Transportation fuels from biomass oxygenates

1. A method of converting biomass oxygenates into hydrocarbon fuels comprising:

a) providing a biomass derived oxygenate feed;

b) hydrogenating the oxygenate feed with hydrogen and a hydrogenation catalyst to produce a hydrogenated product;

c) condensing the hydrogenated product with a condensation catalyst to produce a condensed or oligomerized product;

d) polishing the condensed or oligomerized product with a hydroprocessing catalyst (HPC) to produce hydrocarbon range fuel products; and

e) isolating one or more hydrocarbon range fuel products;

further including the step of separating alcohol from the hydrogenated product prior to condensing the hydrogenated product with the condensation catalyst.

2. The method of claim 1 , wherein said oxygenate feedstock is derived from a biomass selected from the group consisting of sugars, carbohydrates, lignins, fatty acids, proteins, oils, eucalyptus oil, forest residues, dead trees, branches, leaves, tree stumps, yard clippings, wood chips, wood fiber, sugar beets, miscanthus, switchgrass, hemp, corn, corn fiber, poplar, willow, sorghum, sugarcane, palm oil, corn syrup, algal cultures, bacterial cultures, fermentation cultures, paper manufacturing waste, farming residues, food manufacturing waste, meat processing waste, municipal solid waste, animal waste, biological waste, sewage, and combinations thereof.

3. The method of claim 1 , wherein said oxygenate feedstock comprises one or more oxygenates selected from the group consisting of carbohydrates, sugars, pentoses, hexoses, monosaccharides, dextrose, glucose, α-D-glucopyranose, β-D-glucopyranose, α-D-glucofuranose, β-D-glucofuranose, fructose, galactose, disaccharides, levoglucosan, sucrose, manose, glucose, xylose, isosorbide, lactose, maltose, fructose, cellobiose, melibiose, raffinose, glyceraldehyde, erythritol, xylitol, sorbitol, arabitol, mannitol, sorbitol, dulcitol, maltitol, arabinitol, isosorbide, glycerol, glycerin, alcohol, methanol (MeOH), ethanol (EtOH), isopropyl alcohol (IPA), butanol (BuOH), n-butanol, t-butanol, ethers, methyl tert-butyl ether (MTBE), tertiary amyl methyl ether (TAME), tertiary hexyl methyl ether (THEME), ethyl tertiary butyl ether (ETBE), tertiary amyl ethyl ether (TAEE), diisopropyl ether (DIPE), hydroxymethyl-tetrahydrofuran or tetrahydro-2-furfuryl alcohol (THFA), methyl-tetrahydrofuran, 2-methyltetrahydrofuran, 3-methyltetrahydrofuran, tetrahydrofuran, diols, methanediol (H 2 C(OH) 2 ), ethylene glycol, propane diols, 1,2-propanediol, 1,3-propanediol, butanediols, 1,2-butanediol, 1,3-butanediol, 1,4-butanediol, 2,3-butanediol, pentane diols, 1,2-pentanediol, 1,5-pentanediol, octanediol, 1,8-octanediol, etohexadiol, p-menthane-3,8-diol, 2-methyl-2,4-pentanediol, aldehydes, propanal, butanal, 2,5-furan-diacrboxyaldehyde, carboxylates, acetic acid, oxopropanoic acid, acrylic acid, levulinic acid, succinic acid, 2,5-furan-dicarboxylic acid, aspartic acid, glucaric acid, glutamic acid, itaconic acid, acetylacrylic acid, 4-O-Me-glucuronic acid, gluconic acid, xylonic acid, esters, levuninate esters, lactones, valero lactone, α-methylene-γ-valerolactone, angelica lactones, trisaccharides, oligosaccharides, polysaccharides, starch, derivatives, dimers, trimers, and polymers thereof.

4. The method of claim 1 , further comprising one or more of the following reaction conditions:

a) wherein said oxygenate is hydrogenated at temperatures between approximately 100 and 400° C. and pressures between approximately 100-1200 psig;

b) wherein said hydrogenated product is condensed and/or oligomerized at temperatures between approximately 200 and 600° C. and pressures between approximately 100-1200 psig; and

c) wherein said condensed and/or oligomerized product is polished at temperatures between approximately 200 and 400° C. and pressures between approximately 100-2000 psig.

5. The method of claim 1 :

a) wherein said hydrogenation catalysts is selected from the group consisting of ceria (Ce), magnesium (Mg), nickel (Ni), cobalt.(Co), gold (Au), iridium (Ir), osmium (Os), palladium (Pd), platinum (Pt), rhodium (Rh), ruthenium (Ru) and combinations thereof;

b) wherein said condensation catalyst is selected from the group consisting of alumina, silica, silica-alumina, zirconia, titania, ceria, manganese oxide, magnesium, praseodymium oxide, samarium oxide, and combinations thereof;

c) wherein said condensation catalyst has a promoter selected from the group consisting of copper (Cu), nickel (Ni), cobalt (Co), Iron (Fe), gold (Au), iridium (Ir), osmium (Os), palladium (Pd), platinum (Pt), rhodium (Rh), and combinations thereof;

d) wherein said polishing catalyst is selected from the group consisting of molybdenum (Mo), tungsten (W), cobalt (Co), nickel (Ni), NiW, NiMo, CoMo, and combinations thereof; or

e) wherein said polishing catalyst support is selected from the group consisting of carbon, alumina, silica, zeolite, ceramic, Al 2 O 3 , and the like.

6. The method of claim 1 , wherein said hydrocarbon range fuel products are distilled to one or more renewable hydrocarbon fuels selected form the group consisting of gasoline, diesel, and jet-fuel.

7. The method of claim 1 , wherein said renewable hydrocarbon fuel products comprise naphthene hydrocarbons and mixtures thereof.

8. The method of claim 1 , comprising:

a) hydrogenation selected from one of the following conditions:

i) wherein said oxygenate comprises levulinic acid, said hydrogenation catalyst is ruthenia-carbon catalyst, said temperature is approximately 100-150° C., said pressure is approximately 400-1000 psig, or

ii) wherein said oxygenate comprises levulinic acid, said hydrogenation catalyst is a nickel-based catalyst, said temperature is approximately 200-250° C., said pressure is approximately 800-1000 psig;

b) condensation selected from one of the following conditions:

i) wherein said hydrogenated product comprises gamma-valerolactone (GVL), said condensation catalyst is ceria-alumina, said temperature is approximately 400° C. and said pressure is approximately 800-1000 psig,

ii) wherein said hydrogenated product comprises gamma-valerolactone (GVL), said condensation catalyst is magnesia-alumina, said temperature is approximately 400° C. and said pressure is approximately 800-1000 psig,

iii) wherein said hydrogenated product comprises tetrahydrofurfuryl alcohol, said condensation catalyst is ceria-alumina, said temperature is approximately 400° C. and said pressure is approximately 800-1000 psig,

iv) wherein said hydrogenated product comprises levulinic acid, said condensation catalyst is a noble-metal catalyst, said temperature is approximately 200-340° C. and said pressure is approximately 1200 psig,

v) wherein said hydrogenated product comprises sorbitol, said condensation catalyst is a Co/praseodymium oxide-alumina catalyst, said temperature is approximately 280-400° C. and said pressure is approximately 800-1200 psig, or

vi) wherein said hydrogenated product comprises a levulinic acid/formic acid mixture said condensation catalyst is a NiCu/praseodymium oxide-alumina catalyst, said temperature is approximately 280-400° C. and said pressure is approximately 800-1200 psig; and

c) polishing selected from one of the following conditions:

i) wherein said polishing catalyst is a sulfided hydroprocessing catalyst, said temperature is approximately 240-8380° C., and said pressure is approximately 800-81800 psi,

ii) wherein said polishing catalyst is a sulfided hydroprocessing catalyst, said temperature is approximately 240-320° C., and said pressure is approximately 800-1200 psi,

iii) wherein said polishing catalyst is a sulfided hydroprocessing catalyst, said temperature is approximately 280-350° C., and said pressure is approximately 800-1200 psi, wherein said polishing catalyst is a non-sulfided hydroprocessing catalyst, said temperature is approximately 280-350° C., and said pressure is approximately 800-1200 psi, or

iv) wherein said polishing catalyst is a non-sulfided hydroprocessing catalyst, said temperature is approximately 280-380° C., and said pressure is approximately 800-2000 psi.

9. The method of claim 1 , comprising a product with naphtha, renewable distillate, VGO range fraction comprising naphtha range hydrocarbons with, distillate range hydrocarbon fuel comprising hydrocarbons, vacuum gas oil (VGO) range hydrocarbons, and combinations thereof wherein said renewable distillate range fraction comprises:

i) approximately 1 to 12 wt % paraffins;

ii) approximately 60 to 80 wt % naphthenes;

iii) approximately 15 to 40 wt % 1-ring naphthenes;

iv) approximately 20 to 40 wt % 2-ring naphthenes;

v) approximately 5 to 15 wt % 3-ring naphthenes; and

vi) approximately 0 to 20 wt % aromatics.

10. The method of claim 1 , comprising a product with renewable naphtha, distillate, VGO range hydrocarbons with fraction comprising naphtha range hydrocarbon fuel comprising hydrocarbons, distillate range hydrocarbons, vacuum gas oil (VGO) range hydrocarbons, and combinations thereof wherein said renewable naphtha fraction comprises:

i) approximately 2 to 30 wt % paraffins;

ii) approximately 50 to 80 wt % naphthenes; and

iii) approximately 0 to 10 wt % aromatics.

11. The method of claim 1 , comprising a product with renewable distillate or vacuum gas oil (VGO) fraction comprising distillate range hydrocarbons, VGO range hydrocarbons, and combinations thereof wherein said renewable distillate fuel fraction has:

i) a density between approximately 0.75 and 0.95;

ii) an oxygen content between approximately 1.00 and 0.01;

iii) a cetane between approximately 40 and 60;

iv) a cloud point between approximately −55° F. and −75° F.; and

v) a pour point between approximately −70° F. and −88° F.

12. The method of claim 1 , comprising a product with renewable naphtha fuel comprising naphtha range hydrocarbons wherein said renewable naphtha fuel fraction has

i) a density between approximately 0.65 and 0.80;

ii) an oxygen content between approximately 1.00 and 0.01; and

iii) a calculated octane between approximately 45 and 65.