新型Ti/TiOxHy/Sb-SnO2电极上苯胺电化学氧化反应

苯胺是一种重要的化工原料,广泛应用于印染、制药、造纸、橡胶等领域.随着化工行业的迅速发展,苯胺的需求量越来越大.然而,苯胺毒性高,大量使用势必造成水体中苯胺浓度的升高,给人类健康及生态环境造成危害.因此,急需一种高效、洁净、经济的方法处理含苯胺废水.电化学氧化法比较新颖,相比传统废水处理方法,它具有高效、简单、清洁等优点,因此被应用于很多废水处理当中,但过多的能耗限制了其进一步广泛应用.阳极作为电化学氧化技术的核心部件,直接影响到电化学氧化反应性能.因此开发出一种高效、经济的阳极材料很有必要.此外,对苯胺降解条件的优化也同样重要.关于苯胺电化学氧化,已有的研究包括Pt电极、PbO2电极和石墨电极等阳极材料.比较而言, Ti/Sb-SnO2电极具有制备工艺简单,析氧过电位较高,材料廉价和电催化性能较强等优点.然而,它的稳定性仍有待提高.因此本文制备了一种高稳定性的Ti/TiOxHy/Sb-SnO2电极,并用于处理苯胺废水.较为系统地研究了电流密度、苯胺初始浓度、pH、NaCl投加量及反应器类型对苯胺电催化氧化性能的影响,同时采用扫描电镜(SEM)、X射线衍射(XRD)和电化学测试对该电极进行了表征,并应用紫外-可见光谱、化学需氧量、电流效率及能耗对不同参数进行评定和优化. SEM及XRD结果表明, Ti/TiOxHy/Sb-SnO2电极涂层覆盖比较完全、紧实,未出现裂缝的发生,因而有利于提高电极稳定性.循环伏安测试结果表明,此电极具备较高的析氧过电位(2.0 V vs Ag/AgCl)及电化学孔隙度(76.31%),因此有利于电极催化性能的提高.苯胺电化学氧化实验结果发现,该反应符合准一级动力学模型,且高电流密度、酸性环境、适当NaCl投加量(0.2 wt%)更有利于苯胺的降解.另外, Ti/TiOxHy/Sb-SnO2电极在三维反应器中对苯胺的处理效果要远远好于在二维反应器中.可以看出, Ti/TiOxHy/Sb-SnO2电极具有较好的处理苯胺性能,可为苯胺废水处理的应用提供了一定的理论指导.     

NiO@SiO_2核壳催化剂在浆态床中低温甲烷化研究

采用改进的Stber方法,可控制备出具有不同形貌的NiO@SiO_2核壳结构催化剂,并在浆态床反应器(320℃)上,对其合成气低温甲烷化性能进行评价;同时借助XRD、TEM、XPS和N_2物理吸附等方法对反应前后催化剂的物化性质进行了表征。研究表明,实验制备的催化剂形貌规整、粒径均匀,且具有较好的热稳定性。在相同的制备条件下,核颗粒粒径增大,其SiO_2壳层的厚度随之增加。在反应过程中,部分催化剂的核壳结构遭到破坏并出现SiO_2空壳,是CO与壳层内的Ni作用生成易迁移的Ni羰基化物种(Ni(CO)_x)所致。催化剂的甲烷化活性随着核颗粒粒径的增加呈现下降趋势;在不同的反应阶段,催化剂的失活速率存在明显差异,在反应的前20 h内,催化剂出现快速失活,20 h后失活缓慢,但是催化剂的甲烷选择性都保持在80%左右。催化剂的失活,一方面,是因为反应过程中,Ni核颗粒发生了长大;另一方面,是由于壳层中3-5 nm的介孔的减少以及催化剂比表面积、孔容的下降。     

球形托卡马克堆嬗变中子学计算的比较研究

基于对球形托卡马克（ST）聚变堆的研究，提出了ST聚变－嬗变堆的设计概念。运用一维输运燃耗计算程序BISON3.0进行了优化设计，确定了适合于嬗变少额锕系MA核素的堆芯等离子体参数、包层结构及合适的换料周期。在一维计算的基础上，运用二维中子学程序TWODANT进行了二维中子输运计算；结合TWODANT给出的中子通量，运用一维放射性计算程序FDKR进行了燃耗计算，并给出了有关的计算结果。     

Pepsin immobilized in dextran-modified fused-silica capillaries for on-line protein digestion and peptide mapping

On-line digestion of proteins under acidic conditions was studied using micro-reactors consisting of dextran-modified fused-silica capillaries with covalently immobilized pepsin. The proteins used in this study differed in molecular weight, isoelectric point and sample composition. The injected protein samples were completely digested in 3 min and the digest was analyzed with micro-high performance liquid chromatography (HPLC) and tandem mass spectrometry (MS/MS). The different proteins present in the samples could be identified with a Mascot database search on the basis of auto-MS/MS data. It proved also to be possible to digest and analyze protein mixtures with a sequence coverage of 55% and 97% for the haemoglobin β- and α-chain, respectively, and 35-55% for the various casein variants. Protease auto-digestion, sample carry-over and loss of signal due to adsorption of the injected proteins were not observed. The backpressure of the reactor is low which makes coupling to systems such as Surface Plasmon Resonance biosensors, which do not tolerate too high pressure, possible. The reactor was stable for at least 40 days when used continuously.     

Green process of fuel production under porous γ-Al2O3 catalyst: Study of activation and deactivation kinetic for MTD process

One of the methods of industrial dimethyl ether production is the catalytic dehydration of methanol. In this research work, methanol dehydration reactor has been modeled using continuous model and its results have been compared with experimental works and Voronoi pore network model. A 1D heterogeneous dispersed plug flow model was utilized to model an adiabatic fixed-bed reactor for the catalytic dehydration of methanol to dimethyl ether. The mass and heat transfer equations are numerically solved for the reactor. The concentration of the reactant and products and also the temperature varies along the reactor, therefore the effectiveness factor would also change in the reactor. We used the the effectiveness factor that was simulated according to the diffusion and reaction in the catalyst pellet as a Voronoi pore network model. Sensitivity analysis was performed to determine the influence of T, P and weight hourly space velocity on performance of the chemical reactor. Acceptable agreement was reached between the measured and the model data. The results showed that the maximum reaction conversion was obtained about 90 % at WHSV = 10 h^?1 and T = 560 K, while the inlet temperature (T_inlet) had a greater effect on methanol conversion. In addition, the effect of water in the feed on methanol conversion was quantitatively studied. Also, the deactivation kinetics of γ-Al₂O₃ heterogeneous-acidic catalyst in methanol to dimethyl ether dehydration process was studied using integral analysis method. Based on independent deactivation kinetics, a second order was found that accurately fitted the experimental conversion time data. The main reaction activation energies and catalyst deactivation energies were 143.1 and ?102.1 kJ/mol, respectively.     

Fundamental Aspects of Ceria Supported Au Catalysts Probed by In Situ/Operando Spectroscopy and TAP Reactor Studies

The discovery of the activity of dispersed gold nanoparticles three decades ago paved the way for a new era in catalysis. The unusual behavior of these catalysts sparked many questions about their working mechanism. In particular, Au/CeO₂ proved to be an efficient catalyst in several reactions such as CO oxidation, water gas shift, and CO₂ reduction. Here, by employing findings from operando X-ray absorption spectroscopy at the near and extended Au and Ce L_III energy edges, we focus on the fundamental aspects of highly active Au/CeO₂ catalysts, mainly in the CO oxidation for understanding their complex structure-reactivity relationship. These results were combined with findings from in situ diffuse reflectance FTIR and Raman spectroscopy, highlighting the changes of adlayer and ceria defects. For a comprehensive understanding, the spectroscopic findings will be supplemented by results of the dynamics of O₂ activation obtained from Temporal Analysis of Products (TAP). Merging these results illuminates the complex relationship among the oxidation state, size of the Au nanoparticles, the redox properties of CeO₂ support, and the dynamics of O₂ activation.     

Toward Continuous-Flow Hyperpolarisation of Metabolites via Heterogenous Catalysis,Side-Arm-Hydrogenation,and Membrane Dissolution of Parahydrogen

Side-arm hydrogenation (SAH) by homogeneous catalysis has extended the reach of the parahydrogen enhanced NMR technique to key metabolites such as pyruvate. However, homogeneous hydrogenation requires rapid separation of the dissolved catalyst and purification of the hyperpolarised species with a purity sufficient for safe in-vivo use. An alternate approach is to employ heterogeneous hydrogenation in a continuous-flow reactor, where separation from the solid catalysts is straightforward. Using a TiO₂-nanorod supported Rh catalyst, we demonstrate continuous-flow parahydrogen enhanced NMR by heterogeneous hydrogenation of a model SAH precursor, propargyl acetate, at a flow rate of 1.5 mL/min. Parahydrogen gas was introduced into the flowing solution phase using a novel tube-in-tube membrane dissolution device. Without much optimization, proton NMR signal enhancements of up to 297 (relative to the thermal equilibrium signals) at 9.4 Tesla were shown to be feasible on allyl-acetate at a continuous total yield of 33 %. The results are compared to those obtained with the standard batch-mode technique of parahydrogen bubbling through a suspension of the same catalyst.     

Reactor and Product Optimization via Raman Fiber Optics Monitoring: Application to Polymer‐Based Proppants

A setup to characterize polymerization kinetics of polymer‐based proppants produced in an industrial batch reactor by suspension polymerization is presented. A microscale reactor is designed to mimic temperature and pressure conditions of the industrial counterpart. Raman spectroscopy is used to follow the consumption of vinyl bonds of the styrene monomer and the crosslinker via disappearance of the peak at 1632 cm^‐1. Raman data from the microscale reactor are remotely obtained via a fiber optics system. Reaction progress by any generic formulation can be safely followed up to conversions of 90%, well beyond the gel point. Reaction rates are used to define feasible temperature–time profiles for the industrial reactor. In parallel, bulk and suspension polymerizations are carried out under those temperature–time profiles in a 3 L laboratory reactor to produce proppants formulations with the geometry required to perform product characterization, mainly focused on the thermal and mechanical response of the polymer particles. Overall, the whole setup allows optimization of proppant formulations and the cost of their processes of production.     

Polymer nanocomposite membranes and their application for flow catalysis and photocatalytic degradation of organic pollutants

The modern world essentially needs a chemical industry that can operate with reduced production costs, and produce high-quality products with low environmental impact. The polymer nanocomposite-based flow catalytic membrane reactor where the reaction and separation can be amalgamated in one unit is considered as one of the new alternative solutions to solve these problems. In this review, we have discussed state-of-the-art flow-through catalytic reactors based on polymer nanocomposite membranes. The unique advantages of flow catalysis include uninterrupted operation, good recyclability, and reaction product without contamination that leads to simple purification. Various catalytic model reactions such as coupling, hydrogenation, esterification in the flow system are presented. We have also presented an overview of methods adopted for preparing such nanocomposite membranes. In the last section, a discussion has been made on the recent advances on polymer-based nanocomposite membranes for the degradation and separation of organic pollutants.     

Continuous Miniemulsion Polymerization

Most miniemulsion polymerizations are carried out in batch reactors. However, continuous reactors or continuous reactor trains can provide a high level of consistency when operated at steady state. In this feature article, progress in continuous miniemulsion polymerization will be reviewed. Special attention will be given to issues of monomer diffusion and secondary nucleation. A large portion of the paper will be devoted to controlled radical polymerization for two reasons. First, this is a relatively new field, particularly when continuous reactors are considered, and second, for controlled radical polymerization in continuous reactors, the molecular weight distribution of the product is a direct function of the reactor residence time distribution.