A system and method to prevent the oxidizer overheating using cold side bypass during high input for a VOCs treatment system with series rotor are described, which may be used in an organic waste air treatment system. The system is equipped with a Thermal Oxidizer (TO), a First Heat Exchanger, a Second Heat Exchanger, a third heat exchanger, a Fourth Heat Exchanger, a First Cold-Side Transporting Pipeline, a Fourth Cold-Side Transporting Pipeline, a First Adsorption Rotor, a Second Adsorption Rotor, and a Chimney. There is a Cold-Side Proportional Damper installed between the First Desorption-Treated Air Pipeline and the First Cold-Side Transporting Pipeline, the First Desorption-Treated Air Pipeline and the Fourth Cold-Side Transporting Pipeline or between the First Cold-Side Transporting Pipeline and the Fourth Cold-Side Transporting Pipeline, or the damper is installed on the First Desorption-Treated Air Pipeline.

A bale boiler incinerates bales of material, and particularly bales made from waste, garbage and other refuse, in order to provide heat for a steam turbine generator, and includes a conveyor for transporting bales of waste material through a three-stage boiler. The boiler is preferably divided into three stages: 1) the warming stage, 2) the main incineration stage, and 3) the supplemental incineration stage. In the warming stage, the bale is warmed and dried. In the main incineration stage, the bale is burned to create heat that is then used to power a steam turbine electrical generator or the like. In the third, supplemental incineration stage, the remnants of the bale burn down to ash, and the remaining ash and non-combustible waste are then transported out of the boiler by the conveyor and dumped into a receptacle or container for transport and disposal.

Systems and processes provide for a thermal process to transform sludge (and a variety of other natural waste materials) into electricity. Dewatered sludge and other materials containing a high amount of latent energy are dried into a powdered biofuel using a drying gas produced in the system. The drying gas is recirculated and is heated by the biofuel produced in the system, waste heat (from turbines or internal combustion engines), gas (including natural gas or digester gas) and/or oil. The biofuel is combusted in a boiler system that utilizes a burner operable to burn biofuel and produce heat utilized in a series of heat exchangers that heat the recirculating drying air and steam that powers the turbines for electricity production.

In order to provide a method for the purification of a raw gas stream containing water vapour that is simple and cost-efficient to perform, it is proposed that the method should comprise the following: feeding the raw gas stream to a reforming region in which contaminants in the raw gas stream react chemically with the water vapour in the raw gas stream, as a result of which a reformed raw gas stream is obtained; feeding the reformed raw gas stream and an oxidising agent stream to an oxidation region in which constituent parts of the reformed raw gas stream react chemically with oxidising agent of the oxidising agent stream, as a result of which a clean gas stream is obtained. Moreover, optionally a closed-loop control of the oxygen content is provided. Further, it is optionally provided for the clean gas stream to be fed to a condenser, as a result of which the volumetric flow of the clean gas stream is reduced and/or as a result of which energy can be recovered and used for pre-heating the oxidising agent and for other production processes.

The continuous process of the present invention is intended to obtain dry biomass from two treatment steps by drying organic waste. The waste previously sieved and crushed waste are dumped into a first dryer, inside of which temperatures are between 280° C. and 300° C. at the inlet thereof and between 90° C. and 100° C. at the outlet, then passing to a conveyor belt where at room temperature a partial cool-down occurs and the waste is dumped into a second dryer inside of which the temperatures are between 180° C. and 200° C. at the inlet and between 75° C. and 85° C. at the exit, completing the process, during which the interior of the dryers is maintained in negative pressure through exhaust flow and the oxygen content is kept between 5 and 7%.

A waste thermolysis installation includes a first, drying, enclosure able to vacuum dry the incoming waste and a second, calcining, enclosure, able to perform a vacuum calcination treatment on the dried waste coming from the first enclosure, each enclosure including an external-heating system including a combustion chamber and a vacuum pump which makes it possible to maintain the vacuum in the enclosure and is connected to the enclosure by an extraction pipe, the installation being characterized in that it includes a pipe circulating gas coming from the second enclosure to the second enclosure through the system for the external heating of the second enclosure. Thermolysis method implementing the installation.

A fuel material processing system includes a hopper assembly configured to receive a fuel material. A drying system is configured to remove moisture from the fuel material to generate a dried fuel material. A material delivery system is configured to provide the dried fuel material to a combustion system.

In a system and process, organic waste is treated in a reactor to volatilize contaminants such as Perfluoroalkyl substances (PFAS) compounds and/or Contaminants of Emerging Concern (CECs) from the organic waste. Biochar may have reduced or undetectable PFAS compounds or CECs. Most or all of the gas may be thermally oxidized to convert PFAS compounds and/or CECs into less harmful and/or less toxic products or elemental compounds, which may be further removed. Energy may be recovered from one or more parts of the herein described system and process.

In a method for physical and thermochemical treatment of biomass, the biomass moisture content is reduced in a dryer and ammonia (NH.sub.3) is also released from the biomass during drying. The dried biomass is then either pyrolyzed in a pyrolysis reactor and the pyrolysis gas is forwarded to and combusted in a combustion device to form flue gas, or is combusted in a combustion facility unit to form flue gas. In either case the flue gas is fed to a mixer. Oxygen (O.sub.2) is metered to the flue gas in the mixer and is fed directly to the dryer as drying gas. As the drying gas passes through the dryer, the sulfur dioxide (SO.sub.2) contained in the drying gas and/or the sulfur trioxide (SO.sub.3) chemically reacts with the ammonia (NH.sub.3) to form ammonium sulfite ((NH.sub.4).sub.2SO.sub.3) and/or ammonium sulfate ((NH.sub.4).sub.2SO.sub.4). Also a treatment facility physically and thermochemically treats the biomass.

A regenerative thermal oxidizer assembly includes a first housing member and a second housing member. The first housing member defines a regenerative portion and a combustion chamber. The second housing member defines an inlet chamber and an outlet chamber. A regenerator is disposed within the regenerative portion of the first housing member and defines a central axial opening extending to the combustion chamber. A thermal element extends through the axial opening to the combustion chamber for providing heat to the combustion chamber for initiating combustion inside the combustion chamber. The first housing member is rotatable around an axis defined by the axial opening relative to the second housing member for rotating the regenerator relative to the inlet chamber and the outlet chamber.