YG240型循环流化床锅炉临界流化风量的确定

循环流化床锅炉的临界流化风量是锅炉设计、运行的重要参数,结合ＹＧ２４０－３．８２／４５０型循环流化床锅炉临界流化风量的测试,提出了临界流化风量的测试方法,同时对影响循环流化床锅炉临界流化风量的测试,提出了流化风量的测试方法,同时对影响循环流化床锅炉临界流化风量参数的重要因素进行讨论。     

气-气式跨临界二氧化碳空调系统研制

利用一套气－气式跨临界二氧化碳（CO2）空调系统实验装置，对设计要点做了简要介绍，给出了初步的实验结果。     

冷喷涂临界速度及其影响因素

综述了冷喷涂过程中粒子速度和临界速度的模拟计算及实际测定的方法,分析了冷喷涂中影响临界速度的因素,指出合理利用数值计算方法并结合粒子和基体本身的物理性质来设计喷管几何结构、优化涂层制备工艺参数以提高涂层性能将是冷喷涂发展的主要方向之一。     

理论临界冲击拉伸速度研究

分析了理论临界冲击拉伸速度。指出率相关的Karman-Taylor塑性波传播理论、完全热耦合的高应变率本构关系以及绝热升温方程确定了理论临界冲击拉伸速度。对于高导无氧铜,采用典型的两类高应变率本构关系计算了理论临界冲击拉伸速度。研究结果表明:与Johnson-Cook关系对应的理论临界冲击拉伸速度明显小于与Zerilli-Armstrong关系对应的理论临界冲击拉伸速度。该文也强调指出,理论临界冲击拉伸速度仅对应于塑性波速趋于0,而实验临界冲击拉伸速度不仅与应力波效应有关,而且与杆的动态颈缩、损伤演化致断裂有关。     

速度-墨量补偿特性曲线的研究

分析了印刷过程中影响印品墨色稳定性的多种因素,提出印刷速度的改变将导致供墨量的不稳定,从而使产品墨色均匀性差.解决这一问题的方法是在印刷机自动控制中心,设置速度墨量补偿特性曲线,根据特性曲线印刷机可自动调整墨斗辊的转动行程,以满足印刷质量的要求.     

气固两相输送过程节能优化研究

气力输送过程试验研究已得压损经验公式及相关实验数据表明.压损最小值处的气力输送风速为临界速度.根据上述研究结果在MAT-LABR2007b软件的SIMULINK工作环境空间下,本文综合运用模糊控制器等相关运算模块构建气力输送过程控制仿真模型,有效的控制气力输送风速至I临界速度处,从而达到节能优化的目的.     

确定轴向冲击下薄壁圆柱壳第二临界速度的新方法

研究薄壁圆柱壳的动态屈曲模式，有助于构造具有高吸能率的抗冲击结构。根据轴向冲击下的薄壁圆柱壳存在使其屈曲模式由轴对称转换为非轴对称的第二临界速度，且当冲击速度大于第二临界速度时薄壁圆柱壳的屈曲模式先呈现轴对称形式，然后随着冲击响应时间逐渐由轴对称形式转化为非轴对称形式这一理论，基于有限元仿真，比较撞击系统动能的时间历程和屈曲变形的时间历程，提出了用以确定第二临界速度的能量迭代法。应用此方法设计薄壁圆柱壳的动力屈曲结构可有效地减少试验次数，降低实验成本。该方法的可行性和正确性利用落锤实验得到了验证。     

破片头部系数对TNT冲击起爆临界速度影响规律研究

为研究破片头部形状在炸药冲击起爆中的影响,基于破片冲击起爆炸药的临界能量判据准则,结合LS-DYNA有限元软件,分别计算了正四棱柱破片、正六棱柱破片、圆柱破片、模拟弹丸破片(fragment-simulating projectiles,FSP)和球头形破片等5种破片冲击起爆TNT装药的理论和仿真速度阈值,并拟合出FSP冲击起爆炸药的理论头部形状系数。结果表明,在相同质量和撞击横截面积下,不同头部形状的破片撞击TNT装药的起爆阈值不等;起爆时间与破片的动能大小有关,动能越大,起爆时间越短。对于多边正棱柱类型的破片(如正四棱柱破片、正六棱柱破片、正八棱柱破片等),提出了以正棱柱的外接圆柱作为简化模型来计算多边形正棱柱破片冲击起爆TNT速度阈值,发现多边正棱柱破片横截面的边数越多,计算结果与数值模拟结果吻合越好。     

液-固流化床最小流态化速度的数值模拟与验证

为使用计算颗粒流体力学(CPFD)的数值模拟法代替实验法,建立单管的液-固两相流化床实验系统;实验测量5种颗粒的最小流化速度;应用CPFD方法对单管液-固流化床模型进行数值模拟,比较5种颗粒的最小流态化速度的实验值与模拟值,并进行误差分析,验证数值模拟方法的正确性。结果表明：5种实验颗粒的最小流态化速度实验值分别为0.021 6、 0.036 7、 0.029 3、 0.055 5、 0.084 5 m/s; 2种公式验算值与实验值的最大相对误差小于10%,平均相对误差小于5%,证明实验结果是可靠的;5种模拟颗粒的最小流态化速度模拟修正值分别为0.024、 0.044、 0.041、 0.069、 0.062 m/s;颗粒S₁、 S₂、 S₄、 S₅的模拟修正值与颗粒E₁、 E₂、 E₄、 E₅的实验值之间的最小流态化速度的误差分别为11.1%、 19.9%、 24.3%、 26.6%,均为正向偏差且在工程允许范...     

循环流化床锅炉内颗粒速度分布的实验研究

为了研究操作参数对循环流化床锅炉内颗粒速度分布的影响,在冷态模型装置上使用PV6A型颗粒速度光纤测量仪、毕托管对循环流化床锅炉炉膛内的颗粒速度进行了测量与分析。结果表明:在流化风速为2.57 m/s、循环质量流率为0.58 kg/(m2.s)、一次风量为2 300 m3/h、二次风量为1 500 m3/h时,循环流化床锅炉炉膛内颗粒浓度分布、压降、流化状态、质量循环都达到一个较稳定的水平,呈现典型的环核分布特征。     

Velocity of full fluidization of a bed of polydisperse granular materials

Based on the principle of hydrodynamic equivalence, a technique to calculate the velocity of complete fluidization of polydisperse granular materials of different densities with allowance for the transformation of their initial size distribution has been worked out. Translated from Inzhenerno-Fizicheskii Zhurnal, Vol. 82, No. 2, pp. 296–300, March–April, 2009.     

Experimental study on fluidization characteristics of vinegar residue in a vibrated fluidized bed

As a by-product in the vinegar brewing process, vinegar residue always has a high moisture content, which is detrimental to the storage and recycle process. The vibrated fluidized bed can be used to dry the vinegar residue. In present work, inert particles were added to a vibrated fluidized bed to improve the fluidization of vinegar residue. Experimental studies were carried out to investigate the fluidization behaviors of the binary mixtures. Flow pattern maps indicated that there was an upper limit to the vinegar residue mass concentration c_w at which stable fluidization could be achieved. The minimum fluidization velocity u_mf of the binary mixture increased as the vinegar residue mass concentration c_w increased and decreased with the increase of the vibration intensity Λ. As increasing vibration intensity Λ or decreasing vinegar residue mass concentration c_w, the drying rate of vinegar residue increased.     

爆破振动作用下地下洞室临界振速的研究

利用波函数展开法,分析了爆破地震波与邻近圆形洞室的相互作用,推导了爆破地震波作用下圆形地下洞室围岩的应力和位移表达式,求出了爆破地震波频率不同和围岩性质不同时围岩周围的应力和振速分布.结合应力和振速分布及围岩的抗拉强度,得到了不同工况下围岩的临界破坏振速.     

超细无机粉体快速流态化的雾化分级研究

介绍了对无机超细粉的雾化分级处理工艺,结果表明:快速流化床处理超细无机粉体是有效的,并获得了下道工序所需的特性物料。     

Typical Fluidization Characteristics for Geldart's Classification Groups

This article describes a comprehensive experimental analysis that defines typical fluidization characteristic curve for Geldart's classification groups. Geldart defined four types of materials which differ by the cohesion forces between particles. An experimental apparatus containing fluidized beds of four pipe diameters and fully controlled by LabVIEW was used to perform the fluidization tests. All tests were performed automatically by gradually increasing the air velocity and measuring the pressure drop over the bed. For each test, the fluidization curve was recorded and the minimum fluidization, bubbling, and slugging velocities were defined. It was found that the fluidization curve of material define accurately the Geldart's group to which the material belongs. In addition, was reviewed the reason for those materials and under which conditions the pressure drop increases in the slugging state. Finally, the influence of height to bed diameter H/D ratio on the shape of characterization curve was found. The present study has significant interest for researchers and designers since it enables to predict the fluidization characteristics of two-phase (fluid-solids) flows.     

Experimental and numerical studies on a bubble-induced inverse gas-liquid-solids fluidized bed

Hydrodynamics in a newly invented bubble-induced inverse gas–liquid-solids three-phase fluidized bed has been studied via both experimental and numerical methods. With experiments in a 3.0 m column of 0.153 m in diameter, four fluidization regimes including a fixed bed regime, a bed expansion regime, a complete fluidization regime, and a freeboard regime have been identified with the increase in the superficial gas velocity. A three-phase Eulerian-Eulerian CFD model was developed to simulate the hydrodynamics in the inverse three-phase fluidized bed and the simulation results have a good agreement with the experimental data. The effects of the particle property and solids loading on the transitions across the flow regimes were numerically studied. A higher solids loading and/or a larger particle density are reported to contribute to an easier fluidization and a faster flow development to the complete fluidization regime. The radial flow structure becomes less uniform with increased inner circulation of the liquid after introducing more bubbles into the column.     

Viscosity and separation performance of a gas-solid separation fluidized beds

A theoretical model of viscosity in gas-solid separation fluidized beds is established according to the two-phase flow theory of fluidized beds. After comparing theoretical and measured values, the correlation coefficient between the two is as high as 0.99, showing that the model has good predictability for the viscosity of fluidized beds. Meanwhile, the viscosity and its influencing factors were studied using a Brookfield viscometer. The study shows that smaller medium particles (0.074–0.15?mm) can reduce the viscosity of fluidized beds, but they will aggravate the viscosity fluctuation at more than 5?wt% addition, which is unfavorable to the stability of fluidized beds. In addition, in the actual separation process, the external factors (such as moisture and coal powder content) also affect the viscosity of the fluidized beds. Increasing the moisture increases the viscosity of the fluidized bed, whereas coal dust has the opposite effect. In order to ensure the stability of the fluidized bed, the bed moisture content should be controlled below 1?wt%, while the content of coal powder should be limited below 5?wt%. Based on separation tests, reducing the viscosity will improve the separation performance of a fluidized bed at the proper fluidized gas velocity, with the lowest possible error E_p of 0.085.     

Fluidization of palm kernel shell,palm oil fronds,and empty fruit bunches in a swirling fluidized bed gasifier

The increased biomass utilization has triggered the use of palm oil waste as fuel for gasification in Malaysia. In this study, pioneering work was conducted on three types of palm oil wastes namely palm kernel shell (PKS), palm oil fronds (POF), and empty fruit bunches (EFB). Minimum air velocity (U_mf) required for fluidization of the tested biomass was determined experimentally in a swirling fluidized bed, by considering the effect of bed weight, density, particle size, fluidized bed height, pressure drop, and bed voidage. It was revealed that higher the particle size the smaller will be the voidage, which consequently affects the minimum fluidization velocity. U_mf was increased with a decrease in voidage size. However, a direct relationship was found between particle size and U_mf. Overall highest U_mf was determined for EFB followed by POF and PKS. Fluidized bed height was increased by decreasing the particle size regardless of the biomass type. Highest unsettled bed height was obtained with PKS on account of its low density among all the test fuels. It was concluded that optimization of the fluidized bed for each type of biomass, particle size, and density is explicitly required for a low-cost energy conversion process.