Cu-Zn/HZSM-5催化剂上甲烷与丙烷的共活化

 研究了xCu-6%Zn/HZSM-5(x=0～0.9%)系列催化剂对甲烷和丙烷混合气体无氧芳构化反应的催化性能. 结果表明,在此系列催化剂上,丙烷促进了甲烷的活化,使之参与到芳烃的形成过程中. 在600 ℃和甲烷/丙烷摩尔比为1.0的条件下,0.7%Cu-6%Zn/HZSM-5催化剂表现出最佳活性,甲烷转化率达到36%,芳烃选择性达到85.7%. 这说明在Zn/HZSM-5中添加第二组分Cu有助于提高催化剂的活性和稳定性. 考察了反应时间和甲烷/丙烷摩尔比对甲烷和丙烷转化率及产物分布的影响. 13CH4同位素示踪实验发现13C进入到了C6H+6, C7H+8和C8H+10碎片中,这进一步证实甲烷参与了芳烃的形成.     

甲烷在6%Zn/HZSM-5催化剂上的低温转化 Catalytic Conversion of Methane at Low Temperature over 6%Zn/HZSM-5 Zeolite

 采用丙烷和甲烷混合物作为共反应物进行无氧芳构化反应. 在600 ℃,3000 h-1和甲烷/丙烷摩尔比为0.6的条件下,甲烷可以在6%Zn/HZSM-5分子筛催化剂上被有效地活化,甲烷的转化率可达32.4%,丙烷的转化率为89.5%,反应的主要产物为芳烃,其选择性达到89.7%. 甲烷与丙烷的摩尔比对芳烃产物的选择性有影响. 在没有丙烷参与时该催化剂在600 ℃下对甲烷转化没有活性. 推测是丙烷脱氢或裂解过程的中间产物活化了甲烷. 低碳烷烃对甲烷的活化可能是实现甲烷低温转化的一条有效途径.     

乙硼烷离子和自由基结构的量子化学研究

用B₃LYP/6-311G(d,p)密度泛函方法对B₂H₅⁺阳离子和B₂H₅^·自由基的几何异构体的空间构型进行了优化,并在此基础上用QCISD(T)/6-311++G(3df,2p)偶合簇法进行了单点能计算和零点能校正.结果表明,B₂H₅⁺单态有2种稳定的几何构型(D_3h,C₁),其中C₁构型是新发现的.B₂H₅⁺三重态阳离子除已知C_s构型外,又发现两种稳定构型(C₁).对于B₂H₅^·自由基体系,共有4种异构体(包括两种新发现的构型C_s),其中,具有单桥结构的C_2v最稳定.用二级多体微扰理论和密度泛函方法对前人所认为稳定的B₂H₅⁺单态的C_2v构型进行了全优化,结果发现该构型始终具有一个虚频,不是稳定构型.对B₂H₅^-阴离子体系的单态和三重态进行的全优化,理论上得出单态时具有C_2v和C_s两种稳定构型,而三重态只有C_2v一种稳定构型.     

阴离子插层镁铝水滑石结构及相互作用的理论研究

采用密度泛函理论(DFT)计算了MgAl-LDHs层板与无机阴离子(F^-、Cl^-、NO₃^-、CO₃^2-、SO₄^2-)和有机阴离子(水杨酸根离子([HO(C₆H₄)COO]^-)、苯甲酸根离子([(C₆H₅)COO]^-)、对二甲氨基苯甲酸根离子([p-(CH₃)₂N(C₆H₄)COO]^-)、十二烷基磺酸根离子[C₁₂H₂₅SO₃]^-、己烷基磺酸根离子[C₆H₁₃SO₃]^-、丙烷基磺酸根离子[C₃H₇SO₃]^-)间的相互作用,获得稳定超分子几何结构及相互作用能。层板主体与客体间存在较强的超分子作用,包括主客体间静电作用和氢键等。主、客体间相互作用能数值大小顺序为CO₃^2- > SO₄^2- > F^-> Cl^-> NO₃^-;[p-(CH₃)₂N(C₆H₄)COO]^-> [(C₆H₅)COO]^-> [HO(C₆H₄)COO]^-和[C₁₂H₂₅SO₃]^-> [C₆H₁₃SO₃]^- > [C₃H₇SO₃]^-。另外,还采用自然键轨道(NBO)计算和分析了LDHs 层板与阴离子间作用机理,从二阶微扰理论计算得到的稳定化能变化趋势与相互作用能数据基本吻合。     

激光烧蚀Al~+与乙醇团簇的反应研究

利用激光烧蚀-分子束法对Al等离子体与乙醇团簇的反应进行了研究.飞行时间质谱测得的主要反应产物有Al⁺(C₂H₅OH)_n (n=3～10)与H⁺(C₂H₅OH)_n (n=1～14)团簇正离子和(C₂H₅OH)_n(H₂O)OH^- (n=0～8)团簇负离子.实验发现,烧蚀产生的Al等离子体与脉冲分子束的不同位置反应,对团簇离子的类别、大小及强度分布均产生很大影响.Al等离子体与脉冲分子束的前段反应,主要产生金属-复合物团簇离子Al⁺(C₂H₅OH)_n,且信号较强;Al等离子体与脉冲分子束的中段及后段反应,主要产生质子化团簇离子H⁺(C₂H₅OH)_n和团簇负离子(C₂H₅OH)_n(H₂O)OH^-,同时还出现强度较小的其他水合团簇离子,如H⁺(H₂O)m(C₂H₅OH)_n (m=1～2)等.     

三种不同碳桥联双核茂钛配合物的合成及催化乙烯聚合研究

合成了3种不同结构的CnH₂n桥联双核茂钛配合物(CH₃)₂C[(C₅H₄)TiCl₂(C₅H₅)]₂(3),(CH₂)_n[(C₅H₄)TiCl₂(C₅H₅)]₂(6,n=3;7,n=4),并用1HNMR进行了表征.发现以甲苯为溶剂时,不仅提高了产率,而且有效地避免了副产物Cp₂TiCl₂的生成.研究了化合物7/MAO(甲基铝氧烷)催化乙烯聚合的反应,考察了反应条件对催化体系的影响.结果表明,催化活性随着n(Al)/n(Cat.)比的增大而提高,聚乙烯的分子量在n(Al)/n(Cat.)=500和50℃时达到最高值9.0102×10⁴;随着聚合时间的延长,催化活性下降,而产物分子量不断升高;随着温度的上升,50℃时催化活性和聚乙烯的分子量最高,分别为2.4074×10⁵gPE/(molTi·h)和6.8679×10⁴.随着桥联双核茂钛配合物碳桥的增长,催化活性增加,所得聚乙烯的分子量降低.     

多环芳烃与不饱和自由基氢提取反应类的动力学研究

对2~6个环的多环芳烃的氢提取反应类进行了系统研究, 提取氢原子的不饱和自由基包括丙炔基自由基（C₃H₃）、 烯丙基自由基（C₃H₅）、 丁二烯基自由基（nC₄H₅, iC₄H₅）、 环戊二烯基自由基（C₅H₅）以及苯基自由基（C₆H₅）. 采用M06-2X/cc-pVTZ方法得到了多环芳烃的电子结构信息, 利用过渡态理论并结合Eckart隧道校正, 计算了所有反应在500~2500 K范围内的反应速率常数.考察了多环芳烃的大小、 结构对反应速率常数的影响, 对比了不同氢提取自由基及不同氢提取反应类型的速率常数. 结果表明, 多环芳烃的大小对反应速率常数影响不大, 但是多环芳烃的环结构对反应速率常数影响较大. 将不同的氢提取反应类简化为发生在五元环上的C₅类和发生在六元环上的C₆类两类, 结果表明, C₆类的反应活性高于C₅类. 研究了nC₄H₅, iC₄H₅以及C₆H₅自由基与多环芳烃的氢提取反应, 它们的氢提取反应活性大小顺序为C₆H₅>nC₄H₅>iC₄H₅. 通过对每类典型反应的速率常数取平均值, 总结出相应类型的速率规则, 可用于构建多环芳烃和碳烟机理.     

Cu/WO3-TiO2光催化剂上丙烯和二氧化碳合成MAA反应性能

研究了Cu/WO₃-TiO₂对CO₂和C₃H₆的吸附特性和光催化性能.结果表明,在Cu/WO₃-TiO₂催化剂表面存在金属位Cu,Lewis酸位W⁶⁺和Ti⁴⁺以及Lewis碱位W-O-Ti的桥氧和WO的端氧三类活性中心;在金属位Cu和Lewis酸位Ti⁴⁺(或W⁶⁺)的协同作用下,CO₂形成活性较高的卧式吸附态Cu-(CO)-O→Ti⁴⁺(或W⁶⁺),C₃H₆的β-H和β-C分别吸附在Lewis碱位WO与金属位Cu上,形成Cu-(CH₂)C(CH₃)-H→OW吸附态;Cu/WO₃-TiO₂催化剂吸收阈值蓝移和光吸收量的提高均有利于其催化活性的提高,担载质量分数为10%的WO₃光催化剂的催化活性优于其它含量的催化剂,光量子效率最高(19.7%);在383K,0.1MPa,空速200h^-1和125W紫外灯辐照下,C₃H₆转化率为7.4%,甲基丙烯酸(MAA)的选择性超过95%.根据实验结果提出了光促表面催化合成反应的机理.     

Al+与乙硫醇团簇的气相化学反应的实验和理论研究

利用激光溅射-分子束的方法研究了Al⁺和乙硫醇的气相化学反应,结果观察到了Al⁺与1～6个乙硫醇分子形成的团簇离子. 对团簇离子进行了密度泛函理论计算,找到了两种类型的异构体Al⁺(C₂H₅SH)_n和HAl⁺SC₂H₅(C₂H₅SH)_n-1,计算得到了相应的稳定结构和能量.分析质谱信号强度,结合理论计算结果,可推测出实验得到的n=1的产物离子是Al⁺(C₂H₅SH). n=2和3时产物离子开始转变为HAl⁺SC₂H₅(C₂H₅SH)_n-1, n=4时,HAl⁺SC₂H₅(C₂H₅SH)₃和Al⁺(C₂H₅SH)₄两种产物离子都存在,n≥5以后,团簇离子Al⁺(C₂H₅SH)_n开始成为主要的产物离子.     

Ih对称性硼、碳原子簇化合物的从头计算(Ⅱ)─C12B20、C12B20H32的电子结构及稳定性

用价轨道双ζ型基,在B₃₂H₃₂^2-等研究的基础上继续对C₁₂B₂₀、C₁₂B₂₀H₃₂及其正离子进行从头计算,并对照C₂B₃₀、B₃₂和B₃₂H₃₂^2-的计算结果讨论其成键特性、稳定性及得电子反应活性。     

Aromatization of methane by using propane as co-reactant over cobalt and zinc-impregnated HZSM-5 catalysts

The activities of the cobalt and zinc-impregnated HZSM-5 catalysts to the non-oxidative conversion of propane (C3) and methane (C1) into aromatic hydrocarbons were evaluated using a fixed-bed microreactor. C1 conversion reached 36.7% and the selectivity of aromatic products reached above 88.7% at atmospheric pressure, weight (hourly) space velocity (WHSV) 1.6 g h⁻¹/(g cat)⁻¹ and 873 K. The influence of the acidity and the ratio of cobalt in the catalyst on the conversion of methane and propane was evaluated. C1 incorporation was conclusively confirmed by the mass spectral analyses of aromatic products produced in a run with ¹³CH₄ which shows a significant ¹³C enrichment in the C₆H₆⁺, C₇H₈⁺ and C₈H₁₀⁺ fragments. The methane activation could result from its hydrogen-transfer reaction with alkenes. These catalysts were thoroughly characterized using XRD, N₂ adsorption measurements, TPD of NH₃, and FT-IR. The results showed that the activation of methane in low temperature was due to existence of propane. The acidic changes and micropore area of the catalyst severely affected aromatization, and resulted in drastic modifications in product distribution. From this work, we found that only a small fraction of tetrahedral framework aluminum, which corresponds to the Bronsted acid sites, is sufficient to accomplish the aromatization of the intermediates in methane and propane aromatic reaction, while the superfluous strong Bronsted acid sites, which can be decreased by adding Co and Zn, are showed to be related with the aromatic carbonaceous deposits on the catalysts. The density of acidic site and the strength of strong acid decreased when the concentration of Co and Zn in the catalyst increased. Therefore, a much higher benzene yield and a longer durability of the catalysts are obtained when compared with the conventional HZSM-5 catalysts.     

Non-Oxidative Aromatization of CH4-C_3H_8 over La-Promoted Zn/HZSM-5 Catalysts

The non-oxidative aromatization of mixed CH4 with C3H8 over La-promoted Zn/HZSM-5 catalysts was studied in a fixed-bed reactor at 823 K with space velocity 600 h-1 and CH4/C3H8 (mol ratio)=5:1. The propane conversion and the aromatic selectivities were up to 99% and 60% over the catalyst respectively, while methane conversion had an induction period with the highest conversion of 30%. The structure and surface acidity of the catalysts were characterized by XRD, NH3-TPD and TG-DTA. The influences of reaction and regenerative conditions on the activity and selectivity were also investigated.     

Non-oxidative dehydro-oligomerization of methane to higher molecular weight hydrocarbons at low temperatures

The non-oxidative dehydro-oligomerization of methane to higher molecular weight hydrocarbons such as aroma tics and C2 hydrocarbons in a low temperature range of 773-973 K with Mo/HZSM-5,Mo-Zr/HZSM-5 and Mo-W/HZSM-5 catalysts is studied.The means for enhancing the activity and stability of the Mo-containing catalysts under the reaction conditions is reported.Quite a stable methane conversion rate of over 10% with a high selectivity to the higher hydrocarbons has been obtained at a temperature of 973 K.Pure methane conversions of about 5.2% and 2.0% have been obtained at 923 and 873 K,respectively.In addition,accompanied by the C2-C3 mixture,tht- methane reaction can be initiated even at a lower temperature and the conversion rate of methane is enhanced by the presence of tne initiator of C2-C3 hydrocarbons.Compared with methane oxidative coupling to ethylene,the novel way for methane transformation is significant and reasonable for its lower reaction temperatures and high selectivity to the desired prod     

Non-oxidative aromatization of C1 to C3 hydrocarbons over Pd-promoted Ga/HZSM-5 catalyst under mild conditions

The Pd-promoted Ga/HZSM-5 catalyst was prepared by impregnation method and its catalytic activity for non-oxidativearomatization of C1 to C3 hydrocarbons was assessed using a microreactor-GC system operated with temperature at 823 K andspace velocity at 410 h1.The catalyst is more catalytically active for methane conversion than Ga/HZSM-5.The massspectroscopy analyses confirmed that13CH4 was converted to aromatic products.     

Ni整体型催化剂大空速甲烷自热氧化制合成气

随着石油资源的逐渐减少,天然气将是未来基本化学品的主要碳源.因此,天然气的开发利用已日益受到世界范围的广泛重视.当前,天然气的化工利用主要是用于生产合成气,再由合成气制取大量化学品,如合成氨、甲醇和烃类等.目前,工业上生产合成气主要采用水蒸气催化重整工艺.     

Methane direct conversion to aromatic hydrocarbons at low reaction temperature

Conversion of pure methane and natural gas with different methane purity to aromatic hydrocarbons at. 773 and 873 K have been investigated. Conversion of methane to aromatics under non-oxidizing conditions can be initiated by higher hydrocarbon mixtures in the feed and, some special coke deposited on Mo/HZSM-5 catalyst at lower reaction temperature. Methane conversion of about 10–20% is obtained at 773 K. The possible reaction mechanism and product phase transformation process for conversion of pure methane and natural gas at lower temperature are proposed. The thermodynamic limitation for methane conversion under non-oxidizing conditions may be circumvented.     

Low-temperature activation of methane over rare earth metals promoted Zn/HZSM-5 zeolite catalysts in the presence of ethylene

At low temperature of 723 K, methane can be easily activated in the presence of ethylene in the feed, and converted to higher hydrocarbons (C2–C4) and aromatics (C6–C10), through its reaction over rare metals modified Zn/HZSM-5 zeolite catalysts without undesirable carbon oxides formation. Methane can get 37.3% conversion over the above catalysts under low temperature, and the catalysts show a longer lifetime than usual metal supported HZSM-5 zeolite catalysts without adding any rare earth metals. The effects of methane activation over various rare earth metal promoted Zn/HZSM-5 catalysts on the products and influences of several reaction conditions such as temperature, catalyst lifetime and molar ratio of CH4/C2H4 have been discussed.     

Catalytic Oxidation of Methane by Nitrous Oxide on H[Al]ZSM-5 Zeolite, Silicalite, and Amorphous SiO2 Modified by Iron, Silver, and Gadolinium Ions

Methane oxidation by an excess of N₂O on the catalytic sites formed in HZSM-5 zeolite, silicalite, and SiO₂ after modification with iron, silver, and gadolinium cations in different combinations is studied. Introduction of iron and silver ions into H[Al]ZSM-5 zeolite is shown to result in the formation of the sites that are active in methane oxidation, while the systems obtained on the basis of crystalline silicalite or amorphous SiO₂ demonstrate poor or no catalytic activity, respectively. Complete oxidation of methane with 100% conversion is observed on the Fe/HZSM-5 and Ag/HZSM-5 catalysts at temperatures higher than 350 and 450°C, respectively. A decrease in the reaction temperature and in the methane conversion is accompanied by coking of the catalysts and, in the case of Fe/HZSM-5, by the appearance of trace amounts of methanol and formic acid in the gas phase. The temperature dependence of the activity and selectivity for the Ag/HZSM-5 and (Ag + Gd)/HZSM-5 catalysts exhibits a pronounced hysteresis at 330–480°C, and the formation of coke proceeds much faster than in the case of iron-containing samples. Catalytic properties of (Fe + Ag)/HZSM-5 are similar to those of Fe/HZSM-5. The introduction of Gd does not influence significantly the activity and selectivity of the catalysts. ESR and TG–DTA were used to determine the state and distribution of Fe, Ag, and Gd in the samples and to examine the processes of coke formation.     

Bifunctional catalysis of Mo/HZSM-5 in the dehydroaromatization of methane with CO/CO2 to benzene and naphthalene

The catalytic dehydrocondensation of methane to aromatics such as benzene and naphthalene was studied on the Mo carbide catalysts supported on micro- and mesoporous materials such as HZSM-5 (0.6 nm) and FSM-16 (2.7 nm). The Mo catalysts supported on H-ZSM-5 having appropriate micropores (0.6 nm size) and Si/Al ratios (20-70) exhibit higher yields (90-150 nmol/g-cat/s) and selectivities (higher than 74% on the carbon basis) in methane conversion to aromatic products such as benzene and naphthalene at 973 K and 1 atm, although they are drastically deactivated because of substantial coke formation. It was demonstrated that the CO/CO₂ addition to methane effectively improves the catalyst performance by keeping a higher methane conversion and selectivities of benzene formation in the prolonged time-on-stream. The oxygen derived from CO and CO₂ dissociation suppresses polycondensation of aromatic products and coke formation in the course of methane conversion. XAFS and TG/DTA/mass-spectrometric studies reveal that the zeolite-supported Mo oxide is endothermally converted under the action of methane around 955 K to nanosized particles of molybdenum carbide (Mo₂C) (Mo-C, coordination number = 1,R- 2.09 å; Mo-Mo, coordination number = 2.3–3.5;R = 2.98 å). The SEM pictures showed that the nanostructured Mo carbide particles are highly dispersed on and inside the HZSM-5 crystals. On the other hand, it was demonstrated by IR measurements of pyridine adsorption that the Mo/HZSM-5 catalysts having the optimum SiO₂/Al₂O₃ ratios around 40 show the maximum Brönsted acidity among the catalysts with the SiO₂/Al₂O₃ ratios of 20–1900. There is a close correlation between the activity of benzene formation in the methane aromatization and the Brönsted acidity of HZSM-5 due to the bifunctional catalysis.     

强酸促进的W/HZSM-5基催化剂上甲烷非氧化脱氢芳构化

甲烷非氧化催化脱氢芳构化制芳烃是近年来甲烷优化利用的新研究方向之一"－'．迄今已报道的催化剂多为以HZSM－5分子筛为载体的过渡金属（如Pd、I't、Re和MO等）氧化物,其中以改进型的MO／HZSM－5基催化剂效果最佳［'－'j．按化学反应计量式6CH。--C6H。＋gH;进行热力学计算,结果表明：在773K温度下,甲烷平衡转化率（KC。。。,衡）仅为卫·8％;在叮3K和】023K时,xCH。平。分别为】1·3％和15·8％;若使Xo。。,Y＆达25％以上,则要求反应温度不低于1123K（在1123K和1173K时,XCH。,y＆分别为27·2％和33·196）·然…