L'éthanol est converti, à 350°C sous 30 bar et sur des zéolithes protoniques, en un mélange de paraffines légères et d'aromatiques ; produits incorporables dans le pool essence. Cependant, la transformation de EtOH sur zéolithes acides conduit à la formation du coke. Des techniques physiques avancées, en particulier les techniques MALDI et LDI-TOF MS, couplées à la méthode d'analyse qui consiste à récupérer dans un solvant les molécules carbonées après dissolution de la zéolithe dans HF, contribuent à caractériser finement le coke. Sa composition dépend du catalyseur : sur HBEA(11), zéolithe à larges pores, 17 familles ont été détectées contre 4 sur HZSM-5(40) de taille de pore intermédiaire. Sur cette dernière, le coke, composé de polyalkybenzènes / naphtalènes / phénalènes et pyrènes, est localisé à l'intersection des canaux et a une toxicité vis-à-vis des sites acides de Brønsted de 1. En dépit d'un empoisonnement total, cette zéolithe est toujours capable de convertir EtOH, comme MeOH, en hydrocarbures et qui plus est avec les mêmes sélectivités en produits. La transformation de ces deux alcools ne s'explique pas par un mécanisme classique de catalyse acide, mais par un mécanisme concerté radicalaire-acide. La présence d'un inhibiteur de radicaux dans la charge réactionnelle, l'hydroquinone, provoque une désactivation immédiate et une diminution de la concentration des radicaux. La transformation de EtOH et MeOH passe par un intermédiaire réactionnel commun, le carbène :CH2, dont l'oligomérisation radicalaire conduit à la formation d'oléfines. Ces oléfines légères (n-O3-n-O5) sont très réactives et se transforment par catalyse acide (oligomérisation / cyclisation / t / Ethanol is converted into light paraffins and aromatics mixture at 350°C under 30 bar over protonic zeolites. These products can be incorporated in the gasoline pool. Nevertheless, EtOH transformation over acid zeolites leads to the formation of the coke. Advanced physical techniques, in particular MALDI and LDI-TOF MS, were coupled to the coke analysis method. This method consists of the recovery of the carbonaceous molecules in a solvent after zeolite dissolution in hydrofluoric acid solution. This coupling allows characterizing the coke through an extensive way. The coke composition depends on the catalyst morphology: over HBEA(11) zeolite of large pores, 17 families were detected while 4 over HZSM-5(40) of intermediate pore size. Over this latter, the coke, composed of polyalkylbenzenes/naphtalenes/phenalenes and pyrenes, is located in the channels intersections and has toxicity of 1 towards Brønsted acid sites. In spite of a total poisoning, HZSM-5 zeolite is always able to convert EtOH, like MeOH, into hydrocarbons with the same products selectivity. The transformation of the two alcohols cannot be explained by a classical mechanism of acid catalysis, but by a cooperative radical-acid mechanism. The presence of a radical inhibitor in the feed, the hydroquinone, causes an immediate deactivation and a decrease in the concentration of radicals. The transformation of EtOH and MeOH passed by the common reaction intermediate, the :CH2 carbene, which its radical oligomerization leads to the formation of olefins. Olefins (n-O3-n-O5) are very active and can be transformed through acid catalysis (oligomerization/cyclisation/Hydrogen transfer) into aromatics or undergo isomer

Doctor Educationis / The research focused on the synthesis, characterisation and activity of zeolite supported metal catalysts for the Friedel-Crafts alkylation of benzene with t-butyl chloride. Alkyl benzenes are traditionally produced via systems that employ the use of Lewis acids or strong mineral acids. There have been widespread concerns over these approaches based on their environmental impacts and separation difficulties. Recent approaches have endeavoured the much to use more environmentally eco-friendly systems and zeolites have proved to be versatile support materials. The use of zeolites has also shown to greatly improve product selectivity as well as easing separation constraints. However the adoption of zeolites on large scale Friedel-Crafts alkylation has been hampered by the high cost of zeolite production from commercial sources. On the other hand fly ash has been found to be a viable starting material for zeolite synthesis. Apart from that South Africa is faced with fly disposal challenges and there is continual accumulation of fly ash at the coal fired power stations, which provide about 77 % of the power produced in the country. In this light the use of fly ash will help to reduce the disposal constraints as well as providing a cheap starting material for zeolite synthesis. In this study the hierarchical Zeolite X has been successfully synthesised from fly ash via a hydrothermal treatment. The zeolite was then loaded with Fe/Mn via two approaches namely liquid phase ion exchange and incipient wetness impregnation. For comparison purposes seasoned commercial support materials namely HBEA and MCM- 41 were also loaded with the same metals and characterised with various techniques namely; HRSEM, EDS, HRTEM, XRD, SAED, ICP-OES and N2 adsorption analysis, It was found from the characterisation undertaken that the integrity of the respective supports was generally retained upon metal loading. Both the ICP-OES and the EDS proved that the desired metals were successfully introduced onto the zeolitic support materials. The calculated percentage metal loading for the catalysts prepared via incipient wetness impregnation was closely related to the actual values obtained from the ICP-OES analysis for both the monometallic and the bimetallic catalysts (Fe/Mn). It was observed that the amount of metal that can be introduced on a zeolite via liquid phase ion exchange is largely dependent on the cation exchange capacity of the zeolite Supported metal catalysts for FC alkylation Page v and of the catalysts prepared using 0.25 M Fe solution it was found that Zeolite X had the highest Fe wt% loading of 11.4 %, with the lowest loading of 2.2 % obtained with the MCM-41 supported catalyst. The XRD patterns for the both HBEA and the MCM-41 supported metal catalysts resembled the patterns of the respective prestine support materials except in the case of catalysts with anFe wt % of more than 10, which exhibited peaks due to the Fe2O3 crystallites. In the case of the hierarchical Zeolite X, the metal loaded support had a significant reduction in the XRD peak intensities. The prepared catalysts were tested for the alkylation of benzene with t-butyl chloride. The benzene was also used as the solvent. The alkylation reaction was carried out in a round bottomed flask under reflux conditions and stirring at a temperature of 45 oC over a period of 5 h. A total of 18 catalysts was tested and the highest percentage conversion of 100 % was obtained with the 10%FeH after a reaction time of 2 h. The general trend obtained with the majority of the catalysts was characterised with a rapid initial increase and then steady state was achieved. Generally after a reaction time of 3 h almost all the catalysts had reached steady state in terms of the percentage conversion obtained. The outcomes reflect that the inclusion of Mn does not enhance the conversion but rather decreases it. It was also found that the Mn was not active in the alkylation of benzene as shown by the inactivity of the 10%MnM, where 10% by weight Mn was loaded on MCM-41. However the other monometallic catalysts containing Mn supported on Zeolite X and HBEA were found to be active. The activity is attributed to the presence of Brønsted acid sites in these zeolites which are not present in MCM-41. The selectivity studies reflect that the inclusion of Mn does slightly improve the selectivity towards the formation of the monoalkylated product (t-butyl benzene). The highest selectivity of 91.1 % was obtained with the 10%FeMnM after a reaction time of 4 h. MCM-41 supported catalysts had a relatively higher selectivity compared to the other supports. Considering the Fe monometallic catalysts tested it generally can be said that the yield were in the order HBEA > MCM-41 > Zeolite X. It however should be noted that the percentage yield is calculated from the conversion and selectivity percentages, this implies that the factors affecting these parameters will consequently affect the percentage yield obtained. Supported metal catalysts for FC alkylation Page vi The alkylation reaction was found to be characterised by the formation of two intermediate products which could not be identified. These products were formed during the transient start up stages of the reaction and would disappear from the reaction mixture with longer reaction times, and after 3 h in almost all the reactions studied the intermediates were not detected in the reaction mixture. The main products found were the monoalkylated product (desired product) and the para isomer (1,4-t-di-butyl benzene). There were no other dialkylated isomers or trialkylated products detected. The formation of the para isomer was usually after a reaction time of 2 h in most reactions. The research managed to show that the hierarchical Zeolites X can be synthesised from fly ash and ion exchange and incipient wetness impregnation are appropriate approaches that can be used to introduce Fe/Mn onto the support materials studied. The catalysts prepared were active to varying degrees in the Friedel-Crafts alkylation of benzene with t-butylchloride, with the exception of the 10%MnM which was found to be inactive.