循环流化床内颗粒停留时间分布

为进一步了解循环流化床床内复杂的流体动力特性,在200mm×200mm的冷态循环流化床试验台上以从床料中筛分出来的某一粒径的颗粒为示踪颗粒,用脉冲加入示踪剂法直接测量了固体颗粒停留时间分布.对试验所得的固体颗粒停留时间分布曲线的分析明显表明床内存在着由于流体动力特性和几何结构引起的颗粒返混.基于循环流化床内特殊的核心-边壁区流体动力结构,建立了能描述循环流化床和下排气旋风分离器内固体颗粒流体动力特性及固体停留时分布的数学模型.该模型计算结果和实验数据吻合良好.     

密相区表面固体颗粒夹带率数学模型

在研究循环流化床稀相区固体颗粒扬析夹带率分布和固体颗粒浓度分布时,通常需要计算密相区表面固体颗粒夹带率.基于流化床稀相区内固体颗粒呈环核状运动的理论,建立了密相区表面固体颗粒夹带率的数学模型,并与相关文献的实验数据进行了比对,吻合较好.     

喷动流化床传热特性的CFD-DEM模拟

基于颗粒-颗粒、颗粒-流体间的传热机制建立了颗粒尺度下的传热模型,并将其与计算流体力学-离散颗粒模型(CFD-DEM)耦合,建立了CFD-DEM传热模型,在传热计算中采用真实的颗粒接触刚度修正了颗粒-颗粒间的传热。采用典型喷动流化床内的颗粒传热实验数据验证了CFDDEM传热模型的准确性,并利用该模型分析了喷动流化床内的传热特性。结果表明:喷动流化床内颗粒的传热系数受其运动状态的影响,颗粒在环隙区域外循环的传热系数比内循环传热系数大;喷动流化床内平均传热系数呈对称分布,流化区域内的平均传热系数大于非流化区域,床体底部两侧及气体入口处的平均传热系数最大,床层中央区域的平均传热系数较小.     

脉动流化床内颗粒分离行为的数值模拟

脉动流化床可以实现多组分颗粒的分离而受到广泛关注.基于此,这里采用双流体模型,对脉动流化床多组分混合颗粒分离行为开展了数值模拟研究.通过与实验结果比较,模拟可以较好地预测颗粒的分离行为.比较了脉动流和连续流对分离行为的影响,结果表明,脉动流可以极大地促进颗粒的分离效率.同时评估了脉动频率和颗粒粒径的影响,研究发现,脉动...     

气固流化床内颗粒的内循环特性的研究

分析了气固流化床内颗粒内循环产生的原因,进而,分析了流化床气体速度,静态床层高度,颗粒粒径以及压力对颗凿内循环的影响。当流化床循环增强;而压力增大将使颗粒的内循环减弱。当颗粒的内循环增强时,流化床的脉冲信号（温度,浓度和灰度等）响应曲线的振荡加剧,流化床内颗粒的横向混合将得到改善。     

循环流化床锅炉内颗粒速度测量技术的分析比较

在对各种颗粒速度测量原理和使用条件分析比较基础上,结合循环流化床锅炉内颗粒浓度在床内的分布特点,给出了各种颗粒速度测量技术在循环流化床锅炉内颗粒速度测量中的具体应用条件,对开展循环流化床锅炉内颗粒速度的测量研究具有指导意义。     

三维喷动流化床流动特性数值模拟

为了研究喷动流化床煤部分气化炉的气-固流动特性,采用三维欧拉多相流模型和颗粒动能理论相结合的数学模型,对一台直径100 mm的喷动流化床试验台进行了数值模拟研究.研究内容包括喷动流化床不同工况下内部射流的发展、气-固流动特性、典型工况下气体速度分布、颗粒速度分布以及由于颗粒碰撞引起的颗粒相压力分布.模拟结果表明:典型工况下,当喷动风与总风的比例为50%时,流场有利于煤气化;气体曳力和颗粒碰撞对环形区颗粒特别是靠墙区颗粒的运动影响很大.为了验证模型的合理性,采用文献中的试验工况进行计算,计算结果和文献中的测量值吻合较好.     

非均匀布风流化床的DEM模拟

对二维非均匀布风流化床内的颗粒运动进行了数值模拟,用欧拉方法处理气相场的同时用拉格朗日方法处理离散颗粒场,直接跟踪颗粒场中的每个颗粒。模拟结果表明,非均匀布风流化床内存在颗粒的内循环运动,因此颗粒的混合特性优于均匀布风流化床。     

流化床煤燃烧与气化过程中的辐射换热

流化床反应器中颗粒与颗粒之间的传热在一定程度上决定了化学反应的速率及反应的中间历程。本文通过对气固流化床乳化相中颗粒群结构的进一步认识，建立了颗粒间的辐射换热模型，比较了不同颗粒直径、不同床层温度水平及不同流化工况下颗粒间辐射换热与通过气膜导热份额的大小，并预测了流化床反应器中反应颗粒与惰性床料之间的温差，对于流化床反应器选择合理的运行工况和进行操作参数优化具有参考价值     

褐煤在鼓泡流化床和循环流化床燃烧的汞迁移试验研究

对褐煤在小型电加热鼓泡流化床和小型电加热循环流化床中燃烧时的汞迁移特性进行了对比试验研究,重点考察了不同燃烧工况对汞迁移特性的影响。试验结果表明,炉膛温度和给煤量增加,鼓泡流化床和循环流化床的烟气总汞HgT均增加,飞灰颗粒汞含量Hg(p)均减少,并且循环流化床的烟气总汞HgT值均低于相同燃烧工况的鼓泡流化床值,循环流化床的飞灰颗粒汞含量Hg(p)值均高于相同燃烧工况的鼓泡流化床的值;流化风速增加,循环流化床的烟气总汞HgT减少,飞灰颗粒汞含量Hg(p)增加,鼓泡流化床烟气总汞HgT增加,飞灰颗粒汞含量Hg(p)减少。     

不同形式的循环流化床生物质气化炉

循环流化床生物质气化炉相比固定床生物质气化炉有许多优点,更适用于工业化生产,目前在生物质气化领域应用的循环流化床主要有外循环流化床,内循环流化床和双流化床。介绍了这几种循环流化床气化设备的典型结构和研究进展,并对其各类循环流化床气化装置的特点做出了分析和讨论。     

内循环流化床颗粒流动特性的直接数值模拟

内循环流化床是一种新型式的流化床，采用多风室非均匀布风实现床料颗粒的大尺度循环流动，从而增强了颗粒的横向混合。内循环流化床已应用于城市生活垃圾的焚烧制能，其燃烧速度、燃尽率及污染物排放优于传统的链条炉或鼓泡床。但是，目前设计的内循环流化床普遍较小，还不能满足城市垃圾的处理要求．根本原因在于对床内的气-固流动特性，特别是颗粒的运动规律没有深入的认识。内循环流化床内的气一固流动属于稠密的两相流，通过试验手段，如PIV、PDA也很难获得床内单个颗粒的运动特征。因此，采用前言的DEM(Discrete Element Method)模型对二维内循环流化床内的颗粒流动进行直接数值模拟．模拟结果表明非均匀布风内循环流化床内确实存在颗粒的大尺度循环流动。图4表1参5     

Recent Chinese heat-transfer research on bubbling and circulating fluidized beds

Recent research work conducted in China on heat transfer to immersed surfaces in bubbling and circulating fluidized beds, including coal combustors and boilers, is reviewed. Studies include measurements of heat-transfer coefficients (local and total) from horizontal and vertical tubes in bubbling fluidized beds and their variations with operating and system parameters. Special designs developed for heat-transfer probes and theoretical models for the computation of heat-transfer coefficients are discussed. Recent work is presented on circulating fluidized beds with emphasis on hydrodynamics and heat transfer. Proposed correlations and novel designs of thin-film heat-transfer and capacitance probes are included.     

Experimental study on coal multi-generation in dual fluidized beds

An atmospheric test system of dual fluidized beds for coal multi-generation was built.One bubbling fluidized bedis for gasification and a circulating fluidized bed for combustion.The two beds are combined with two valves:one valve to send high temperature ash from combustion bed to the gasification bed and another valve to sendchar and ash from gasification bed to combustion bed.Experiments on Shenhua coal multi-generation were madeat temperatures from 1112 K to 1191 K in the dual fluidized beds.The temperatures of the combustor are stableand the char combustion efficiency is about 98%.Increasing air/coal ratio to the fluidized bed leads to theincrease of temperature and gasification efficiency.The maximum gasification efficiency is 36.7% and thecalorific value of fuel gas is 10.7 MJ/Nm3.The tar yield in this work is 1.5%,much lower than that of pyrolysis.Carbon conversion efficiency to fuel gas and flue gas is about 90%.     

An experimental investigation of burning rate and mass transfer in a turbulent fluidized bed

Burning rates of carbon spheres are measured in a 102 mm diameter bed fluidized in the turbulent regime. Results suggest carbon burns much faster than in a bubbling fluidized bed operating under otherwise similar conditions—excepting velocity. The enhanced burning rate is attributed to high mass transfer rates in a turbulent fluidized bed. This indirect observation of high mass transfer rate in turbulent fluidized beds is confirmed by a series of mass transfer (sublimation of naphthalene) experiments in the same bed. For the prediction of mass transfer in turbulent fluidized beds, a correlation of the Sherwood number is proposed. It shows a fair agreement with experimental data.     

流化床锅炉燃烧室的流体动力学模拟

流化床的放大效应十分显著,使得流化床的试验研究在大型工业流化床设计中的应用发生问题。近年来在国外发展起来的流化床模拟放大技术是从流态化现象的基本控制方程出发,根据相似原理导出一组无量纲相似准则数。这些准则数建立了不同条件下(结构尺寸、温度、压力和床料特性等)的流化性能间相似的内在关系,对流化床的试验研究及设计实践有重要的指导意义及应用前景。     

Flow pattern identification of fluidized beds using ECT

IntroduchonPeople's understanding of the solids distribution inthe bottom zone of ~ating lluldized beds (CFB) isvery limited. There are divided assUInptions for thebottom aeon Of CFBs, e.g. turbulent flow and fastfiuldization (such as' ~ and the']) as oPPosed tobubbling fiuldized bed (e.g. Werther and Hirschberglz]).Also, different models ealst for the reactions in thisaeon, such as Plug flow model (Van Sw~['], Wen['],Fane and benal), anally dispersed Plug flow of gas(Avidant'], Edward…     

Mitigation of ice crystallization fouling in stationary and circulating liquid–solid fluidized bed heat exchangers

Liquid–solid fluidized bed heat exchangers are attractive ice crystallizers since they are able to mitigate ice crystallization fouling and exhibit high heat transfer coefficients. Experiments show that the fouling removal ability of stationary fluidized beds increases with decreasing bed voidage (95–80%) and increasing particle size (2–4 mm). The removal of ice crystallization fouling appears to be more effective in circulating fluidized beds, especially at high circulation rates. Fouling removal is realized by both particle–wall collisions and pressure fronts induced by particle–particle collisions. A comparison between ice crystallization experiments and impact characteristics shows that the removal rate is proportional to the impulse exerted on the wall. A model based on these phenomena is discussed and predicts the transition temperature difference for ice crystallization fouling in both stationary and circulating fluidized beds with an average absolute error of 9.2%.     

双室内循环流化床煤气化系统的冷态实验研究

本文发展并建了双室并列流化床煤气化系统的冷态模型。在此基础上,对影响气化系统操作的两个主要因素－两流化床之间颗粒物料的循环技术及流化床床层的膨胀特性进行了实验研究。     

Prevention of fouling and scaling in stationary and circulating liquid–solid fluidized bed heat exchangers: Particle impact measurements and analysis

Fluidized particles in liquid–solid fluidized bed heat exchangers are able to remove deposits from the walls and thus to prevent fouling or scaling. This fouling prevention ability is believed to depend strongly on the frequency and force of particle–wall collisions. This paper presents piezoelectric measurements of impacts on the wall in both stationary and circulating fluidized beds of various particle sizes and bed voidages. Two types of impacts were measured, namely by collisions of particles on the sensor and by liquid pressure fronts induced by particle–particle collisions close to the sensor. The characteristics of both impact types are used to analyze the total impulse and energy exerted by impacts on the wall for various fluidized beds.