A plant for the disposal of wastes includes a supercritical water oxidation reactor, a supercritical water gasification reactor, and a feeding system configured for feeding at least two organic currents of wastes to the supercritical water oxidation reactor and supercritical water gasification reactor and configured for feeding at least one aqueous flow within said plant. The feeding system is configured for feeding the at least one aqueous current with a series flow through the supercritical water oxidation reactor and supercritical water gasification reactor. The feeding system is configured for feeding the at least two organic currents of wastes with a parallel flow through the supercritical water oxidation reactor and supercritical water gasification reactor and so as to selectively feed each of the organic currents of wastes to the supercritical water oxidation reactor or to the supercritical water gasification reactor.

A system for pyrolysis or gasification having a first pyrolysis or gasification unit 50 connected to a second pyrolysis or gasification unit 53 by a hermetically sealed gas path. Pyrolysis is used to destroy calorific waste and/or to produce gas therefrom.

Systems and methods for reducing or eliminating corrosion of components of a reactor system, including a supercritical water gasification system, are described. The reactor system may include a reactor vessel configured to receive a reactor fluid through a reactor fluid inlet and a product source fluid corrosive to portions of the reactor system through a product source fluid inlet. The product source fluid may react with the reactor fluid to produce one or more reaction products, such as a fuel gas. The product source fluid inlet may be arranged within the reactor fluid inlet such that the product source fluid entering the reactor vessel is encased by a fluid conduit formed by the flow of reactor fluid entering the reactor vessel. The layer may operate to reduce corrosion by forming a barrier between the product source fluid and the surface of the reactor fluid inlet and/or the reactor vessel.

Provided herein are corrosion-resistant reactors that can be used for gasification, and methods of making and using the same. Some embodiments include a corrosion-resistant ceramic layer. According to some embodiments, the corrosion-resistant ceramic layer has a negative charge. At temperature above water's critical point (for example, 374 CC and at 22.1 MPa I 218 atm), water can behave as an adjustable solvent and can have tunable properties depending on temperature and pressure.

A process for the gasification of wet biomass. The process comprises heating wet biomass at a pressure in the range of from 22.1 MPa to 35 MPa. The wet biomass is heated from a temperature of at most T.sub.1 to a temperature of at least T.sub.2 by heat exchange with a first heating fluid. The gasification product is further heated. The further heated gasification product is used as the first heating fluid, upon which the further heated gasification product is cooled down from a temperature of at least T.sub.3 to a temperature of at most T.sub.4. The temperatures T.sub.1, T.sub.2, T.sub.3 and T.sub.4 can be calculated by using certain mathematical formulae. Also claimed: a reaction apparatus for the gasification of wet biomass.

A process for the gasification of wet biomass. The process comprises heating wet biomass at a pressure in the range of from 22.1 MPa to 35 MPa. The wet biomass is heated from a temperature of at most T.sub.1 to a temperature of at least T.sub.2 by heat exchange with a first heating fluid. The gasification product is further heated. The further heated gasification product is used as the first heating fluid, upon which the further heated gasification product is cooled down from a temperature of at least T.sub.3 to a temperature of at most T.sub.4. The temperatures T.sub.1, T.sub.2, T.sub.3 and T.sub.4 can be calculated by using certain mathematical formulae. Also claimed: a reaction apparatus for the gasification of wet biomass.

A gasification system includes a countercurrent type heat exchanger that includes a low-temperature side flow channel through which a gasification feedstock flows, and a high-temperature side flow channel to which treated water in a supercritical state is introduced. The treated water raises a temperature of the gasification feedstock by exchanging heat with the gasification feedstock. The system further includes a reactor that gasifies the gasification feedstock, whose temperature has been raised by the countercurrent type heat exchanger, by heating and pressurizing the gasification feedstock to be in a supercritical state. The reactor discharges the gasification feedstock as treated water in the supercritical state. The system further includes a treated water flow channel that introduces, to the countercurrent type heat exchanger, the treated water that has been discharged from the reactor, and a feedstock introduction port that introduces the feedstock to the low-temperature side flow channel.

The present disclosure provides a supercritical fluid gasification system. In some embodiments, the system includes a reactor having a reactor shell including sidewalls that extend between a top reactor cover and a bottom reactor cover, where the sidewalls, the top cover, and the bottom cover enclosing a reactor shell channel. In some embodiments, the reactor includes a thermal shield positioned within the reactor shell channel, the thermal shield having sidewalls that extend between a top thermal shield cover and a bottom thermal shield cover, where the sidewalls, the top thermal shield cover, and the bottom thermal shield cover enclosing a thermal shield channel. In some embodiments, the reactor includes a fluid feed supply conduit in fluid communication with the thermal shield channel, a supercritical fluid conduit in fluid communication with the thermal shield channel, and a product conduit in fluid communication with the thermal shield channel.

The process described herein converts biomass directly into a combination of hydrogen, methane and carbon dioxide. A portion of the gases are collected at pressures above the thermodynamic critical pressure for water, which is 3200 psi (pounds per square inch). Typical operating pressure at the point where the first portion of gas collected can range from 3200 psi to 6000 psi. Upon cooling, most of the CO.sub.2 condenses to a liquid. At this density and pressure, the CO.sub.2 can be injected into a deep well aquifer to sequester the carbon dioxide. The overall process is superior to carbon neutral processes, can be carbon negative, and possesses the potential to reverse atmospheric CO.sub.2 trends if implemented on a global scale.

Combining multiple subsystems involving biomass processing, biomass gasification of the processed biomass where a synthesis gas is produced then converted to hydrogen fuels or other transportation fuels for use in coupled transportation systems sized to consume all the transportation fuel produced. Carbon in the biomass is converted to CO.sub.2 in the conversion process and a portion of that CO.sub.2 is captured and sequestrated for long term storage.