Gas phase process for monoalcohol production from glycerol
A method of producing short chain alcohols from glycerol generated as a byproduct of biodiesel production is provided.
1. A method for converting glycerol to monohydric alcohol, the method comprising:
reacting a gaseous mixture comprising glycerol, water and hydrogen in a first reaction bed comprising a heterogeneous catalyst system comprising a dehydration catalyst and a hydrogenation catalyst, whereby a first reacted mixture is produced, the first reaction mixture comprising propionaldehyde;
separating at least a portion of the first reacted mixture into a more volatile fraction and a less volatile fraction in a first condenser;
reacting a mixture of hydrogen and at least a portion of the more volatile fraction from the first reacted mixture in a second reactor bed comprising a hydrogenation catalyst, whereby a second reacted mixture comprising a monohydric alcohol is produced;
separating at least a portion of the second reacted mixture into a less volatile fraction comprising a monohydric alcohol and a more volatile fraction in a second condenser.
2. The method of claim 1 , further comprising introducing at least a portion of the less volatile fraction of the first reacted mixture into the first reaction bed.
3. The method of claim 1 , further comprising introducing at least a portion of the less volatile fraction of the second reacted mixture into the second reaction bed.
4. The method of claim 2 , further comprising volatilizing at least a portion of the less volatile fraction of the first reacted mixture prior to introducing it into the first reaction bed.
5. The method of claim 3 , further comprising volatilizing at least a portion of the less volatile fraction of the second reacted mixture prior to introducing it into the second reaction bed.
6. The method of claim 1 , wherein the first reaction bed catalyzes dehydration reactions requiring heat and hydrogenation reactions generating heat, wherein the heat required by the dehydration reactions approximately balances the heat generated by the hydrogenation reactions.
7. The method of claim 6 , wherein an absolute value of the heat required by the dehydration reactions is provided by an absolute value of the heat generated by the hydrogenation reactions.
8. The method of claim 6 , wherein an absolute value of the heat generated by the hydrogenation reactions provides an absolute value of the heat required by the dehydration reactions and other processes.
9. The method of claim 6 , wherein the heat required by the dehydration reactions and the heat generated by the hydrogenation reaction are balanced by controlling a ratio of an amount of dehydration catalyst to hydrogenation catalyst in the first reaction bed.
10. The method of claim 6 , wherein the heat required by the dehydration reactions and the heat generated by the hydrogenation reactions are balanced by controlling an amount of hydrogen present in the gaseous mixture.
11. The method of claim 6 , wherein the heat required by the dehydration reactions and the heat generated by the hydrogenation reactions are balanced by controlling a ratio of hydrogen to glycerol.
12. The method of claim 11 , wherein a molar ratio of hydrogen to glycerol in the gaseous mixture is from about 0.05:10 to about 10:10.
13. The method of claim 11 , wherein a molar ratio of hydrogen to glycerol in the gaseous mixture is from about 0.1:10 to about 2:10.
14. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of glycerol to acrolein, the selectivity being greater than about 75 (wt.) %.
15. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of glycerol to acrolein, the selectivity being greater than about 85 (wt.) %.
16. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of glycerol to acrolein, the selectivity being dependent on the catalysts present, the time for the reaction, the temperature of the reaction, and the pressure of the reaction, the selectivity being greater than about 95 (wt.) %.
17. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of acrolein to propionaldehyde, the selectivity being greater than about 65 (wt.) %.
18. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of acrolein to propionaldehyde, the selectivity being greater than about 75 (wt.) %.
19. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of acrolein to propionaldehyde, the selectivity being greater than about 85 (wt.) %.
20. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of propionaldehyde to propanol, the selectivity being less than about 25 (wt.) %.
21. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of propionaldehyde to propanol, the selectivity being less than about 15 (wt.) %.
22. The method of claim 1 , wherein the heterogeneous catalyst system has a selectivity for conversion of propionaldehyde to propanol, the selectivity being less than about 5 (wt.) %.
23. The method of claim 1 , wherein the first reacted mixture comprising at least one carbonyl contains less than about 10 mol % of a monohydric alcohol.
24. The method of claim 1 , wherein the first reacted mixture comprising at least one carbonyl contains less than about 3 mol % of a monohydric alcohol.
25. The method of claim 1 , wherein the first reacted mixture comprising at least one carbonyl compound comprises monohydric alcohol and propionaldehyde present in a weight ratio of from about 0:10 to about 3:7.
26. The method of claim 1 , wherein the first reacted mixture comprising at least one carbonyl compound comprises monohydric alcohol and propionaldehyde present in a weight ratio of from about 0.1:10 to about 1:9.