γ-Al2O3 supported Co-W based catalysts with varying Co (1 - 3 wt %) and W (7 - 13 wt %) loadings were prepared using impregnation and sonochemical methods. All prepared catalysts were characterized with elemental analysis, BET analysis, X-ray diffraction (XRD), NH3 temperature programmed desorption (TPD), temperature programmed reduction (TPR) and thermogravimetry analysis (TGA). <p>The performances of all the synthesized catalysts were tested at a pressure of 8.9 MPa, LHSV of 2 h-1 and temperatures of 340, 350 and 360 °C in a laboratory trickle bed microreactor for hydrodesulphurization (HDS) and hydrodenitrogenation (HDN) of light gas oil (LGO) derived from Athabasca bitumen. The performance tests with impregnated catalysts indicated a maximum in activity for HDS and HDN reactions (sulfur and nitrogen conversions at 93.0 and 57.1 % at 360 °C) for Co(3 wt %)-W(10 wt %)/γ-Al2O3 whereas the performance tests with sonochemically prepared catalysts showed a maximum in activity (sulfur and nitrogen conversions at 87.9 and 42.5 % at 360 °C) for Co(3 wt %)-W(11.5 wt %)/ γ-Al2O3. These two catalysts were selected for detail performance, optimization and kinetic studies. The effects of reaction temperature (340 - 380 °C), pressure (7.6 - 10.3 MPa), liquid hourly space velocity (1.5 - 2.0 h-1) and hydrogen gas/gas oil ratio (400 - 800 mL/mL) were examined on HDS and HDN of LGO with these catalysts. The reaction kinetics for HDS was best fitted with a Power Law model whereas same for HDN was found to be best represented by a Langmuir-Hinshelwood model with a reasonable accuracy (0.90 <R2 <0.95). The activation energy for HDS of LGO were 14 and 12 kJ/mol for selected impregnated and sonochemically prepared catalysts whereas the same for HDN were 9 and 14 kJ/mol for these catalysts, respectively. Calculation showed that the fitted HDS rate expressions were apparent and HDN rate expressions were intrinsic under existing reaction conditions. It also showed that the pore diffusion resistances for both HDS and HDN increased with an increase in reaction temperature from 340 to 380 °C.

γ-Al2O3 supported Co-W based catalysts with varying Co (1 - 3 wt %) and W (7 - 13 wt %) loadings were prepared using impregnation and sonochemical methods. All prepared catalysts were characterized with elemental analysis, BET analysis, X-ray diffraction (XRD), NH3 temperature programmed desorption (TPD), temperature programmed reduction (TPR) and thermogravimetry analysis (TGA). <p>The performances of all the synthesized catalysts were tested at a pressure of 8.9 MPa, LHSV of 2 h-1 and temperatures of 340, 350 and 360 °C in a laboratory trickle bed microreactor for hydrodesulphurization (HDS) and hydrodenitrogenation (HDN) of light gas oil (LGO) derived from Athabasca bitumen. The performance tests with impregnated catalysts indicated a maximum in activity for HDS and HDN reactions (sulfur and nitrogen conversions at 93.0 and 57.1 % at 360 °C) for Co(3 wt %)-W(10 wt %)/γ-Al2O3 whereas the performance tests with sonochemically prepared catalysts showed a maximum in activity (sulfur and nitrogen conversions at 87.9 and 42.5 % at 360 °C) for Co(3 wt %)-W(11.5 wt %)/ γ-Al2O3. These two catalysts were selected for detail performance, optimization and kinetic studies. The effects of reaction temperature (340 - 380 °C), pressure (7.6 - 10.3 MPa), liquid hourly space velocity (1.5 - 2.0 h-1) and hydrogen gas/gas oil ratio (400 - 800 mL/mL) were examined on HDS and HDN of LGO with these catalysts. The reaction kinetics for HDS was best fitted with a Power Law model whereas same for HDN was found to be best represented by a Langmuir-Hinshelwood model with a reasonable accuracy (0.90 <R2 <0.95). The activation energy for HDS of LGO were 14 and 12 kJ/mol for selected impregnated and sonochemically prepared catalysts whereas the same for HDN were 9 and 14 kJ/mol for these catalysts, respectively. Calculation showed that the fitted HDS rate expressions were apparent and HDN rate expressions were intrinsic under existing reaction conditions. It also showed that the pore diffusion resistances for both HDS and HDN increased with an increase in reaction temperature from 340 to 380 °C.

In China, the textile industry is important for the economy. However, the industry contributes to emissions of organic material and other pollutants. This affects the environment and the quality of life for people and animals. All over the world, water scarcity is becoming an increasing problem, which is why the UN has water purification as one of the goals for sustainable development. To achieve these goals and the regulations in countries, wastewater is purified in water treatment plants before it is discharged. One of the methods that can be used to purify water is catalytic ozonation, an oxidation process in which ozone is used as an oxidant to break down organic material. Catalysts, usually metal oxides, are used to increase the selectivity and the reaction rate. However, this is a relatively unexplored area in water purification and several details within the process are unknown, such as optimal conditions for various catalysts and the exact reaction mechanism. In this work, catalytic ozonation treatment with the metal oxide MnOx-CeOx/γ-Al2O3 has been investigated. Firstly, a literature study was carried out to find earlier research in the field. Then experiments were conducted, varying four different factors and the impact these factors had on the catalytic ozonation was analyzed. The factors examined were contact time, ozone dosage, gas flow and amount of catalyst. All factors had three different levels. COD and UV254 were analyzed to find the conditions that gave the highest reduction of organic matter. The highest reduction of COD was 67 % which gave a COD concentration of 23 mg/L and UV254 90 %. Since the regulations on COD emissions in China are 30 mg/L, the catalytic ozonation gave a satisfying result. The result showed that the highest yield was achieved at the highest level for contact time (40 min), ozone dosage (0.3 mg/L) and amount of catalyst (100 % filled reactor), but the second highest for the gas flow (0.3 L/min). However, the contact time was calculated to be the only significant factor for reducing COD in water. The other factors did not have a significant effect on the reduction of COD or UV254. Furthermore, the conditions that were calculated to give the greatest reduction were used to analyse the reduction of impurities in the wastewater with three dimensional fluorescence. Three dimensional fluorescence showed that the wastewater contained organic compounds, mainly aromatic proteins, soluble microbial by-products and humic acids. All of these compounds were reduced during the catalytic ozonation with MnOx-CeOx/ γ-Al2O3. The residual amount of ozone was analyzed in effluent gas flow was measured with different incoming gas flows. The residual ozone after the ozone treatment was approximately 45 % of the ingoing gas flow. / I Kina är textilindustrin viktig för ekonomin. Dock bidrar industrin till utsläpp av organiskt material och andra föroreningar. Detta påverkar miljön och livskvalitén för människor och djur. Världen över börjar vattenbrist bli ett allt större problem, varför FN har med vattenrening som ett av målen för hållbar utveckling. För att nå dessa mål och de regleringar som gäller renas avloppsvatten i vattenreningsanläggningar innan det släpps ut. En av de metoder som kan användas för att rena vattnet är katalytisk ozonbehandling, vilket är en oxidationsprocess där ozon används som oxidationsmedel för att bryta ned organiskt material. För att öka selektiviteten och reaktionshastigheten används katalysatorer, vanligen metalloxider. Detta är dock ett relativt outforskat område inom vattenrening och flera detaljer inom processen är okända, såsom optimala betingelser och reaktionsmekanismen. I detta arbete har därför katalytisk ozonbehandling med metalloxiden MnOx-CeOx/ γ-Al2O3 undersökts. Först utfördes en litteraturstudie för att ta fram tidigare forskning inom området. Därefter utfördes experiment där fyra olika faktorers påverkan på den katalytiska ozonbehandlingen analyserades. De faktorer som undersöktes var uppehållstid, ozondosering, gasflöde och mängd katalysator. Samtliga faktorer hade tre olika nivåer. De faktorer som analyserades var COD och UV254 för att hitta de förhållanden som gav högst reduktion av organiskt material. Den högsta reduktionen av COD var 67 %, vilket gav en COD-koncentration på 23 mg/L och UV254 reducerades upp till 90 %. Eftersom gränsen på COD-utsläpp i Kina är 30 mg / L gav den katalytiska ozonbehandlingen ett tillfredsställande resultat. Det nivåer som gav bäst utbyte var de högsta för uppehållstiden (40 min), ozondoseringen (0.3 mg/L) och mängden katalysator (100 % fylld reaktor), men den näst högsta för gasflödet (0.3 L/min). Den enda faktorn som hade en signifikant påverkan på reduktionen av organiskt material var dock uppehållstiden. Övriga faktorer hade ingen signifikant påverkan på varken reduktionen av COD eller UV254. Vidare användes ändå de nivåer som beräknats ge störst reduktion av organiskt material för att analysera reduktionen av föroreningar i avloppsvattnet med tredimensionell fluorescens. Avloppsvattnet innehåller organiskt material som aromatiska proteiner, lösliga mikrobiella biprodukter och humussyror och dessa föroreningar reducerades vid katalytiska ozonbehandlingen med MnOx-CeOx/ γ-Al2O3. Dessutom analyserades resterande mängd ozon i utgående gasflöde vid olika storlek på ingående gasflöde. Resterande mängd ozon efter ozonbehandlingen var ungefär 45 % av ingående mängd.

La valorisation de la biomasse lignocellulosique en molécules plateforme pour l'industrie chimique rend nécessaire l'adaptation des méthodes de raffinage à la transformation de composés organiques oxygénés. La déshydratation des alcools connaît dans ce contexte un fort regain d'intérêt. Les travaux de cette thèse s'attachent à comprendre à l'échelle moléculaire la réactivité d'un alcool modèle (isopropanol) sur catalyseurs aluminiques, au travers d'une étude mettant en jeu expériences et modélisation aux échelles moléculaire (DFT) et du réacteur (modélisation cinétique). En combinant expériences de spectroscopie infrarouge, mesures cinétiques et modélisation moléculaire appliquée à l'adsorption et aux chemins réactionnels de l'isopropanol sur l'alumine gamma, il est montré que la réactivité de cet alcool est principalement gouvernée par la facette (100) de l'alumine. Les formations compétitives de propène, majoritaire, et de diisopropyléther, minoritaire, impliquent un même intermédiaire alcoolate, adsorbé sur un atome d'aluminium acide de Lewis, qui évolue soit par élimination directe d'une molécule d'eau (mécanisme E2), soit par condensation avec une seconde molécule d'alcool adsorbée à proximité (mécanisme SN2). Un modèle microcinétique fondé sur ce site unique de réaction, incluant de surcroît la décomposition de l'éther en isopropanol et en propène, permet de reproduire les résultats expérimentaux à condition de prendre en compte l'effet de molécules d'eau et d'alcool co-adsorbées dans l'environnement du site actif, la formation de dimères eau - intermédiaire et la stabilisation de la seconde molécule d'alcool contribuant à l'ajustement du rapport éther/propène. / The upgrading of lignocellulosic biomass into strategic molecules for the chemical industry requires the adaptation of refining procedures to the transformation of oxygenated species. In this context, the dehydration of alcohols has seen renewed interest over the last decade. The work presented here aims at unravelling the reactivity of a model alcohol (isopropanol) over aluminic catalysts at the molecular scale. To this purpose, a study combining experiments and modelling at the molecular scale (DFT) and at the reactor scale (kinetic modelling) has been set up. By combining infrared spectroscopic experiments, kinetic measurements and molecular modelling of the adsorption and reaction pathways of isopropanol on gamma alumina, it is shown that this reactivity is mainly governed by the (100) facets of alumina. The competing formation of propene (major product) and diisopropylether (minor product) involves a common alcoolate intermediate adsorbed on a Lewis acidic aluminium atom, either by direct elimination of a water molecule (E2 mechanism) or by condensation with a second alcohol molecule adsorbed in vicinity (SN2 mechanism).A micro-kinetic model involving this single reaction site and including the transformation of the ether into isopropanol and propene allows reproducing the experimental results, provided that the effect of co-adsorbed water and alcohol molecules in the environment of the active site is taken into account, as the formation of water – intermediate dimers and the stabilization of the second alcohol molecule both contribute to an adjustment of the ether/propene ratio.

Mesoporous γ-alumina is the most extensively used catalysts support in a wide range of catalytic processes. The usefulness of γ-alumina relies on its favorable combination of physical, textural, thermal, and chemical properties. Pore structure properties are among the most important properties, since high surface area and large pore volume enable higher loading of active catalytic phases, while design of pore size and pore size distribution is critical to optimize pore diffusional transport and product selectivity. In addition, accurate determination of surface area (SA), pore volume (PV) and pore size distribution (PSD) of porous supports, catalysts, and nanomaterials is vital to successful design and optimization of these materials and to the development of robust models of pore diffusional resistance and catalyst deactivation.In this dissertation, we report a simple, one-pot, solvent-deficient process to synthesize mesoporous γ-alumina without using external templates or surfactants. XRD, TEM, TGA and N2 adsorption techniques are used to characterize the morphologies and structures of the prepared alumina nanomaterials. By varying the aluminum salts or the water to aluminum molar ratio in the hydrolysis of aluminum alkoxides, γ-alumina with different morphologies and pore structures are synthesized. The obtained alumina nanomaterials have surface areas ranging from 210 m2/g to 340 m2/g, pore volumes ranging from 0.4 cm3/g to 1.7 cm3/g, and average pore widths from 4 to 18 nm. By varying the alcohols used in the rinsing and gelation of boehmite/bayerite precursors derived from a controlled hydrolysis of aluminum alkoxides, the average pore width of the γ-aluminas can be tuned from 7 to 37 nm. We also report improved calculations of PSD based on the Kelvin equation and a proposed Slit Pore Geometry model for slit-shaped mesopores of relatively large pore size (>10 nm). Two structural factors, α and β, are introduced to correct for non-ideal pore geometries. The volume density function for a log normal distribution is used to calculate the geometric mean pore diameter and standard deviation of the PSD. The Comparative Adsorption (αs) Method is also employed to independently assess mesopore surface area and volume.

Το π–κυμένιο (p–ισοπρόπυλο τολουόλιο) είναι ένα πολύ σημαντικό προϊόν με μεγάλο εμπορικό ενδιαφέρον, καθώς αποτελεί κύριο συστατικό πολλών καλλυντικών, αρωμάτων, φαρμακευτικών προϊόντων, καθώς και την πρώτη ύλη για την παραγωγή της p–κρεσόλης. Η τρέχουσα διαδικασία παραγωγής του π–κυμενίου είναι η κατά Friedel–Crafts αλκυλίωση του τολουολίου με προπυλένιο ή προπανόλη–2, η οποία χρησιμοποιεί μεγάλες ποσότητες επιβλαβών οξέων, προκαλώντας πολλά προβλήματα χειρισμού στους εργαζόμενους με αυτό, προβλήματα διάβρωσης και προβλήματα διάθεσης των παραγόμενων αποβλήτων. Τα τελευταία χρόνια, η Πράσινη Χημεία έχει παρουσιασθεί ως η νέα προσέγγιση της Χημείας για την πρόληψη της μόλυνσης του περιβάλλοντος, καθώς και του σχεδιασμού χημικών προϊόντων και διεργασιών που είναι περισσότερο φιλικά προς το περιβάλλον. Η κατάλυση αποτελεί μία από τις κύριες αρχές, αλλά ταυτόχρονα και εργαλείο της Πράσινης Χημείας. Πιο συγκεκριμένα η ετερογενής κατάλυση, που εξυπηρετεί τους στόχους της Πράσινης Χημείας, λόγω της εξάλειψης της ανάγκης διαχωρισμού του παραγόμενου προϊόντος από τον καταλύτη. Επίσης, μία άλλη βασική παράμετρος της Πράσινης Χημείας είναι η χρήση της βιομάζας, ως ανανεώσιμη πρώτη ύλη, με σκοπό την παραγωγή ενέργειας και χημικών προϊόντων. Στην παρούσα εργασία, μελετάται η δυνατότητα καταλυτικής παραγωγής π–κυμενίου, βασιζόμενη στις αρχές της Πράσινης Χημείας. Για το σκοπό αυτό χρησιμοποιείται ως αντιδρών το α–λεμονένιο, ένα μονοτερπένιο το οποίο αποτελεί ανανεώσιμη πρώτη ύλη, καθώς είναι παραπροϊόν της βιομηχανίας χυμών λεμονιού και πορτοκαλιού, καθώς και της βιομηχανίας χάρτου και πολτού. Πιο αναλυτικά, μελετήθηκε η καταλυτική συμπεριφορά οξειδίων με μεγάλη ειδική επιφάνεια, όπως η SiO2, το MCM–41, ο ζεόλιθος NaY, η γ–Al2O3 και δύο δείγματα TiO2, με διαφορετικές ειδικές επιφάνειες, στην αντίδραση μετατροπής του λεμονενίου προς π–κυμένιο. Επίσης, ερευνήθηκε η επίδραση στη διεργασία τόσο της θερμοκρασίας της αντίδρασης, όσο και της σύστασης της ατμόσφαιρας κάτω από την οποία διεξαγόταν η αντίδραση. Τα πειράματα διεξήχθησαν σε αντιδραστήρα σταθερής κλίνης – ατμοσφαιρικής πίεσης, ενώ για την ανάλυση των λαμβανόμενων προϊόντων χρησιμοποιήθηκε αέριος χρωματογράφος – φασματογράφος μάζας (GC–MS). Από τους καταλύτες που μελετήθηκαν ο πιο αποτελεσματικός αποδείχθηκε η τιτάνια με τη σχετικά μεγάλη ειδική επιφάνεια ακολουθούμενη από την τιτάνια με την χαμηλότερη ειδική επιφάνεια, τον ζεόλιθο NaY και τη γ–Al2O3. Τόσο η σίλικα όσο και το MCM–41 παρουσίασαν μάλλον αμελητέα δραστικότητα. Επίσης, παρατηρήθηκε ότι η απόδοση σε π–κυμένιο αυξανόταν γενικά με τη θερμοκρασία, ενώ δεν επηρεαζόταν πρακτικά από την ατμόσφαιρα που διεξαγόταν η αντίδραση. Τέλος, στους 300 οC και χρησιμοποιώντας την τιτάνια με τη σχετικά μεγάλη ειδική επιφάνεια ως καταλύτη επιτεύχθηκε 90% απόδοση για το π–κυμένιο και 100% μετατροπή για το λεμονένιο. Η αυξημένη απόδοση της τιτάνιας αποδόθηκε σε επιτυχή συγκερασμό ανάμεσα στη σχετικά μεγάλη οξύτητα Brönsted και στη σχετικά εύκολη μεταβολή του λόγου Ti(IV)/Ti(III) κατά τη διάρκεια της αντίδρασης. Τα κινητικά αποτελέσματα επέτρεψαν να γραφεί ένα κινητικό σχήμα για τη διεργασία. / P–cymene is a very important product with great commercial interest because of its use as a main ingredient of cosmetics, perfumes and pharmaceutical products as well as raw material for the production of p–cresol. Current production is achieved by using the Friedel–Crafts reaction of toluene with propylene or propanol–2 which uses large quantities of harmful acids which, in turn, leads to industrial accidents, corrosion problems and the general difficulty of handling toxic wastes. A new concept of chemistry has been developed for confronting environmental problems. Green Chemistry is related to products and processes that are environmentally friendly. One of the basic tools of Green Chemistry is catalysis, mainly heterogeneous catalysis, because it allows the easy separation of the catalysts used from the final product. Moreover, following the principles of the Green Chemistry, biomass should be used in the production of renewable energy and chemical products. The present Thesis deals with the catalytic production of p–cymene based on the principles of Green Chemistry. In particular, we use a–limonene, by–product of the juice of orange and lemon industry as well as the paper industry, to produce p–cymene. A number of oxides with large specific surface area, such as SiO2, MCM–41, zeolite NaY, γ–Al2O3 and two samples of TiO2, were studied as catalysts. The effect of the reaction temperature and the composition of the atmosphere were also studied. All experiments were conducted on a fixed bed micro–reactor operating under atmospheric pressure coupled with an on–line Gas Chromatograph–Mass Spectrometer (GC – MS). The titania with the relatively high specific surface area was proved to be the most efficient catalyst among those studied. The following activity series has been obtained: «high surface area titania > small surface area titania > zeolite NaY > γ–Al2O3 > MCM–41 > SiO2». Negligible activity is exhibited by MCM–41 and SiO2. The percentage yield for p–cymene increases with temperature whereas is practically independent from the carrier gas. Very high percentage yield for p–cymene was obtained at 300οC over the high specific surface area titania (~90%). Complete transformation of a–limonene was obtained over the above catalyst at the same temperature. The very high activity obtained over this catalyst was attributed to good compromise between high acidity and easy transformation of the ratio Ti(IV)/Ti(III) during reaction. The kinetic results allow the clarification of the reaction scheme.

La magnétite Fe3O4 est un matériau prometteur pour l'électronique de spin, puisque des calculs de structure de bande la prédisent demi-métallique, ce qui laisse supposer des effets de magnétorésistance importants pour des jonctions tunnel magnétiques utilisant Fe3O4 comme électrode. Nous avons fait croître des films minces de Fe3O4 de 3 à 50 nm d'épaisseur sur α-Al2O3 par épitaxie par jets moléculaires. Les films sont monocristallins mais contiennent des parois d'antiphase. Celles-ci sont responsables des anomalies magnétiques observées sur les films, que nous avons pu reproduire à l'aide d'un modèle unidimensionnel, les résultats ayant étés confrontés avec la taille caractéristique des parois mesurée par une analyse<br />fractale. <br /><br />Nous avons de plus mis au point la croissance de couches minces de γ-Al2O3 épitaxiée sur les films de Fe3O4, en contrôlant la stoechiométrie à l'interface entre oxydes. Les films de γ-Al2O3 d'épaisseur supérieure à 2 nm sont continus, et assurent le découplage magnétique entre les électrodes. Les mesures directes par photoémission résolue en spin conduisent à une polarisation en spin de -40 % pour l'interface Fe3O4/ γ-Al2O3 tandis que l'on mesure<br />une magnétorésistance tunnel, réduite du fait du désordre magnétique induit par les parois d'antiphase, de +3 % à température ambiante pour les jonctions Fe3O4/ γ-Al2O3/Co, ce qui implique une polarisation effective positive pour l'interface Fe3O4/ γ-Al2O3 dans les mesures de transport tunnel.

Mesoporous γ-Al2O3 is one of the most widely used catalyst supports for commercial catalytic applications. The performance of a catalyst strongly depends on the combination of textural, chemical and physical properties of the support. Pore size is essential since each catalytic system requires a unique pore size for optimal catalyst loading, diffusion and selectivity. In addition, high surface area and large pore volume usually result in higher catalyst loading, which increases the number of catalytic reaction sites and decreases reaction time. Therefore, determination of surface area and porosity of porous supports is critical for the successful design and optimization of a catalyst support. Moreover, it is important to produce supports with good thermal stability since pore collapsing due to sintering at high temperatures often results in catalyst deactivation. In addition, the ability to control the acidity of the catalyst enables us to design desirable acid sites to optimize product selectivity, activity, and stability in different catalytic applications. This dissertation presents a simple, one-pot, solvent-deficient method to synthesize thermally stable silica-doped alumina (SDA) without using templates. The XRD (X-ray diffraction), HTXRD (high temperature X-ray diffraction), SS NMR (solid state nuclear magnetic resonance), TEM (transmission electron microscopy), TGA(thermogravimetric analysis), and N2 adosorption techniques are used to characterize the structures of the synthesized SDAs and understand the origin of increased thermal stability. The obtained SDAs have a surface area of 160 m2/g, pore volume of 0.99 cm3/g, and a bimodal pore size distribution of 23 and 52 nm after calcination at 1100◦C. Compared to a commercial SDA, the surface area, pore volume, and pore diameter of synthesized SDAs are higher by 46%, 155%, and 94%, respectively. A split-plot fractional-factorial experimental design is also used to obtain a useful mathematical model for the control of textural properties of SDAs with a reduced cost and number of experiments. The proposed quantitative models can predict optimal conditions to produce SDAs with high surface areas greater than 250 m2/g, large pore volume greater than 1 cm3/g, and large (40-60 nm) or medium (16-19 nm) pore diameters. In my approach, I control acid sites formation by altering preparation variables in the synthesis method such as Si/Al ratio and calcination temperatures. The total acidity concentration (Brønsted and Lewis) of the synthesized SDAs are determined using ammonia temperatured program, pyridine fourier transform infrared spectroscopy (FTIR), and MAS NMR. The total acidity concentration is increased by introducing a higher mole ratio of Si to Al. In addition, the total acidity concentration is decreased by increasing calcination temperature while maintaining high surface area, large porosity, and thermal stability of γ-alumina support. I also present an optimized synthesis of various aluminum alkoxides (aluminum n-hexyloxide (AH), aluminum phenoxide (APh) and aluminum isopropoxide (AIP)) with high yields (90-95%). One mole of aluminum is reacted with excess alcohol in the presence of 0.1 mole % mercuric chloride catalyst. The synthesized aluminum alkoxides are used as starting materials to produce high surface area alumina catalyst supports. Aluminum alkoxides and nano aluminas are analyzed by 1H NMR, 13C NMR, 27Al NMR, gCOSY (2D nuclear magnetic resonance spectroscopy), IR (infrared spectroscopy), XRD, ICP (induced coupled plasma), and elemental analysis.