Catalysts for the deoxygenation of esters of free fatty acids and triglycerides
It is provided solid, heterogeneous catalysts for the deoxygenation of esters of free fatty acids and triglycerides, and for the production of hydrocarbons that can be used as biofuels. More particularly, the catalyst comprises at least one metal oxide, the catalyst having a formula Al a Cu b Ni c Si d Ti e Zn f Zr g La h Ce i W j Sn k Ga l Fe m MO n Mn o CO p O x , wherein a, b, c, d, g, h, i, j, k, l, m n, o, p and x are the molar ratios of the respective elements, wherein a, b, c, d, h, i, j, k, l, m, n, o and p are >0, e, f and g are >0 and x is such that the catalyst is electrically neutral.
1. A catalyst comprising at least three metal oxides having a formula Al a Cu b Ni c Si d Ti e Zn f Zr g La h Ce i W j Sn k Ga l Fe m MO n Mn o CO p O x , wherein a, b, c, d, e, f, g, h, i, j, k, l, m n, o, p and x are molar ratios for the respective elements, wherein a, b, c, d, h, i, j, k, l, m, n, o and p are ≥0, e, f and g are >0 and x is such that the catalyst is electrically neutral, and the catalyst is substantially free of any one of Pd, Pt, Ru, Ir, and Rh.
2. The catalyst of claim 1 , wherein the catalyst is one of:
Cu 0.45 Ni 0.34 Zn 0.45 Zr 4.38 O 10
Ti 1.25 Zn 1.23 Zr 2.67 La 0.12 Ce 0.38 O 10
Ti 1.85 Zn 1.82 Zr 1.88 La 0.09 Ce 0.29 O 10
Ti 2.39 Zn 2.34 Zr 1.21 La 0.06 Ce 0.19 O 10
Ti 2.79 Zn 2.74 Zr 0.71 La 0.03 Ce 0.11 O 10
Al 1.81 Ti 1.15 Zn 1.13 Zr 1.64 La 0.07 Ce 0.23 O 10
Ti 1.27 Zn 1.24 Zr 2.71 W 0.27 O 10
Al 0.11 Si 3.54 Ti 0.84 Zn 0.82 Zr 0.13 O 10
Al 0.09 Si 2.85 Ti 0.45 Zn 0.44 Zr 1.23 W 0.12 O 10
Ti 1.05 Zn 1.05 Zr 3.42 O 10
Al 0.07 Si 2.15 Ti 1.20 Zn 1.17 Zr 0.86 La 0.02 Ce 0.13 O 10
Ti 1.23 Zn 1.21 Zr 2.75 Ce 0.40 O 10
Ti 1.22 Zn 1.19 Zr 2.60 La 0.11 Ce 0.37 Sn 0.25 O 10
Al 4.42 Ti 0.43 Zn 0.42 Zr 0.91 WV 0.09 Sn 0.09 O 10
Ti 1.24 Zn 1.22 Zr 2.65 La 0.06 Ce 0.20 W 0.13 Sn 0.13 O 10
Al 0.07 Si 3.36 Ti 0.39 Zn 0.38 Zr 0.83 W 0.82 Sn 0.09 O 10
Ti 1.17 Zn 1.15 Zr 2.50 La 0.11 Ce 0.36 Ga 0.41 O 10
Al 4.30 Ti 0.42 Zn 0.41 Zr 0.90 WV 0.09 Ga 0.16 O 10
Ti 1.22 Zn 1.19 Zr 2.60 La 0.06 Ce 0.19 W 0.12 Ga 0.22 O 10
Al 0.07 Si 3.31 Ti 0.39 Zn 0.38 Zr 0.83 W 0.08 Ga 0.15 O 10
Ni 0.25 Ti 1.18 Zn 1.16 Zr 2.52 La 0.11 Ce 0.36 Ga 0.21 O 10
Al 4.32 Ni 0.09 Ti 0.42 Zn 0.41 Zr 0.90 W 0.09 Ga 0.08 O 10
Ni 0.13 Ti 1.22 Zn 1.20 Zr 2.61 La 0.06 Ce 0.19 W 0.12 Ga 0.11 O 10
Al 4.28 Ni 0.09 Ti 0.42 Zn 0.41 Zr 0.90 WV 0.09 Mo 0.06 O 10
Al 4.25 Ti 0.42 Zn 0.41 Zr 0.90 W 0.09 Mo 0.11 O 10
Ti 1.20 Zn 1.17 Zr 2.56 La 0.06 Ce 0.19 W 0.12 Mo 0.16 O 10
Al 4.27 Ti 0.42 Zn 0.41 Zr 0.89 WV 0.09 Fe 0.20 O 10
Al 3.65 Ni 0.22 Ti 0.44 Zn 0.43 Zr 0.93 W 0.09 Mo 0.28 O 10
Cu 1.04 Ni 1.08 Ti 0.99 Zn 0.97 Zr 2.10 La 0.09 Ce 0.30 O 10 .
3. The catalyst of claim 1 , wherein the catalyst has a surface area between about 10 m 2 /g and about 500 m 2 /g.
4. The catalyst of claim 1 , wherein the catalyst has a total pore volume between about 0.01 mL/g and about 1 mL/g.
5. The catalyst of claim 1 , wherein the catalyst is in powdered, pelleted, extruded form or coated on a metal or any suitable surface with or without an added binder.
6. The catalyst of claim 1 , wherein the catalyst is calcined.
7. A method for performing a deoxygenation reaction of a starting material, comprising contacting the starting material with at least one catalyst as defined in claim 1 .
8. The method of claim 7 , wherein the starting material comprises triglycerides, diglycerides, monoglycerides, fatty acids, esters of fatty acids, biomass derived biooils, ketone, alcohol or a combination thereof.
9. The method of claim 7 , wherein the starting material is vegetable oil, used cooking oil, derived from animal fat, tall oil or any combination thereof.
10. The method of claim 7 , wherein the starting material is diluted with a hydrocarbon or co-fed with a hydrocarbon or methanol or water or a hydrogen donor.
11. The method of claim 10 , wherein the hydrogen donor is formic acid, methyl formate, methanol, ethanol, propanol, butanol, or any other suitable hydrogen donor agents or any combination thereof.
12. The method of any one of claim 7 , wherein the deoxygenation reaction is conducted in the absence of added hydrogen or in the presence of added hydrogen.
13. The method of claim 7 , wherein the deoxygenation reaction is conducted at a temperature between about 250° C. and about 500° C.
14. The method of claim 7 , wherein the deoxygenation reaction is conducted at a pressure between about ambient pressure and about 5,000 psi.
15. The method of claim 7 , wherein the deoxygenation reaction is conducted at a weight hourly space velocity between about 0.09 hr −1 and about 3 hr −1 .
16. The method of claim 7 , wherein at least one hydrocarbon product is produced.
17. The method of claim 16 , wherein the at least one hydrocarbon product comprises one or more of alkanes, iso-alkanes, cycloalkanes, cycloolefins, aromatics, alkyl-aromatics, poly-aromatics, naphthenes, indanes or any combination thereof.
18. The method of claim 16 , wherein the at least one hydrocarbon product is fractioned into gasoline, jet fuel, diesel and marine fuel boiling range or higher boiling hydrocarbons.
19. The method of claim 7 , wherein a conversion efficiency of the deoxygenation reaction of the starting material is at least 20%.
20. The method of claim 7 , wherein the deoxygenation reaction comprises at least one of a decarboxylation reaction, decarbonylation reaction and a dehydration reaction.
21. The method of claim 7 , wherein a conversion efficiency of the deoxygenation reaction of the starting material is at least 90%.