초록 ▼

A process for the direct conversion of lipid biomass fuel stock to combustible fuels include the steps of hydrolyzing a lipid biomass to form free fatty acids, catalytically deoxygenating the free fatty acids to from n-alkanes, and reforming at least a portion of the n-alkanes into a mixture of comp

A process for the direct conversion of lipid biomass fuel stock to combustible fuels include the steps of hydrolyzing a lipid biomass to form free fatty acids, catalytically deoxygenating the free fatty acids to from n-alkanes, and reforming at least a portion of the n-alkanes into a mixture of compounds having the correct chain length, conformations and ratio to be useful as transportation fuels. The process exhibits an overall energy efficiency of at least about 75%, wherein energy efficiency is calculated as the lower heating value of the produced transportation fuel over the sum of the lower heating value of the process reactants and the total energy input into the process.

대표청구항 ▼

That which is claimed: 1. A process for the direct conversion of lipidic biomass to a transportation fuel, said process comprising: (A) performing thermal hydrolysis on a lipidic biomass to form a product stream comprising a free fatty acid and form a by-product stream comprising glycerol; (B) perf

That which is claimed: 1. A process for the direct conversion of lipidic biomass to a transportation fuel, said process comprising: (A) performing thermal hydrolysis on a lipidic biomass to form a product stream comprising a free fatty acid and form a by-product stream comprising glycerol; (B) performing catalytic deoxygenation on the free fatty acid stream to form a product stream comprising an n-alkane; and (C) performing one or more reforming steps on the n-alkane stream to form a product stream comprising a mixture of hydrocarbon compounds selected from the group consisting of n-alkanes, isoalkanes, aromatics, and cycloalkanes; wherein, after step (C), the hydrocarbon compounds in the product stream are in a combination and ratio necessary to form an overall composition useful as the transportation fuel, wherein the process exhibits an overall energy efficiency of at least about 75%, wherein energy efficiency is calculated as the lower heating value of the produced transportation fuel over the sum of the lower heating value of the process reactants and total energy input into the process. 2. The process according to claim 1, wherein the lipidic biomass comprises a material selected from the group consisting of triglycerides, diglycerides, monoglycerides, free fatty acids, and combinations thereof. 3. The process according to claim 1, wherein the lipidic biomass comprises a material selected from the group consisting of animal fat, vegetable oil, algae lipids, waste grease, or mixtures thereof. 4. The process according to claim 3, wherein the lipidic biomass source comprises animal fat selected from the group consisting of beef fat, hog fat, turkey fat, and chicken fat. 5. The process according to claim 1, wherein one or more process steps requires application of heat, and wherein the process further comprises recovering at least a portion of the glycerol stream and using the glycerol as a fuel for producing at least a portion of the process heat. 6. The process according to claim 1, wherein said thermal hydrolysis step comprises introducing the lipidic biomass into the bottom of a reactor column, introducing water near the top of the reactor column, and heating the reactor to a temperature of about 220° C. to about 300° C. under a pressure sufficient to prevent the water in the reactor from flashing to steam. 7. The process according to claim 1, wherein said catalytic deoxygenation step comprises gas-phase deoxygenation. 8. The process according to claim 7, wherein said catalytic deoxygenation step comprises the use of a fixed-bed catalyst. 9. The process according to claim 8, wherein the fixed-bed catalyst comprises a noble metal. 10. The process according to claim 8, wherein the fixed-bed catalyst comprises palladium. 11. The process according to claim 1, wherein said catalytic deoxygenation step comprises liquid-phase catalytic deoxygenation carried out in a hydrocarbon solvent. 12. The process according to claim 11, wherein said liquid-phase catalytic deoxygenation is carried out at a temperature of up to 325° C. 13. The process according to claim 11, wherein said catalytic deoxygenation step comprises the use of a catalyst slurry or catalyst dispersion. 14. The process according to claim 13, wherein the catalyst in the catalyst slurry or catalyst dispersion comprises a noble metal. 15. The process according to claim 13, wherein the catalyst in the catalyst slurry or catalyst dispersion comprises palladium. 16. The process according to claim 11, further comprising recovering a portion of the n-alkane stream formed in said catalytic deoxygenation step and using the n-alkane stream as at least a portion of the hydrocarbon solvent in which the liquid phase catalytic deoxygenation step is carried out. 17. The process according to claim 1, wherein said catalytic deoxygenation step further comprises the addition of H2. 18. The process according to claim 11, wherein said catalytic deoxygenation is carried out at a temperature at which deoxygenation does not substantially proceed by thermal action alone. 19. The process according to claim 1, wherein the one or more reforming steps are selected from the group consisting of hydroisomerization, hydrocracking, dehydrocyclization, and aromatization. 20. The process according to claim 1, wherein said reforming comprises the use of a solid catalyst. 21. The process according to claim 20 wherein the solid catalyst comprises a metal functional component. 22. The process according to claim 21, wherein the solid catalyst further comprises an acidic-functional component. 23. The process according to claim 1, wherein said reforming comprises the use of two or more different catalysts. 24. The process according to claim 1, wherein step (C) comprises a first reaction carried out in a first reactor and at least a second reaction carried out in at least a second, separate reactor. 25. The process according to claim 24, wherein step (C) further comprises separating the n-alkane stream into two or more reforming streams and directing the two or more reforming streams separately into the first reactor and the at least second reactor. 26. The process according to claim 24, wherein the first reactor and the at least second reactor are in series such that a first reforming product stream is formed in the first reactor and the first reforming product stream proceeds to the at least second reactor, wherein is formed a second reforming product stream. 27. The process according to claim 1, wherein step (C) comprises a first reaction carried out in a first reactor, a second reaction carried out in a second, separate reactor, and at least a third reaction carried out in at least a third, separate reactor. 28. The process according to claim 1, wherein the hydrocarbon compounds in the product stream are in a combination and ratio necessary to form an overall composition useful as a jet engine fuel. 29. The process according to claim 1, wherein the hydrocarbon compounds in the product stream are in a combination and ratio necessary to form an overall composition useful as a gasoline engine fuel. 30. The process according to claim 1, wherein the hydrocarbon compounds in the product stream are in a combination and ratio necessary to form an overall composition useful as a diesel engine fuel. 31. The process according to claim 1, wherein the overall composition formed is substantially identical to a petroleum-derived transportation fuel selected from the group consisting of jet engine fuel, gasoline engine fuel, and diesel engine fuel. 32. The process according to claim 1, wherein steps (A)-(C) are carried out separately and sequentially.