TECHNOLOGY FOCUS - BIOLOGY - Preferred Components: The microorganism is Clostridium butyricum, Clostridium acetobutylicum, Clostridium saccharoperbutylacetonicum or Clostridium beijerickii. The microorganism is a temperature resistant microorganism. The microorganism is viable at 20-95 degrees C. The microorganism has a productivity of at least 0.5 g/l per hour.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The step of increasing the activity is: addition of a hydrophilic solute; distilling a vapor phase comprising water and (I); reverse osmosis; dialysis; adsorption of (I) on an alcohol-selective adsorbent; extraction of (I) into an alcohol-selective extractant; adsorption of water on a water-selective adsorbent; and extraction of water into a water-selective extractant. The method further comprises cooling the 3-6C alcohol-rich phase to increase the ratio of (I) to water in the 3-6C alcohol-rich phase; recovering (I) from the 3-6C alcohol-rich phase by a process of distillation, dialysis, water adsorption, extraction of (I) by solvent extraction, contact with a hydrocarbon liquid that is immiscible in water and contact with a hydrophilic compound to produce a first phase comprising (I) and water and a second phase comprising (I), where the ratio of water to (I) in the second phase is less than in the first phase. The step of recovering comprises distilling the 3-6C alcohol-rich phase, where the first phase comprises a vapor phase comprising (I) and water and the second phase comprises a high boiling product comprising (I). The method further comprises combining the fermentation broth with the water-rich phase from the separating step or the high boiling product comprising (I), prior to the step of increasing the activity of (I); and after the step of increasing the activity, conducting the remaining portion of the dilute aqueous solution to a fermentation vessel. The remaining portion comprises an impurity and the method further comprises removing at least a portion of the impurity from at least a portion of the remaining portion before the step of conducting. The step of increasing the activity comprises distilling a vapor phase comprising water and (I), and condensing the vapor phase and the method further comprises treating the portion of the fermentation broth for water removal before the step of distilling or simultaneously with it, or treating the 3-6C alcohol-rich phase for water removal, by a step of: selective removal of water, selective binding of water or selective rejection of water; or addition of a hydrophilic solute, addition of a carbon source, reverse osmosis, dialysis, adsorption of (I) on an alcohol-selective adsorbent, extraction of (I) into an alcohol-selective extractant, adsorption of water on a water-selective adsorbent or extraction of water into a water-selective extractant. The step of distilling is conducted at below atmospheric pressure and at 20-95 degrees C in a distillation vessel. The portion of the fermentation broth is at 20-95 degrees C prior to introduction into the distillation vessel. The portion of the fermentation broth is subjected to the below atmospheric pressure in the distillation vessel. The method further comprises after the step of distilling, conducting the remaining portion of the fermentation broth from the distillation vessel to a fermentation vessel. The fermentation vessel is at atmospheric pressure or at below atmospheric pressure or at above atmospheric pressure. The step of distilling is conducted at a pressure of 0.025-10 bar. The step of distilling is conducted in a fermentation vessel. The method further comprises processing the 3-6C alcohol-rich phase. The step of processing is distilling substantially pure (I) from the 3-6C alcohol-rich phase; distilling an azeotrope of (I) from the 3-6C alcohol-rich phase; contacting the 3-6C alcohol-rich phase with a 3-6C alcohol-selective adsorbent; converting (I) in the 3-6C alcohol-rich phase to an olefin; and combining the 3-6C alcohol-rich phase with a hydrocarbon liquid that is immiscible in water. The step of processing comprises combining the 3-6C alcohol-rich phase with a hydrocarbon liquid that is immiscible in water and the combination forms a single uniform phase; combining the 3-6C alcohol-rich phase with a hydrocarbon liquid that is immiscible in water and the combination forms a light phase and a heavy phase, where the ratio of (I) to water in the light phase is greater than the ratio of (I) to water in the heavy phase. The method to recover (I) from a fermentation broth comprising microorganisms and (I), comprises decreasing the activity of water in a portion of the fermentation broth to at least that of saturation of (I) in the portion; forming a water-rich liquid phase and a 3-6C alcohol-rich phase from the portion of the fermentation broth; and separating the water-rich phase and the 3-6C alcohol-rich phase. The step (a1) is a process of a batch fermentation, a fed-batch fermentation, a continuous fermentation, a cell recycle fermentation or an enzyme reaction process. The step (b1) comprises saccharification. In the method of producing (I), at least two of the steps of hydrolyzing, fermenting and increasing the activity of (I) are conducted simultaneously for at least a portion of time. The step (b2) is conducted with a microorganism that is capable of hydrolyzing the feedstock. In the method of producing (I) comprising steps (c1 and c2): If (I) is propanol, then the ratio of (I) to water in the vapor phase is greater than 0.2 (wt/wt); If (I) is butanol, then the ratio of (I) to water in the vapor phase is greater than 1 (wt/wt); If (I) is pentanol, then the ratio of (I) to water in the vapor phase is greater than 4 (wt/wt); and the step of reacting is carried out in the presence of a catalyst (a heterogeneous catalyst). In the method of producing (I) comprising steps (d1-d4), the ratio of (I) to water in the portion of the fermentation medium is less than 7.5/92.5, 5/95 or 2.5/97.5 (wt/wt). In step (d3), the liquid phase comprises an impurity and the method further comprises removing at least a portion of the impurity from at least a portion of the liquid phase before the step of conducting. The step (d2) comprises a step of: selective removal of water; selective binding of water; or selective rejection of water; or addition of a hydrophilic solute; addition of a carbon source; reverse osmosis; dialysis; adsorption of (I) on a selective adsorbent; and adsorption of water on a selective adsorbent. The method of producing (I) comprising steps (d1-d4), further comprises condensing the vapor phase to form a 3-6C alcohol-rich liquid phase and a water-rich liquid phase and separating the 3-6C alcohol-rich phase from the water-rich phase; treating the 3-6C alcohol-rich phase for water removal; treating the 3-6C alcohol-rich phase for water removal by a step of addition of a hydrophilic solute, addition of a carbon source, reverse osmosis, dialysis, adsorption of (I) on an alcohol-selective adsorbent, extraction of (I) into an alcohol-selective extractant, adsorption of water on a water-selective adsorbent or extraction of water into a water-selective extractant. The method to recover (I) from a dilute aqueous solution that comprises a first amount of (I), comprises: distilling a portion of the dilute aqueous solution to a vapor phase comprising (I) and water, where the vapor phase comprises 1-45 wt.% of the first amount of (I) from the portion of the dilute aqueous solution; and condensing the vapor phase. The method to recover (I) from a dilute aqueous solution further comprises forming a 3-6C alcohol-rich liquid phase and a water-rich liquid phase from the condensed vapor phase; and separating the 3-6C alcohol-rich phase and the water-rich phase. The step of distilling is a single stage distillation. The step of distilling is adiabatic and isothermal. The acidic amine-based extractant is formed by acidifying an organic amine solution. In the method of extracting (I) from aqueous solution, two phases form after the contacting. Preferred Components: The ratio of (I) to water in the fermentation broth is less than 9/91, 6/94 or 3/97 (wt/wt). When (I) is propanol, then the ratio of (I) to water in the 3-6C alcohol-rich phase is greater than 0.2 (wt/wt). (I) is propanol (preferably 1-propanol or 2-propanol), butanol, (preferably 1-butanol, 2-butanol, tert-butanol(2-methyl-2-propanol), or iso-butanol(2-methyl-2-propanol) (preferred)), pentanol (1-pentanol, 2-pentanol, 3-pentanol, 2-methyl-1-butanol, 3-methyl-1-butanol, 2-methyl-2-butanol, 3-methyl-2-butanol, or 2,2-dimethyl-1-propanol) or hexanol (1-hexanol, 2-hexanol, 3-hexanol, 2-methyl-1-pentanol, 3-methyl-1-pentanol, 4-methyl-1-pentanol, 2-methyl-2-pentanol, 3-methyl-2-pentanol, 4-methyl-2-pentanol, 2-methyl-3-pentanol, 3-methyl-3-pentanol, 3,3-dimethyl-1-butanol, 2,2-dimethyl-1-butanol, 2,3-dimethyl-1-butanol, 2,3-dimethyl-2-butanol, 3,3-dimethyl-2-butanol, or 2 ethyl-1-butanol). When (I) is butanol, then the ratio of (I) to water in the 3-6C alcohol-rich phase is greater than 1 (wt/wt). When (I) is pentanol, then the ratio of (I) to water in the 3-6C alcohol-rich phase is greater than 4 (wt/wt). The fermentation broth comprises an impurity and the ratio of the impurity to (I) in the 3-6C alcohol-rich liquid phase is greater than the ratio in the water-rich phase. The ratio of (I) to water in the 3-6C alcohol-rich phase is greater than the ratio of (I) to water in the fermentation broth by at least 5 fold. The second phase comprises at least 90 (preferably at least 99) wt.% of (I). The vapor phase comprises an azeotrope of water and (I). The ratio of (I) to water in the 3-6C alcohol-rich phase is greater than the ratio in the azeotrope. The vapor phase comprises preferably 5-25 wt.% of (I) from the dilute aqueous solution. The ratio of (I) to water in the dilute aqueous solution is less than 9/91, 6/94 or 3/97 (wt/wt). EXAMPLE - GEVO1780 was a modified bacterial biocatalyst that contains genes on two plasmids which encode a pathway of enzymes that convert pyruvate into isobutanol. When the biocatalyst GEVO1780 was contacted with glucose in a medium for growth of the biocatalyst, at 30 degrees C, the biocatalyst produced isobutanol from the glucose. An overnight starter culture was started in a flask with GEVO1780 cells from a freezer stock with a modified M9 medium (40 ml) consisting of glucose (85 g/l), yeast extract (20 g/l), ferric citrate (20 mM), boric acid (5.72 mg/l), manganese chloride tetrahydrate (3.62 mg/l), zinc sulfate heptahydrate (0.444 mg/l), sodium manganate dihydrate (0.78 mg/l), copper sulfate pentahydrate (0.158 mg/l), cobalt chloride hexahydrate (0.0988 mg/l), sodium hydrogenphosphate (6 g/l), potassium dihydrogenphosphate (3 g/l), sodium chloride (0.5 g/l), ammonium chloride (2 g/l), magnesium sulfate (0.0444 g/l) and calcium chloride (0.00481 g/l). The starter culture was grown for 14 hours in a 30 degrees C shaker at 250 rpm. Some of the starter culture was then transferred to a fermentor vessel containing modified M9 medium (1500 ml). The vessel was attached to a computer control system to monitor and control pH at 6.5 through addition of base, at 30 degrees C, dissolved oxygen, and agitation. After continuing growth for 8-10 hours, the dissolved oxygen content was decreased to 5%. Continuous measurement of the fermentor vessel off-gas by garbage collection-mass spectrometry analysis was performed for oxygen, isobutanol, isobutanol, ethanol, and carbon dioxide throughout the experiment. The culture was concentrated by centrifugation and then added to the fermentor. A glucose feed of 500 g/l glucose in deionized water was used intermittently during the production phase of the experiment. The fermentor vessel was attached by tubing to a smaller 400 ml fermentor vessel that served as a flash tank (30) and operated in a recirculation loop with the fermentor. The biocatalyst cells within the fermentor vessel were isolated from the flash tank. The filter only allowed cell-free fermentation broth to flow from the fermentor vessel into the flash tank. Heat and vacuum were applied to the flash tank. The distillate recovered in the experiment was strongly enriched for isobutanol. Isobutanol formed an azeotrope with water and usually lead to a two phase distillate: an isobutanol rich top phase and an isobutanol lean bottom phase. Distillate samples were analyzed. Isobutanol production reached a maximum at around 118 hours with a batch concentration of 87 g/l. The percent theoretical yield of isobutanol was 90.4% at the end of the experiment.