余热锅炉技术改造--蒸汽压力的自控调节

1 前言 我公司联合车间拥有一条400吨级的浮法玻璃生产线,配备了三台F40/500-5/13型的余热锅炉,其作用是在保证玻璃熔窑窑压正常的前提条件下,利用余热生产蒸汽,以满足玻璃生产所需蒸汽的需要.     

凤凰出版传媒集团重组耀华玻璃获成功

金晶科技公告，拟对本部500T／D浮法玻璃生产线的部分设施和工艺进行技术改造，以建成525T／D太阳能温室玻璃生产线。该线于7月4日停产，预计期限四个月。本次技改将利用现有主线厂房及设备加以改造，增加关键设备，改造和检修原料车间、公用工程及联合车间动力系统，以满足525吨／天熔窑熔化的生产能力。     

富氧燃烧技术在浮法玻璃熔窑中的应用

文章介绍了利用浮法玻璃生产线保护气车间提供的富氧空气,通过一系列方法和控制手段,经输送管道、阀门和利用罗茨风机将加压后的富氧空气引入玻璃熔窑两侧的蓄热室进行助燃,本系统不会时气保车间有任何影响。也不会影响到玻璃生产线的正常生产。     

玻璃纤维池窑拉丝联合厂房结构设计要点分析

联合厂房作为玻纤生产线中核心建筑物,结构设计通常分为熔制与拉丝工段两部分进行。但由于结构布置受到工艺条件的要求,其结构布置及性能等方面具有一些特殊性。通过对现行联合厂房熔制与拉丝工段结构体系进行分析,提出了结构设计中涉及的要点,针对设计要点提出了一些具体措施,为工业厂房中类似车间的结构设计提供了参考。     

玻纤厂配料车间的结构设计要点分析

介绍了配料车间作为玻纤生产线中重要的建筑物,由于结构受到工艺条件的要求,其结构布置及性能等方面的特殊性。通过对现行配料车间混凝土框支剪力墙结构体系进行分析,提出了结构设计中涉及的要点,针对设计要点提出了一些具体措施。同时提出了配料车间结构设计合理化建议,为工业厂房中类似车间的结构设计提供参考。     

浅谈彩釉玻璃的生产

针对彩釉玻璃生产的车间环境要求,对网版选择、印刷中相关工艺参数的设置及烘干烧结等方面进行了阐述,并根据实际工作经验给出了建议,以更好地控制彩釉玻璃的质量。     

富氧燃烧技术在浮法玻璃熔窑中的使用

利用浮法玻璃生产线保护气车间提供的富氧空气,通过一系列方法和控制手段,经输送管道、阀门和利用罗茨风机将加压后的富氧空气引入玻璃熔窑蓄热室两侧,沿小炉中心线下引支管,支管上安置流量控制阀门,后由富氧喷嘴引入蓄热室清灰门上端,,喷口与小炉中心线成一定角度,富氧气体以一定的角度和足够的压力与助燃风混合预热后,喷入窑内进行助燃。将富氧空气喷嘴安装在3#～4#蓄热室下部,节能效果较好。本系统不会对气保车间有任何影响,也不会影响到玻璃生产线的正常生产。     

PLC在玻璃工厂自动配料系统中的应用

原料配料是玻璃工艺过程中的第一道工序,也是保证玻璃质量的必要条件。只有对各种原料进行精确的计量才能确保准确的玻璃组分,只有对配料全过程实行准确的控制才能保证配料的工艺质量。我厂配料车间自动控制生产线是由贵州省化工设计院设计,采用日本ＯＭＲＯＮ公司生产...     

玻璃厂结构设计的几点探讨

针对玻璃厂的特点,说明了联合车间楼面活荷载的折减,探讨了联合车间的结构形式以及发展方向,对锡槽柱底的结构计算进行了科学的分析比较,可以作为成熟经验运用在玻璃厂的结构设计中.     

浮法玻璃在线无触厚度测量仪

本文介绍一种在线无触玻璃厚度测量仪,它能满足玻璃生产线的所有要求,也可用于其他生产工艺.该设备是Beta Instrament Europe和比利时G1averbel SA的工程部联合研制的.     

填料塔栅板设计

介绍了填料塔栅板的结构设计和强度计算方法,分桁了不同填料对栅板强度的影响.     

Modeling bubble column reactor with the volume of fluid approach: Comparison of surface tension models

This work aims at comparing surface tension models in VOF (Volume of Fluid) modeling and investigating the effects of gas distributor and gas velocity. Hydrodynamics of a continuous chain of bubbles inside a bubble column reactor was simulated. The grid independence study was first conducted and a grid size of 1.0 mm was adopted in order to minimize the computing time without compromising the accuracy of the results. The predictions were validated by comparing the experimental studies reported in the literature. It was found that all surface tension models can describe the bubble rise and bubble plume in a column with slight deviations.     

用于分离三氯氢硅合成过程中主副产品的隔壁塔模拟

以三氯氢硅合成过程中得到的主副产品混合物二氯二氢硅-三氯氢硅-四氯化硅为分离物系,提出采用隔壁塔代替常规精馏序列分离的新工艺.利用Aspen Plus软件对隔壁塔进行模拟,考察回流比、隔板位置、进料位置、侧线采出位置、液相分配比以及气相分配比对塔顶、侧线以及塔釜产品摩尔分数的影响,得到隔壁塔的最佳工艺参数,并通过模拟比较隔壁塔与常规精馏序列分离此混合物的能耗情况.模拟结果表明:当回流比为6、隔板位置为主塔的第8块板和第24块板、进料位置为预分馏塔的第10块板、侧线采出位置为主塔的第15块板、液相分配比为0.21、气相分配比为0.5时,隔壁塔的分离效果最佳,主产品三氯氢硅的摩尔分数为99.999%;相比于常规精馏序列,隔壁塔再沸器节能29.09%以上,冷凝器节能29.48%以上.     

网格和数值格式对TBPBM-CFD模型模拟鼓泡塔的影响

基于气泡动力学属性的现有认识,把气泡分成大、小气泡,首次建立了完整的双气泡相-群平衡模型(TBPBM)以预测气泡尺寸.通过编写用户自定义程序实现了TBPBM模型、Luo破碎模型以及Prince 聚并模型,并耦合TBPBM与CFD双流体模型对直径440 mm鼓泡塔进行数值模拟,详细考察了网格与数值格式对TBPBM-CFD模型模拟结果的影响.结果表明,网格与数值格式对各物理变量的模拟结果影响非常大,特别是网格和体积分数方程对流项离散格式的影响最为显著.随着计算精度的提高,湍流耗散率和整体气含率分布梯度增大,气泡平均直径减少,大气泡所占气相比率降低,液相速度及气含率径向分布与实验值更趋吻合.     

Effect of Feed Location on the Performance of Single-Stage Membrane Permeators

Abstract

The effect of feed location on the performance of single-stage membrane permeators was determined based on the minimum unit compressor load (recycle ratio). Since certain feed locations correspond to several well-known permeator configurations (e.g., simple recycle permeator, continous membrane column), it is possible to characterize the relative performance of these configurations for separating binary gas mixtures. For separations involving oxygen, nitrogen, and carbon dioxide, it was found that the location of feed introduction was related to the apparent difficulty of separation. For binary seprations of low to moderate difficulty, the optimum feed location was at a dimensionless axial distance of 0.6 to 0.75 from the top of the column. This feed location corresponded to the continuous membrane column configuration. For difficult separations, the optimum feed location was at the top of the column which corresponded to the simple recycle permeator. Based on this study, the simple recycle permeator configuration outperforms the continuous membrane column for the most difficult separations such as in the separation of oxygen from air. However, the continuous membrane column configuration can be used effectively for less difficult gas separations which cannot be accomplished by a membrane permeator without recycle, but do not require high recycle ratios to achieve the desired separation.     

Oxygen mass transfer in bubble columns

The mass transfer of oxygen between air and water has been studied in a bubble column over wide ranges of liquid and gas velocity. An oxygen probe was used to map the steady-state liquid phase concentration of oxygen throughout the column.At any given point in the column, the oxygen concentration increased with gas velocity. Minima were observed in plots of concentration against liquid velocity.Two distinct absorption regions were observed. Close to the distributor the concentration decreased rapidly with height and volumetric mass transfer coefficients ranged from about 0.2 to 2.1 s^?1. These high values were attributed to enhanced mass transfer due to turbulence induced by the liquid and gas jets in the grid region. In the bulk of the column, axial concentration gradients were much smaller and the mass transfer coefficients were up to two orders of magnitude lower than in the grid region.     

Pressure drop through multiorifice gas distributors in fluidized bed columns

Good grid design is essential for the satisfactory performance of large gas fluidized beds and requires the accurate prediction of the grid pressure drop. Experiments conducted with various perforated plate distributors in a 0.6 m I.D. fluidized bed column showed that the presence of fluidized solids could increase the grid pressure drop by more than 100%. This increase was around 25% for a grid pressure drop to bed pressure drop ratio of 0.4. It was greatly affected by the bed height. An investigation of various possible causes for this increase demonstrated that it is primarily caused by the backflow of fluidized solids into the grid holes under the influence of waves at the bed surface.     

Grid leakage (weeping and dumping) in a pilot plant size gas fluidized bed

Substantial grid leakage in large industrial fluidized beds is highly undesirable because it can lead, among other things, to grid erosion or plugging. Experiments have been carried out to study grid leakage using a cracking catalyst (arithmetic mean diameter 65 μm) in a 0.6 m diameter column. The flow pattern under the grid was charted with a hot wire anemometer. Micro-isokinetic probes were developed to study the particle flux returning from the windbox towards the grid. Particles were sucked in isokinetically, recovered in a filter, weighed and analyzed for particle size in a Coulter counter. Upward particle fluxes at the grid were determined by extrapolation of the flux at various distances below the grid. Grid leakage was studied for grids of various geometries which had holes of 1.27 cm diameter. Various measurement methods, a model for re-entrainment and correlations are given.     

Optimization of coproduction of ethyl acetate and n-butyl acetate by reactive distillation☆

Based on a previous investigation, a simulation model was used for optimization of coproduction of ethyl acetate and n-butyl acetate by reactive distil ation. An experimental setup was established to verify the simulated results. The effects of various operating variables, such as ethanol feed location, acetic acid feed location, feed stage of reaction mixture of acetic acid and n-butanol, reflux ratio of ethyl acetate reactive distillation column, and distil-late to feed ratio of n-butyl acetate column, on the ethanol/n-butanol conversions, ethyl acetate/n-butyl acetate purity, and energy consumption were investigated. The optimal results in the simulation study are as follows:ethanol feed location, 15th stage;acetic acid feed location, eighth stage;feed location of reaction mixture of acetic acid and n-butanol, eighth stage;reflux ratio of ethyl acetate reactive distillation column, 2.0;and distillate to feed ratio of n-butyl acetate, 0.6.     

Measurement and CFD simulation of single-phase flow in solvent extraction pulsed column

A CFD (computational fluid dynamics) model of a solvent extraction pulsed column has been developed and run with a single water phase. The results are compared with experimental measurements taken on a pilot scale column using PIV (particle image velocimetry).The pulsed column investigated had disk-doughnut internals and was operated under pulsing intensities ranging from 10 to 32.5 mm/s. PIV measurements of velocity were used to validate the CFD model and to characterise the pulsing flow of a single phase through the column. The CFD modelling was performed for the same geometry and operating conditions using a 2D computational grid and a low Reynolds Number k-ε turbulence model. An improved velocity prediction was achieved by adding a gap between the doughnut internal and the pulsed column wall. The combined measurements and predictions give insight into the effect of the geometry internals on the flow hydrodynamics in the pulsed column.