Chemiluminescence Determination of Benzoic Acid Using A Solid-Phase Verdigris Reactor

Benzoicacidisacommonadditiveusedwidelyasfoodpreservativeandplasticizer.Itcouldpromoteseverereactiontoallergicpopulationevenatlowconcentrationlevel1.Routinemethodsfortheassayofbenzoicacidincludeschromatographic2-6,spectrophotometry7,8,capillaryelectrophoresis9-13andelectrochemicaltitration14.Stokes15etal.monitoredairbornebenzoicacidbasedonsurface-enhancedRamanscatteringtechniques.Thereisalsoreportonamicrobialsensorusingpseudomonasforbenzoicacidandtheirderivativesinaqua16.Interestofusinglumines…     

中空纤维催化膜反应器中环戊二烯的选择加氢反应

将聚乙烯吡咯烷酮（ＰＶＰ）负载钯催化剂（ＰＶＰ－Ｐｄ）镶嵌到三种醋酸纤维（ＣＡ）中空膜（ＣＡ－Ｉ，ＣＡ－Ⅱ，ＣＡ－Ⅲ）内制各中空纤维催化膜，并进一步制成催化膜反应器，在４０℃和０．１ＭＰａ的反应条件下，在催化膜反应器中进行了环戊二烯的选择加氢反应，考察了具有不同氢气渗透率的醋酸纤维丝组成的三种膜反应器对反应的转化率及选择性的影响，并在此基础上考察了各种反应参数对反应的影响，ＣＡ中空纤维催化膜对环戊     

Silicalite-1膜反应器中的丙烷芳构化

在丙烷芳构化反应中，氢气起着相当重要的作用；根据理论分析，消除氢气将会有利于芳构化反应的进行。在Ｓｉｌｉｃａｌｉｔｅ－１沸石分子筛膜反应器，丙烷芳构化反应中的芳烃选择性提高了１０％－２０％。针Ｓｉｌｉｃａｌｉｔｅ－ｌ膜反应器与氧化铝膜反应器中的反应结果相比较，表明膜反应器效果不仅取决于膜的渗透选择性，而且还取决于膜的渗透率。     

外循环式耐硫甲烷化反应器分析

建立了耐硫甲烷化循环式反应器的拟均相一维模型，考察了床层直径，循环比，入口气体温度及压力和温度范围对反应器操作的影响，结果表明：循环比和温度操作范围是反应器操作的决定因素，对日产５万标准立方煤气的反应器进行了优化设计分析。     

聚乙烯塑料在连续超临界水反应器中的油化研究

在连续超临界水（SCW）反应器中考察了反应温度、停留时间和反应压力对聚乙烯（PE）降解油化的影响。实验结果表明，在120s、25MPa下，从500℃提高到550℃，液体收率呈现先升后降的趋势，在530℃达到最大值（79%）；在520℃、25MPa下，随停留时间的延长，PE裂解程度加深，产物轻质化程度提高，导致液体收率降低，停留240s时，气体收率达到43%；反应压力对产物收率的影响较小，气、液产物中烯/烷比随反应压力的增加而增大。     

Pulverized coal plasma gasification

A number of experiments on the plasma-vapor gasification of brown coals of three types have been carried out using an experimental plant with an electric-arc reactor of the combined type. On the basis of the material and heat balances, process parameters have been obtained: the degree of carbon gasification (_c), the level of sulfur conversion into the gas phase (_s), the synthesis gas concentration (CO+Hz) in the gaseous products, and the specific power consumption for the gasification process. The degree of gasification was 90.5-95.0%, the concentration of the synthesis gas amounted to 84.7–85.7%, and the level of sulfur conversion into the gas phase was 94.3–96.7%. Numerical study of the process of plasma gasification of coals was carried out using a mathematical model of motion, heating, and gasification of polydisperse coal particles in an electric-arc reactor of the combined type with an internal heat source (arc). The initial conditions for a conjugate system of nonlinear differential equations of the gas dynamics and kinetics of a pulverized coal stream interacting with the electric arc and oxidizer (water vapor) agree with the initial conditions of the experiments. The computation results satisfactorily correlate with the experimental data. The mathematical model can be used for the determination of reagent residence time and geometrical dimensions of the plasma reactor for the gasification of coals.Nomenclature c _i volume concentration of components (kmol m^–3) - x longitudinal coordinate (m) - f _i source members, determined by variation of the ith component due to chemical reactions in unit volume in unit time (kmol m^–3s^–1) - velocity (m s^–1) - M _s ash mass in one particle (kg) - C _D particle drag coefficient - 3.14 - r _s particle radius (m) - d particle diameter (m) - density (kg m^–3) - C _p heat capacity of components (J mol^t– K^–1) - Q _j thermal effect of reaction (J kmol^–1) - E_j activation energy of reaction - N _l volume concentration of particles of thelth fraction (m^–3) - T temperature (K) - emissivity factor of coal particles - 5.67 × 10^–8, blackbody emissivity coefficient (W m^–2 K^–4) - P pressure (Pa) - S reactor cross section (m²) - D reactor diameter (m) - V reactor volume (m³) - L _R reactor length (m) - F _W friction force on the wall (N) - f _g friction coefficient - residence time (s) - Nu Nusselt number - Re Reynolds number - Pr Prandtl number - thermal conductivity of gas (J m^– s^–1 K^–1) - R 8.3 × 10³, universal gas constant (J kmol K^–1) - µ _i molecular mass of component (kg kmol^–1) - dynamic viscosity coefficient of gas (kg m^–1 s^–1) - thermal efficiency of plasma reactor - q_arc specific heat flow from arc (W m^–3) - P ₁ heat supplied in vapor at T = 405 K (W) - P ₂ heat loss to wall (W) - P ₃ heat loss in the gas and slag separator chamber (W) - P ₄ heat loss in the synthesis gas oxidation chamber (W) - P ₅ heat loss in the slag catcher (W) - P ₆ heat carried away in the off-gas (W) - P heat input of arc (W) - P _arc electric power of arc (W) - Q_sp specific power consumption (kw Hr kg^–1) - d _w specific heat flow to wall (W m^–2) - _c degree of carbon gasification (%) - _s level of sulfur conversion into gas phase (%)     

Diamond synthesis by DC thermal plasma CVD at 1 atm

Diamond crystals and films have been success full y synthesized by DC thermal plasma jet CVD at a pressure of I atrn. A novel triple torch plasma reactor has been used to generate a convergent plasma volume to entrain the participating gases. Three coalescing plasma jets produces! by this reactor direct the dissociated and ionized gaseous species onto ( 100) silicon wafer substrates where the diamond grows. In a typical 10-min run, depending on the method of .substrate preparation, either microcrystals with sizes up to 8 m or continuous films with thicknesses of 1–2 m have been obtained. X-ray diffraction, scanning electron microscopy, and Raman spectroscopy have been used for the characterization of the crystals and of the films.     

Voltammetry Under Microfluidic Control,a Flow Cell Aproach

A generic approach to the design, construction and experimental characterization of novel microelectrochemical reactors (MECR) is presented. Structurally well‐defined rectangular microchannels incorporating electrochemical sensors were fabricated using a propriety photosensitive glass and photolithographic techniques. Microelectrode sensors were produced via evaporation to yield, gold, silver or platinum bands of approximate lengths 10–50 μm. The approach outlined permits cells of dimensions in the range: height 50–100 μm, width 100–500 μm and length 1–3 cm to be accurately constructed, in single or array configurations and were characterized via a voltammetric study utilizing electrolyte solutions containing N,N,N′N′‐Tetramethyl‐1,4‐phenylenediamine. In all cases, the test cells were constructed so that the three dimensional hydrodynamic boundary layer within the cells would significantly influence the reagent transport and therefore the observed current density at the microelectrodes. The current/flow rate relationship observed was analogous to the response of the observed within the macroscopic channel flow cells, where typically the cell design is restricted to configurations where a two dimensional transport analysis can be performed.