TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Support: The support comprises a member selected from nitride, carbon, silica, alumina, zirconia, titania, vanadia, ceria, boron nitride, heteropolyacid, kieselguhr, hydroxyapatite, zinc oxide and/or chromia. The support comprises a hydrogen peroxide treated carbon. The support is modified by treating it with a modifier selected from silanes, alkali compounds, alkali earth compounds, or lanthanides. The support is selected from carbon nanotubes, carbon fullerenes and/or zeolites. Preferred Method: The in situ generated H2 is generated by catalytically reacting in a liquid phase and/or vapor phase a portion of the water and oxygenated hydrocarbon in the presence of an aqueous phase reforming catalyst at a reforming temperature and reforming pressure to produce in situ generated H2. When the reforming temperature is 100-450 (preferably 100-300) degrees C, the reforming pressure is a pressure where the water and the oxygenated hydrocarbon are gaseous. When the reforming temperature is 80-400 degrees C, the reforming pressure is a pressure where the water and the oxygenated hydrocarbon are liquid. When the deoxygenation temperature is 100-600 degrees C, the deoxygenation pressure is at least 0.1 atmosphere or a pressure where the water and the oxygenated hydrocarbon are gaseous. When the deoxygenation temperature is 80-300 (preferably 200-280) degrees C, the deoxygenation pressure is a pressure where the water and the oxygenated hydrocarbon are liquid or when the deoxygenation temperature is 200-280 degrees C, the deoxygenation pressure is a pressure where the water and the oxygenated hydrocarbon are gaseous. When the reforming temperature and deoxygenation temperature are 100-450 (preferably 120-300, especially 200-280, particularly 250-425) degrees C, the reforming pressure and deoxygenation pressure are 72-1300 (preferably 72-1200, especially 200-725) psig. When the condensation temperature is 80-500 (preferably 125-450, especially 125-250) degrees C, the condensation pressure is 0-1200 psig (preferably 0.1 atmosphere, especially 0-700 psig). The reaction stream further comprises water, and the method further involves dewatering the reaction stream prior to reacting the oxygenate in the presence of the condensation catalyst. The step of catalytically reacting the oxygenated hydrocarbon with H2 in the presence of the deoxygenation catalyst is conducted in the presence of an insignificantly effective amount of external H2. The molar ratio of the total oxygen atoms in the oxygenated hydrocarbons to the total hydrogen atoms in the external H2 is less than 1:1. The method further involves catalytically reacting in the liquid and/or vapor phase a sugar, sugar alcohol or polyhydric alcohol with H2 in the presence of a hydrogenolysis catalyst at a hydrogenolysis temperature and hydrogenolysis pressure to produce the oxygenated hydrocarbon. The hydrogenolysis temperature is 110-300 (preferably at least 110) degrees C and the hydrogenolysis pressure is 10-2400 psig. The method further involves catalytically reacting in the liquid and/or vapor phase a sugar, furfural, carboxylic acid, ketone, or furan with H2 in the presence of a hydrogenation catalyst at a hydrogenation temperature and hydrogenation pressure to produce the oxygenated hydrocarbon; catalytically reacting the greater than 4C compound in the liquid phase and/or vapor phase in the presence of a finishing catalyst at a finishing temperature and a finishing pressure; providing supplemental H2 and catalytically reacting a portion of the oxygenated hydrocarbon with supplemental H2 in the presence of the deoxygenation catalyst to produce the oxygenate; catalytically reacting in the liquid and/or vapor phase a member selected from sugar, furfural, carboxylic acid, ketone and/or furan, with H2 in the presence of the hydrogenation catalyst at a hydrogenation temperature and hydrogenation pressure to produce the oxygenated hydrocarbon; and catalytically reacting in the liquid and/or vapor phase a member selected from sugar, sugar alcohol and/or polyhydric alcohol, with H2 in the presence of a hydro genolysis catalyst at a hydrogenolysis temperature and hydrogenolysis pressure to produce the oxygenated hydrocarbon. The hydrogenation temperature is 80-250 degrees C and the hydrogenation pressure is 100-2000 psig. The method is performed in a reactor system preferably in a continuous flow reactor system at steady-state equilibrium. Each catalytic reaction occurs at steady-state equilibrium. Preferred Catalyst: The condensation catalyst comprises a member selected from an acid catalyst, base catalyst, or an acid-base catalyst, carbide, nitride, zirconia, alumina, silica, aluminosilicate, phosphate, zeolite, titanium oxide, zinc oxide, vanadium oxide, cerium oxide, lanthanum oxide, yttrium oxide, scandium oxide, magnesium oxide, barium oxide, calcium oxide, hydroxide, heteropolyacid, inorganic acid, acid modified resin and/or base modified resin. The condensation catalyst further comprises a modifier (M1) selected from Ce, La, Y, Sc, Li, Na, K, Rb, Cs, Mg, Ca, Sr, Ba, P, B and/or Bi; and a metal (M2) selected from Cu, Ag, Au, Pt, Ni, Fe, Co, Ru, Zn, Cd, Ga, In, Rh, Pd, Ir, Re, Mn, Cr, Mo, W, Sn, and/or Os or their alloys. The acid catalyst comprises a member selected from an acidic alumina, aluminum phosphate, silica-alumina phosphate, amorphous silica-alumina, aluminosilicate, zirconia, sulfated zirconia, tungstated zirconia, tungsten carbide, molybdenum carbide, titania, sulfated carbon, phosphated carbon, phosphated silica, phosphated alumina, acidic resin, heteropolyacid and/or inorganic acid and further comprises the modifier selected from (M1), Ga, In, Zn, Fe, Mo, Ag, Au, Ni, or Ta; an oxide (O1) selected from Ti, Zr, V, Nb, Ta, Mo, Cr, W, Mn, Re, Al, Ga, In, Fe, Co, Ir, Ni, Si, Cu, Zn, Sn, Cd and/or P and the metal selected from (M2). The acid catalyst comprises an aluminosilicate zeolite (preferably bifunctional pentasil ring-containing aluminosilicate zeolite). The base catalyst comprises a member selected from hydrotalcite, zinc-aluminate, phosphate, Li, Na, K, Cs, B, Rb, Mg, Ca, Sr, Si, Ba, Al, Ce, La, Sc, Y, Zr, Ti and/or Zn, or their alloys; the oxide selected from (O1); and the metal selected from (M2). The base catalyst comprises a metal oxide of a member selected from Cu, Ni, Zn, V and/or Zr and zinc aluminate. The acid-base catalyst comprises a member selected from hydrotalcite, zinc-aluminate, phosphate, Li, Na, K, Cs, B, Rb, Mg, Ca, Sr, Si, Ba, Al, Ce, La, Sc, Y, Zr, Ti, Zn, and/or Cr and further comprises the oxide selected from (O1) and metal selected from (M2). The acid-base catalyst comprises a binary oxide selected from magnesium oxide (MgO) and aluminum oxide (Al2O3) combination, MgO and zirconium oxide (ZrO2) combination, or zinc oxide (ZnO) and Al2O3 combination. The deoxygenation catalyst comprises a support and a member selected from Re, Cu, Fe, Ru, Ir, Co, Rh, Pt, Pd, Ni, W, Os, Mo, Ag and/or Au or their alloys and further comprises a member selected from Mn, Cr, Mo, W, V, Nb, Ta, Ti, Zr, Y, La, Sc, Zn, Cd, Ag, Au, Sn, Ge, P, Al, Ga, In and/or Tl. The deoxygenation catalyst and the condensation catalyst are atomically identical. The aqueous phase reforming catalyst comprises a support and a member selected from Fe, Ru, Os, Ir, Co, Rh, Pt, Pd and/or Ni or their alloys and further comprises a member selected from Cu, B, Mn, Re, Cr, Mo, Bi, W, V, Nb, Ta, Ti, Zr, Y, La, Sc, Zn, Cd, Ag, Au, Sn, Ge, P, Al, Ga, In and/or Tl, or their alloys. The aqueous phase reforming catalyst, deoxygenation catalyst, and condensation catalyst are atomically identical. The aqueous phase reforming catalyst and deoxygenation catalyst comprise Pt alloyed or mixed with a member selected from Ni, Ru, Cu, Fe, Rh and/or Re or their alloys; Ru alloyed or mixed with a member selected from Ge, Bi, B, Ni, Sn, Cu, Fe, Rh and/or Pt, or their alloys; or Ni alloyed or mixed with a member selected from Sn, Ge, Bi, B, Cu, Re, Ru, and/or Fe or their alloys. The hydrogenolysis catalyst comprises a member selected from phosphate, Cr, Mo, W, Re, Mn, Cu, Cd, Fe, Ru, Os, Ir, Co, Rh, Pt, Pd and/or Ni, or their alloys and further comprises a member selected from Au, Ag, Zn, Sn, Bi, B, Cr, Mn and/or O or their alloys; an alkaline earth metal oxide and the support. The hydrogenation catalyst comprises the support and a member selected from Fe, Ru, Os, Ir, Co, Rh, Pt, Pd, Ni, Re and/or Cu, or their alloys and further comprises a member selected from Ag, Au, Cr, Zn, Mn, Sn, Bi, Mo, W, B and/or P, or their alloys. The finishing catalyst comprises a support and a member selected from Cu, Ni, Fe, Co, Ru, Pd, Rh, Pt, Ir and/or Os, or their alloys and further comprises a modifier selected from Au, Ag, Cr, Zn, Mn, Sn, Cu, Cr and/or Bi, or their alloys. Preferred System: The reactor system comprises at least one reactor vessel, where the reactor system is adapted to be configured as continuous flow, batch, semi-batch and/or multi-system and further comprises at least one of a fluidized catalytic bed, a swing bed, fixed bed and/or moving bed, where each bed is adapted to be housed within a reactor vessel; a reforming bed adapted to contain the aqueous phase reforming catalyst, a deoxygenation bed adapted to contain the deoxygenation catalyst, and a condensation bed adapted to contain the condensation catalyst. The reforming bed and deoxygenation bed are oriented in a stacked, side-by-side or parallel configuration, and, where the reforming and deoxygenation beds are housed within a single reactor vessel. The reforming bed is housed within a reforming reactor vessel, and where the deoxygenation bed is housed within a deoxygenation reactor vessel. The condensation bed is housed within a condensation reactor vessel. The single reactor vessel is further adapted to house the condensation bed. The reforming bed, deoxygenation bed, and condensation bed are oriented in a stacked, side-by-side or parallel configuration within the single reactor vessel. The continuous flow reactor system is oriented to provide horizontal, vertical or diagonal flow. The deoxygenation bed is housed within a deoxygenation reactor vessel providing up-flow, and, where the condensation bed is housed within a condensation reactor vessel providing down-flow.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The H2 comprises in situ generated H2, external H2 and/or recycled H2. The oxygenated hydrocarbon comprises a 1-12C and 1-11O hydrocarbon or a 1-6C and 1-6O hydrocarbon. The oxygenated hydrocarbon further comprises recycled greater than 1C and greater than one oxygen hydrocarbon. The oxygenate comprises a member selected from an alcohol, ketone, aldehyde, furan, diol, triol, hydroxy carboxylic acid and/or carboxylic acid (preferably methanol, ethanol, n-propyl alcohol, isopropyl alcohol, butyl alcohol, pentanol, hexanol, cyclopentanol, cyclohexanol, 2-methylcyclopentanol, hydroxyketones, cyclic ketones, acetone, propanone, butanone, pentanone, hexanone, 2- methyl-cyclopentanone, ethylene glycol,1,3-propanediol, propylene glycol, butanediol, pentanediol, hexanediol, methylglyoxal, butanedione, pentanedione, diketohexane, hydroxyaldehydes, acetaldehyde, propionaldehyde, butyraldehyde, pentanal, hexanal, formic acid, acetic acid, propionic acid, butanoic acid, pentanoic acid, hexanoic acid, lactic acid, glycerol, furan, tetrahydrofuran, dihydrofuran, 2-furan methanol, 2-methyl-tetrahydrofuran, 2,5-dimethyl-tetrahydrofuran, 2-ethyl-tetrahydrofuran, 2-methyl furan, 2,5-dimethyl furan, 2-ethyl furan, hydroxylmethylfurfural, 3-hydroxytetrahydrofuran, tetrahydro-3-furanol, 5- hydroxymethyl-2(5H)-furanone, dihydro-5-(hydroxymethyl)-2(3H)-furanone, tetrahydro-2-furoic acid, dihydro-5-(hydroxymethyl)-2(3H)-furanone, tetrahydrofurfuryl alcohol, 1-(2-furyl)ethanol and/or hydroxymethyltetrahydrofurfural, or their isomers). The oxygenate further comprises recycled greater than 1C and 1-3O hydrocarbon. The greater than 4C alkane comprises a branched or straight chain 4-30C alkane selected from 4-9C, 7-14C and/or 12-24C alkanes. The greater than 4C alkene comprises a branched or straight chain 4-30C alkene selected from 4-9C, 7-14C and/or 12-24C alkenes. The greater than 5C cycloalkane comprises a mono-substituted or multi-substituted greater than 5C cycloalkane, and at least one substituted group is a member selected from a branched greater than 3C alkyl, a straight chain greater than 1C alkyl, a branched greater than 3C alkylene, a straight chain greater than 1C alkylene, and/or phenyl. The mono-substituted or multi-substituted greater than 5C cycloalkane is substituted with a member selected from a branched 3-12C alkyl, a straight chain 1-12C alkyl, a branched 3-12C alkylene, a straight chain 1-12C alkylene, and/or phenyl. The substituted group is a member selected from branched 3-4C alkyl, a straight chain 1-4C alkyl, a branched 3-4C alkylene, straight chain 1-4C alkylene, and/or phenyl. The greater than 5C cycloalkene comprises a mono-substituted or multi-substituted greater than 5C cycloalkene, and the substituted group is a member selected from a branched greater than 3C alkyl, a straight chain greater than 1C alkyl, branched greater than 3C alkylene, a straight chain greater than 2C alkylene, and/or phenyl. The aryl comprises an unsubstituted aryl, a mono-substituted or multi-substituted aryl, and, where the substituted group is a member selected from a branched greater than 3C alkyl, a straight chain greater than 1C alkyl, a branched greater than 3C alkylene, a straight chain greater than 2C alkylene, and/or phenyl. The substituted group is a member selected from branched 3-12C alkyl, a straight chain 1-12C alkyl, a branched 3-12C alkylene, a straight chain 2-12C alkylene, and/or phenyl. The fused aryl comprises an unsubstituted fused aryl, mono-substituted or multi-substituted fused aryl, and, where the substituted group is a member selected from a branched greater than 3C alkyl, a straight chain greater than 1C alkyl, a branched greater than 3C alkylene, a straight chain greater than 2C alkylene, and/or phenyl. The substituted group is a member selected from branched 3-4C alkyl, a straight chain 1-4C alkyl, a branched 3-4C alkylene, a straight chain 2-4C alkylene, and/or phenyl. Preferred Compound: The greater than 4C alcohol comprises a compound according to the formula R1-OH. The greater than 4C ketone comprises a compound according to the formula (R3)(R4)C=O.R1=greater than 4C alkyl (branched or straight chain), greater than 4C alkylene (branched or straight chain), greater than 5C cycloalkane (optionally substituted), greater than 5C cycloalkene (optionally unsubstituted), aryl and/or phenyl;andR3 and R4=branched greater than 3C alkyl, a straight chain greater than 1C alkyl, branched greater than 3C alkylene, straight chain greater than 2C alkylene, greater than 5C cycloalkane (optionally substituted), greater than 5C cycloalkene (optionally substituted), aryl, and/or phenyl.Preferred Composition: The composition comprises a member selected from benzene, toluene, xylene, ethyl benzene, para xylene, meta xylene, ortho xylene and/or 9C aromatics, or their isomers.    TECHNOLOGY FOCUS - POLYMERS - Preferred Components: The oxygenated hydrocarbon comprises a member selected from polysaccharides, disaccharides, monosaccharides, cellulose derivatives, lignin derivatives, hemicellulose, sugars and/or sugar alcohols. The 1-12C and 1-11O hydrocarbon comprises a member selected from sugar alcohol, alditol, cellulosic derivative, lignocellulosic derivative, glucose, fructose, sucrose, maltose, lactose, mannose, xylose, arabitol, erythritol, glycerol, isomalt, lactitol, malitol, mannitol, sorbitol and/or xylitol. EXAMPLE - A bimetallic catalyst system containing platinum (pt) and rhenium (Re) (5 wt.% platinum with a molar ratio of Pt:Re of 1:2.5) supported on activated carbon was prepared. Activated carbon was added slowly to a 30% hydrogen peroxide solution. After addition of the carbon was completed, the mixture was left overnight. The aqueous phase was decanted and the carbon was washed three times with of deionized water, and then dried under vacuum at 100 degrees C. An aqueous solution, with a volume equal to incipient wetness volume for the carbon to be impregnated, 10.4 ml, and containing dihydrogen hexachloroplatinate (IV) hexahydrate and perrhemic acid solution (76.41%) was applied drop wise, while stirring, to hydrogen peroxide functionalized carbon. The wetted carbon was dried at 100 degrees C under vacuum. 1:2.5 Pt/Re catalyst (104.4 g) were loaded into a long reactor tube (63.5 cm), except that the temperature profile was controlled by heat exchange with a hot air stream provided by a blower and heater. The catalyst was reduced with flowing hydrogen at 350 degrees C for two hours before liquid feed was introduced to the catalyst bed. A 50 wt% glycerol containing sulfate (20 ppm) in water solution was fed downflow across the reactor after preheated to 182 degrees C at a weight hourly space velocity of 0.97 g of glycerol per gram of catalyst per hour. Hot air was fed upflow through the annular space at 409 degrees C. The separator pressure was maintained at 600 psig. The effluent from the reactor was cooled down with a water cooled condenser and separated in a three-phase separator. The gas-phase products were analyzed and an organic phase was collected and analyzed for gasoline. The aqueous-phase was collected and weighed, and then analyzed. In this system, there was complete conversion of the glycerol. The results showed that the method provides %carbon/carbon in feed of 5-10C olefins (5.67); 8-11C naphthalene/naphthenes 1.89; 6-12C aromatics (3.87); 4-13C isoparaffins (2.87) and 7-13C normal paraffins 0.87.