分形理论分析填料塔内件的发展

综述了乱堆填料、规整填料和气液分布装置的发展概况,应用分形理论分析填料的几何结构对气液传质的影响,并提出了今后填料塔研究的方向。     

塔器分离技术最新进展

介绍了近几年来大型填料塔用新型规整填料、塔内件 (气液分布器、进气初始分布器 )的开发设计和应用 ;国内外新开发的几种新型塔板的技术及工业应用。预计未来塔器分离技术将向行业化、复合化、节能化、大型化方向发展。     

填料塔开发应用新进展

综述了国内外填料塔的发展现状,包括近几年开发成功的新型散堆填料,规整填料及填料塔塔内件结构特点,同时介绍新型规整填料、塔内件的一些工业应用成功实例,展望了填料塔今后发展方向。     

气液两相逆流状态下金属板波纹填料塔内液体流动分布

<正>填料塔内液体流动分布状况直接关系到塔内气液两相的有效接触,影响塔的操作性能.由于液体分布不良,造成填料塔内局部区域的气液比与全塔宏观的气液比有显著差别,从而大大降低塔的总传质效率.因此,填料塔内的液体分布     

新型塔内件技术——金属格栅填料开发及其在造气洗涤塔的应用

填料塔作为一种传统的气、液传质设备，近年来有很：赶发展。由于填料结构的不断改进，在很多生产过程中填料塔已代替了传统的板式塔。填料主要有散堆填料和规整填料2类。散堆填料有拉西环、鲍尔环、阶梯环、矩鞍环、海尔环、泰勒花环等，其主要优点在于安装方便，具有通用性；但是通量较小，流体分布性能较差，阻力较大，如果有沉淀物生成，易造成填料塔堵塞等缺点。随着化学工业的发展，对塔没备不断提出新要求：有的要求分离热敏性物系，有的要求通过技术改造提高生产能力和产品质量，有的要求降低回流比，减少系统阻力以求节能；     

我国塔器技术的进展

(接上期)2　填料塔填料塔与板式塔相比,具有压降低、效率高(指单位高度的分离效果,下同)、持液量小的优点。进入80年代以来,我国的填料塔技术得到了迅速的发展,在工业生产上得到大量的应用。填料塔主要包括塔填料和塔内的液体分布器。21　塔填料塔填料简称填料,归纳起来主要有4种类型:环型、鞍型、球型、规整填料,如图18所示。图18　各种类型的填料举例我国对鲍尔环、阶梯环、矩鞍型、矩鞍环、波纹填料等进行了大量的研究[53～57],并在此基础上开发出了网孔波纹板、压延孔波纹板、共轭环、改进矩鞍环、扁环等[68～71]新型填料,获得了成功的…     

一种新型单体填料性能的研究

一种新型单体填料性能的研究陈伟琳，肖如亭（天津理工学院天津３００１９１）１．前言填料塔是应用在化工生产中的塔型之一，它已成为主要的气、液传质的设备之一。而填料塔的发展和改进，主要反映在填料的发展和改进上。填料是填料塔的核心组成部分，为塔内气、液两相接...     

新型填料在恩德粉煤气化洗涤除尘系统中的应用

介绍了大型填料塔用新型规整填料、塔内件(气液分布器、进气初始分布器)在恩德炉净化系统中的应用情况.改进后,煤气中粉尘含量降至65～75 mg/m3(标态),基本可满足后序工段要求.     

新型塔内件技术在脱硫塔和造气洗涤塔的开发与应用

1 概述。填料塔作为一种传统的气、液传质设备，近年来有很大发展。由于填料结构的不断改进，在很多生产过程中已代替了传统的板式塔。填料主要有两大类：散堆填料和规整填料。散堆填料有拉西环、鲍尔环、阶梯环、矩鞍环、海尔环、泰勒花环等。散堆填料主要优点在于安装方便，具有通用性。但是通量较小，流体分布性能较差，阻力较大，如果有沉淀物生成，易造成填料塔堵塞等缺点。随着化学工业的发展，对塔设备不断提出新要求：有的要求分离热敏性物系，有的要求通过技术改造提高生产能力和产品质量，有的要求降低回流比，减少系统阻力以求节能；有的因环保要求，在三废处理时必须进一步提高效率以达到国家有关标准等等。随着塔器的大型化，散堆填料难以满足这种要求。因而结构与排列整齐、有效传质面积大、阻力小的规整填料应运而生，很到广泛应用。     

填料塔液泛气速,压力降计算方法的讨论

使用部分Ｄｇ５０瓷质填料在水－空气实验系统中测得的填料塔液泛气速和压力降,根据所确定的液泛气速,压力降的计算方法,推算出９３％Ｈ２ＳＯ４－空气９３％Ｈ２ＳＯ４－ＳＯ２烟气,９８％Ｈ２ＳＯ４－ＳＯ３烟气等操作系统中,填料塔采用不同填料的液泛气和压力降。     

Liquid Holdup in a Pilot‐Scale Turbulent Contact Absorber – An Experimental and Comparative Study

Liquid holdup in a turbulent contact absorber was determined experimentally. Experiments were performed in a 44.7 cm diameter Perspex column. Hollow spherical high‐density polyethylene balls were used as packing. The effect of liquid and gas velocities, static bed height, diameter and density of packing on liquid holdup was investigated for the range of gas velocities greater than minimum fluidization velocities. Also, the effect of gas and liquid distributors on liquid holdup was studied. Correlations for liquid holdup were developed and compared with those in the literature. It was observed that liquid holdup increased with the increase in liquid velocity, packing density, and the decrease in static bed height. Liquid holdup also increased with gas velocity when the gas distributor section was included, while no effect was observed for the bed. Lack of information on the contribution of liquid and gas distributors seems to be the logical explanation for the wide variation in data reported in the literature.     

Gas-liquid dispersions in structured packing with high-viscosity liquids

Gas holdup in bubble columns containing structured packing was determined for varying liquid phase viscosity and different construction materials of the packing. Three columns, containing packing made from smooth nickel plate, perforated nickel plate and plastic sheets, respectively, were tested. The gas holdup in a column with no internals was also measured for comparison purposes. The effect of viscosity on gas holdup was studied by using water, aqueous glycerol and aqueous CMC solutions as the liquid phase; some of the solutions showed non-Newtonian behavior.The experimental results of gas void fraction were correlated in terms of superficial gas velocity and liquid viscosity through a simple homographic expression. The geometric characteristics of the structured packings were found to influence gas holdup, thus yielding slightly different equations for each structured packing. This effect is discussed in detail. Nevertheless, for engineering purposes a single equation representing all the data is also proposed, which permits the prediction of gas holdup in structured packing with sufficient accuracy.     

气液两相逆流状态下金属板波纹填料塔内液体流动分布

填料塔内液体流动分布状况直接关系到塔内气液两相的有效接触,影响塔的操作性能.由于液体分布不良,造成填料塔内局部区域的气液比与全塔宏观的气液比有显著差别,从而大大降低塔的总传质效率.因此,填料塔内的液体分布     

Mass Transfer In Trickle‐Bed Reactors With Structured Packing

An experimental investigation was carried out to examine the fluid dynamic and mass transfer behavior of structured packing, with the liquid and gas phase flowing co‐currently downwards in the column. Liquid to packing mass transfer coefficients for three positions within the pack were measured by an electrochemical method, varying both the liquid and gas loads as well as the physical properties of the liquid phase. Due to the high void fraction of structured packing, much higher liquid flow rates can be used than in traditional particle trickle‐beds. It was found that in the range studied, the gas superficial velocity has no effect on the mass transfer rate and thus, a general mass transfer correlation in terms of liquid Reynolds number only, was developed. Wetted areas and the radial distribution of liquid through the packing element were determined by a colorimetric method. Within the range of liquid flow rates investigated, complete wetting is not achieved, even with the low viscosity solutions. The measured ratios of hydraulic to geometric area, agree reasonably well with values predicted by existing relationships.     

Hydrodynamics and mass transfer of gas–liquid flow in micropacked bed reactors with metal foam packing

Hydrodynamics and mass transfer of gas–liquid flow such as pressure drop, liquid holdup, and gas–liquid mass-transfer coefficient in micropacked bed reactors (μPBRs) with metal foam packing are investigated with an automated platform. Parametric studies are conducted varying gas and liquid superficial velocities, pore diameters of foam packing, and liquid physical properties. Experimental results show that μPBRs with foam packing have comparative mass transfer rate and 10 times lower pressure drop compared to the microparticles. The values of mass-transfer coefficient for three types of foam packing in μPBRs are 1–2 orders of magnitude larger than those in large-scale trickle bed reactors with foam packing. Furthermore, empirical correlations of pressure drop, liquid holdup, and gas–liquid mass-transfer coefficient in μPBRs with foam packing are proposed and the predicted values are found to be in good agreement with the experimental values.     

Hydrodynamic characteristics in an inverse internal-loop airlift-driven fibrous-bed bioreactor

An inverse internal loop airlift-driven fibrous bed bioreactor (ALFBB) was designed by combining the advantages of an internal loop airlift bioreactor and packed bed bioreactor into one column. This bioreactor, with a high degree of design flexibility, is expected to handle genetically engineered cells as well as fragile cells, which are shear-sensitive. The hydrodynamic characteristics of the combined system have been investigated. Woven cotton was set in the downcomer of the I-IL-ALB to represent the fibrous bed packed bed and the outcome results were compared with those of the polyurethane foam (PUF) packed system and the unpacked I-IL-ALB system. The effects of the packing nature, packing height, packing top and bottom clearances, gaps between adjacent fiber surfaces, and superficial gas velocities were investigated. The hydrodynamic output variables included the gas holdup and liquid circulation velocity. Gas holdup for all packed systems continuously increased with increases in packing height, packing top clearance and superficial gas velocity. It was found highest in the downcomer of the cotton packed system than in the PUF counter part due to the roughness and hydrophilicity of the woven cotton fibrous material. Increased amounts of packing in the I-IL-ALB, whether in the form of cotton or PUF decreased the liquid circulation velocity in the bioreactor because of the increased frictional resistance and tortuosity. The reduction in liquid circulation velocity was significant for large packing with small gaps between fiber surfaces and increased bottom clearances of the cotton packed system. Empirical models based on packing properties are presented which accurately predict the gas holdup, whereas energy based model was proposed to predict liquid circulation velocities. The optimum hydrodynamic conditions were observed with cotton packing.     

陶瓷球填料生物滴滤塔降解甲苯废气

The Purification experiments of waste gas containing low concentration toluene were made in trickling biofilter with ceramic spheres. The effects of liquid flow rate,gas flow rate,pH of circulation liquid, and toluene concentration in inlet gas on the purification efficiency of trickling biofilter were investigated. The pressure drop of the trickling biofilter was also measured during experiments.Increasing liquid flow rate and gas flow rate resulted in the decrease of purification efficiency of trickling biofilter. The highest purification efficiency of trickling biofilter was found at the circulation liquid pH of 7. The porosity of the packing material at the inlet of gas was higher than that at the outlet of gas in biofilter after continuous operation in 50 days. The decrease in the porosity of packing material caused a great increase in the pressure drop of the biofilter.     

Liquid Flow on Structured Packing: CFD Simulation and Experimental Study

A CFD model of the two‐phase countercurrent flow in the geometry of the plate‐type structured packing Mellapak 250.Y was built, tested and verified. The model was applied to determine the effect of liquid and gas flow rates and physicochemical properties of the flowing liquids on the interfacial area formed on structured packing. The CFD model allowed us to determine the minimum liquid flow rate at which an unbroken liquid film was observed on the packing surface. The simulations confirmed that with an increase of the wetting rate the surface of the packing covered with a liquid film increased until the surface was totally covered up, while further slight changes of an interfacial area were the result of wave formation. The effect of gas load (F factor) on the film surface was in the range of a calculation error. Results of the CFD simulation allow us to predict the stages of film formation during liquid flow, to follow local velocity oscillations, film thickness and velocity profiles of phases.