浸没循环撞击流反应器——极具应用潜力的液相和液固相反应装置

理论分析和实验研究结果表明,浸没循环撞击流反应器（ＳＣＩＳＲ）与传统的搅拌槽反应器（ＳＴＲ）相比,虽然在可测量尺度上的混合特性并不占优;但由于撞击区中流体元间剪切速率更高,因而微观混合更强烈。这对于在分子尺度上进行的化学反应具有重要意义。制取“超细”白炭黑研究的结果佐证了ＳＣＩＳＲ强化微观混合的特性。除此以外,ＳＣＩＳＲ在结构方面还具有多项胜过ＳＴＲ的优点,极具开发应用的潜力。     

己内酰胺水解聚合过程数学模型化与优化研究进展

综述了己内酰胺水解聚合反应动力学模型，并系统论述了ＰＡ６工业聚合反应器包括高压间歇釜反应器（ＢＳＴＲ）、活塞流反应器（ＰＦＲ）、连续搅拌釜反应器（ＣＳＴＲ）和ＣＳＴＲ与ＰＦＲ组合反应器模型化与优化研究，对数值计算方法也作了简要评价，同时就ＰＡ６聚合过程有待进一步研究的问题提出了几点建议。     

撞击流反应器内涡特性研究进展

撞击流技术具有良好的混合效果,广泛应用于能源、环保、化工等工程领域。由于撞击流反应器流场内存在大量无序的湍流涡结构,使其具有良好的混合效果。本文基于撞击流的混合原理,详细叙述了撞击流反应器内不同混合尺度下的混合过程以及涡的演变对混合的影响。结合实验和数值模拟等研究结果,阐述了不同类型撞击流反应器和撞击流反应器多相流场涡特性,归纳了撞击流反应器流场涡的特点。论述了撞击流反应器涡的产生和脱落机理。着重对圆柱射流、平板射流和撞击流流场内涡特性的本征正交分解（POD）分析进行总结,利用流场能量的角度揭示涡演化和消散规律。最后,对开发新型撞击流反应器、优化分析方法等研究前景进行展望。     

英语翻译技巧（13）

英语翻译技巧（１３）涂学忠（化工部北京橡胶工业研究设计院１０００３９）２．６ＣＯＮＶＥＲＳＩＯＮＯＦＭＡＳＴＥＲＢＡＴＣＨＥＳＭａｓｔｅｒｂａｔｃｈｅｓＣａｎｂｅｃｏｎｖｅｒｔｅｄｔｏｃｏｍｐｏｔｌｎｄｓｂｙｔｈｅａｄｄｉｔｉｏｎｏｆｃｕｒａｔｌｖｅ...     

撞击流强化混合特性及用于制备超细粉体研究进展

撞击流以其强化微观混合的优异特性在化学反应、结晶、制备超细粉体等方面有广泛应用。本文在撞击流技术强化混合特性的基础上对近年来几种撞击流反应器制备超细粉体研究进行了综述。简述了流体流动、受限空间、喷嘴形式及结构、外部激励等因素对浸没循环撞击流反应器、受限撞击流反应器、T形撞击流反应器、微小型撞击流反应器、撞击流-旋转填料床反应器混合性能的影响。从结晶、微观混合时间等角度分析了撞击流微观混合特性对化学反应及制备超细粉体的影响。并与常规反应器及方法对比,从超细粉体的粒度大小、形貌、表面、能量、分散性、电性能及稳定性等方面进行评估。提出一种双层对置撞击流反应器用于工业上大规模制取超细粉体的中试研究,并展望了撞击流技术用于制备超细粉体的前景。     

化工档案特性及其作用

化工档案特性及其作用ＣＨＡＲＡＣＴＥＲＩＳＴＩＣＳＡＮＤＦＵＮＣＴＩＯＮＯＦＣＨＥＭＩＣＡＬＩＮＤＵＳＴＲＹＡＲＣＨＩＶＥＳ杨丽颖化工档案是人们在科学研究、工业生产和经营管理中形成的是具有一定保存价值的各种形式的原始记录材料。它是集体智慧的结晶，是宝...     

CODcr分析废液中银的回收利用

ＣＯＤｃｒ分析废液中银的回收利用ＲＥＣＯＶＥＲＹＡＮＤＲＥＣＩＲＣＵＬＡＴＩＯＮＯＦＳＩＬＶＥＲＦＲＯＭＷＡＳＴＥＷＡＴＥＲＯＦＣＯＤＣＲＡＮＡＬＹＳＩＳ佟素兰张宏滨１前言化学需氧量（ＣＯＤ）是评价水体中有机物相对含量的一项重要综合性指标,也是废水处...     

反应器操作方式对酶动力学拆分立体选择性的影响

描述了在批式反应器和连续流搅拌反应器（ＣＳＴＲ）中酶动力学拆分对映异构体的不同之处，从宏观反应器平衡角度，推导出了在ＣＳＴＲ反应器中不同于在批式反应器中的一定酶立体选择性（Ｅ）下，底物或产物的对映体过量值与反应的转化率之间关系的定量关系式。并通过商品脂肪酶及芽胞杆菌Ｅ－５３脂肪酶催化的萘普生甲酯的不对称水解反应得到了证实。分别在批式反应器和ＣＳＴＲ反应器中进行萘普生的酶法拆分，在一定转化率下，批式     

CALIXE［4］ARENE AS A TEMPLATE FOR CONTROLLING REGIOCHEMISTRY OF PHOTODIMERIZATION OF 9－SUBSTITUTED AN

ＣＡＬＩＸＥ［４］ＡＲＥＮＥＡＳＡＴＥＭＰＬＡＴＥＦＯＲＣＯＮＴＲＯＬＬＩＮＧＲＥＧＩＯＣＨＥＭＩＳＴＲＹＯＦＰＨＯＴＯＤＩＭＥＲＩＺＡＴＩＯＮＯＦ９－ＳＵＢＳＴＩＴＵＴＥＤＡＮＴＨＲＡＣＥＮＥＬＩＹＩ；ＴＯＮＧＺＨＥＮ－ＨＥ（ＣＨＥＮ－ＨＯＴＵＮＧ...     

搅拌塔式反应器传热特性研究

分析了搅拌塔式反应器（ＳＣＲ）中多级冷却盘管隔板的传热特性,用稳态和非稳态的传热方法进行了实验研究。提出了同时考察拌雷诺数和轴向液流雷诺数影响的ＳＣＲ中多级冷却盘管隔板表面传热膜系数的关联式。研究结果表明,对于ＳＣＲ中冷却盘管隔板表面的传热膜系数,轴向液轩诺系数的影响与搅拌雷诺数的影响相比具有同等的重要性。     

Characterization of micro-mixing in a novel impinging streams reactor

This paper presents an experimental investigation of a novel impinging stream reactor (ISR) with the aim of high mixing intensity. The integral mixing quality in the reactor was measured with the iodide-iodate reaction and showed excellent mixing performance. The impact of the operating parameters, such as fluxes, circulation and internozzle distances, was investigated in terms of segregation index. The results showed that the increase of flux, the decrease of inter-nozzle distance and a suitable circulation can improve the micro-mixing efficiency. Based on turbulence theory, it was estimated that the characteristic micro-mixing time was 0.002–0.02 s, which was much shorter than that in the stirred tank reactor. The micro-mixing time was related to the segregation index, which was in good agreement with those in the literature.     

Influence of centrifugal field on free‐radical polymerization kinetics

It has been observed that when a prepolymer mix of styrene, poly(styrene), toluene, and benzoyl peroxide is transferred from a conventional stirred tank reactor (STR) to a spinning disc reactor (SDR), the rate of polymerization is substantially increased. Furthermore, the molecular weight and the molecular weight distribution of the polymer formed at conversions up to about 80% in the SDR is virtually unchanged from that of the polymer formed at 60% conversion in the STR. These results seem to indicate that the increase in polymerization rate is not the result of the well‐known Trommsdorff–Norrish effect, which would be expected to lead to an increase in polydispersity. We believe that shear and centrifugal forces experienced by the film provide intense mixing and extension flow effects, which are responsible for the above‐described observations. In this report an explanation has been put forward to describe the observed effects. © 2002 Wiley Periodicals, Inc. J Appl Polym Sci 85: 2283–2286, 2002     

Reduced power consumption compared to a traditional stirred tank reactor (STR) for enzymatic saccharification of alpha-cellulose using oscillatory baffled reactor (OBR) technology

Enzymatic saccharification of pure α-cellulose was conducted in oscillatory baffled (OBR) and stirred tank (STR) reactors over a range of mixing intensities requiring power densities (P/V) from 0 to 250 Watts per cubic metre (W/m³). Both reactor designs produced similar saccharification conversion rates at zero mixing. Conversion increased with increasing mixing intensity. The maximum conversion rate occurred at an oscillatory Reynolds number (Re_o) of 600 in the OBR and at an impeller speed of between 185 and 350 rpm in the STR. The OBR was able to achieve a maximum conversion rate at a much lower power density (2.36 W/m³) than the STR (37.2–250 W/m³). The OBR demonstrated a 94–99% decrease in the required power density to achieve maximum conversion rates and showed a 12% increase in glucose production after 24 h at 2.36 W/m³.     

撞击流反应制取“超细”白炭黑

用反应-沉淀法制取超细固体产物最重要的条件之一是高且均匀的过饱和度环境.在有关撞击流性质研究的基础上，研发了浸没循环撞击流反应器(SCISR).它具有全混流-无混合流串联循环的特殊流动结构和撞击区微观混合强烈的特点.后者可以创造高且均匀的过饱和度，产生大量晶核；低过饱和度的无混合区有利于微晶表面稳定和钝化.利用该反应器进行普通沉淀法制取“超细”白炭黑的实验研究，确定了最优操作条件，并与传统的搅拌槽反应器(STR)进行了比较.SCISR可以半间歇或连续操作.制得产品粒径范围0.5～2.0μm，平均粒径1.1～1.6μm，比STR产品细、粒径分布窄.反应产物干燥实验结果表明后处理过程中粒径稳定，不发生微细颗粒并聚.     

Modeling of an industrial scale hydrodynamic cavitation multiphase reactor for Prileschajew epoxidation

The hydrodynamic cavitation multiphase reactor (HCMR) is emerging as a promising alternative for the intensification of liquid–liquid heterogeneous reactions, but research on HCMR modeling is lacking. In this article, an HCMR model was developed using Prileschajew epoxidation as the model system. First, based on experimental measurements of oil/water two-phase flow downstream of hydrodynamic cavitation devices, semiempirical correlations were proposed to describe the droplet size and droplet size distribution (DSD) as functions of flow conditions and geometry parameters. Then, with boundary conditions calculated by the DSD correlation, a droplet dynamics simulation in a reaction tank was performed by computational fluid dynamics coupled with population balance model to obtain the two-phase interfacial area. Finally, the acquired reactor model was substituted into an overall kinetic model, to simulate the epoxidation reaction in HCMR. Model predictions were verified by experimental results measured on an industrial scale HCMR.     

The effect of the draft tube geometry on mixing in a reactor with an internal circulation loop – A CFD simulation

The main topic of this paper is to describe the effect of geometrical parameters on mixing time in a reactor with an internal circulation loop. The design of the draft tube inside the reactor is an important geometric parameter and has a big influence on two phase hydrodynamics as well as on mass transfer in the reactor. In the first section, the validation of the selected mathematical model is carried out. The results of experimental measurements (liquid velocity and gas hold-up) obtained on the laboratory scale reactor are compared with the CFD simulations. The CFD simulation (bubbly flow and mass transfer models) was made using COMSOL Multiphysics 3.5a. The results of the numerical simulation are in good agreement with the experimental data. In the second section, the study of mixing in the reactor is described with the new geometry of the draft tube. The standard experimental techniques for testing mixing processes are quite problematic because common tracers (soluble salts) have significant influence on two phase hydrodynamics inside the reactor. Though, an alternative nontrivial method had to be used. The split of the draft tube into two or three section has a significant effect on mixing (mass transfer) in the reactor.     

Membrane‐dispersion reactor in homogeneous liquid process

For homogeneous liquid processes, mixing at molecular scale may influence selectivity, yield and quality of final products. In a membrane‐dispersion reactor, microporous membranes are employed as dispersion media for controlled feeding of one solution into another one to intensify micromixing. The reactor has been widely used in the preparation of nanoparticles, preparation of nanocapsules and liposomes, synthesis of polymers, parallel and consecutive reactions to improve nanoparticles quality, molecular weight distribution of polymer, or selectivity of complex reactions. This paper reviewed the progress of the membrane‐dispersion reactor in homogeneous liquid processing including features, applications, advantages and limits. © 2012 Society of Chemical Industry .     

Reactor development for the ultrapyrolysis process

A new impinging-jet reactor system has been developed for the fast pyrolysis (ultrapyrolysis) of particulate carbonaceous materials. The reactor system serves to promote rapid uniform mixing between a fine particulate heat carrier and a particulate feedstock in order to achieve the high heat transfer rates necessary for fast pyrolysis. Flow visualization experiments in a cold model testing unit indicated that the system performed effectively over a wide range of conditions. A sampling system utilizing isokinetic sampling probes was developed to investigate the small scale solids mixing. The effects of reactor geometry and operating conditions upon the solids mixing are reviewed.     

Experimental and numerical study of turbulent mixing in a model of a polymerization reactor

In this study the turbulent mixing in a model of a polymerization reactor is analyzed experimentally and numerically. The model corresponds to a zone of an autoclave reactor equipped with a stirrer. Two different configurations of the stirrer, with different arrangement of the paddles, have been considered. The mixing process has been monitored by following the time-evolution of injections of a passive scalar through the different inlets of the model. The time-evolution of the mixing quality in a laboratory scale model of the reactor has been measured using water and the Planar Laser Induced Fluorescence (PLIF) technique. Numerical simulations of the flow and of the mixing processes were carried out and results of the evolution of the mixing are compared successfully with measurements. The mixing processes are dominated by the flow topology generated by the rotation of the stirrer. Superimposed to the tangential flow, secondary flows divide the length of the reactor in different zones. It has been found that macro mixing in each individual zone is a relatively fast process and that the mixing rates within each zone are very similar. However, the mixing rate between different zones is a relatively slow process.     

Liquid flow and mixing in concentric tube air-lift reactors

Liquid velocity and mixing were measured in two concentric tube air-lift reactors (ALR) of 30 and 300 dm³ (nominal volume). The influences of the geometrical design and the reactor scale were studied as a function of gas flow rates. The mixing in the 30 dm³ ALR, which had an enlarged cross-sectional area in the gas separator region, indicates that in this geometrical configuration most of the mixing occurs in this region. It is demonstrated that the location of the injection and measuring points influence the measurement of mixing time in air-lift reactors. Correlations for pressure drop at the bottom, gas hold-up and mass transfer coefficients, which were published in a previous paper, are extended to include the effect of the ratio of downcomer-to-riser cross-sectional areas.