TECHNOLOGY FOCUS - CHEMICAL ENGINEERING - Preferred Component: The conversion system further comprises a storage for feeding residual product to the fluid in a feeding direction; a pre-treating unit situated after the feedstock and before the first heating unit in the feeding direction; a first particle separating unit situated after the first heating unit in the feeding direction; a second heating unit situated after the first particle separating unit and before the catalyst reactor in the feeding direction; a second particle separation unit after the catalyst reactor in the feeding direction; and feed re-circulating mechanism for re-circulating part of the feed of fluid after the catalyst reactor into the feed of fluid before the second heating unit in the feeding direction. The first heating unit is a first heat exchanger, which besides heating cools the fluid from conversion system before entering the product recovery system. The pre-treating unit further comprises a heat exchanger, which besides heating the fluid in the pre-treating system cools the fluid from conversion system before entering the product recovery system; and a first expansion unit, which is situated between the first heat exchanger and the second heat exchanger. The product recovery system further comprises a gas separating unit for separation of gas, such as fuel gas, where gas separating unit is situated after the second heat exchanger and before the separation unit, preferably being a membrane-filter, in the feeding direction; gas re-circulating mechanism for re-circulating gas, such as fuel gas for heating the fluid in the second heating unit; a second expansion unit situated after the separation unit, preferably being a membrane-filter, in the feeding direction; a phase separator unit for separation of oil from the first stream, where phase separator unit is situated after the separation unit, preferably being a membrane-filter, in the feeding direction; first stream re-circulating mechanism for re-circulating part of the first stream into the pre-treating unit of the conversion system; direct methanol fuel cell for generating electricity from the second stream; separation unit(s) comprising phase separators, centrifuges, membrane processes comprising ultra-filtration, nano-filtration, reverse osmosis, and/or pervaporation; a second separation unit, preferably being a second membrane-filter, for separating a purified methanol compound from the second stream; and purified methanol compound recirculating mechanism re-circulating the purified methanol compound from the second stream to the pre-treating unit of the conversion system. The plant further comprises supply mechanism for supplying residual product to the conversion apparatus and removal mechanism for removal of the products from the apparatus. It further comprises a refinery.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The separation process comprises separating out a first stream of oils and a second stream of water and water soluble organics, preferably water soluble salts are separated out to the first and/or the second stream. It comprises filtration. Conversion into energy includes a conversion into thermal energy such as heat. The method further comprises pre-treatment process(es) producing a mash from the organic material for the fermentation process. The pre-treatment process further comprises a liquefaction step, where enzymes are added to the pulp in the liquefaction process; and a saccharification step, where enzymes are added. greater than or equal to 50% of the energy required for pre-treatment process, fermentation process, and separation process is supplied by the energy distribution process. The fermentation process takes place in a fluid, preferably water. It comprises converting sugar(s) and/or addition of micro organism(s), such as yeast, and/or bacteria such as thermolabile bacteria directly and/or indirectly into the fermentation broth comprising hydrocarbon fuel(s). The fermentation process takes place at 24-36degrees C for 24-96 hours in an environment with a pH around 4-5. The separation process comprises distilling the fermentation broth where a part(s) of the hydrocarbon fuel is separated from the fermentation broth. All of the hydrocarbon fuel and residual products present in the fermentation broth is separated subsequent to the fermentation process, where all of the hydrocarbon fuel present in the fermentation broth is distilled off. The conversion step is a gasification and/or pyrolysis process. The conversion process involves a combustion process. It is conducted in a high pressure fluid such as in a fluid at greater than or equal to 50, preferably greater than or equal to 250 bars. The conversion process includes a hydrothermal and/or solvothermal conversion. It is supercritical water oxidation, wet gasification, and/or liquefaction processes. The conversion process comprises pressurizing the residual product in a fluid above 225 bars; heating the residual product in the fluid above 200degrees C in the presence of a homogeneous catalyst comprising a compound of group IA element(s); contacting the residual product in the fluid with a heterogeneous catalyst comprising a compound of group IVB element(s) and/or alpha -alumina; assuring that the fluid has initially a pH of above 7, preferably by adjusting the fluid to have a pH above 7; maintaining the pH of the fluid containing residual product at 7-14, preferably 8-10; pre-treating the residual product at 4-15 bars at 100-170degrees C for 0.5-2 hours; and separating the fluid into water and water soluble organics from oil and water soluble salts in a first separation unit. The water soluble organic comprising up-concentrated methanol is re-circulated to the pre-treating step. Contacting the residual product in the fluid with a heterogeneous catalyst is performed while the temperature is kept constant. The method comprises recirculating carbonates and/or hydrogen carbonates; recirculating alcohol(s); recirculating a fluid containing hydrogen; recirculating carboxylic acid(s); and recirculating aldehyde(s) and/or ketone(s). Preferred Component: The fluid is water and/or alcohol. Homogeneous and/or heterogeneous catalyst(s) is present in the high pressure fluid. They comprise compound(s) from group (I) element(s) and/or compound(s) from group IV element(s). Homogeneous and/or heterogeneous catalyst is contained in the ash fraction of the substances being fed to the conversion step. The heterogeneous catalyst is in the form of suspended particles, tablets, pellets, rings, cylinders, honey comb structure, and/or fibrous structure. The fluid comprises water. The residual product is sludge, such as sewage sludge, liquid manure, corn silage, clarifier sludge, black liquor, residues from fermentation, residues from juice production, residues from edible oil production, residues from fruit and vegetable processing, residues from food and drink production, leachate, and/or seepage water. Preferred Parameter: The temperature in the contacting step is 200-650, preferably 275-350degrees C. The pressure for conversion is 225-600, preferably 240-300 bars. Preferred Composition: The water has a concentration of greater than or equal to 5, preferably greater than or equal to 40 wt.% of the fluid. The residual product in the fluid is greater than or equal to 5, preferably greater than or equal to 50 wt.%.    TECHNOLOGY FOCUS - POLYMERS - Preferred Component: The residual product comprises lignocellulosic materials comprising biomass, straw, grasses, stems, wood, bagasse, wine trash, sawdust, wood chips, and/or energy crops. It comprises a waste, such as house hold waste, municipal solid waste, paper waste, auto shredder waste, plastics, polymers, rubbers, scrap tires, cable wastes, chromated copper arsenate treated wood, halogenated organic compounds, polychlorinated biphenyl bearing transformer oils, electrolytic capacitors, halones, medical waste, risk material from meat processing, meat and bone meal, and liquid streams, such as process or waste water streams containing dissolved and/or suspended residual product. EXAMPLE - Pretreated sewage sludge (140 g/hour) was pressurized to 250 bars and heated to 230degrees C in the pre-heating step. This stream was mixed with 414 g/hour of pressurized water heated to a temperature to obtain a constant temperature of 300plus minus 5degrees C after mixing. The mixed flow was subsequently contacted with the heterogeneous catalyst in the reactor. The feed to water ratio translated into a water to feed ratio of 3:1, and the total flow of 545 g/hour translated into a contact time of 3.3 minutes. After the contact with heterogeneous catalyst, the fluid containing the converted organic material was cooled to ambient temperature, filtered through a particle filter for collection of suspended particles, and expanded to ambient pressure. The liquid fraction on the stream was collected in a liquid trap, and the gas was vented off. No carbon was detected in the solid product after extraction of adsorbed oil, indicating 100% conversion of the organic material in the feed.