TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Apparatus: The apparatus (A1) comprises an enclosure providing a fractional condensation volume for the mixture, where the enclosure having an internal surface in contact with the fractional condensation volume, where the temperature of the internal surface is controllable, and the enclosure having an inlet adapted for receiving the feed mixture and an outlet for providing recovered compound; a second surface positioned centrally within the fractional condensation volume, where the temperature of the second surface is controllable; and first packing material between the internal surface and the second surface. In the apparatus (A1), the first packing material provides thermal contact between the internal surface of the enclosure and the second surface. When the feed mixture is a vapor feed, and the compound has an initial concentration in the vapor feed of 0.5-10 mol.%, and then the apparatus (A1) is adapted in the presence of a suitable temperature conditions to recover the compound with a purity of 40% and a recovery yield of at least 20%. When the feed mixture is a vapor feed and the compound has an initial concentration in the vapor feed of 0.5-3 mol.%, and then the apparatus (A1) is adapted in the presence of a suitable temperature conditions to recover the compound with a purity of 77% and a recovery yield of 84%. When the feed mixture is a vapor feed, and the compound has an initial concentration in the vapor feed of 0.5-3 mol.%, then the apparatus (A1) is adapted in the presence of a suitable temperature conditions to recover the compound with a purity of 90% and a recovery yield of 90%. When the feed mixture is a feed solution, and the compound has an initial concentration in the feed solution of 0.5-5 wt.%, then the apparatus (A1) is adapted in the presence of a suitable temperature conditions to recover the compound with a purity of 40% and a recovery yield of 20% within 8 hours. When the feed mixture is a feed solution, and the compound has an initial concentration in the feed solution of 0.5-5 wt.%, then the apparatus (A1) is adapted in the presence of a suitable temperature conditions to recover the compound with a purity of 74% and a recovery yield of 74% within 8 hours. When the feed mixture is a feed solution, and the compound has an initial concentration in the feed solution of 0.5-3 wt.%, then the apparatus (A1) is adapted in the presence of a suitable temperature conditions to recover the compound with a purity of 90% and a recovery yield of 74% within 8 hours. The apparatus (A1/A3) is adapted to be modular. The apparatus (A1) further comprises a bottom opening and a top opening in the enclosure adapted for connecting the apparatus with another apparatus, where the apparatus is adapted to allow flow of the feed mixture through the bottom opening and the top opening. The apparatus (A1/A3) is adapted for control of temperature within the fractional distillation volume, both across and along the column. The apparatus (A2) further comprises a unit for culturing microorganisms in a photobioreactor under suitable conditions using light, CO2 and water to produce carbon-based products of interest. In the apparatus (A3), the reactive zone is part of the fractional condensation volume. The reactive distillation apparatus (A3) comprises a fractional condensation column providing a fractional condensation volume, containing a column jacket, a fluid tube positioned centrally within the column and along the length of the column, and first packing material between the column jacket and the fluid tube; and a reactive zone, where the column jacket extends around the circumference of the column and along the length of the column, and is entirely filled with second packing material. Preferred Column: In the fractional condensation column (C1), the first packing material provides thermal contact between the column jacket and the fluid tube, where the column jacket is adapted to be evacuated. The column jacket is adapted for flowing a fluid and contains second packing material. In the column (C1), the column jacket extends around the circumference of the column and along the length of the column, and is entirely filled with the second packing material, where the first packing material are in direct contact with an internal wall of the column jacket and the fluid tube. The column (C1) is adapted to be modular. The column (C1) further comprises a bottom opening and a top opening adapted for connecting the fractional condensation column with another fractional condensation column, where the fractional condensation column is adapted to allow flow of the feed mixture through the bottom opening and the top opening. The column (C1) is adapted for control of temperature within the column, both across and along the column, where the fluid tube has an inlet at the top of the fractional condensation column and an outlet at the bottom of the fractional condensation column, and the column jacket has an inlet at the top of the fractional condensation column and an outlet at the bottom of the fractional condensation column, where the first and second packing material are beads. Preferred System: In the solar biofactory system (S3), the product of interest is at least one primary, secondary or tertiary alcohol, where the products are produced with a rate of at 4-9 g/m2/hour. Preferred Components: The enclosure comprises a columnjacket which is adapted to be evacuated and/or is adapted for flowing fluid, and the column jacket has an internal wall providing the internal surface. The columnjacket contains second packing material. The temperature control unit within the fractional condensation volume is a fluid tube positioned centrally within the column and along the length of the column. The first packing material is in direct contact with the internal surface and the fluid tube. The packing material is beads.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: In the process (P1), the top condenser is an integral part of the fractional condensation apparatus. The feed mixture is a vapor feed with a concentration of the volatile organic compound of 1-3 mol.% and a temperature of 37-38 degrees C before fractional condensing, and the top condenser has a temperature of 6-9 degrees C. The feed mixture is a vapor feed with a concentration of the volatile organic compound of 1-3 mol.% and a temperature of 54-56 degrees C before fractional condensing, and the top condenser has a temperature of 7-11 degrees C. In the process (P1), the compound is ethanol. When the feed mixture is a vapor feed with a concentration of ethanol of 1.5-2.5 mol.% and a temperature of 37-38 degrees C before fractional condensing, where the top condenser has a temperature of 6-9 degrees C, then the method further involves providing a total cooling duty of not greater than primary energy unit (PEU) 6 MJ/kg ethanol to recover the ethanol with a concentration of at least 80 wt.% in the product stream and a recovery of 90 wt.%. When the feed mixture is a vapor feed with a concentration of ethanol of 1.5-2.5 mol% and a temperature of 55-56 degrees C before fractional condensing, where the top condenser has a temperature of 7.5-9.5 degrees C, then the method further involves providing a total cooling duty of not greater than PEU 8 MJ/kg ethanol to recover the ethanol with a concentration of 80 wt.% in the product stream and a recovery of 90 wt.%. When the feed mixture is a vapor feed with a concentration of ethanol of 1.5-2.5 mol.% and a temperature of 37-38 degrees C before fractional condensing, where the top condenser has a temperature of 7-8 degrees C, then the method further involves providing a total cooling duty of not greater than (PEU) 6 MJ/kg ethanol to recover the ethanol with a concentration of 85 wt.% and a recovery of 95 wt.%. The product condenser has a temperature of -25 to -45 degrees C (preferably -35 degrees C). The product condenser further produces a cold vent stream, and the method further involves heating the cold product stream and the cold vent stream by providing cooling duty to the fractional condensation apparatus, where the fractional destination apparatus has a temperature profile from entry of the feed mixture to exit of the first condensed fluid which is controlled to improve recovery and concentration of the volatile organic compound in the product stream. In the method (P2/P3), controlling the temperature profile of the internal surface includes flowing a fluid through the enclosure, where controlling the temperature profile of the second surface includes flowing a fluid through a fluid tube providing the second surface. In the method (P4/P5), controlling the temperature profile of the column jacket includes flowing a fluid through it, where controlling the temperature profile of the fluid tube includes flowing a fluid through the fluid tube. The method (P6) for recovering volatile products involves introducing a feed mixture that contains at least one volatile product at a concentration of 1.5-5 wt.% into a fractional condenser; separating the volatile products under optimized operating conditions; and withdrawing the products at a concentration of 90.4% recovery yield and 90 wt.% concentration. In the method (P6), the products are withdrawn at a concentration of 90.4 wt.% (relative to water) for mesophiles or about 93.8 wt.% (relative to water) for thermophiles. In the method (P6), the products are withdrawn at a concentration of 96.7% recovery for mesophiles or about 96.9% recovery for thermophiles. The method (P6) further involves using PEU cooling 4.05 MJ/Kg product for mesophiles. The method (P6) further involves using PEU cooling 5.92 MJ/Kg product, where the volatile product are produced by thermophiles. The method (P6) further involves using PEU heating about 1.12 MJ/Kg product, where the volatile products are produced by thermophiles. The method (P6) further involves reducing cooling duty to be provided by at least about (PEU) 1 MJ/Kg product by energy integration, where the volatile products are recovered with an energy saving of PEU about 1.36 MJ/(Kg product) for volatile products produced by mesophiles or 1.05 MJ/Kg product for volatile products produced by thermophiles. In the method (P6), introducing the feed mixture is at a temperature of 38 degrees C for volatile products produced by mesophiles, and 55 degrees C degrees for volatile products produced by thermophiles. In the method (P6), separating the volatile products at optimized operating conditions further comprises operating the top of the fractional condenser at 6.4-7.9 degrees C (preferably 7.4 degrees C) for mesophiles. In the method (P6), separating the volatile products at optimized operating conditions further comprises operating the top of the fractional condenser at 9 degrees C for thermophiles, where recovering volatile products reduces water loss or maintains water level circulated, and the feed mixture comprises air, water and gas. The process for recovering a volatile organic compound from a feed mixture involves fractionally condensing the feed mixture in a fractional condensation apparatus (A1), in a multi-sectional modular distillation system (S1/S2), or in a fractional condensation column (C1) to form a first condensed fluid, where the feed mixture having a temperature of 36 degrees C before fractional condensing; condensing the first condensed fluid in a top condenser to form a second condensed fluid, where the top condenser having a temperature of 6-14 degrees C; and condensing the second condensed fluid in a product condenser to form a cold product stream, where the product condenser having a temperature that is below the temperature of the top condenser, where the feed mixture contains the volatile organic compound (1-5 mol.%), water (5 mol.%), and gases (80 mol.%) selected from the N2, O2 and CO2, and the cold product stream contains at least 80 wt.% of the volatile organic compound. The process (P8) for ethanol production involves cultivating an engineered phototroph in cultivation medium contained in a photobioreactor, where the cultivation medium being controlled to have a temperature of 30-60 degrees C, and the phototrophic organism being engineered to secret ethanol into the cultivation medium; seperating a feed mixture from the cultivation medium containing the phototroph; and recovering the ethanol. In the process (P8), the engineered phototroph is a mesophile and the cultivation medium is controlled to have a temperature of 37-38 degrees C. In the process (P8), the engineered phototroph is a thermophile and the cultivation medium is controlled to have a temperature of 54-56 degrees C. The process (P8) further involves heating or cooling the feed mixture seperated from the cultivation medium prior to introducing it into the fractional condensation apparatus. The method (P2) involves flowing the feed mixture through a bottom inlet of a fractional condensation apparatus (A1) into the fractional condensation volume; controlling, independently, temperature profile of the internal surface and the second surface to provide an internal temperature profile within the fractional condensation volume extending from the bottom inlet to a top outlet of the apparatus, which is effective to recover the compound from the feed mixture at the top outlet with improved purity; and collecting the compound at the top outlet. The method (P3) involves flowing the feed mixture through a bottom inlet of the multi-sectional modular distillation system (S1) into a fractional condensation volume of a first fractional condensation apparatus; controlling, independently, temperature profiles of the internal surfaces and the second surfaces of the fractional condensation apparatuses of the multi-sectional modular distillation system to provide an internal temperature profile within the fractional condensation volumes within the several apparatuses, extending from the bottom inlet of the first fractional condensation apparatus to a top outlet of a last fractional condensation apparatus, which is effective to recover the compound from the feed mixture at the top outlet with improved purity; and collecting the compound at the top outlet. The process (P4) involves flowing the feed mixture through a bottom inlet of the fractional condensation column (C1) into a fractional condensation volume provided between the column jacket and the fluid tube; controlling, independently, temperature profile of the column jacket and the fluid tube to provide an internal temperature profile within the fractional condensation volume extending from the bottom inlet to a top outlet of the column, which is effective to recover the compound from the feed mixture at the top outlet with improved purity; and collecting the compound at the top outlet. Preferred Components: The feed mixture comprises at least one of alcohol, hydrocarbon or biodiesel. The feed mixture further comprises at least one gas selected from nitrogen gas and oxygen gas. The feed mixture comprises ethanol, nitrogen gas and oxygen gas. EXAMPLE - No suitable example given.