Method of producing lower alcohols from glycerol
View Patent ↗A reactive-separation process converts glycerin into lower alcohols, having boiling points less than 200° C., at high yields. Conversion of natural glycerin to propylene glycol through an acetol intermediate is achieved at temperatures from 150° to 250° C. at pressures from 1 and 25 bar. The preferred applications of the propylene glycol are as an antifreeze, deicing compound, or anti-icing compound. The preferred catalyst for this process in a copper-chromium.
1. A process for converting glycerol to a product at high selectivity to propylene glycol and low selectivity to ethylene glycol, comprising:
providing a gas phase reaction mixture that is essentially free of liquid and contains
glycerol with a partial pressure of glycerol in a range from 0.01 bars and 0.5 bars of glycerol, and
hydrogen,
the reaction mixture being maintained at a total pressure between 0.02 and 10 bars; and
contacting the gas phase reaction mixture with a heterogeneous catalyst at a temperature between 150° C. and 280° C. to form propylene glycol.
2. The process of claim 1 , wherein the heterogeneous catalyst used in the step of contacting contains at least one element from Groups I, VI, and VIII of the Periodic Table.
3. The process of claim 1 , wherein the heterogeneous catalyst used in the step of reacting contains at least one metal selected from the group consisting of copper and chromium.
4. The process of claim 3 , wherein the heterogeneous catalyst is a copper chromite catalyst.
5. The process of claim 1 , wherein the temperature of the contacting step is within a range from 180° C. to 240° C.
6. The process of claim 1 , wherein the pressure of the contacting step is within a range from 1 bar to 10 bars.
7. The process of claim 1 , wherein a reaction product formed from the reaction mixture contains acetol.
8. The process of claim 7 , wherein acetol is removed from the reaction product and recycled to form a mixture with the glycerol feed.
9. The process of claim 1 including a step of contacting a glycerol containing feed with a gas in an evaporating step at a temperature between 150° C. and 280° C. to evaporate glycerol to form a reactor feed.
10. The process of claim 9 wherein the contacting of glycerol with the gas occurs at a temperature within a range from 200° C. to 260° C.
11. The process of claim 10 wherein the temperature range is from 210° C. to 230° C.
12. The process of claim 9 wherein the glycerol feed contains a non-volatile salt and the evaporating step partially separates the non-volatile salt from the glycerol.
13. The process of claim 9 including the step of recycling the gas through a condenser that separates the reaction product from the gas.
14. The process of claim 1 wherein reaction conditions of the contacting step include a partial pressure of glycerol being
less than glycerol's dew point partial pressure in the reaction mixture,
and greater than one fourth the dew point partial pressure in the reaction mixture.
15. The process of claim 14 wherein the partial pressure of glycerol is greater than half the dew point partial pressure in the reaction mixture.
16. The process of claim 1 wherein the reaction conditions of the contacting step includes the temperature being less than 230° C.
17. The process of claim 1 further comprised of at least two reaction steps where a first reaction step has reaction temperatures greater than 200° C. and the second reaction step has temperatures less than 220° C. and
where the glycerol concentration entering the second reaction step is less than half the glycerol concentration entering the first reaction step.
18. The process of claim 17 wherein the first reaction step has reaction temperatures greater than 210° C. and the second reaction step has temperatures less than 210° 0 C.
19. A process for converting glycerol to a product at high selectivity to propylene glycol and low selectivity to ethylene glycol, comprising:
contacting a gas phase reaction mixture with a heterogeneous catalyst,
wherein the gas phase that contains essentially no liquid and has a partial pressure of glycerol between 0.01 and 0.5 bars of glycerol and a total pressure between 1 and 15 bars; and
establishing a temperature between 150° C. and 280° C. to facilitate a reaction.
20. The process of claim 19 , wherein the heterogeneous catalyst used in the step of contacting contains at least one element from Groups I or VIII of the Periodic Table.
21. The process of claim 18 where the partial pressure of glycerol is less than glycerol's dew point partial pressure in the reaction mixture and
greater than one fourth the dew point partial pressure in the reaction mixture.
22. The process of claim 21 where the partial pressure of glycerol is greater than half the dew point partial pressure in the reaction mixture.
23. A process for converting glycerol to a product at high selectivity to a mixture of acetol and propylene glycol and low selectivity to ethylene glycol, comprising:
contacting a gas phase reaction mixture with a heterogeneous catalyst,
wherein the gas phase reaction mixture contains essentially no liquid and has a partial pressure of glycerol between 0.01 and 0.5 bars of glycerol and a partial pressure of hydrogen between 0.01 and 5 bars of hydrogen and a total pressure between 0.02 and 5 bars; and
establishing a temperature between 150° C. and 250° C. to facilitate a reaction.
24. The process of claim 23 , wherein the heterogeneous catalyst used in the step of contacting contains at least one element from Groups I or VIII of the Periodic Table.
25. The process of claim 23 , wherein the total pressure of reaction between 0.02 and 25 bars.
26. The process of claim 25 where the partial pressure of glycerol is
less than glycerol's dew point partial pressure in the reaction mixture and
greater than one fourth the dew point partial pressure in the reaction mixture.
27. The process of claim 26 where the partial pressure of glycerol is greater than half the dew point partial pressure in the reaction mixture.
28. The process of claim 1 wherein the reaction mixture is maintained at a total pressure between 0.02 and 5 bars.
29. The process of claim 28 wherein the partial pressure of hydrogen is maintained at a total pressure between 0.01 and 5 bars.
30. The process of claim 1 wherein the reaction mixture is maintained at a total pressure between 1 and 5 bars.
31. The process of claim 1 wherein the reaction mixture is maintained at a total pressure between 0.5 and 3 bars.
32. The process of claim 19 wherein the reaction mixture is maintained at a total pressure between 1 and 5 bars.
33. The process of claim 23 wherein the reaction mixture is maintained at a total pressure between 1 and 5 bars.
34. The process of claim 23 wherein the reaction mixture is maintained at a total pressure between 0.5 and 3 bars.