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Catalytic Oxidation of Glycerol to Dihydroxyacetone

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Catalytic Oxidation of Glycerol to Dihydroxyacetone CATALYTIC OXIDATION OF GLYCEROL TO DIHYDROXYACETONE Wenbin Hu, Brian Lowry and Arvind Varma * School of Chemical Engineering, Purdue University, West Lafayette, IN 47907, USA Summary Selective oxidation of glycerol to dihydroxyacetone was investigated using Pt-Bi/C bi-metallic catalyst. The catalysts with different metal loadings, supports and synthesis methods were synthesized and tested in a semi-batch reactor. The optimum catalyst was 3wt%Pt, with sequential 0.6wt%Bi impregnation on Norit Darco 20-40 mesh activated carbon, followed by NaBH 4 reduction, for reaction rate and DHA selectivity. With the optimum catalyst, the reaction conditions (temperature, pressure, pH, etc) in the semi-batch reactor were optimized, with which the maximum DHA yield of 46% was obtained at nearly full glycerol conversion. The catalysts were characterized using BET, ICP-OES, TEM, XRD and XPS techniques. Keywords Glycerol; Dihydroxyacetone; Selective Oxidation; Platinum-Bismuth catalyst Introduction Identifying new uses of glycerol, a waste of biodiesel Experimental production from transesterification of vegetable oils, is of Catalyst Synthesis great current interest. Towards this end, many value-added Pt-Bi/C catalysts with different loadings, supports, chemicals, such as propanediol, propylene, impregnation sequences and reduction methods were epichlorohydrin and methanol, have been explored by synthesized. A typical synthesis procedure is described as chemical companies. The use of glycerol to synthesize follows: activated carbon (AC) was submerged in water these chemicals, however, is less attractive due to the with sonication. A predetermined amount of chloroplatinic limited amount of value added. We use glycerol as a acid hydrate was dissolved in 1.2N HCl and added feedstock for its selective oxidation to produce high-value dropwise to the well-stirred AC slurry. Next, complete chemical dihydroxyacetone (DHA). DHA is a specialty reduction of Pt with NaBH 4 was conducted. Bi chemical currently used in the cosmetics, wine-making, impregnation and reduction followed the same procedure and nutritional supplement industries. The challenge, as for Pt. After this, the mixture was rinsed and dried in air however, is the relatively complex glycerol oxidation at 100 °C before use. The opposite impregnation sequence network, Fig. 1. Note that DHA is formed by oxidation of and co-impregnation were also applied. Similarly, other the secondary hydroxyl group in glycerol which is less AC supports and reducing agents, e.g. H2 and reactive than primary ones. formaldehyde were also employed. OH OH OH OH The catalysts were characterized before and after reaction HO O HO O O O OH by using BET, ICP-OES, TEM, XRD and XPS techniques. O Glyceraldehyde OH OH OH Glycolic Acid OH Glyceric Acid Tartronic Acid OH Glycerol Oxidation HO OH O Glycerol O The prepared catalysts were tested in a semi-batch reactor Glyoxalic Acid O O O (Parr), see Fig. 2. The vessel was first charged with OH HO OH HO O O O O catalyst and glycerol solution, purged with argon and O Dihydroxyacetone heated to the reaction temperature. The gas was then OH OH OH OH Hydroxypyruvic Acid Mesoxalic Acid Oxalic Acid switched to O 2 at the desired reactor pressure. Liquid Fig. 1. Glycerol oxidation network samples were collected periodically and analyzed using an Agilent 1100 series HPLC instrument with Hitachi GL- C610-S column. * Email address: [email protected]; Tel.: +1 765 494 4075; Fax: +1 765 494 0805. as 70 °C, 30 psig, >550 rpm, initial pH=2 and glycerol/catalyst ratio 0.04 mol/g. With these conditions, a maximum DHA yield of 46% was achieved. 7 TOF S 51 6 50, DHA 5 50 S ) 50, DHA 50, -1 4 (%) 49 TOF (min TOF 3 2 Fig. 2. Semi-batch reactor schematics 48 1 30 40 50 60 70 Results and Discussion Temperature ( oC) The absence of mass transfer limitations was verified by experiments and calculations for the most severe case. Fig. 4. Influence of time on TOF and S 50, DHA Thus, all experiments were conducted in the reaction rate limiting regime. Various techniques were used to characterize the catalyst. XRD patterns of the catalyst show no additional peaks as A typical glycerol oxidation result is shown in Fig. 3. compared to the support, suggesting that the metal particles are in amorphous state. XPS measurements show that the Glycerol was fully converted after about 4 hours, while the 0 3+ DHA yield exhibited a maximum value of 43% at 2 hours. metals are in Pt and Bi chemical states and no The yield of other oxidation products was low. deactivation was observed after use. A TEM image (Fig. 5) shows that the metal particles are about 5-6 nm in size, 1.0 in accordance with the chemisorption results (~20% Glycerol dispersion). DHA 0.8 Glyceric Acid Glyceraldehyde 0.6 0.4 Concentration (mol/L) Concentration 0.2 0.0 0 2 4 6 8 10 Reaction Time (hours) Fig. 3. Glycerol and product concentrations with time To evaluate the performance of different catalysts, the Fig. 5. TEM micrograph of 3%Pt-0.6Bi/C glycerol oxidation turnover frequency, selectivity to DHA at 50% glycerol conversion and maximum DHA yield were compared for every catalyst. The optimum catalyst was Concluding Remarks determined to be 3wt% Pt then 0.6wt% Bi by sequential In this work, for the first time, the Pt-Bi/C catalyst and impregnation on Norit Darco 20-40 mesh activated carbon, reaction conditions were optimized systematically towards glycerol oxidation rate, DHA selectivity and maximum followed by NaBH 4 reduction. yield. The maximum DHA yield of 46% was achieved, In addition to the catalyst, the reaction conditions in the which is the highest value reported in a semi-batch reactor. semi-batch reactor were also optimized using the same These results can be used for large-scale production of criteria stated above, by conducting experiments in the DHA from glycerol, thus increasing the economics of range of temperature 30-70 °C, oxygen pressure 30-180 biodiesel production. psig, stirring speed 300-680 rpm, initial pH 2-12, and glycerol/catalyst ratio 0.04-0.32 mol/g. For example, the Reference influence of temperature is shown in Fig. 4, indicating that Kimura, H. et al., Selective oxidation of glycerol on a higher temperature is preferred for both TOF and DHA platinum-bismuth catalyst. Appl. Catal. A: Gen. 1993, 96, selectivity. Finally the optimum conditions were identified 217. .
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