SULFUR RECOVERY WITH REDUCED EMISSIONS, LOW CAPITAL INVESTMENT AND HYDROGEN CO-PRODUCTION

The main disadvantage of the Claus process is that by introducing air as oxidant a large volume of tail gas is produced. This must be treated to reduce atmospheric emissions of sulfur-containing gases. The costs of the tail-gas unit are a significant fraction of the total capital and operating costs for sulfur recovery. A new process uses thermal decomposition of hydrogen sulfide in the presence of carbon dioxide instead of air oxidation. The products of this reaction are hydrogen, carbon monoxide, elemental sulfur, water vapor and carbonyl sulfide. Carbonyl sulfide is easily converted to H₂S and C0₂ by liquid- or vapor-phase hydrolysis. Unreacted H₂S and C0₂ are recovered by absorption and recycled to the reactor. Since no air is introduced, there is no tail gas and the tail-gas unit is eliminated, giving a substantial reduction in capital investment. The concentrations of sulfur-containing gases in the product streams depend only on the operation of the absorber and stripper units and can be controlled to very low levels by increasing stripper boil-up. Process operating costs depend on the level of sulfur recovery required and can also be much lower than those of the modified Claus Process.

The process chemistry depends on a shift in the equilibrium of H₂S decomposition caused by reaction of hydrogen with C0₂ by the reverse of the water-gas-shift reaction. Catalysts for this chemistry have been identified. Reactor conversion is further improved by rapid cooling of the reactor effluent gas. Other aspects of process design and operation confer further advantages with respect to the Claus process; however, the process equipment used is similar to that used in a Claus plant. Retrofit of existing plant to the new technology can therefore be considered.     

Sintering of Pt/Al2O3 reforming catalysts: EXAFS study of the behavior of metal particles under oxidizing atmosphere

The effect of an oxidative atmosphere (300 °C) is studied on fresh and sintered unchlorinated naphtha reforming catalysts containing 0.6–1% Pt. The TPR profiles show that only one species is formed using our experimental conditions, regardless of the mean crystallite size of the metal particles. The structural information supplied by EXAFS compared with cuboctahedral particle modeling, implies that such species is a surface platinum oxide, the structure of which is close to that of PtO₂, but largely distorted. This is true whether the catalyst is sintered or not.     

多孔TiO2陶瓷光催化剂降解糠醛废水

以钛酸四丁酯等为原料，采用简单工艺制得多孔TiO2陶瓷光催化剂；并研究了利用多孔TiO2陶瓷光催化降解糠醛废水。结果表明，在紫外灯下照射60min，糖醛废水的COD去除率可达59．8％，而通入空气有利于污染物的去除。     

2-乙氧基丙烯的合成

介绍了2-乙氧基丙烯(EPP)的用途及合成方法，采用自制催化剂由2，2-二乙氧基丙烷(DEP)合成2-乙氧基丙烯．总收率达到84．5％。     

5—烃基—2,3—二甲基吡嗪的合成

2,3-二基-5,6-二氢吡嗪与醛或酮在氢氧化钠的乙醇溶液中反应制得16种5-烃基-2,3-二甲基吡嗪。产率66%～90%。其中6种为新合成的化合物。产率17%～87.9%。     

有机过氧化物对CPE硫化性能的影响

采用DCP或双2，5硫化CPE，通过改变硫化时间，研究CPE的硫化过程及性能。发现DCP对CPE的硫化速度快、硫化胶的物理机械性能好，但易使硫化胶产生异味；使用双2，5作硫化剂，则不产生异味，但其硫化速度较慢，双2，5的用量一般在4～4．5份之间为宜。     

2-羟丙基三甲基氯化铵壳聚糖的制备及其表征

以脱乙酰度为90%的壳聚糖(CTS)为原料,异丙醇为溶剂,w(NaOH)=40 0%的水溶液为催化剂,3 氯 2 羟丙基三甲基氯化铵(CTA)为改性剂,在m(NaOH)∶m(CTS)=1 0∶1 0,m(CTA)∶m(CTS)=4 0∶1 0,反应温度65 0℃下制备了2 羟丙基三甲基氯化铵壳聚糖(HTCC)。实验结果表明,在反应时间达到或超过9 0h时,得到的HTCC产品的接枝度超过90 0%,在pH=6 7～7 0的水中可完全溶解形成w(HTCC)=3 0%的溶液。IR和1HNMR的结果表明,接枝反应主要发生在CTS的氨基上。     

国外过氧化氢在化学合成中应用研究进展

介绍了近期国外过氧化氢在部分化学品合成中应用研究新进展 ,产品包括过碳酸钠、过碳酰胺、4Na2 SO4·2H2 O2 ·NaCl加合物、叔胺氧化物、水合肼、二羟基苯、季铵盐过氧化氢和甲乙酮肟。内容涉及产品质量 (纯度、安定性、溶解速率、外观等 )、产品收率、催化剂、工艺过程等方面改进。主要介绍专利技术。     

缩醛法合成1,1-二甲氧基丙酮

1,1-二甲氧基丙酮是一种重要有机中间体,本文采用缩醛化反应,以丙酮醛为原料,与甲醇在浓硫酸催化作用下合成1,1-二甲氧基丙酮,反应较佳条件为浓硫酸:丙酮醛:甲醇=0.03:1:7(摩尔比),反应温度为65℃.     

SO_4~(2-)/TiO_2-MoO_3催化合成己二酸二丁酯

以固体超强酸SO2 -4/TiO2 MoO3 为催化剂 ,通过己二酸和正丁醇反应合成了己二酸二丁酯 ,并探讨了诸因素对产率的影响。正交实验结果表明 :SO2 -4/TiO2 MoO3 具有良好的催化活性 ,醇酸物质的量比为 6∶1,催化剂用量为反应物料总质量的 3.3% ,反应时间 1.5h ,反应温度 10 6～ 10 9℃ ,酯收率可达 77.6 %。