TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The methanol-to-olefins catalyst comprises an aluminosilicate zeolite, which is ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35 or ZSM-48. The methanol-to-olefins catalyst comprises a silicoaluminophosphate (SAPO). The SAPO is SAPO-5, SAPO-8, SAPO-11, SAPO-16, SAPO-17, SAPO-18, SAPO- 20, SAPO-31, SAPO-34 (preferred), SAPO-35, SAPO-36, SAPO-37, SAPO-40, SAPO-41, SAPO-42, SAPO-44, SAPO-47 or SAPO-56. The SAPO further includes one or more transition metals, which are manganese, nickel (preferred), or cobalt. The methanol-to-olefins catalyst is nickel (Ni)-SAPO-34. The ratio of silicon to the transition metal is 1-500, preferably 10-200.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The syngas is derived from biomass. The step (c) is conducted in the presence of one or more olefin-hydration catalysts. The step of hydrating ethylene and propylene is conducted substantially simultaneously. The process further comprises: separating the ethylene from the propylene generated in step (b) and then separately hydrating the ethylene and the propylene during step (c); generating butenes during step (b); hydrating the butenes to 2-butanol during step (c); separating unhydrated olefins from alcohols by distillation; separating unhydrated olefins from alcohols by absorption of the alcohols into water; separating unhydrated olefins from alcohols by absorption of the alcohols into dimethyl ether; and separating the ethanol and/or the 2-propanol from water; separating the ethanol from the 2-propanol. During step (c), one or more dialkyl ethers are generated, where the method further comprises removing at least a portion of the dialkyl ethers during or after step (c). The hydrating of the propylene is substantially conducted prior to hydrating of the ethylene. The hydrating is conducted in a first reaction zone for converting propylene into 2-propanol and a second reaction zone for converting ethylene into ethanol, where the first reaction zone is located in a first reactor and the second reaction zone is located in a second reactor; and both of the reaction zones are located in a single reactor. The temperature within the first reaction zone is lower than the temperature within the second reaction zone. The temperature within the first reaction zone is 125-200 degrees C and the temperature within the second reaction zone is 200-250 degrees C. In the process: at least a portion of water produced from reactions during step (b) is used for the hydrating during step (c); and substantially all of the water produced during step (b) is fed to step (c). The removing step comprises evaporation of dimethyl ether. The olefins are derived from methanol, and the alcohols are generated from hydration of the olefins. During the step (b1), ethanol and 2-propanol absorb into the dimethyl ether, where ethylene and propylene do not substantially absorb into the dimethyl ether. The dimethyl ether is derived from the methanol. The combined yield of the ethanol and the 2-propanol from the biomass is at least 70 gallons, preferably at least 120 gallons per dry ton biomass. The yield of ethanol is at least 100 gallons per dry ton biomass. The yield of 2-propanol is at least 50 gallons per dry ton biomass. The process comprises blending at least some of the 2-propanol into gasoline. Preferred Components: The molar ratio of ethylene to propylene is greater than 2, preferably greater than 10. The olefin-hydration catalysts are zeolites, supported acids, acidic resins, or heteropoly acids. The olefin-hydration catalysts include sulfuric acid; a catalyst for ethylene hydration; and a catalyst for propylene hydration. The catalyst for ethylene hydration includes supported phosphoric acid. The olefins include ethylene and propylene. The alcohols include ethanol and 2-propanol. EXAMPLE - None given.