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A method for producing liquid hydrocarbons from biomass includes hydropyrolizing biomass with a gaseous exhaust stream formed from one of gasification and reforming of carbon containing moiety (CCM). The gaseous exhaust stream includes hydrogen (H2) and at least one of carbon monoxide (CO), carbon d

A method for producing liquid hydrocarbons from biomass includes hydropyrolizing biomass with a gaseous exhaust stream formed from one of gasification and reforming of carbon containing moiety (CCM). The gaseous exhaust stream includes hydrogen (H2) and at least one of carbon monoxide (CO), carbon dioxide (CO2) and water (H2O).

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1. A method for producing liquid hydrocarbons from a biomass, the method comprising: hydropyrolizing the biomass with a gaseous exhaust stream formed from gasification and/or reforming of a carbon-containing moiety (CCM), the gaseous exhaust stream comprising hydrogen (H2) and a material selected fr

1. A method for producing liquid hydrocarbons from a biomass, the method comprising: hydropyrolizing the biomass with a gaseous exhaust stream formed from gasification and/or reforming of a carbon-containing moiety (CCM), the gaseous exhaust stream comprising hydrogen (H2) and a material selected from the group consisting of carbon monoxide (CO), carbon dioxide (CO2), water (H2O), and combinations thereof; wherein the hydropyrolizing comprises fast pyrolysis in presence of hydrogen. 2. The method according to claim 1, wherein the gaseous exhaust stream is used for the hydropyrolizing without separating out the CO, the CO2, the H2O and the H2 subsequent to being formed by the gasification and/or reforming. 3. The method according to claim 2, wherein pollutants are removed from the CCM prior to the gasification and/or reforming of the CCM. 4. The method according to claim 2, wherein the gaseous exhaust stream is free of cooling between the gasification and/or reforming of the CCM via a gasifier/reformer and the hydropyrolizing via a biomass hydropyrolysis unit. 5. The method according to claim 1 further comprising cooling and water-gas shift reacting the gaseous exhaust stream to increase concentration of the H2 in the gaseous exhaust stream, and then successively reheating the gaseous exhaust stream, and feeding the gaseous exhaust stream to a hydropyrolysis reactor. 6. The method according to claim 1, wherein the CCM comprises a carbon-containing material that forms syngas during the gasification and/or reforming to define the gaseous exhaust stream, the carbon-containing material comprising pet coke, methane, natural gas, naphtha, coal, biomass, municipal waste, or a mixture thereof. 7. The method according to claim 1, wherein the liquid hydrocarbons comprise chemically bonded carbon and hydrogen atoms, and are in liquid form when in a closed container at a temperature of 20° C. and a pressure of 1 atmosphere. 8. The method according to claim 1, wherein the liquid hydrocarbons comprise methanol, ethanol, long chain alcohols, alkanes, alkenes, aromatics, substituted aromatics compounds thereof or mixtures thereof. 9. The method according to claim 1, wherein the biomass comprises carbon, plant material, tree material, aquatic material or a mixture thereof. 10. The method according to claim 1, wherein the gaseous exhaust stream defines syngas and the hydropyrolizing occurs in a hydropyrolysis reactor, and wherein the biomass and the syngas react in the hydropyrolysis reactor to define fast hydropyrolysis. 11. The method according to claim 10, wherein a residence time of the biomass reacting with the syngas in the hydropyrolysis reactor is less than about 1 minute. 12. The method according to claim 10, wherein a temperature during fast hydropyrolysis is between about 400° C. and about 600° C. 13. The method according to claim 10, wherein the hydropyrolysis reactor comprises a hydrodeoxygenation (HDO) catalyst facilitating fast hydropyrolysis. 14. The method according to claim 13, wherein the hydropyrolysis reactor further comprises sand mixed with the HDO catalyst and a water-gas shift (WGS) catalyst, and wherein the WGS catalyst is mixed with and disposed on the sand. 15. The method according to claim 10, wherein the hydropyrolizing produces a gas-phase effluent, and the method further comprises sending at least a majority of the gas-phase effluent to a hydrodeoxygenation reactor. 16. The method according to claim 15, wherein the sending of the gas-phase effluent comprises removing char from the gas-phase effluent prior to reception of the gas-phase effluent by the hydrodeoxygenation reactor. 17. The method according to claim 15, wherein the gasification and/or reforming of the CCM is conducted in the hydropyrolysis reactor providing the syngas in-situ and process heat for fast-hydropyrolysis of the biomass. 18. The method according to claim 15, wherein the gasification and/or reforming of the CCM occurs in a reformer, and wherein the CCM comprises natural gas (NG) and at least a portion of the gas-phase effluent, the NG being a lesser proportion of the CCM than the gas-phase effluent. 19. The method according to claim 18, wherein a portion of the gas-phase effluent is separated into a CO2-rich stream and a CO2-deficient stream, wherein the CO2-rich stream is fed to burners of the reformer, and wherein the CO2-deficient stream is sent to the reformer for reforming. 20. The method according to claim 15, wherein the hydrodeoxygenation reactor comprises a hydrodeoxygenation (HDO) catalyst. 21. The method according to claim 20 wherein the hydrodeoxygenation reactor further comprises a water-gas shift (WGS) catalyst. 22. The method according to claim 21, wherein the WGS catalyst is disposed within the hydrodeoxygenation reactor such that the gas-phase effluent interfaces with the WGS catalyst prior to interfacing with the HDO catalyst. 23. The method according to claim 21, wherein the WGS catalyst comprises a linearly decreasing or a sharply decreasing profile within the hydrodeoxygenation reactor. 24. The method according to claim 21, wherein the WGS catalyst is interspersed with the HDO catalyst. 25. The method according to claim 20, wherein the HDO catalyst comprises a multifunctional catalyst having both WGS and HDO activity. 26. The method according to claim 20, wherein a temperature of the gas-phase effluent being fed to the hydrodeoxygenation reactor is adjusted prior to reception of the gas-phase effluent by the hydrodeoxygenation reactor. 27. The method according to claim 26, wherein a temperature of the hydrodeoxygenation reactor is lower than the temperature of the gas-phase effluent prior to adjustment. 28. The method according to claim 15, wherein the hydrodeoxygenation reactor comprises a fixed bed reactor. 29. The method according to claim 15, wherein the hydrodeoxygenation reactor comprises a fluidized bed reactor. 30. The method according to claim 15, wherein effluent from the hydrodeoxygenation reactor is cooled to a condensed liquid bio-oil that is collected as a product stream. 31. The method according to claim 30, wherein at least a portion of the syngas is fed to the hydrodeoxygenation reactor. 32. The method according to claim 30, wherein the gaseous exhaust stream supplies substantially all process heat requirements for the hydropyrolizing. 33. The method according to claim 32, wherein a heat transfer process involving sand recirculation is not used to supplement the process heat requirements for the hydropyrolizing. 34. The method according to claim 30, wherein the sending of the gas-phase effluent comprises removing char from the gas-phase effluent, and wherein the method further comprises sending a portion of the char to a combustor to produce heat, thereby supplying process heat for the gasification and/or reforming of the CCM. 35. The method according to claim 30, wherein the effluent from the hydrodeoxygenation reactor comprises unreacted syngas and non-condensable gases formed during the hydropyrolizing, and wherein the unreacted syngas and non-condensable gases are collected and separated from the bio-oil. 36. The method according to claim 35 wherein at least a portion of the collected unreacted syngas and non-condensable gases is combusted to provide heat for the gasification and/or reforming of the CCM. 37. The method according to claim 35, wherein at least a portion of the collected unreacted syngas and non-condensable gases is sent to a gas turbine for power production. 38. The method according to claim 30, wherein a HDO catalyst is used in the hydropyrolysis reactor and/or the hydrodeoxygenation reactor. 39. The method according to claim 30, wherein the gas-phase effluent comprises unreacted syngas and is sent to the hydrodeoxygenation reactor for use therein.