45000 m3/h恩德气化炉气固流动特性模拟

将常规45 000 m³/h恩德气化炉对冲布置的喷嘴结构改良为旋切均布喷嘴结构,炉膛内流场发生了变化。为了研究旋切结构喷嘴恩德气化炉炉内的流场结构以及喷嘴气化剂速度对气固流动特性的影响,应用欧拉-欧拉双流体模型(TFM)对炉膛内的流场进行冷态数值模拟。得到了炉膛内颗粒轴向速度分布、颗粒体积分数分布以及流场结构分布结果。研究表明：旋切喷嘴结构下恩德气化炉炉内颗粒流动轨迹为螺旋上升式结构,并在炉膛中下部形成颗粒内循环;增大喷嘴气化剂速度能够提升颗粒内循环倍率;随喷嘴气化剂速度的增加,炉内气固流动特性越佳,喷嘴速度为50,60 m/s时,炉内流场较为紊乱,喷嘴速度增加到70,80 m/s时,颗粒分布更加规则,但气固流动特性变化已不明显,考虑到喷嘴速度过大会影响系统的稳定性,则喷嘴速度70 m/s时,为较优工况。模拟结果为热态数值模拟以及提高工业气化炉气化效率的研究提供一定的理论依据。     

喷射式环流反应器内流速分布的实验研究

主要研究了喷嘴位置和喷嘴出口速度对底部是圆锥台的喷射环流反应器(JLR)的影响,从而确定最优出口速度和喷嘴位置。对JLR内部流速进行测量,绘出JLR内的速度分布图,并从速度场和内外循环比2个方面进行分析,从而确定最优参数。结果表明:在实验室范围内,当喷嘴出口速度为2.1 m/s,喷嘴位置为40 mm时较优。导流筒内速度呈抛物线分布;喷嘴出口速度增加,环隙速度对应增大,内外循环比也增加;随着喷嘴位置逐渐靠近导流筒,内外循环比先增加,再减小。     

基于VOF方法的多孔陶瓷快速成型喷嘴流场数值分析

为改善多孔陶瓷坯体中泥料开裂、分层现象,利用VOF方法和层流模型,以等效的二维网格模型对多孔陶瓷快速成型喷嘴流场进行数值分析,分析泥料进口速度对速度分布、压力分布和泥料体积分数的影响。结果表明:泥料进口速度为0.001 m/s时,喷嘴内速度分布均匀,没有出现空气涡;进口速度为0.002 m/s时,喷嘴内部存在压力差,在喷嘴轴线1/5处出现约占喷嘴总面积0.5%的空气涡;进口速度为0.003 m/s时,空气涡约占喷嘴总面积6%;数值分析和实验结果基本吻合,误差在12.5%以内,在用快速成型技术制备多孔陶瓷时,泥料进口速度需控制在临界值0.002 m/s以下。     

多喷嘴对置式撞击流反应器流场的数值模拟

为探讨多股撞击流反应器内流场的特点,利用Fluent软件对两喷嘴对置式和四喷嘴对置式撞击流反应器内流场进行模拟,研究了在不同工况下这两种撞击流反应器内的流场结构,设定进口流速分别为5 m/s、10 m/s、15 m/s、20 m/s、25 m/s。模拟结果表明,进口流速由5 m/s增加到25 m/s时,反应器内流体流动的平均速度及压力波动增大为原来的4.1倍和16.2倍,其速度梯度和压力平均波幅也增大为原来的5.0倍和25.4倍。通过对两种不同结构的撞击流反应器的比较可以得到四喷嘴对置式撞击流反应器内流体流动产生的速度梯度和压力平均波幅更大,其值都约为二喷嘴对置式撞击流反应器的1.2倍,因而四喷嘴对置式撞击流反应器内剪切力场更强,脉动更强烈,更有利于反应器内的湍动混合。     

新型催化裂化提升管进料段内原料射流浓度分布的大型冷模实验研究

通过大型冷模实验研究了喷嘴射流与催化剂逆向接触的新型提升管进料段内喷嘴射流浓度沿径向的分布,考察了喷嘴气速、预提升气速的影响. 结果表明,喷嘴气速Uj=78.5 m/s和预提升气速Ur=4.1 m/s条件下可获得较好的油剂混合效果. 与传统形式相比,新型结构可促进油剂混合,在轴向距离H<0.7 m内完成油剂混合,油剂初始接触区域内喷嘴射流相浓度分布更均匀. 给出了新型进料段中不同区域喷嘴射流浓度沿径向分布的经验模型,计算值与实验值吻合较好.     

新型扇形雾化喷嘴的实验研究

在对Y型喷嘴结构和雾化机理研究分析的基础上,设计了一种新型的扇形雾化喷嘴,并对该喷嘴进行了实验研究. 实验测量了不同气、液压力下扇形雾化喷嘴的流量、雾化角和索特尔平均粒径及其在空间上的横向和纵向分布. 通过对液流量用Y型喷嘴设计公式进行拟合,得到了公式中适合扇形雾化喷嘴设计的系数取值：m=0.39, b=0.98. 喷雾雾化角a大约在90o~98o之间,变化不大. 喷雾的索特尔平均粒径在空间横向呈类似"W"的分布,在空间纵向呈逐渐降低并趋于稳定的分布.     

熔渣气化炉喷嘴燃烧区行为的数值模拟研究

燃烧区是熔渣气化炉的重要区域,其对熔渣气化炉的工作状态具有明显影响。基于双欧拉模型探究了燃烧区的速度场、温度场和组分场的分布特征及燃烧区空腔的形成过程。研究发现：工业级熔渣气化炉燃烧区呈“羽”状,其先向炉中心延伸再斜向上发展;气体在熔渣气化炉中心区域的流动速度为2.5 m/s左右,但未形成“高速对撞区”;高温区出现在燃烧空腔外表面附近特别是正对喷嘴且靠近炉中心的区域,该区域的温度可以达到约2000℃;氧气主要分布在气化剂喷嘴前端约0.5 m的空腔内,一氧化碳的分布区域与水蒸气在空间上有较大程度重叠,二氧化碳主要在喷嘴前端空腔外壳附近生成,氢气浓度较高的区域则出现在燃烧区对应空腔的上沿;沿喷嘴轴线方向,气体温度呈先升至峰值再逐渐下降的趋势。随着气化剂流量的增大,燃烧温度极大值出现的位置逐渐朝炉中心处移动,并呈较明显的线性变化规律。     

基于PIV技术的七喷嘴气化炉流场研究

为研究七喷嘴气化炉的流场分布,建立了顶置七喷嘴气化冷模试验装置,采用激光粒子成像测速系统(PIV)在气化炉的上部、中部及下部视窗进行了流场测试,比较分析了颗粒流量、分散风流量对气化炉流场的影响。结果表明,在颗粒流量20~150 kg/h,分散风流量740~880 m3/h的工艺条件下,气化炉上部流场呈现自由射流特点,射流长度为40 cm,平均射流速度为25 m/s,中下部流场则以返混区为主,流速在8 m/s以下;颗粒流量增大会使得最大射流速度由40 m/s降低至15 m/s,且气化炉上部射流粒子束的径向脉动增强,造成射流弥散;分散风流量增大使得最大射流速度由25 m/s增至35 m/s,射流长度无明显变化。颗粒流量和分散风流量对流场的影响主要体现在气化炉上部,对中下部流场的影响逐渐减弱。     

无挡板CSTR内部流场及颗粒分布的CFD模拟研究

为探究无挡板连续搅拌式反应釜（CSTR）内部流场分布及颗粒运动情况,采用计算流体力学（CFD）,在欧拉-拉格朗日模型的基础上对三种搅拌釜工况进行了研究分析。同时,探讨了粒径为100,300和500μm的颗粒在各个工况下的混合情况。研究表明：在时间为0～100 s时,初始搅拌釜内颗粒的平均速度相较于初始时增加了39.22%,达到了1.479 7 m/s,搅拌釜内的流场平均速度为1.737 2 m/s,颗粒的平均速度与流场速度呈现相近的趋势;搅拌桨位于罐内中间位置时,颗粒分布最为均匀;采用双层搅拌桨时,颗粒速度得到了显著的提升,最大颗粒速度可达到4.238 3 m/s。     

旋流组合式进料喷嘴雾化性能实验研究

针对6种构型的旋流组合式进料喷嘴的雾化性能进行了实验研究。采用相位多普勒粒子分析仪(PDPA)测量了雾化粒径,同时验证了喷嘴的雾化角和各段的压降分配方案。结果显示:该旋流组合式喷嘴雾化效果较好,雾化粒径的空间分布比较均匀,各构型喷嘴在测量范围内的雾化粒径在63—76μm;喷嘴雾化粒径在流量20%操作弹性范围内的变化均在6μm之内;气液质量比从6%增加到7%会减小雾化粒径增加喷射速度;喷嘴压降分配合理,且采用四组合式旋流器以及球头双槽互击喷头的喷嘴压降分配较优。     

隔板式内循环气化炉的设计和运行

介绍了一种新型的隔板式内循环气化炉的设计和运行。通过在气化炉的中间设置隔板,可使流化床气化炉的床层形成2个流化速度不等的流化区域,在高速区没有反应的原料或炭粒,在床层上部随流化介质流入低速区,在低速区内进行气化反应;未反应完的炭粒再经底部流回高速区,进一步进行气化反应,形成一个内部循环,从而达到延长原料在炉内的反应时间、增强气化效率的效果。实验结果表明:这种气化炉反应温度在790—850℃时,气化效果最好,产气率为1.6—1.9m3/kg,气体热值为5340kJ/m3(木质类原料)或4880kJ/m3(稻壳),气化效率可达70%。     

强制液体外循环气升式内环流反应器的流体力学特性

在有机玻璃制成的主体反应器(φ0.286 m×3.0 m)内,采用空气-水的气液两相体系考察了不同表观气速下带有中心下料管和环管式气体分布器的环流反应器内局部气含率和内环气泡上升速度的流体力学特性。结果表明：气含率均随表观气速的增大而增大;从外环流入内环的气泡数量比较少;在相同条件下外环的气含率远远低于内环的气含率;新型气体分布器的采用和液体外循环的引入可以增大床层气含率并使其分布趋于均匀,从而增大了内环中气液两相的接触面积和湍动强度,使传递过程得到强化。在此基础上采用商业软件ANSYS CFX10.0对该反应器进行了数值模拟研究,模拟结果与实验数据基本吻合,说明了基于实验验证的Euler-Euler法可以用于该反应器开发和放大研究。     

活性炭脱除SO2的工艺研究

针对化工行业二氧化硫废气浓度高,间歇排放的特点,提出了活性炭吸附脱除S02的方法。考察了废气相对湿度、温度、气速、活性炭炭层高度、预处理温度对S02脱除率的影响,结果表明,在相对湿度为20％,炭层高度为60cm,温度25℃,气速0．3m／s,活性炭预处理温度600℃时,脱除率可以达到97．2％。     

A Parametric Study of the Gas Flow Patterns and Drying Performance of Co-current Spray Dryer: Results of a Computational Fluid Dynamics Study

A computational fluid dynamic study was carried out to investigate airflow pattern, temperature, and humidity profile at different levels in the drying chamber. Good agreement was obtained with published experimental data. The effects of operating pressure, heat loss from the chamber wall and inlet air conditions on the gas flow pattern, droplet trajectories, and overall dryer performance also were investigated. Results are presented and discussed in terms of the gas velocity, temperature, and humidity profiles within the chambers. The volumetric evaporation values, heat transfer intensity, and thermal energy consumption per unit evaporation rate were computed and compared for drying of a 42.5% solids solution in a spray chamber 2.215 m in diameter with a cylindrical top section 2.005 m high and a bottom cone 1.725 m high. Wall regions subject to formation of undesirable deposits are also identified.     

A Parametric Study of the Gas Flow Patterns and Drying Performance of Co-current Spray Dryer: Results of a Computational Fluid Dynamics Study

Abstract

A computational fluid dynamic study was carried out to investigate airflow pattern, temperature, and humidity profile at different levels in the drying chamber. Good agreement was obtained with published experimental data. The effects of operating pressure, heat loss from the chamber wall and inlet air conditions on the gas flow pattern, droplet trajectories, and overall dryer performance also were investigated. Results are presented and discussed in terms of the gas velocity, temperature, and humidity profiles within the chambers. The volumetric evaporation values, heat transfer intensity, and thermal energy consumption per unit evaporation rate were computed and compared for drying of a 42.5% solids solution in a spray chamber 2.215 m in diameter with a cylindrical top section 2.005 m high and a bottom cone 1.725 m high. Wall regions subject to formation of undesirable deposits are also identified.     

3000m~3/h排烟循环流化床脱硫工艺中试实验研究

介绍了采用真实烟气的 30 0 0m3 /h排烟循环流化床烟气脱硫工艺 (CFB FGD)及其中间试验装置 ,通过实验研究了钙硫摩尔比 (Ca/S)、近绝热饱和温度差 (ΔT)、烟气湿度、喷水量、入口SO2 浓度、浆液雾化质量、脱硫灰循环等对脱硫效果的影响。实验表明 ,CFB FGD工艺在停留时间小于 6s、烟气流速v =4— 6m/s、Ca/S =1.2、ΔT =10— 12℃时可实现高达 90 %的脱硫效率。     

Kinetics of cure,cross link density and adhesion of water-reactive alkoxysilicone sealants

When a silicone sealant is exposed to wet air, a surface skin is formed, which becomes thicker with time. For a 1-part room temperature vulcanization (1-RTV), neutral cure system based on the hydrolysis and condensation reactions of alkoxysilanes, it has been observed that, at constant temperature and humidity, the thickness of the cured layer is initially proportional to the square root of time, but later the gradient of such a plot increases. There are thus two regions of cure, an outer region and an inner one. Swelling in toluene, which has been measured for samples taken at various depths, shows that the cross link density is greater in the outer regions. Single lap joints of aluminium or glass have been cured in these two regions and joints from the outer region are always stronger than the corresponding ones from the inner region. This behaviour has been ascribed to the mobility of low molar mass cross linking and coupling agents. During the initial stages of cure they migrate into the outer region, but once cure has passed into the inner region there is now a paucity of these compounds. Young's modulus and the concentration profile of silane crosslinking agent have also been measured. All observations confirm migration of crosslinking species, and gradient formation for most physical properties in the final joint. Measurement of the water vapour permeability coefficient (P) of the cured siloxane network has shown that P is independent of humidity and stretching of the material. A plot of log P against reciprocal absolute temperature is non-linear with positive slope, showing that the heat of permeation is negative and varies with temperature. This can be explained by the formation of water-clusters. When the network is formed water is absorbed and alcohol is released.     

Stereoscopic PIV studies on the swirling flow structure in a gas cyclone

Understanding the swirling flow in a gas cyclone is of great importance in improving the cyclone design. Once the three-dimensional strong swirling flow is fully understood, cyclone performance such as pressure drop and separation efficiency can be improved by optimizing the cyclone design. The swirling flow was investigated by the stereoscopic particle image velocimetry (Stereo-PIV) in this work. The instantaneous whole-field tangential, axial, and radial velocities were measured simultaneously in the cylindrical and conical separation zone, and in the dust hopper area of the cyclone with gas inlet velocity of .The time-averaged flow pattern in the cylindrical and conical sections of the cyclone showed: a typical Rankine vortex with inner quasi-forced vortex and outer quasi-free vortex which is generated by tangential gas velocity; inner upward flow and outer downward flow of axial gas velocity; and centripetal flow in the region close to the wall due to the presence of radial gas velocity. In the dust hopper, a secondary longitudinal circular flow is formed in the annulus area between the conical body and the cylindrical wall. Experimental results indicate that the separated particles may be re-entrained into the cyclone from the bin to degrade the separation efficiency of the cyclone.     

Destabilisation of homogeneous bubbly flow in an annular gap bubble column

Experimental results are presented to show that there are very significant differences in the mean gas void fractions measured in an open tube and a annular gap bubble column, when operated at the same gas superficial velocity, using a porous sparger. Measurements were carried out in a vertical 0.102 m internal diameter column, with a range of concentric inner tubes to form an annular gap, giving diameter ratios from 0.25 to 0.69; gas superficial velocities in the range 0.014–0.200 m/s were investigated. The mean gas void fraction decreases with increasing ratio of the inner to outer diameter of the annular gap column and the transition to heterogeneous flow occurs at lower gas superficial velocities and lower void fractions. Two reasons are proposed and validated by experimental investigations: (1) the presence of the inner tube causes large bubbles to form near the sparger, which destabilise the homogeneous bubbly flow and reduce the mean void fraction; this was confirmed by deliberately injecting large bubbles into a homogeneous dispersion of smaller bubbles, and (2) the shape of the void fraction profiles changes with gap geometry and this affects the distribution parameter in the drift‐flux model. Both of these effects serve to reduce the mean gas void fraction in an annular gap bubble column compared to an open tube at the same gas superficial velocity.     

旋风分离器高温流场的实验测量

引言 对旋风分离器内流场的认识是研究其分离过程的基础.长期以来,人们对旋风分离器内流场的结构、速度分布等进行了大量的测量和分析,认识到旋风分离器内是一个三维强旋旋湍流场.