用于燃油节能环保的有机稀土活性复合物的制备及应用

由有机稀土配体化合物、表面活性剂、助表面活性剂、稳定剂、溶剂等原料制备出有机稀土活性复合物。通过柴油机台架实验发现,该种复合物的加入不仅对柴油机节能、抗磨损及保护发动机起到积极的作用,同时能有效降低尾气中有害物质的排放。     

乙酸苄酯的合成新工艺研究

报道了合成乙酸苄酯的新工艺 ,以有机溶剂丙酸丁酯作为反应介质 ,三乙胺为催化剂 ,合成了乙酸苄酯。产品收率可达 99 1%,产品纯度 >99 5 %,溶剂可反复回收使用。     

相转移催化氧化合成苯甲酸

研究了季铵盐CTAB催化高锰酸钾氧化氯化苄合成苯甲酸的反应。考察了CTAB用量、高锰酸钾用量、反应温度、反应时间对反应的影响。结果表明,合成苯甲酸的最优条件为:高锰酸钾与氯化苄的摩尔比为2∶1,CTAB的摩尔分数为氯化苄的8%,反应温度90℃,反应时间为3h,苯甲酸的产率可达89%。     

高选择性合成1-甲氧基-2-丙醇固体催化剂的筛选和催化作用

对碱土金属氧化物和两性氧化物等10种氧化物作为合成1 甲氧基 2 丙醇固体催化剂进行了催化性能筛选。发现在碱土金属氧化物MgO、CaO和BaO中,中强碱MgO具有较高的环氧丙烷(PO)转化率(71 07%)和1 甲氧基 2 丙醇(PPM)选择性(92 53%)。在两性氧化物中,ZnO具有较高的PO转化率(55 26%)和PPM选择性(92 37%)。系统考察了反应温度、催化剂用量、反应时间和原料摩尔配比对MgO、ZnO的催化作用特点的影响,发现MgO在催化性能和1 甲氧基 2 丙醇选择性方面表现出的综合性能优于其他催化剂。     

一水硫酸氢钠催化合成乙二醇单甲醚乙酸酯

以一水硫酸氢钠为催化剂,由乙二醇单甲醚和冰乙酸合成了乙二醇单甲醚乙酸酯。考察了乙二醇单甲醚和冰乙酸摩尔比及催化剂用量对酯化率的影响。适宜反应条件为:乙二醇单甲醚∶冰乙酸∶一水硫酸氢钠=1∶1.75∶0.036(摩尔比),苯作带水剂,回流分水60min,酯化率达90.0%。产品经元素分析和红外光谱表征。     

PPESK／PS共混物流变性能的研究

以溶液共沉淀的方法制备了含二氮杂萘联本结构的聚芳醚砜酮（PPESK）。聚苯乙烯（PS）共混物，用毛细管流变仪测定了共混物的流为性能。结果表明，在本实验条件下，PPESK／PS共混物熔体属假塑性非牛顿汉体，其熔体粘度随PS含量的增加、温度的升高、剪切速率的增大而下降。PS的加入有利于改善PPESK的熔融加工流动性。     

烷基二苯醚的合成

分别以烷基化剂溴代十二烷、溴代十四烷、溴代十六烷与二苯醚反应，制得系列烷基二苯醚产品。通过正相高效液相色谱法监测烷基系二苯醚曲合成，优化其合成工艺。色谱条件为：色谱柱，C18 kromasil（5μm，250×4．6mm）；流动相，体积比V正己烷：V异丙醇=18：1；流速，1mL/min。最佳合成工艺为：各反应物的摩尔比n二苯醚：n催化剂：n澳代烷=1：2：5；反应温度为75℃。反应时间为6h。双十二烷基二苯醚、双十四烷基二苯醚、双十六烷基二苯醚的产率分别为79．62％、72．38％、66．83％。     

特种工程塑料聚芳醚酮

介绍了聚芳醚酮的发展概况、分类及其物化性能;重点对PEEK的性能及应用进行详细阐述;概述了PEEK 的最新研究成果,并指出其今后发展趋势。     

Phase diagrams for oil/methanol/ether mixtures

One-phase transmethylations of vegetable oils with methanol to form methyl esters occur considerably faster than conventional two-phase reactions. Addition of simple ethers is an efficient method for producing a single phase. Ternary phase diagrams have been determined at 23°C for oil/methanol/ether mixtures; these are useful when applying the one-phase method across a wide range of conditions. Soybean, canola, palm, and coconut oils were used in combination with five ethers, namely, tetrahydrofuran (THF), 1,4-dioxane (DO), diethyl ether (DE), diisopropyl ether (DI), andtert-butyl methyl ether (TBM). All five ethers can produce miscibility for all methanol/oil compositions. The ether/methanol volumetric ratios required for miscibility at a methanol/soybean or canola oil volumetric ratio of 0.20 (5.4 molar ratio) at 23°C are: THF, 1.15; DO, 1.60; DE, 1.38 DI, 1.57; and TBM, 1.57. For THF, this results in one-phase mixtures that contain 65 vol% oil. Soybean and canola oil form identical diagrams. Palm oil requires slightly less ether at the lower methanol concentrations, but coconut oil requires considerably less across the whole concentration range. Acid-catalyzed reactions, when performed at the boiling point of the most volatile component, require less ether than predicted from the diagrams.     

Generating hydrogen-rich fuel-cell feeds from dimethyl ether (DME) using physical mixtures of a commercial Cu/Zn/Al2O3 catalyst and several solid–acid catalysts

Homogeneous physical mixtures containing a commercial Cu/ZnO/Al₂O₃ catalyst and a solid–acid catalyst were used to examine the acidity effects on dimethyl ether hydrolysis and their subsequent effects on dimethyl ether steam reforming (DME-SR). The acid catalysts used were zeolites Y [Si/Al = 2.5 and 15: denoted Y(Si/Al)], ZSM-5 [Si/Al = 15, 25, 40, and 140: denoted Z(Si/Al)] and other conventional catalyst supports (ZrO₂, and γ-Al₂O₃). The homogeneous physical mixtures contained equal amounts, by volume, of the solid–acid catalyst and the commercial Cu/ZnO/Al₂O₃ catalyst (BASF K3-110, denoted as K3). The steam reforming of dimethyl ether was carried out in an isothermal packed-bed reactor at ambient pressure.

The most promising physical mixtures for the low-temperature production of hydrogen from DME contained ZSM-5 as the solid–acid catalyst, with hydrogen yields exceeding 90% (T = 275 °C, S/C = 1.5, τ = 1.0 s and P = 0.78 atm) and hydrogen selectivities exceeding 94%, comparable to those observed for methanol steam reforming (MeOH-SR) over BASF K3-110, with values equaling 95% and 99%, respectively (T = 225 °C, S/C = 1.0, τ = 1.0 s and P = 0.78 atm). Large production rates of hydrogen were directly related to the type of acid catalyst used. The hydrogen production activity trend as a function of physical mixture was