Geldart B 类颗粒气固流化床内的压力波动特性(英文)

采用多通道压力采集系统测量了Geldart B类颗粒（树脂）矩形流化床(2.000m×0.300m×0.025m)内的压力波动,探索了流化床内的压力波动特征;同时采用标准方差、自相关和互相关函数分析了表观气速和静床高度对压力波动、压力波速度和压力波主频的影响。结果表明,气泡行为（如：气泡的形成、发展、聚并和破碎）是影响流化床内压力波动的主要因素;密相和稀相界面处的压力波动幅值主要由气泡崩塌决定;压力波在流化床内进行传播,并且具有明显的周期性特征;此外,压力波动、压力波速度和压力波主频均与表观气速和静床高度密切相关。     

加压流化床流化性质的实验与模拟研究

在二维射流流化床装置中,考察了压力对颗粒和气泡运动的影响规律.通过使用摄像技术详细的记录了压力下气泡的行为,并对其进行了分析,由此解决了较高压力下测量流态化性质较为困难的问题.数值研究通过CFD双欧拉模型模拟了带有V形分布器和中心射流的二维流化床内压力对气泡大小、床的膨胀率和射流深度的影响.实验和理论结果表明,在加压状态下,射流气速和分布板气速对气泡的产生、大小及形状有不同的影响.在较高的操作压力下,射流气速增加,气泡变长;分布器气速增大,气泡则变大;射流高度随着分布器气速的增加而降低.模拟结果与实验数据吻合较好,由此该模型为研究较高操作压力下射流流化床流化性质提供了有利的工具.     

气固流化床内射流特性的研究

采用Brandani等的数学模型模拟了中心射流宽度为0.01m的二维气固流化床(高1.6m、宽0.3m)内鼓泡和射流的瞬态及时均流体动力学特性。一种典型的Geldart B颗粒――砂子(粒径为500mm、密度为2660kg/m3)作为研究的模拟物料。瞬态结果表明，床内射流产生和发展、射流崩塌后所形成气泡尺寸以及全床内的气体速度场和空隙率均存在明显的非对称性，但是由压力信号功率谱密度得到的时均压力特性则有较好的对称性。因此，对于商业化稳定运转的射流床，可以用半床模拟结果近似解释整床特性；然而，在考察射流床的瞬态特性时，半床模拟结果与整床结果存在明显偏差。     

Pressure drop in CIM disk monolithic columns

Pressure drop analysis in commercial CIM disk monolithic columns is presented. Experimental measurements of pressure drop are compared to hydrodynamic models usually employed for prediction of pressure drop in packed beds, e.g. free surface model and capillary model applying hydraulic radius concept. However, the comparison between pressure drop in monolith and adequate packed bed give unexpected results. Pressure drop in a CIM disk monolithic column is approximately 50% lower than in an adequate packed bed of spheres having the same hydraulic radius as CIM disk monolith; meaning they both have the same porosity and the same specific surface area. This phenomenon seems to be a consequence of the monolithic porous structure which is quite different in terms of the pore size distribution and parallel pore nonuniformity compared to the one in conventional packed beds. The number of self-similar levels for the CIM monoliths was estimated to be between 1.03 and 2.75.     

A model for the pressure drop in gas—liquid cocurrent downflow through packed beds

A model for pressure drop is proposed for gas—liquid flow through packed beds on the basis of the observed absence of radial pressure gradients and taking into consideration the structure of the bed and the physical properties of the fluids. The model divides the total voitage of the bed into internal and external voidage and appropriately distributes the total liquid holdup into internal and external holdup.Over 2500 experimental data, from the present study as well as those reported in literature, are correlated by the model with an r.m.s. deviation of less than ±9%. The significant parameters affecting the two-phase pressure drop are found to be the bed porosity, the Reynolds number, and the product of the Eötvos and the Morton numbers.     

循环流化床生物质气化炉内计算流体动力学模拟——鼓泡流化床内改进的颗粒床模型（英文）

采用改进颗粒床模型的CFD方法模拟了实验室规模冷模装置内鼓泡床的流体流动时空特性。模拟结果表明表观气速是影响气固动态特征和压力波动的主要因素之一：随表观气速的增大，气泡数目增加，气泡体积增大，压力波动增强；气速越高时均压降越大；在内循环鼓泡流化床内固体颗粒呈“单室”流型。上述与实验观察相吻合的模拟结果将有助于放大和设计商业化的内循环流化床生物质气化炉。     

Hydrodynamics in a Gas-Solids Fluidized Bed Using X-Ray Fluoroscopy and Pressure Fluctuation Measurements

In this work, non-intrusive techniques were used to characterize the hydrodynamics in a gas-solids bubbling fluidized bed using polyethylene powder and glass beads of comparable mean diameter (d_p = 360 µm) but different density. X-ray fluoroscopy measurements and pressure fluctuations were performed on a pseudo 2-dimensional gas-solids fluidized bed. Bubble properties were captured from X-ray fluoroscopy measurements. Similarities and differences of flow behavior of the two particle systems were revealed from comparison of bubble properties. Bubble properities normally varied similary with operating conditions for the two particle systems, while bubble sizes for the glass beads system are larger than those for the polyethylene system. Wavelet analysis of pressure fluctuations was applied to investigate the gas and solids phase flow behavior. Multi-scale flow behavior was extracted from the standard deviation of the decomposed coefficient series. Flow behavior due to particles and bubbles of different sizes were captured at different decomposition levels of pressure fluctuations, which is difficult to know from analysis of the original signal. Results extracted from X-ray fluoroscopy and pressure fluctuation measurements were consistent, suggesting that conventional pressure fluctuation measurements can be effectively used for investigation of the bubbling behavior.     

生物质洁净能源研究中的流化床动力学模型

分别对最小流化床、鼓泡流化床和腾涌流化床及相应的全混模型、鼓泡模型、气泡汇集模型等加以综述,分析其优缺点,并在此基础上提出动力学模拟研究的新思路.根据流化床内在的本质--流化态的不同,将流化床分为最小流化床、鼓泡流化床和腾涌流化床三种.总结了前人针对各种流化床提出的全混模型、鼓泡模型、气泡汇集模型等思想,建议今后可以在以下几个方面进行深入研究: ⑴使得模型更有普适性.⑵由于气泡有效直径尚不能在理论上求得,可以在理想气泡直径变化公式的基础上,加入非线性化学的计算.⑶确定不同情况下的参数,使得工作更有延续性,也使得模型更加具有生命力.⑷从高压的角度去进行模型的计算,并得到相应的试验数据支持.     

多组分气固射流床流动特性 Ⅱ流型的划分

在３００×５０×２６００ｍｍ的二维射流流化床中,使用压力波动的功率谱分析方法,考察了９种单一、双组分混合物物性因素（粒径、密度）、操作因素（射流气速、喷口直径、静床高度、环隙气量）对射流流化床的三种流型：气泡串、射流、喷流相互转变的影响。结果表明,在较低静床高时,随着射流气速的增大,射流床内流型由气泡串、射流过渡到喷流;而静床高较高时,射流气速增大仅由气泡串过渡到射流。环隙气量增大、粒径增大、密度增大,喷流流型出现较困难,最后得出了流型转变图及转变的定量关系式     

Hydrodynamics and mixing in three-phase fluidized bed bioreactors

The effects of solid particles on hydrodynamics and mixing in a three-phase fluidized bed bioreactor were discussed. The gas holdup, bubble size, and liquid-phase axial dispersion coefficient were measured in a 0.25-m id bubble column bioreactors containing low-density particles. The presence of low-density solid particles slightly increased gas holdup. The decrease in average bubble diameter with solid presence was found. For the three-phase system, the liquid-phase axial dispersion coefficients were higher than for the two-phase system. We extended a model for a gas holdup developed for a gas-liquid two-phase bubble column bioreactor to a gas-liquid-solid three-phase fluidized bed bioreactor. Using the present data and available data in the literature, the predictions of the proposed model were examined. The proposed model agreed with a wide range of the experimental data. A theoretical correlation for liquid-phase axial dispersion coefficient was developed using Kolmogoroff's theory of isotropic turbulence. Reasonable agreement was obtained between the predicted and experimental values of axial dispersion coefficient.     

Fluidized Bed Polyethylene Reactor Modeling in Condensed Mode Operation

Summary: Modeling of fluidized bed reactor for polyethylene production in the condensed mode operation is proposed in this paper. A two-phase model including the emulsion and bubble phases with the constant bubble size is employed to describe hydrodynamic behavior of the reactor. The kinetics of Ziegler-Natta polymerization is also modeled with a two active site model. The phase behavior and solubility of low molecular weight components in polyethylene are estimated with the Sanchez-Lacombe equation of state. The validation of the model is carried out with industrial data for an ethylene and 1-butene copolymerization with the isopentane as a condensable component. The simulation results are in good agreement with industrial data. The model is also used to study quantitatively the effect of the inlet stream temperature to the reactor and isopentane concentration in the reactor on the production rate. For instance, in a typical process, when the inlet stream temperature changes 10 °C, the production rate will alter about 40%. Furthermore, the change of the isopentane concentration around 1 mole percentage leads to a variation of production rate about 14%.     

Drying of granules in vibrating suspended bed: Engineering simulation

Engineering algorithm for simulation and designing of a continuous convective drying apparatus serving for drying heat-stable and heat-labile granules in a vibratory fluidized bed (vibrating, suspended bed) was suggested. The algorithm was based on a joint use of mass and heat balance equations, empirical dependences, and comparison of technological parameters with parameters got by the mathematical simulation of dynamics in the vibratory fluidized bed of variable weight. For example, we suggested a calculation algorithm of technological parameters of drying the heat-stable zeolite granules in the vibrating suspended bed. The results for a unit cost of heat and moisture evaporation standards in 3-stage drying were compared with the same for pneumatic drying apparatus, with devices of the fluidized and vibratory fluidized beds, and with sublimation dryers known in industry.     

Numerical simulation of the hydrodynamics of an inverse liquid–solid fluidized bed using combined Lattice Boltzmann and smoothed profile methods

Knowledge of an inverse fluidized-bed fluid hydrodynamics is advantageous in optimal adjustment and designing high-efficiency beds. In the present study, a combination of a single relaxation time collision operator lattice Boltzmann method (LBM) and the smoothed profile method (SPM) is employed to simulate the hydrodynamics of an inverse liquid–solid fluidized bed comprising circular monodisperse and polydisperse particles in a rectangular channel. A numerical instance of inverse fluidization involving 231 particles is illustrated to show the capability of the combined methods. Moreover, comparison of the numerical results is performed with the Ergun equation and the Richardson–Zaki correlation. The comparison demonstrates that the present model can simulate the fluid flow behavior in an inverse fluidized bed. Several different models were also presented to investigate the effect of different fluid properties and size of particles in the bed. Simulations indicate that the more the superficial liquid velocity, the higher the porosity of the bed. The present simulations show that porosity of the bed increases by increasing the particles size, and also the vertical velocity of the bed decreases with an increase in liquid viscosity. Finally, polydisperse particle systems are also simulated. The results show that porosity in an inverse fluidized bed comprising polydisperse particles is more than that of a monodisperse particle bed.     

Temperature variations and amyloglucosidase levels at different bed depths in a solid state fermentation system

Studies on moist wheat bran medium, inoculated with Aspergillus niger CFTRI 1105, indicate steep gradients in the temperature and enzyme levels at different depths in deep bed rectangular fermenters with different loads. An increase of about 2.5 °C over a bed depth of 40 mm in a fermenter with a load of 49.7 kg m⁻² was due to metabolic heat generation in the initial fermentation period. This was found to result in a doubled fermentation time to attain enzyme levels which were comparable, although still lower by 4.6%, with those in a fermenter with a load of 17.8 kg m⁻². The temperature variations were about 10–18 °C for a bed depth of 80 mm and the highest enzyme levels were lower by 23.4%, even after 48 h, with a load of 49.7 kg m⁻² compared with those for a load of 17.8 kg m⁻² . The metabolic heat and enzyme biosynthesis functions were found to be significantly affected by an increase in bed depth. The maximum temperature variations recorded in the fermenter with a load of 126.1 kg m⁻² were 19.5 °C at 12 h and 21.2 °C at 60 h for 80 and 160 mm bed depths respectively. Consequently, the maximum enzyme levels were lower by 81%–86% and required a 2.5-fold increase in fermentation time compared with a fermenter with a load of 17.8 kg m⁻².The results indicate that the temperature gradients play a key role in the biosynthesis of the enzyme in a solid state fermentation system involving deep beds.     

压力下流化床流动特性的实验研究

利用摄像技术在φ60mm×800mm压力为0.1MPa～1.5MPa的冷模加压流化床实验装置上, 对两种不同粒径颗粒的最小流化速度和床层膨胀高度进行了研究。研究结果表明,大粒径聚苯乙烯颗粒的Umf与p-0.3成比例,小粒径石英砂的Umf与p-0.21成比例,并根据实验值拟合出压力下最小流化速度公式为: Umf=μdp ρg｛［(34.15)2+0.05916×dp3 ρg( ρs- ρg)gμ2］12-34.15｝ 床层膨胀高度随气速的增大而不断增高,在相同U Umf下床层膨胀高度随压力的增大而增高,在大于0.7MPa时,压力对膨胀高度的影响减弱。对于聚苯乙烯颗粒,相同的H/Hmf下,U Umf随压力的增大而逐渐减小,当H/Hmf＝1.4～1.6时,U Umf与p-0.52～p-0.58成比例。     

Glucoamylase immobilization on a magnetic microparticle for the continuous hydrolysis of maltodextrin in a fluidized bed reactor

Glucoamylase (GA) has been successfully immobilized through its carbohydrates previously oxidized with periodate onto a low-cost magnetic microparticle made of polyethyleneimine-coated magnetite crosslinked with glutaraldehyde (M-GAD) and derivatized with adipic dihydrazide (ADH). A stabilization posttreatment consisting of cross-linking its carbohydrates with ADH, increased the remaining activity from 54 to 71%, calculated on theV _m values and measured at 50°C and pH 4.5 with maltodextrin (DE 11-14) as substrate. This treatment also improved the enzyme stability and lowered the deactivation rate constantk _d to a third of its value. A 30% maltodextrin solution has been continuously hydrolyzed at 50°C and pH 4.5 in a recycled, fluidized bed reactor (FBR) containing GA immobilized on these magnetic microparticles. They easily settled in this highly viscous medium because of their high density (5 g/mL), and washout of ultrafines was prevented by surrounding the top of the bed with an electromagnet. The small particle size (20 μm) allowed a high enzyme loading in the reactor and also a high bed voidage, which is recommended to avoid extensive pressure drop and consequent channeling problems. The kinetic of hydrolysis fitted with the plug-flow model; this is explained by the insignificant backmixing effects observed. After 2 wk of hydrolysis under process conditions leading to a conversion of 70%, which corresponds to a high-conversion syrup, the immobilized GA only lost 4% of its initial activity.     

Wettability of acrylate copolymer surfaces after ageing in water

Contact angle measurements (captive bubble and sessile drop techniques) were used to determine the surface energy of several acrylic based polymers at the early stage of immersion (t₀) in pure and salt water or after several days (t_x). The sessile drop technique using various liquid probes allows the calculation of the dispersive, acid and basic components of the surface energy. Significant differences of wettability are observed between the polymers at t₀ which tend to remain after immersion along with a general increase of the surface hydrophilicity. The same trend is observed by the “in-situ” captive bubble technique. The surfaces become more hydrophilic with a final contact angle, θ, ranging from 110 to 150 ± 3° in pure water and 130 to 150 ± 4° in 0,51 M salt water. The modifications of surface energy between t₀ and t_x are not only dependent on water diffusion. One assumption is that the degree of swelling of the immersed surface layer along with the particular dynamics resulting from a surface gel-like structure are significant factors in the measured surface thermodynamics.     

RDF流化床燃烧过程NOx生成比较研究

随着中国经济的迅速发展和城市化进程的加快,由此带来的负作用凸现：各种资源的消耗不断增加;同时这种传统的高消耗、低产出、高污染的经济发展带来的环境污染也非常严重。据不完全统计,2003年中国城市生活垃圾总量为1．9亿t,并以每年8％～10％的速度递增,对垃圾进行简单填埋、焚烧不但污染土壤和地下水,     

Structuring bubbles and foams in gelatine solutions within a circular microchannel device

A flow-focusing device with circular cross-section to produce monodispersed air bubbles and foams in several gelatine solutions is presented. Four flow regimes were studied by varying the gas pressure: dripping, bi-disperse bubbly, bubbly and foam flows. Bubble formation at the flow-focusing exit is discussed in detail and compared with that in rectangular microchannels. The bubble volume was shown to depend on the viscosity of the gelatine solution but not on the surface tension. For the bubbly flow, the frequency of bubble formation in this geometry was similar to that found in rectangular microchannels. For the foam flow the frequency was independent of the pressure. Study in the outlet microchannel for the bubbly and foam flows showed that the gas flow followed a power law with the applied pressure. Finally, the viscous resistance was measured and a pressure drop law was determined for each regime.     

Axial dispersion in a liquid fluidized bed of particles akin to immobilized enzymes

The axial dispersion of a liquid fluidized bed of controlled pore silica (CPS) particles has been determined by the pulse tracer method. The CPS used was the same as for enzyme immobilization, having an average diameter of 0.436 mm and mean pore size of 37.5 nm. The fluidization liquid is α-amylase liquefied manioc starch, 30% w/v, 45°C pH=4.5. Nominal bed porosities tested were 0.7 and 0.8. The results show that the axial dispersion coefficient increases with greater superficial liquid velocities. Various available correlations tested disagree with each other to a large extent and are unable to represent collected experimental data.