液体喷射环流反应器的研究（I）——“DSD酸”合成中非水介质法氧化过程的应用

在直径149mm液体喷射环流反应器热模装置中对“DSD酸”合成中非水介质法氧化过程进行了研究。与釜式反应器相比,反应时间由5小时缩短至25分种,目的产物的含量由52％提高至97％,耗碱量降低了50％,能耗降低了20％。研究工作为工业应用提供了依据。     

液体喷射环流反应器的研究(Ⅱ)--对羟基苯甲醛合成中氧化过程的应用

在直径349毫米液体喷射环流反应器(LJLR)中对4-羟基苯甲醛合成的氧化过程进行了研究。在优化的催化剂、碱量、反应时间和温度条件下,考察了LJLR不同操作条件对反应结果的影响,为工业生产提供了实验数据。     

液体喷射环流反应器的研究（Ⅲ）——三氯氧磷合成中氧化过程的应用

在直径149 mm液体喷射环流反应器(LJLR)中对三氯氧磷合成的氧化过程进行了研究,与釜式反应器相比反应时间由40 h缩短至8 h,氧气消耗量为理论量并且无尾气排放,研究结果已经用于工业生产.     

液体喷射环流反应器在液相催化氧化制备芴酮中的应用

以液体喷射环流反应器为氧化反应装置,液相催化氧化芴制备芴酮。通过考察物料循环速度、反应温度、催化剂用量和溶剂的含水量等因素对芴酮收率的影响,得出最佳氧化反应条件。     

液体喷射环流反应器在2，3，5-三甲基苯醌合成中的应用

在直径149mm液体喷射环流反应器热膜装置中采用空气氧化法对2,3,5-三甲基苯醌合成中三甲基苯酚氧化成三甲基苯醌过程进行了研究.与釜式反应器相比,反应时间由4小时缩短1小时,目的产物的含量由88%提高至98%,催化剂用量降低了70%,溶剂比例减小50%.研究工作为工业应用提供了依据.     

对硝基甲苯邻磺酸溶剂法氧化生产DSD酸的研究

在ＤＳＤ酸含合成中，对氧化缩合工序采用非水介质法－溶剂法，可将氧化缩合收率由７３％提高至９２％以上，解决了该工序的废水问题，采用改进后的工艺，最终还原产品含量可达９６％以上。     

我国DSD酸溶剂法氧化合成工艺工业化解脱瓶颈制约的建议

介绍了国内有关单位用溶剂法氧化合成DSD酸的清洁生产工艺研究进展,分析了该工艺目前还未能用于工业化生产的原因:①工业化生产的一些工程技术难题还有待解决;②溶剂法工艺生产的总成本高于传统的水法工艺;③不少地区的环保执法存在"盲区",地方保护痼疾难除;④政策支持力度不够,企业缺乏积极性;⑤产能过剩竞相降价,企业无力承担科研费用。讨论了溶剂法氧化合成DSD酸工业化的瓶颈制约所在,指出了解决途径,提出了发展建议。     

环流反应器中双甘膦氧化过程研究

在装液体积约为300 L的下喷式环流反应器中以活性炭为催化剂,氧气为氧化剂对双甘膦的氧化过程进行了实验研究。分析了双甘膦氧化反应过程,考察了反应时间、循环流量、反应温度对低浓度双甘膦氧化反应的影响。结果表明:在双甘膦氧化反应过程中,双甘膦的溶解阻力可以忽略,而气液传质阻力较大,对表观反应速率有较大影响;反应时间的增长使草甘膦收率先增大后降低;随着循环流量的加大,达到最佳收率时的反应时间缩短,但对草甘膦的收率影响不大;升高反应温度可以减少反应达到最佳收率所需的时间,但会使草甘膦收率降低。     

喷射环流生物反应器性能及处理染料废水的研究

对气液固三相喷射环流生物反应器中液体流速进行了测量,得到了不同操作压力,气本进料量和液体进料量下液速的分布规律。结合这种高效的喷射环流生物反应,采用活性污泥法对碱性绿染料废水的降解过程进行了研究。     

喷射环流三相流化床反应器轴向液速分布的研究

在喷射环流三相流化床反应器中，应用本文所开发的内热式热膜流体速率探头，获得了带有沉降分离区的夹套式环流反应器在不同压力、气量、流量条件下，不同轴向位置的液体速率分布规律。对于本文所述这类反应器，喷射区流体运动速率最大；自喷口向上，速率先是随距离的增大易急骤下降，然后逐渐向一渐近点逼近；当进入环隙转折口处时，由于气体的逸出及流道的变化液速急骤下降；凝固相进入环隙时，液速随距离的变化也存在渐近点。当采用变径结构时，流道面积突变处的液速变化率仅次于喷射入口区。在环流反应器中，液速主要取决于喷射动能及气提推动力，受液体进料量及压力的影响较小。     

High shear jet-mixers as two-phase reactors: An application to the oxidation of phenol in aqueous media

Jet-mixers are known as devices capable of greatly enhancing the gas-liquid interfacial areas. Their application to chemical reactions is discussed in this paper. The oxidation of phenols in aqueous media is considered. Rates of oxidation fifty times higher than those previously observed can be achieved through a jet-mixer discharging a fine mist into the reactor side operating at plug flow regime. The presence of hydrogen peroxide accelerates the oxidation. Kinetic information is provided.     

水合肼生产中氧化反应的研究和应用

分析了尿素法生产水合肼的氧化反应历程及影响因素，改进了反应器，并找到了最佳的工艺控制条件：①控制n(尿素)：n(次氯酸钠)=(1．05～1．10)：1，各原料的消耗较低，总经济效益佳；②采用-5℃冷冻盐水移走尿素、次氯酸钠混合段内氯化反应放出的热量，控制物料混合终点温度在15～30℃；③采用列管式加热器，将氯化反应与水解反应在不同的设备中进行，水合肼的收率提高到83％～85％；④采用列管式加热器代替双夹套反应器，提高了加热强度，生产能力大，1套合成反应器可生产1万t／a80％的水合肼。     

A comparative study of a fluidised bed reactor and a gas lift loop reactor for the ibe process: Part III. Reactor performances and scale Up

Continuous fermentations using Clostridium spp. DSM 2152 immobilised in calcium alginate beads to produce butanol and isopropanol from glucose were carried out in a fluidised bed reactor with liquid recycle (FBR, 10.9 dm³ working volume, 41 % solids) and in a gas lift loop reactor (GLR, 11.4 dm³ working volume, 32% solids). In the FBR in-situ produced non-coalescing gas bubbles had a negligible influence on the fluidisation pattern and the steady state results of the fermentation were in accordance with those predicted by a reactor model. The FBR was operated reliably for 5 weeks without decrease of activity. The GLR behaved as a three phase reactor because of the recycled fermentation gas. The steady state fermentation results were as predicted by the GLR model. Scale up to a 50 m³ FBR and a 65 m³ GLR led to development of a plug flow with recycle model for the FBR and a stirred tank model for the GLR. On the basis of overall reactor performance and ease of integration with a simultaneous product recovery the FBR is preferred to the GLR for application in a large scale butanol/isopropanol process using immobilised Clostridia spp.     

Electrolytic oxidation of Ce(III) in nitric acid and sulfuric acid media using a flow type cell

The electrochemical oxidation behavior of Ce(III) in nitric acid and sulfuric acid media with various concentrations and compositions were investigated by cyclic voltammetry (CV) and potentiostatic electrolysis. In nitric acid media, the peak potential separation for the redox reactions of the Ce(III)/Ce(IV) couple shifted to base side with the increasing concentration of nitric acid from 1 to 6 M. The kinetics of the Ce(III)/Ce(IV) couple is rapid in high concentration nitric acid. The formal potential is independent of both proton and nitrate concentrations while the standard rate constant increases with added protons but is independent of nitrate concentration. Constant-potential electrolysis also shows that a high proton concentration is electrochemically favorable for the electron transfer of the Ce(III)/Ce(IV) couple and for a high Ce(IV) yield in nitric acid media. The current efficiency was ca. 75% for the oxidation process of Ce(III) at 298 K. A Ce(IV) yield of ca. 80% was achieved for the electrolysis of 100 mM Ce(III) in 6 M HNO₃ solution. In sulfuric acid media, the peak potential separation for the redox reactions of the Ce(III)/Ce(IV) couple shifted to noble side with rising concentration of sulfuric acid from 0.1 to 2 M and then shifted to base side with further increase in the concentration. A Ce(IV) yield of ca. 95% was achieved for the potentiostatic electrolysis of 100 mM Ce(III) in 3 M H₂SO₄ solution.     

Complex metal-oxide catalysts for selective oxidation of propane and derivatives: I. Catalysts preparation and application in propane selective oxidation to acrylic acid

Several parameters involved in preparing the complex metal-oxide (CMO) catalysts (M_aV_bTe_cNb_dO_n, M: Mo and W) for the selective oxidation of propane to acrylic acid (AA) were investigated and discussed. These include the role each metal element plays and the effects on the performance of the catalysts exerted by the proper metal ratio, as well as various preparation methods, such as the mixing of starting chemicals to form an aqueous precursor mixture, the solvent removal, and the proper calcination atmosphere and gas flow. It was found that each metal element plays a critical role and while an appropriate MoVTeNb metal ratio is critical to the formation of an effective catalyst, each and every step of the preparation methods also have profound effects on the structures and performance of the resulting catalysts. The preferred preparation method for an effective MoVTeNb oxide catalyst includes the intimate mixing of all starting chemicals to form a precursor solution, drying via rotavap for solvent removal followed by calcination under a non-flow inert atmosphere. Using this preferred preparation method, effective complex metal-oxide catalysts can be prepared which affords up to 73% propane conversion and 42% one-pass yield to acrylic acid, while undesirable preparation methods, in contrast, lead to very ineffective catalysts of the identical composition.     

葡萄糖催化氧化制备葡萄糖酸（盐）催化剂研究进展

综述了近年来葡萄糖催化氧化制备葡萄糖酸的催化剂的研究进展，分别就多相催化氧化法和均相催化氧化法进行了论述，讨论了各种催化剂的优缺点，并对今后的研究方向进行了展望。     

A comparative study of a fluidised bed reactor and a gas lift loop reactor for the IBE process: Part I. Reactor design and scale down approach

For the continuous production of isopropanol-butanol mixtures by immobilised Clostridium spp. (the IBE process) two reactor types were studied: a fluidised bed reactor with liquid recycling (FBR) and an external loop gas lift reactor (GLR). A large scale design (50–65 m³) was made for both reactors. A regime analysis, by evaluating the time constants for e.g. mixing and conversion, identified the ruling regime. Via the scale down approach two representative model reactors were developed: a 10 dm³ FBR reactor (H/D=25, D=0.08 m) and a 15 dm³ external loop GLR (H/D = 12.5, D_r=D_d=0.08 m). For both reactors the hydrodynamical behaviour and the total reactor performance were studied and are described in parts II and III of this study.     

4-(2-甲-4-氯苯氧基)丁酸氯化工艺改进—水相氯化法

介绍了以４－（２－甲基苯氧基）丁酸为原料在催化剂存在下用次氯酸钠为氯化剂在水相中氯化制备４－（２－甲－４－氯苯氧基）丁酸的过程。催化剂有高的选择性。整个过程有好的生产环境。该过程也可用于其它２－甲－４－氯苯氧基羧酸类的氯化过程。