Abstract: A method is provided to transform biomass. Non-food biomass is preprocessed. Then, fermentation is processed to generate ethanol. Ethanol is dehydrated through a catalyst to generate ethylene. After the dehydration, oligomerization is processed with a catalyst to transform ethylene into olefins having 6˜20 carbon atoms (C6˜C20). The olefins are hydrotreated into alkanes. Thus, C6˜C20 hydrocarbons having long carbon chains are formed. The hydrocarbons having 6˜10 carbon atoms can be used as gasoline; those having 8˜16 carbon atoms, jet fuel; and those having 16˜20 carbon atoms, diesel. On generating ethanol, byproducts of lignin may be generated. The byproducts can be processed through depolymerization/deoxygenation to generate aromatic hydrocarbons or can be gasified to generate methanol or dimethyl ether. By further processing dehydration, aromatic hydrocarbons are generated to be mixed into gasoline, jet fuel or diesel. Or, the lignin byproducts are gasified to generate syngas.

Abstract: A method is provided to transform biomass. Non-food biomass is preprocessed. Then, fermentation is processed to generate ethanol. Ethanol is dehydrated through a catalyst to generate ethylene. After the dehydration, oligomerization is processed with a catalyst to transform ethylene into olefins having 6˜20 carbon atoms (C6˜C20). The olefins are hydrotreated into alkanes. Thus, C6˜C20 hydrocarbons having long carbon chains are formed. The hydrocarbons having 6˜10 carbon atoms can be used as gasoline; those having 8˜16 carbon atoms, jet fuel; and those having 16˜20 carbon atoms, diesel. On generating ethanol, byproducts of lignin may be generated. The byproducts can be processed through depolymerization/deoxygenation to generate aromatic hydrocarbons or can be gasified to generate methanol or dimethyl ether. By further processing dehydration, aromatic hydrocarbons are generated to be mixed into gasoline, jet fuel or diesel. Or, the lignin byproducts are gasified to generate syngas.

Abstract: An oil product of gasoline is fabricated. The product contains hydrocarbon compound ranged as a gasoline composition. The purification process of dimethyl ether (DME) used in the present invention greatly reduces the feed rate for obtaining a smaller reactor with cost down. Carbon dioxide (CO2) is separated to be recycled back to the gasifier to be reused, archived or used otherwise for improves global environment. At the same time, CO2 is reacted with hydrocarbons, water vapor, etc. through a novel high-temperature plasma torch to generate a synthesis gas (syngas) of carbon monoxide (CO) and hydrogen (H2) for regulating a hydrogen/carbon ratio of a biomass- or hydrocarbon-synthesized compound and helping subsequent chemical synthesis reactions. In the end, the final gasoline production has a high yield, a high octane rate, low nitrogen and sulfur pollution and a highly ‘green’ quality.

Abstract: Disclosed is a method for making dimethyl ether by reactive distillation. The method provides a reactive distillation tower with a top, a bottom, and rectification, reaction and stripping zones defined therein. The top of the reactive distillation tower is retained at 25° C. to 40° C. while the bottom of the reactive distillation tower is retained at 84.6° C. to 170° C. Each of the rectification, reaction and stripping zones includes several sieving trays. The reaction zone of the reactive distillation tower is filled with catalyst. The pressure in the reactive distillation tower is lower than 8.0 bars. Methanol is introduced into the reactive distillation tower so that the methanol travels from the reaction zone toward the bottom for contact with the catalyst to provide a top stream and a bottom stream. The top stream includes dimethyl ether. The bottom stream includes water and a remaining portion of the methanol. Finally, the dimethyl ether is collected in the top of the reactive distillation tower.

Abstract: The present invention provides a plasma torch device. The device comprises a front electrode, a back electrode and a vortex flow generator. The torch roots of the back electrode are moved by fixed magnets. By controlling the magnets coordinated with vortex air flow, the torch roots are moved back and forth periodically on inner surface of the back electrode. The torch roots do not stay at the same place for long for preventing increasing local heat burden of the electrode. Thus, life time and maintenance cycle of the electrode is prolonged with reduced operational cost of plasma torch and enhanced reliability of the device.

Abstract: Disclosed is a method for increasing the yield of a slurry bed reactor. The method provides a slurry bed reactor with a recycling unit or a replacing unit. An absorbing agent is fed into the slurry bed reactor. The absorbing agent is a substance that can react with at least one product of a primary reaction or at least one reactant of a side reaction. Then, the absorbing agent is transmitted into the recycling unit or the replacing unit. The recycling unit renews the absorbing agent and sends the renewed absorbing agent back into the slurry bed reactor for reuse. The replacing unit replaces the absorbing agent with new absorbing agent and sends the new absorbing agent into the slurry bed reactor for use.

Abstract: Disclosed is a method for increasing the yield of a slurry bed reactor. The method provides a slurry bed reactor with a recycling unit or a replacing unit. An absorbing agent is fed into the slurry bed reactor. The absorbing agent is a substance that can react with at least one product of a primary reaction or at least one reactant of a side reaction. Then, the absorbing agent is transmitted into the recycling unit or the replacing unit. The recycling unit renews the absorbing agent and sends the renewed absorbing agent back into the slurry bed reactor for reuse. The replacing unit replaces the absorbing agent with new absorbing agent and sends the new absorbing agent into the slurry bed reactor for use.

Abstract: Disclosed is a method for making dimethyl ether by reactive distillation. The method provides a reactive distillation tower with a top, a bottom, and rectification, reaction and stripping zones defined therein. The top of the reactive distillation tower is retained at 25° C. to 40° C. while the bottom of the reactive distillation tower is retained at 84.6° C. to 170° C. Each of the rectification, reaction and stripping zones includes several sieving trays. The reaction zone of the reactive distillation tower is filled with catalyst. The pressure in the reactive distillation tower is lower than 8.0 bars. Methanol is introduced into the reactive distillation tower so that the methanol travels from the reaction zone toward the bottom for contact with the catalyst to provide a top stream and a bottom stream. The top stream includes dimethyl ether. The bottom stream includes water and a remaining portion of the methanol. Finally, the dimethyl ether is collected in the top of the reactive distillation tower.