CATALYTIC OXIDATION OF GLYCEROL TO DIHYDROXYACETONE · PDF fileSelective oxidation of glycerol...
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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 * Email address: [email protected]; Tel.: +1 765 494 4075; Fax: +1 765 494 0805. Identifying new uses of glycerol, a waste of biodiesel production from transesterification of vegetable oils, is of great current interest. Towards this end, many value-added chemicals, such as propanediol, propylene, epichlorohydrin and methanol, have been explored by chemical companies. The use of glycerol to synthesize these chemicals, however, is less attractive due to the limited amount of value added. We use glycerol as a feedstock for its selective oxidation to produce high-value chemical dihydroxyacetone (DHA). DHA is a specialty chemical currently used in the cosmetics, wine-making, and nutritional supplement industries. The challenge, however, is the relatively complex glycerol oxidation network, Fig. 1. Note that DHA is formed by oxidation of the secondary hydroxyl group in glycerol which is less reactive than primary ones. HO OH OH HO OH HO OH O HO OH OH HO OH O OH OH O OH OH O O OH OH OH O OH O O OH OH O O O O O O O Glycerol Dihydroxyacetone Glyceraldehyde Hydroxypyruvic Acid Mesoxalic Acid Glyceric Acid Tartronic Acid Glycolic Acid Glyoxalic Acid Oxalic Acid Fig. 1. Glycerol oxidation network Experimental Catalyst Synthesis Pt-Bi/C catalysts with different loadings, supports, impregnation sequences and reduction methods were synthesized. A typical synthesis procedure is described as follows: activated carbon (AC) was submerged in water with sonication. A predetermined amount of chloroplatinic acid hydrate was dissolved in 1.2N HCl and added dropwise to the well-stirred AC slurry. Next, complete reduction of Pt with NaBH 4 was conducted. Bi impregnation and reduction followed the same procedure as for Pt. After this, the mixture was rinsed and dried in air at 100 °C before use. The opposite impregnation sequence and co-impregnation were also applied. Similarly, other AC supports and reducing agents, e.g. H 2 and formaldehyde were also employed. The catalysts were characterized before and after reaction by using BET, ICP-OES, TEM, XRD and XPS techniques. Glycerol Oxidation The prepared catalysts were tested in a semi-batch reactor (Parr), see Fig. 2. The vessel was first charged with catalyst and glycerol solution, purged with argon and heated to the reaction temperature. The gas was then switched to O 2 at the desired reactor pressure. Liquid samples were collected periodically and analyzed using an Agilent 1100 series HPLC instrument with Hitachi GL- C610-S column.
Transcript of CATALYTIC OXIDATION OF GLYCEROL TO DIHYDROXYACETONE · PDF fileSelective oxidation of glycerol...
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 NaBH4 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
* Email address: [email protected]; Tel.: +1 765 494 4075; Fax: +1 765 494 0805.
Identifying new uses of glycerol, a waste of biodiesel production from transesterification of vegetable oils, is of great current interest. Towards this end, many value-added chemicals, such as propanediol, propylene, epichlorohydrin and methanol, have been explored by chemical companies. The use of glycerol to synthesize these chemicals, however, is less attractive due to the limited amount of value added. We use glycerol as a feedstock for its selective oxidation to produce high-value chemical dihydroxyacetone (DHA). DHA is a specialty chemical currently used in the cosmetics, wine-making, and nutritional supplement industries. The challenge, however, is the relatively complex glycerol oxidation network, Fig. 1. Note that DHA is formed by oxidation of the secondary hydroxyl group in glycerol which is less reactive than primary ones.
HO OH
OH
HO
OH
HO OH
O
HO
OH
OH
HO
OH
O
OH
OH
O
OH
OH
O
O
OH
OH
OH
O
OH
O
O
OH
OH
O
OO
O
O
OO
Glycerol
Dihydroxyacetone
Glyceraldehyde
Hydroxypyruvic Acid Mesoxalic Acid
Glyceric Acid Tartronic Acid
Glycolic Acid
Glyoxalic Acid
Oxalic Acid Fig. 1. Glycerol oxidation network
Experimental Catalyst Synthesis Pt-Bi/C catalysts with different loadings, supports, impregnation sequences and reduction methods were synthesized. A typical synthesis procedure is described as follows: activated carbon (AC) was submerged in water with sonication. A predetermined amount of chloroplatinic acid hydrate was dissolved in 1.2N HCl and added dropwise to the well-stirred AC slurry. Next, complete reduction of Pt with NaBH4 was conducted. Bi impregnation and reduction followed the same procedure as for Pt. After this, the mixture was rinsed and dried in air at 100 °C before use. The opposite impregnation sequence and co-impregnation were also applied. Similarly, other AC supports and reducing agents, e.g. H2 and formaldehyde were also employed. The catalysts were characterized before and after reaction by using BET, ICP-OES, TEM, XRD and XPS techniques. Glycerol Oxidation The prepared catalysts were tested in a semi-batch reactor (Parr), see Fig. 2. The vessel was first charged with catalyst and glycerol solution, purged with argon and heated to the reaction temperature. The gas was then switched to O2 at the desired reactor pressure. Liquid samples were collected periodically and analyzed using an Agilent 1100 series HPLC instrument with Hitachi GL-C610-S column.
Fig. 2. Semi-batch reactor schematics
Results and Discussion The absence of mass transfer limitations was verified by experiments and calculations for the most severe case. Thus, all experiments were conducted in the reaction rate limiting regime. A typical glycerol oxidation result is shown in Fig. 3. Glycerol was fully converted after about 4 hours, while the DHA yield exhibited a maximum value of 43% at 2 hours. The yield of other oxidation products was low.
0 2 4 6 8 100.0
0.2
0.4
0.6
0.8
1.0
Con
cent
ratio
n (m
ol/L
)
Reaction Time (hours)
Glycerol DHA Glyceric Acid Glyceraldehyde
Fig. 3. Glycerol and product concentrations with time
To evaluate the performance of different catalysts, the glycerol oxidation turnover frequency, selectivity to DHA at 50% glycerol conversion and maximum DHA yield were compared for every catalyst. The optimum catalyst was determined to be 3wt% Pt then 0.6wt% Bi by sequential impregnation on Norit Darco 20-40 mesh activated carbon, followed by NaBH4 reduction. In addition to the catalyst, the reaction conditions in the semi-batch reactor were also optimized using the same criteria stated above, by conducting experiments in the range of temperature 30-70 °C, oxygen pressure 30-180 psig, stirring speed 300-680 rpm, initial pH 2-12, and glycerol/catalyst ratio 0.04-0.32 mol/g. For example, the influence of temperature is shown in Fig. 4, indicating that higher temperature is preferred for both TOF and DHA selectivity. Finally the optimum conditions were identified
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.
30 40 50 60 701
2
3
4
5
6
7
TOF S
50, DHA
Temperature (oC)
TO
F (
min
-1)
48
49
50
51
S50, D
HA (%
)
Fig. 4. Influence of time on TOF and S50, DHA
Various techniques were used to characterize the catalyst. XRD patterns of the catalyst show no additional peaks as compared to the support, suggesting that the metal particles are in amorphous state. XPS measurements show that the metals are in Pt0 and Bi3+ chemical states and no deactivation was observed after use. A TEM image (Fig. 5) shows that the metal particles are about 5-6 nm in size, in accordance with the chemisorption results (~20% dispersion).
Fig. 5. TEM micrograph of 3%Pt-0.6Bi/C
Concluding Remarks In this work, for the first time, the Pt-Bi/C catalyst and reaction conditions were optimized systematically towards glycerol oxidation rate, DHA selectivity and maximum yield. The maximum DHA yield of 46% was achieved, which is the highest value reported in a semi-batch reactor. These results can be used for large-scale production of DHA from glycerol, thus increasing the economics of biodiesel production.
Reference Kimura, H. et al., Selective oxidation of glycerol on a platinum-bismuth catalyst. Appl. Catal. A: Gen. 1993, 96, 217.
