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Slovak University of Technology , Bratislava Faculty of Chemical and Food Technology Dep . of Organic Technology Joint Slovak-Hungarian Laboratory for Development of Catalyzed Chemical Processes of Biomass Utilization *. Catalytic transformation of bio-glycerol to diols. Andrej Ševčík

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Catalytic transformation of bio-glycerol to diols


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catalytic transformation of bio glycerol to diols

Slovak UniversityofTechnology, Bratislava

FacultyofChemical and FoodTechnology

Dep. ofOrganicTechnology

Joint Slovak-Hungarian Laboratory for

Development of Catalyzed Chemical

Processes of Biomass Utilization*

Catalytic transformation of bio-glycerol to diols

Andrej Ševčík

Alexander Kaszonyi

*Founded by financial support of project No. HUSK/1101/1.2.1/0318

“Chemical Processes of Biomass Utilization in the Slovak-Hungarian Frontier Region”

17thOctober, 2012, Bratislava

diols
Diols
  • selective catalytic hydrogenolysis of glycerol represents a low cost and green route for 1,2-propanediol which is a major commodity chemical used in the production of antifreeze functional fluids, paints and polyester resins.
  • due to a presence of -OH functional groups, diols can be converted to aldehydes, esters, amines and carboxylic acids
slide3
Hydrogenolysis of glycerol to 1,2-PD

Supported catalysts

- Batch reactor :

  • Yuan (2010) - 180°C, 3 MPa, cat. CuO/MgO, conv. of GLY - 72%, sel. to 1,2-PD - 97 %
  • Zhao(2010) - 200°C, 6 MPa, cat. Ni/Na-X, conv. of GLY - 86 %,sel. to 1,2-PD - 94 %
  • Xia (2012) - 180°C, 2 MPa, cat. Cu-Pd/solid base, conv. of GLY - 70%, sel. to 1,2-PD - 98%

- Down-flow reactor:

  • Zhou (2010) - 220°C, 4MPa, cat. CuO-ZnO-Al2O3, conv. of GLY - 81%, sel. to 1,2-PD - 93%
  • Zheng(2010) - 250°C, 4 MPa, cat. Cu/SBA-15, conv. of GLY - 96%, sel.to 1,2-PD - 90 %
slide4
Hydrogenolysis of glycerol to 1,2-PD

Unsupported catalysts

- batch reactor:

  • Kim(2010) - 220°C, 8 MPa, Cu-Cr-O cat., different methods of catalyst preparation (wet impregnation, co-precipitation), important is the formation of CuCr2O4 structure
  • different activity for the hydrogenolysis of glycerol is caused by various forms of copper in the catalyst structure
  • Mane (2011) - 220°C, 7 MPa, effect of promoters (Al, Ba, Zn) to Cu-Cr-O cat.
influence of different supports to activity and selectivity of catalysts
Influence of different supports to activity and selectivity of catalysts

Reaction conditions:

5g catalyst, 150 °C, flow rate of GLY 1ml/h, inicial concentration of GLY 50 wt.%,

flow rate of hydrogen 30ml/min, 5h time on stream

effect of different amount of metals loaded on g alumina
Effect of different amount of metals loaded on g-alumina

Reaction conditions:

5g of catalyst (K10-0 is 10 wt.% of Cu and K5-5 is 5 wt.% of Cu and 5 wt.% of Cr), inicial concentration of GLY 50 wt.%, flow rate of GLY 1ml/h, flow rate of hydrogen 30ml/min, 5h time on stream

hydrotalcite types of catalysts on hydrogenolysis of glycerol
Hydrotalcite types of catalysts on hydrogenolysis of glycerol

Reaction conditions:

5g catalyst, flow rate of GLY 1ml/h, flow rate of hydrogen 30ml/min,

5h time on stream

aim of work
Aim of Work
  • Preparation of catalysts based on copper on different supports
  • Modification of these catalysts with other metals, especially with chrome
  • Study of the influence of catalyst preparation method and reaction conditions on the catalytic activity
  • Study of the influence of impurities in glycerol on properties of catalytic systems
  • Chemical and physical characterization of prepared catalysts
  • Optimization of reaction conditions with regard to maximize the yield of the diols
slide9

Thankyouforyourattention

This work was supported by the

Slovak Research and Development Agencyunder the contract No. APVV-0133-11