乙烯裂解炉内传递和反应过程综合数值模拟Ⅱ.反应管内传递和反应过程的数值模拟

采用乙烯裂解炉传递反应过程综合数学模型中的反应管数学模型，对工业裂解炉反应管进行了系统的数值模拟，得到了反应管内流场、温度场和浓度场的详细信息，揭示了反应管内流动、传热、传质和裂解反应的基本特点。模拟结果表明，沿反应管轴向油气吸热升温，裂解反应加剧，产物产率逐渐发生变化；沿反应管径向存在明显的流体流速和温度的变化，而产物产率的变化不如流体流速和温度的变化明显。通过比较湍流粘度和分子粘度的大小，认为29．975～30mm的径向区域为层流层，层流层的存在使得临近管壁的区域内流体流速和温度变化显著。     

钛铁矿选择氯化法制取人造金红石的热力学与动力学

研究了钛铁矿选择氯化制取人造金红石反应的Fe-Ti-C-O2-Cl2系平衡图，计算了氧与某些氯化物相互作用的自由能变化，采用“通氧一步选择氯化法”，解决了选择氯化“自热”反应持续进行的技术关键，对反应参数进行了实验室，半工业和工业化生产试验研究，研究证明，选择氯化过程的动力学模型是“固体颗粒粒度保持不变的缩核反应模型”，动力学区的活性能为34．33kJ/mol；扩散区的活化能为0．80kJ/mol，研究开发的无筛板沸腾氯化炉可以长期稳定地连续运转，生产出的人造金红石品位为92．10％，经摇床和磁选，品位达到95％，床层单位炉产能达12．4t/(m2.d)，该工艺和设备已成功地应用于工业生产。     

Adaptation of the microscopic properties of redox catalysts to the type of gas-solid reactor

Catalysts of selective oxidation usually work in a simultaneous redox mode in reactant/air cofed reactors. The solid must provide selective lattice oxygen according to a kinetic mechanism depending on operating conditions that differ from one reactor to another. Better catalytic performance can be obtained in a recirculating solids reactor because it allows separate optimization of the reduction and oxidation steps. Among the microscopic properties of the catalyst, the crystal morphology is to be taken into account because it influences its reactivity on stream. These considerations lead to a new approach of the catalyst-reaction-reactor trio.     

液态金属钠高温沸腾实验回路应力分析与强度计算

本文主要完成了液态金属钠高温沸腾实验回路的应力分析与计算，确定了回路高温区连接管系的布置型式和支吊架系统，是该回路总体设计的重要组成部分。     

双焊缝方矩形钢管生产工艺介绍

介绍了双焊缝方矩形钢管生产技术的特点及冷弯等边槽钢孔型设计参数.通过双焊缝方矩形钢管用冷弯等边槽钢的孔型设计、生产,实现了大截面双焊缝方、矩形钢管的生产,满足了客户的需求.     

膜催化氧化正丁烷制顺酐

以多孔玻璃管为基体，制备４种用于正丁烷氧化制顺酐的膜反应器。在一定的操作条件下，考察了固定床反应器与这４种膜反应器在正丁烷氧化制顺酐中的反应性能并加以比较，发现ＹＳＺ膜反应器可获得高于固定床反应器的选择性和收率。     

新型废水厌氧处理工艺——内循环厌氧反应器

介绍内循环(IC)厌氧反应器的发展、基本结构、运行机理。分析该反应器的工艺过程,指出该工艺具有处理效率高、抗冲击能力强等优点。针对IC反应器存在的缺陷,人们对该反应器进行技术改进:通过提高它的内循环的气量进行处理低浓度有机废水;增加外循环装置缩短IC反应器的启动周期。     

灰熔聚粉煤气化炉存在的问题及改进

对灰熔聚粉煤气化炉运行中存在的问题进行了分析、讨论，并提出了解决方案和建议。     

Optimal Conditions for Preparing Ultra-Fine CeO2 Powders in A Submerged Circulative Impinging Stream Reactor

Cerium carbonate powders were produced in a submerged circulation impinging stream reactor (SCISR) from Ce(NO3)3·6H2O. NH4HCO3 was used as a precipitant in the reaction. Cerium carbonate powders were roasted to produce ultra-fine cerium dioxide (CeO2) powders. The optimal conditions of such production process were obtained by orthogonal and one-factor experiments. The results showed that ultra-fine and narrowly distributed cerium carbonate powders were produced under the optimal flowing conditions. The concentrations of Ce(NO3)3 and NH4HCO3 solutions were 0.25 and 0.3 mol·L-1, respectively. The concentration of PEG4000 added in these two solutions was 4 g·L-1. The stirring ratio, reaction temperature, feeding time, solution pH, reaction time and digestion time were 900 r·min-1, 80 ℃, 20 min, 5～6, 5 min and 1 h, respectively. The final product, CeO2 powders, was obtained by roasting the produced cerium carbonate in air for 3 h at 500 ℃. The finally produced CeO2 powders were torispherical particles with a narrow size distribution of 0.8～2.5 μm. The crystal structure of CeO2 powders belonged to cubic crystal system and its space point group was O5H-FM3M. Under optimal conditions, powders produced by SCISR were finer and more narrowly distributed than that by Stirred Tank Reactor (STR).     

Kinetics of phenol oxidation in a trickle bed reactor over active carbon catalyst

The wet air oxidation of phenol over a commercial active carbon catalyst was studied in a trickle bed reactor (TBR) in the temperature and oxygen partial pressure ranges of 120–160 °C and 0.1–0.2 MPa, respectively. The performance of the active carbon was compared in terms of phenol and COD destruction. The weight change of active carbon due to reaction was also measured. Finally, oxic phenol adsorption isotherms were assessed in batch conditions at 25, 125 and 160 °C. In order to use the conversion data obtained from the TBR for a kinetic study, special care was taken to check the kinetic control in the TBR experiments. Several kinetic models including power law or Langmuir–Hinshelwood expressions were considered to describe the catalytic oxidation of phenol over active carbon. The simple power law model with first order dependence on both phenol and oxygen concentration predicted satisfactorily the experimental data not only over the entire range of operating conditions studied, but also outside its validity range. Copyright © 2005 Society of Chemical Industry