密相流化床中介尺度流动结构的流体力学特性研究

在一套流化床冷模实验装置中对黄沙颗粒和黄沙-硅微粉 （20 μm）混合颗粒进行实验。测量固含率时间序列信号并进行统计分析,提出并建立复杂光纤脉动信号的解耦方法,实现稠密气固流中介尺度流动结构的准确识别。基于统计矩一致性原理提出气泡阈值的计算方法,通过遍历法确定气泡阈值。对气泡阈值变化规律进行分析,发现加入细颗粒有助于改善流化质量,随表观气速的增加,气泡阈值减小。对气泡、乳化和聚团三相的相分率进行统计,发现在黄沙颗粒中加入少量（5%,质量分数）细颗粒能够显著改善流化质量,细颗粒添加量过多时（10%）,对流化质量的改善将减弱。对气泡的流体力学特性进行分析,发现加入10%硅微粉后,气泡弦长增大,频率降低,速度略有降低。对颗粒聚团流体力学特性进行分析,发现随硅微粉含量增加,表观气速对聚团速度的影响减弱,聚团弦长略有减小。加入5%硅微粉后,颗粒聚团的出现频率较小且径向上分布均一。加入10%硅微粉后,聚团频率有所增大,说明加入过多硅微粉会促进聚团的形成。     

高密度浓相流化床中气泡的兼并与分裂特性

利用先进的高速动态分析系统对二维床中气泡的行为进行了研究,通过对所拍摄图象的分析处理．得到了不同介质流化床内形成的气泡形状、大小、聚并及分裂的基本规律和特点．实验研究表明．气泡的兼并主要是两气泡问的合并、被合并气泡总是从气泡的尾涡区曳入气泡;气泡分裂主要发生在操作气速较大或大气泡中,是由于其顶部粒子流(或“剪切流”)的侵入造成的;操作气速较低,粒度、密度较大粒子形成的流化床更易于造成气泡的湮灭。     

流化床密相区内固体颗粒对流换热模型研究进展

为深入理解流化床密相区内活性颗粒表面换热过程,论述了乳化相模型、单颗粒和双颗粒模型、变物性模型以及接触热阻模型等流化床密相区内固体颗粒对流换热模型的研究进展,提出了模型发展方向。当流化风速较低时,固体颗粒对流换热系数可采用乳化相模型进行预测。针对流化风速较大的工况,有学者提出了单颗粒和双颗粒模型、变物性模型以及接触热阻模型,并采用适当假设简化模型,然而模型的可靠性仍需进一步验证。最后提出现应加强固体颗粒对流换热过程的模型研究,提高模型在较宽风速范围内对固体颗粒对流换热系数预测的适用性;重点研究活性颗粒在密相区内的运动形式及活性颗粒表面固体颗粒对流换热关键参数测量方法。     

Gas backmixing in the dense region of a circulating fluidized bed

The gas backmixing characteristics in a circulating fluidized bed (0.1 m-IDx5.3-m high) have been determined. The gas backmixing coefficient (D_ba) from the axial dispersion model in a low velocity fluidization region increases with increasing gas velocity. The effect of gas velocity onD _ba in the bubbling bed is more pronounced compared to that in the Circulating Fluidized Bed (CFB). In the dense region of a CFB, the two-phase model is proposed to calculate D_bc from the two-phase model and mass transfer coefficient (k) between the crowd phase and dispersed phase. The gas backmixing coefficient and the mass transfer coefficient between the two phases increase with increasing the ratio of average particle to gas velocities (U_p/U_g).     

Gas transfer from bubbles in a fluidized bed to the dense phase—I. Theory

Gas transfer from bubbles to the dense phase in a fluidized bed is described as a combination of diffusional and convective processes. In the convective process the cloud formation is important as is the adsorption of the gas at the solid interface. The resulting differential equations are worked out numerically and for many cases the theoretical transfer coefficients are given.     

Gas transfer from bubbles in a fluidized bed to the dense phase — II. Experiments

An experimental check was made upon the theory given in Part I. Cracking catalyst was used as a solid and differently adsorbed tracer gases were used. In a two-dimensional fluidized bed bubbles were formed underneath a gauze cap, while solid flowed along the bubble at the corresponding bubble velocity. Tracer injections provided the value for the transfer coefficient. In three-dimensional beds of 18 and 90 cm dia. large traced gas bubbles were injected. Tracer concentration was detected at certain heights. From the decrease the transfer coefficient was calculated. In the 90 cm bed the transfer coefficient was also calculated from residence time distribution measurements when the dense phase was perfectly mixed.It shows, that the two-dimensional bubble confirms the theory. For three-dimensional bubbles the transfer is higher than theoretically predicted, especially when the dense phase is expanded.     

流化床密相区颗粒扩散系数的CFD数值预测

应用离散颗粒模型直观获得颗粒运动情况,并从单个颗粒和气泡作用的角度分析颗粒运动和混合,证实气泡在床层中上升、在床层表面爆破以及气泡上升引起的乳化相下沉运动对颗粒混合起关键作用。应用基于颗粒动理学的双流体模型系统地对床宽分别为0.2、0.4、0.8 m的二维流化床在鼓泡区和湍动区的气固两相流动行为进行数值模拟。受离散颗粒模型启发,在双流体模型计算结果基础上,引入理想示踪粒子技术计算床内平均颗粒扩散系数。计算结果表明,颗粒横向扩散系数(D_x)总体上随流化风速增大而增大,但受床体尺寸影响较大;颗粒轴向扩散系数随流化风速增大而增大,受床体尺寸影响较弱。文献报道的密相区颗粒横向扩散系数分布在10^-4～10^-1 m²·s^-1数量级。本文提出的计算方法在数量级上与文献实验结果吻合,表明在大尺寸流化床且高流化风速下,颗粒横向扩散系数远大于小尺寸鼓泡流化床,为不同研究者实验结果的分歧提供了理论依据,也为预测大型流化床内颗粒扩散速率提供了放大策略。     

空气重介流化床干法选煤技术的研究

从水资源短缺的现状入手,结合科学技术的发展现状,重新探讨了空气重介流化床干法选煤技术的定位问题,并对空气重介流化床干法选煤的工艺设计进行了剖析,阐明了该工艺的发展潜力,旨在推动空气重介流化床干法选煤技术的推广与应用。     

空气重介干法选煤的应用与展望

从干法选煤领域中空气流态化技术应用的背景及实现环境出发,综述了实现该技术的必要性和正确性。回顾了空气重介流化床选煤中的一些重要历程,展望流态化技术在选煤中发挥更大效用,促进选煤事业的发展,实践建设环境资源友好型社会。     

High-pressure fluidized bed coating utilizing supercritical carbon dioxide

Various particles with sizes between 100 and 200 μm were encapsulated with waxes commonly used in technical coating applications. For this, a homogeneous mixture of molten paraffin and supercritical carbon dioxide was prepared in an autoclave and injected into the high-pressure fluidized bed through a nozzle from the bottom. Due to the different conditions in the mixing autoclave and the fluidized bed, the paraffin precipitated in the vicinity of the nozzle and adhered to the solid particles. A complete, thin, uniform, and solvent-free coating was produced. The use of two paraffins with different alkane compositions resulted in dissimilar spreads on glass beads due to their different glass transition temperatures. A smaller pressure drop across the nozzle led to more uniform and even coatings. Glass beads, ceramic spheres, potassium chloride, and lactose showed similar coating results, whereas different morphologies were observed with a plastic material, characterized by a rougher surface and a lower surface energy. The high quality of the coating was confirmed by standard dissolution tests with coated potassium chloride crystals and lactose agglomerates.     

空气重介质流化床流化特性及密度梯度分布研究

为实现物料的有效分选,以磁铁矿粉和玻璃微粉为混合加重质,研究了混合加重质的流化特性及空气重介质流化床床层密度梯度分布情况。结果表明:空气重介质流化床形成了均匀稳定的流化状态,当流化气速大于7.10 cm/s后,床层压降基本维持在510 Pa,床层密度基本不变,为1.71~1.74 g/cm3。当流化气速为7.95 cm/s时,流化床内气泡直径为15~25 mm,且分布均匀,流化床各层平均密度从上至下依次为1.72、1.74、1.74、1.74、1.73 g/cm3。流化床上部区域,超微细玻璃微粉被气流带到床层表面,使表面床层密度较小;流化床底部区域,气体分布相对均匀,并未形成大气泡,使该区域流化床床层平均密度偏小;而床层大部分区域床层平均密度均为1.74 g/cm3,比较稳定。因此,当流化气速为7.95 cm/s时,流化床内并未形成明显的分层和分级现象,说明加重质混合比较均匀,为空气重介质流化床分选物料创造良好条件。     

Characteristics of carbon dioxide hydrogenation in a fluidized bed reactor

Characteristics of CO₂ hydrogenation were investigated in a fluidized bed reactor (0.052 m IDxl.5 m in height). Coprecipitated Fe-Cu-K-Al catalyst (d_ρ=75–90 Μm) was used as a fluidized solid phase. It was found that the CO₂ conversion decreases but the CO selectivity increases, whereas the space-time-yield attains maximum values with increasing gas velocity. The CO₂ conversion has increased, but CO selectivity has decreased with increasing hydrogenation temperature, pressure or H₂/CO₂ ratio in the fluidized bed reactor. Also, the CO, conversion and olefin selectivity appeared to be higher in the fluidized bed reactor than those of the fixed bed reactor. Presented at the Int’l Symp. on Chem. Eng. (Cheju, Feb. 8–10, 2001), dedicated to Prof. H. S. Chun on the occasion of his retirement from Korea University     

Synthesis of multi-walled carbon nanotube in a gas-solid fluidized bed

Multi-walled carbon nano-tubes (MWCNTs) were produced by acetylene decomposition on Fe-catalyst in a fluidized bed reactor (0.056 m-IDx1.0 m-high) with a sintered metal distributor (40 μm pore size). The Fe-catalysts were tested in decomposition of the different ratios of acetylene, hydrogen and nitrogen at the temperature range of 823–973 K. The physical properties of the carbon nano-tubes were determined by HR-TEM, SEM and Raman spectroscopy. The multi-walled carbon nano-tubes produced from the fluidized bed reactor are sub-aggregates and entangled with each other. The synthesized MWCNTs have outer diameters of a few tens of nanometers at 823–973 K. It has been found that the synthesized CNT agglomerates are in good condition with less amorphous carbon with the reaction time of 30 to 60 minutes from the analyses of Raman Spectra, SEM and TEM, The ratio (I _D /I _G ) of amorphous carbon (I _D = 1,295 cm^-1) and crystalline carbon (I _G =1,590 cm^-1) range from 1.15 to 1.49.     

Modelling of heavy metal adsorption into activated carbon from apricot stones in fluidized bed

The purpose of the present study is to investigate the behaviour of activated carbon from apricot stones (ACAS) in a closed circuit fluidized bed (CCFB) for removal of Pb, Cu, Cd and Zn ions from aqueous solution. The expansion characteristics of the bed are studied. A homogeneous solid phase diffusion model was used to describe the mass transfer inside the adsorbent particles. A piston-dispersion model was applied for the liquid phase in the bed and compared to the calculations, assuming perfect mixing conditions in the whole CCFB adsorber. The close correspondence between the experimentally determined adsorption in batch and fluidized bed operation modes support the observation that the CCFB can be described by a stirred batch adsorption model. The concentration profile at the bed exit is satisfactorily predicted by the model, thus confirming the equilibrium and kinetic parameters, determined from the laboratory batch adsorption runs.     

Similarity in dense gas-solid fluidized bed, influence of the distributor and the air-plenum

Similitude parameters that govern the dynamics of dense gas-fluidized beds in possible interaction with the air-supply system (distributor and plenum) are found by nondimensionalizing both differential equations that rule the bed dynamics and the coupling with the upstream fluid inlet conditions. In addition to classical dimensionless groups, two new parameters θ_p and θ_d are evidenced. It is shown that their match, along with the other numbers, is required to ensure dynamic similarity for scaled systems. Their influence on the bed dynamics is also investigated and we propose (θ_p,θ_d) maps that illustrate the existence of a coupling zone with an associated frequency modification.     

Small-sized dense magnetic pellicular support for magnetically stabilized fluidized bed adsorption of protein

A small-sized dense magnetic pellicular support (MPS) for magnetically stabilized fluidized bed (MSFB) adsorption of protein has been fabricated by introducing magnetic colloids and glass beads during the emulsification of 4% agarose solution. The MPS was identified with a mean density of 1.40 g/ml and a size range of 70-. The support has a good magnetization property with little residual magnetization after the field was removed. After cross-linking and reducing, the MPS was coupled with diethylaminoethyl (DEAE) groups to create an anion exchanger DEAE-MPS. The fluidization behavior of the support was examined in an MSFB with transverse magnetic field and the results were compared with those obtained in expanded bed. As a result, an optimum field intensity of 250 Gs was found to give the lowest axial dispersion of the MSFB. At the optimum field intensity, BSA adsorption at 208 and 283 cm/h showed that the dynamic binding capacity in MSFB was about 60% higher than that in expanded bed mode. It was attributed to the reduced backmixing in the MSFB compared to that in expanded bed. The results indicate that the dense MPS is promising for MSFB protein adsorption at elevated flow rates.     

A particle-to-particle heat transfer model for dense gas-solid fluidized bed of binary mixture

A particle-to-particle collisional heat transfer model in the frame of Eulerian-Eulerian approach was proposed in this paper. By incorporating it into the multi-fluid model to close the enthalpy equations, the heat transfer between different particle classes in a gas bubbling fluidized bed of binary mixture was investigated, based on the CFD simulations of particle mixing in literature (Cooper and Coronella, 2005). The results showed that the particle-to-particle heat exchange coefficient between different particle classes increases with increasing the size of large particle class and the superficial gas velocity. The ratios of the particle-to-particle heat transfer to the gas-to-particle heat transfer range from 8.04% to 15.0% for various calculating conditions. In order to better understand the heat transfer behavior in a dense gas-solid fluidized of binary mixture, it is important to take the particle-to-particle heat transfer into account.     

Mechanical properties of isotropic pyrolytic carbon deposited in a tumbling bed

The relation between the coating conditions and mechanical properties of the isotropic pyrolytic carbons deposited in a tumbling bed have been investigated. At a constant total flow rate of mixed gases and a constant revolution rate of the reaction tube, pure and Si-alloyed pyrolytic carbons were deposited using a wide range of deposition conditions.The structures of the pyrolytic carbons were characterized by density and crystallite size. The mechanical properties (Young's modulus, fracture strength and strain energy to fracture) were measured by three point bend tests with a knife edge span of 0.35 in.In spite of similar density and crystallite size, all of the mechanical properties of pyrolytic carbons deposited in this process were lower than those of carbons deposited in a fluidized bed. These differences were caused by soot inclusions which had a non-load bearing character and behaved as cracks under load, which were not present in carbons deposited in a fluidized bed.By alloying silicon with the carbon, the number of soot inclusions was not changed, and the fracture strength increased linearly with the SiC content.     

Heat transfer between an isolated bubble and the dense phase in a fluidized bed

Heat transfer between the bubble and dense phases of a bubbling fluidized bed plays a very important role in the system performance, especially for applications involving solids drying and gas‐phase combustion. However, very few experimental data are available on this subject in the literature. An experimental and modelling investigation on the heat transfer behaviour of isolated bubbles injected into an incipiently fluidized bed is reported in this paper. A new single‐thermocouple technique was developed to measure the heat transfer coefficient. The effects of bed particle type and size, and bubble size on the heat transfer coefficient were examined. The heat transfer coefficient was found to exhibit a maximum as the bubble size increased in the bubble size range investigated. The bed particle size had a comparatively small effect on the heat transfer coefficient. A simple mathematical model was developed which provides good agreement with experimental data.     

Production of hydrogen and carbon nanotubes from methane decomposition in a two-stage fluidized bed reactor

Methane decomposition over a Ni/Cu/Al₂O₃ catalyst is studied in a two-stage fluidized bed reactor. Low temperature is adopted in the lower stage and high temperature in the upper stage. This allows the fluidized catalysts to decompose methane with high activity in the high temperature condition; then the carbon produced will diffuse effectively to form carbon nanotubes (CNTs) in both low and high temperature regions. Thus the catalytic cycle of carbon production and carbon diffusion in micro scale can be tailored by a macroscopic method, which permits the catalyst to have high activity and high thermal stability even at 1123 K for hydrogen production for long times. Such controlled temperature condition also provides an increased thermal driving force for the nucleation of CNTs and hence favors the graphitization of CNTs, characterized by high resolution transmission electron microscopy (HRTEM), Raman spectroscopy and XRD. Multistage operation with different temperatures in a fluidized bed reactor is an effective way to meet the both requirements of hydrogen production and preparation of CNTs with relatively perfect microstructures.