2-氯-5-氯甲基吡啶在气升环流反应器中的合成研究

A new process for the direct chlorination of 2-chloro-5-methylpyridine to yield 2-chloro-5-chloro-methylpyridine in an airlift loop reactor (ALR) has been studied.Five main reaction conditions including TR,na/ns,cp,Qg and dD/dR were optimized.The average molar yield and purity of 2-chloro-5-chloromethylpyridine obtained were 79% and 98.5% respectively under the optimum operating conditions.Finally,the efficiency for the preparation of 2-chloro-50chloromethylpyridine with ALR and stirred tank reactor(STR) respectively was compared.     

微量有机化合物催化燃烧反应器数学模拟

建立了甲苯、二甲苯、环己烷催化燃烧反应器的一维拟均相数学模型 ,在MnCuOx/Al2 O3 催化剂上催化燃烧反应动力学采用Langmuir双曲型动力学方程。模拟计算了废气处理量、废气中有机化合物的浓度、床层入口温度对净化率的影响     

采用高速剪切反应器生产超细氧化铋工艺探讨

利用硝酸铋溶液和碳酸铵溶液为原料，采用高速剪切反应器，500℃煅烧后可以生产出高纯、超细的氧化铋粉末。该方法制备出的氧化铋平均粒度0．71μm且粒度范围分布窄，颗粒形貌为类球形，晶相为纯α相，指标达到电子压敏陶瓷要求。由于粒度细小，可以在电子压敏陶瓷球磨工艺减少球磨工艺，并具有更好的分散效果。本文对超细的氧化铋粉末形成机理也进行了探讨。     

AlCl3/活性炭催化甲基三氯硅烷与低沸物再分配反应研究

甲基三氯硅烷(M1)与低沸物(LBR)是工业上"直接法"生产二甲基二氯硅烷单体过程中产生的副产物,两者之间通过再分配反应可转化为高价值的有机硅单体.以活性炭为载体,采用浸渍蒸发煅烧法制备了负载型AlCl3固体酸催化剂,在固定床反应器中进行甲基三氯硅烷与低沸物的再分配反应,制得二甲基二氯硅烷和三甲基氯硅烷.考察了活性炭载体预处理方式及反应条件对再分配反应的影响.结果表明,经过高温扩孔处理的活性炭载体负载的AlCl3催化剂具有较好的反应活性;优化的反应条件为:W(M1/LBR)为2.0～3.0,反应温度为310℃,LHSV为1.5 h-1;该催化剂的制备过程简单,催化反应条件温和且表现出良好的催化稳定性.     

新型光化学反应器及二氧化碳光解反应研究

研究设计了可产生波长小于200 nm真空紫外光的光化学反应器,首次利用该波段的光在该反应器中进行了CO2光解反应的研究。用氮气为发光介质对其进行光强标定,实验表明主要产生120、149、174 nm波长的光(N原子谱线);实验条件下CO2光解后生成产物CO,结果表明光源电流一定时产生CO的量与光源工作气体的压力有关,在CO2和N2反应物系中,光源内发光介质N2的压力在2 500 Pa左右时CO的产率最大,而在该反应物系中加入甲烷后,CO的产率明显增大。     

自热制氢反应器研究进展

介绍了同心圆式反应器、板式反应器、壁反应器、微通道反应器在自热重整反应制氢中的特点。同心圆式反应器的传热是控制步骤,为强化传热而开发了空间形状不同和流体经过反应器不同腔体的先后顺序不同的反应器;板式反应器易于组装、拆卸和放大,而且热效率也比较高,是目前十分活跃的研究领域,重点在于操作参数和设计的优化及其高效壁载制氢催化剂的研制;壁反应器的反应表面和换热表面不分离,具有较高的热量耦合效果;微通道反应器具有优越的传热性能,但对加工和流体的性质有比较苛刻的要求。另外,不同燃料制氢机理的研究及其过程参数的稳态、瞬态模拟,为反应器的设计提供了理论依据。而制氢过程并行单元的研究为系统的集成奠定了基础。最后,指出开发板式壁反应器以及开展其在CO变换、净化方面的研究有较好的发展前景。     

High-Throughput Experimentation in Oxidation Catalysis

High-throughput experimentation in catalysis comprises the following components: (i) automated high-throughput synthesis, (ii) testing in Stage I and Stage II, for which to some extent novel assays are necessary, (iii) data handling and experimental design tools, and (iv) robotics. This contribution covers these topics, using examples from the research of the authors, but also from the literature, in order to illustrate the problems and opportunities associated with high-throughput experimentation in catalysis, focusing particularly on heterogeneous catalysis.     

UASB-SBR工艺处理城市生活污水的研究

研究了UASB工艺处理城市生活污水的可行性，通过UASB与SBR组合工艺的运行实验，得出在水力停留时间3h时，COD去除率为61．67％-82．32％，出水COD达到国家污水排放二级标准。在氮磷去除效果不佳的情况下，采用SBR工艺处理后，其出水COD、SS、氮、磷等指标均达到国家污水一级排放标准。     

Syngas production from methane reforming with CO2/H2O and O2 over NiO–MgO solid solution catalyst in fluidized bed reactors

Catalyst performance of NiO–MgO solid solution catalysts for methane reforming with CO₂ and H₂O in the presence of oxygen using fluidized and fixed bed reactors under atmospheric and pressurized conditions was investigated. Especially, methane and CO₂ conversion in the fluidized bed reactor in methane reforming with CO₂ and O₂ was higher than those in the fixed bed reactor over Ni_0.15Mg_0.85O catalyst under 1.0 MPa. In contrast, conversion levels in the fluidized and fixed bed reactor were almost the same over MgO-supported Ni and Pt catalysts. It is suggested that the promoting effect of catalyst fluidization on the activity is related to the catalyst reducibility. On a catalyst with suitable reducibility, the oxidized and deactivated catalyst can be reduced with the produced syngas and the reforming activity regenerates in the fluidized bed reactor during the catalyst fluidization. In addition, the catalyst fluidization inhibited the carbon deposition.     

COMPUTER SIMULATION OF HYDRODEMETALLATION IN FIXED-BED REACTORS

An isothermal model for hydrodemetallation (HDM) of crude oils in catalytic fixed-bed reactors is proposed. This model involves a consecutive reaction mechanism, which is capable of accounting for particle deposit profiles with interior maxima. Consistent with the fact that HDM catalysts are conglomerates formed by precipitation, the porous catalyst itself is modeled as randomly overlapping spheres of equal size. The metal is deposited as growing metal sulfide crystallites on the inner surface of the catalyst. These crystallites originate from a certain number of randomly scattered nuclei and increase in size as the deposition proceeds. The random sphere model for the catalyst and the deposit provides the changes in the catalyst pore structure—local porosity and surface area.

The mass transport within the domain of the particle is due to restricted liquid diffusion, since the diameter of the metal bearing compound (porphyrin) and the intermediate are comparable to the pore size. The diffusion restrictions taken into account are the enhanced drag imposed on a molecule by adjacent pore walls and steric partitioning.

Since the deposition process is much slower than diffusion and reaction, the pseudo-steady-state assumption can be justified. The equations of conservation for mass are solved by orthogonal collocation on finite elements. Based on this solution technique a computer simulation program of HDM is designed that allows two modes of operation: constant temperature and constant conversion. The simulation program “SIMULA” is highly flexible with regard to reaction kinetics, catalyst structure, reactor design, and operating conditions. In comparison to a base case with uniform activity, the effect of intraparticle (radial) and bed (axial) activity profiles on the conversion rate is discussed. For the case investigated, a radial distribution of activity higher at the center of the particle than at the edge can increase catalyst life by 25%, but axial distribution was less successful.