magnitude prediction of the axial dispersion coefficient but it can inform about the dominant mechanisms of dispersion.