氯醇化新工艺

介绍用于环氧氯丙烷或环氧丙烷生产的氯醇化新工艺,并与传统工艺进行了对比。     

氯醇化反应和氯醇化反应器

讨论了氯醇化反应过程及其影响因素,分析了三类氯醇化反应器和原理的特点。     

丙烯氯醇化反应设计

氯醇化反应是氯醇法生产环氧丙烷工艺中的关键一步,它直接影响丙烯、氯气的消耗,进而影响生产成本、产品市场的竞争。1987年委托北京石化工程公司设计环氧丙烷装置时,通过总结化工厂环氧丙烷装置技术,确定了合理的丙烯氯醇化反应器工艺参数。根据该工艺参数设计的鼓泡反应器,从1994年工艺技术指标逐年提高,在2000年已接近日本昭和电工指标。2004年后,装置进行了操作优化,进一步提高了转化率,2012年后,通过设计优化,进一步提高了氯丙醇选择性。     

氯醇化塔的运行管理

着重对环氧丙烷生产中的关键工序——氯醇化工序中氯醇化塔的运行情况进行总结,分别对塔压、塔温、爆炸三角区和安全管理等方面进行阐述,同时提出优化控制指标,以达到降低原料消耗、提高产品产量和质量、保证生产正常运转的目的。     

对我厂环氧丙烷氯醇化工序存在问题的探讨

对引进旭硝子公司的环氧丙烷生产装置中氯醇化工序存在的原料、氯气压力波动等问题进行了分析和讨论，为氯醇化工序稳定运行，实现高产低耗提出了参考意见。同时，还论及了有关设备、管道、仪表及阀门等部件的腐蚀及国产化问题。     

氯醇化法生产环氧丙烷的一种工艺过程

简述了氯醇化法生产环氧丙烷的一种工艺过程及有关节能技术和安全措施。     

氯醇化塔进行部件的国产化

通过对原设备部件如氯气分布器、防爆膜的一些结构特点的考查,并对原件存在的问题进行了改进,研制出了国产替代件,该国产化部件无论从材质选择、工艺合理性和使用效果上看,均达到原设备对部件使用性能的要求,取得了可观的经济效益。     

丙烯氯醇化反应器操作优化

以１０,０００吨／年环氧丙烷装置氯醇化反应工段为对象,采用简化的机理模型,通过两相法实施过程的操作优化,考察了操作变量对反应过程的影响,并比较了不同优化目标对优化效果的影响,通过优化显著地提高过程的运行效益,并提出了进一步提高生产能力和优化效果的途径。     

氯醇化管式反应器的设计计算方法

根据氯醇化反应的特点，利用气液反应的双膜理论，导出了宏观反应速率式，结合管式反应器的流动模型，提出了一个简便、有效的反应器的设计计算方法     

PRESSURE DROP AND MASS TRANSFER COEFFICIENTS IN CONCURRENT SCREEN PLATE BUBBLE COLUMN

Pressure drop and oxygen desorption from water and four other aqueous CMC solutions were determined in a 5 cm diameter multistage bubble column with and without plate reciprocation. The plates were made from stainless steel wire screens of porosities greater than 0.62. The column pressure loss was found to increase with plate agitation, phase velocities and screen mesh number. A modified Reynolds number was proposed to permit a reasonable prediction of the pressure loss, based on the model of Noh and Baird (1984). At a specific power consumption, the present volumetric mass transfer coefficients arc considerably larger than those reported in earlier studies with sieve plates. The coefficients were correlated with specific power input, phase flow velocities and system physical properties.     

等温气液混合器压降研究

实验研究空气-水两相流体通过等径90°T型管混合器进行混合的压降.结果表明,在实验范围内,混合后气液两相混合物的流动流型为环雾流,其压降主要与两股混合物流的动量比有关.根据混合后气液两相混合物的流动流型,模拟计算空气-水系统的压降,计算结果与实验结果较为吻合.利用该计算模型分析气液流量对混合器压降的影响.     

苏尔士静态混合器压降和停留时间的测定

实验测定了直径为２０～５０ｍｍ４种苏尔士静态混合器的压降，获得了摩擦因子的经验关联式，苏尔士静态混合器的压降比空管大１０～３０倍。用脉冲示踪法测定了物料的停留时间分布，发现在苏尔士静态混合器中无明显返混，可作理想柱塞流处理     

南方稀土矿浸出传质的研究

本文从传质的角度，研究了淋侵速度、浸出剂浓度、矿石粘度、原矿稀土品位对南方某稀土矿浸出效果的影响；用色层塔板理论和vanDeemter方程进行分析，找出了然浸速度与浸出效果之间的规律，为高效、低耗、合理地开采南方稀土矿提供了理论依据．     

SOLID-LIQUID MASS TRANSFER STUDY OF THE OZONATION OF PHENANTHRENE

Phenanthrene, a priority, hazardous pollutant, is found in the vapor and paniculate phase in the atmosphere as well as in aquatic ecosystems. Water droplets can form around the particulates and dissolve the phenanthrene. Subsequent oxidation of the phenanthrene by ozone can result in the formation of secondary pollutants. Thus the mass transfer of solid phenanthrene with and without ozonation reactions in water is investigated and a simple mathematical model based on film theory is formulated to predict the changes in bulk ozone concentrations and enhancement factors. Physical mass transfer coefficients for phenanthrene in water measured at room temperature in an agitated vessel increased from 1·174 ×10^-5 to 2·932 × 10^-5 m/s as the agitation speed increased from 65 to 315 RPM. The ozonation of phenanthrene significantly increases the mass transfer rates of phenanthrene into water as indicated by enhancement factors which range from 2 to 7·8. At low agitation speeds, the film model agreed well with the experimental data regarding the rates of disappearance and concentrations of the bulk ozone. However, the calculated and measured concentrations of ozone deviated as much as 55% at high speeds of agitation probably due to turbulent effects. Nevertheless, the model is useful for estimating the enhancement factor; the theoretical and experimental values are in good agreement with the maximum deviation of 25%.     

MASS TRANSFER EFFECTS IN LIQUEFACTION OF COAL BY SRC-II PROCESS PART II STUDY OF BUBBLE COLUMN REACTORS

The effects of hydrogen mass transfer resistance in large-scale SRC-II bubble column reactors (BCR), over large ranges of process variables, are studied. Due to the interactive effects of mass transfer resistance and gas hold up, the hydrogen consumption or liquid yield in a BCR has a maximum with respect to the specific mixing power. Under normal SRC-II process conditions a superficial gas velocity of about 0.01 m/s represents the optimum with respect to the hydrogen consumption or liquid yield. In general, the product quality requirement rather than the rate of hydrogen consumption determines the minimum specific mixing power requirement. Increase in hydrogen partial pressure can be used to reduce the level of mixing power required to maintain the desired product quality. Interrelations between mass transfer and gas hold effects and the variations in hydrogen concentration in slurry over large ranges of process conditions are also illustrated. This work provides some bases for the selection of reactor dimensions and process conditions for an SRC-II bubble column reactor (BCR).     

MASS TRANSFER EFFECTS IN LIQUEFACTION OF COAL BY SRC-II PROCESS PART II STUDY OF BUBBLE COLUMN REACTORS

The effects of hydrogen mass transfer resistance in large-scale SRC-II bubble column reactors (BCR), over large ranges of process variables, are studied. Due to the interactive effects of mass transfer resistance and gas hold up, the hydrogen consumption or liquid yield in a BCR has a maximum with respect to the specific mixing power. Under normal SRC-II process conditions a superficial gas velocity of about 0.01 m/s represents the optimum with respect to the hydrogen consumption or liquid yield. In general, the product quality requirement rather than the rate of hydrogen consumption determines the minimum specific mixing power requirement. Increase in hydrogen partial pressure can be used to reduce the level of mixing power required to maintain the desired product quality. Interrelations between mass transfer and gas hold effects and the variations in hydrogen concentration in slurry over large ranges of process conditions are also illustrated. This work provides some bases for the selection of reactor dimensions and process conditions for an SRC-II bubble column reactor (BCR).     

APPLICATION OF LINEARIZED MODELS OF MULTICOMPONENT MASS TRANSFER FOR CALCULATION OF EVAPORATION-CONDENSATION PROCESS IN TERNARY SYSTEMS

Results of calculations based on a linearized multicomponent mass transfer theory developed by Burghardt and Krupiczka are compared with experimental data of Modine for condensation-evaporation process in ternary systems. These data have been obtained for acetone-benzene-nitrogen and acetone-benzene-helium in a welted wall column. Models I and II, which take into account diffusional interactions of components in a mullicomponent mixture show good agreement with the experiments as well as with other calculation methods (Krishna-Standart and Toor-Stewart-Prober). When multicomponent mass transfer occurs in the presence of inert species, a straightforward Model II is recommended. Model I, which is more universal, requires some iterative calculations with respect to the sum of mass fluxes. According to theoretical considerations the latter model is limited to the case of low total mass flux. The results of calculations for the systems studied were reasonably good though the total mass fluxes were not small. The calculation procedure based on the presented linearized models are convergent to the proper solutions in contrast to the Krishna-Standart Model IV which in some cases can be unstable.