The present invention relates to a device and a method for low-temperature pyrolysis, wherein: waste tire chips are continuously supplied; since a pneumatic method of an intake method and a blowing method is adopted, the waste tire chips may be quickly fed (supplied) by a simple method, and only the waste tire chips may be supplied into a pyrolysis reactor but the inflow of air thereinto may be fundamentally blocked, thereby increasing the pyrolysis efficiency of the pyrolysis reactor and preventing the explosion reaction thereof; and unlike the prior art, a mechanical conveyor supply method is not used, and thus waste tire chip supply equipment can be miniaturized and modularized, thereby enabling the compact design of the pyrolysis equipment, facilitating a pyrolysis operation, facilitating maintenance, and significantly reducing the site area of the pyrolysis equipment or the cost of manpower input for supplying waste tire chips.

A methodology for the removal of the harmful components of the ash of biomass of agro/forest/urban origin and of low-quality coal fuels, as peat, lignite, sub-bituminous and bituminous coals, is invented. The harmful components are alkaline metals, chlorine and sulphur. They are removed before the thermochemical conversion in order to prevent or minimise the corrosion, scaling/deposition, ash agglomeration problems, as well as the alkaline metal, chlorine, sulphur emissions. Furthermore, it aims in the production of materials of low moisture content, low hygroscopicity, which can be easily ground, and mixed with various other materials, easily fed to commercial boilers for energy production, which can be easily pelletised with or without other materials at various proportions and with very low energy requirements. The removal is achieved with pre-pyrolysis/pre-gasification at 250-320 C. for 5 min to 2 h of biomass of agro/forest/urban origin, as well as, of low-quality coal fuels, as peat, lignite, sub-bituminous and bituminous coals. Then the pre-pyrolysed/pre-gasified sample is washed with a 0.5%-20% weight basis aqueous calcium acetate and/or magnesium acetate and/or aluminum acetate and/or ammonium acetate solution. These acetate salts can be mixed in a proportion of 0% to 100% to form an active salt which is used for the preparation of the aqueous solution. Any kind tap water from a public water supply system, spring, etc. can be used for the preparation of aqueous solution. The solid-to-liquid ratio is 33 g/L to 600 g/L, the temperature varies from 13 C. to 95 C., and the treatment duration between 5 min to 24 h.

A methodology for the removal of the harmful components of the ash of biomass of agro/forest/urban origin and of low-quality coal fuels, as peat, lignite, sub-bituminous and bituminous coals, is invented. The harmful components are alkaline metals, chlorine and sulphur. They are removed before the thermochemical conversion in order to prevent or minimise the corrosion, scaling/deposition, ash agglomeration problems, as well as the alkaline metal, chlorine, sulphur emissions. Furthermore, it aims in the production of materials of low moisture content, low hygroscopicity, which can be easily ground, and mixed with various other materials, easily fed to commercial boilers for energy production, which can be easily pelletised with or without other materials at various proportions and with very low energy requirements. The removal is achieved with pre-pyrolysis/pre-gasification at 250-320 C. for 5 min to 2 h of biomass of agro/forest/urban origin, as well as, of low-quality coal fuels, as peat, lignite, sub-bituminous and bituminous coals. Then the pre-pyrolysed/pre-gasified sample is washed with a 0.5%-20% weight basis aqueous calcium acetate and/or magnesium acetate and/or aluminum acetate and/or ammonium acetate solution. These acetate salts can be mixed in a proportion of 0% to 100% to form an active salt which is used for the preparation of the aqueous solution. Any kind tap water from a public water supply system, spring, etc. can be used for the preparation of aqueous solution. The solid-to-liquid ratio is 33 g/L to 600 g/L, the temperature varies from 13 C. to 95 C., and the treatment duration between 5 min to 24 h.

Processes and facilities for providing recycled content hydrocarbon products (r-products) from the pyrolysis of waste plastic are provided. Processing schemes are described herein that increase energy efficiency and help reduce overall environmental impact while producing valuable final products from chemically recycled waste plastic.

Processes and facilities for providing recycled content hydrocarbon products (r-products) from the pyrolysis of waste plastic are provided. Processing schemes are described herein that increase energy efficiency and help reduce overall environmental impact while producing valuable final products from chemically recycled waste plastic.

A process and apparatus are provided in the present invention for treatment of particulate biomass. The present process comprises a densification stage, a first treatment stage, a second treatment stage, a cooling stage; the present apparatus comprises a thermo-chemical treatment chamber which is a two-stage compact moving bed type including two compartments for pre-torrefaction and torrefaction and having a star or spider or ring formic hot gas distribution system equipped with at least one hot gas input and at least one hot gas output for each compartment, and at least one particulate biomass inlet and at least one particulate biomass outlet.

A process and apparatus are provided in the present invention for treatment of particulate biomass. The present process comprises a densification stage, a first treatment stage, a second treatment stage, a cooling stage; the present apparatus comprises a thermo-chemical treatment chamber which is a two-stage compact moving bed type including two compartments for pre-torrefaction and torrefaction and having a star or spider or ring formic hot gas distribution system equipped with at least one hot gas input and at least one hot gas output for each compartment, and at least one particulate biomass inlet and at least one particulate biomass outlet.

The torrefaction unit 1 comprises at least one multiple hearth furnace 2 which is heated by a heat transfer fluid 16 comprising hot water taken form a water space 21 of a steam drum 11. The heat transfer fluid 16 is guided through a water circuit 20 to a heating system 19 of the at least one multiple hearth furnace 2. This means the multiple hearth furnace 2 is heated to a torrefaction temperature indirectly by the use of hot water as heat transfer fluid 16. This is environmentally advantageous. The torrefaction gas 3 created by the torrefaction of material comprising biomass such as municipal solid waste is preferably partially oxidized in a partial oxidation reactor 23 for creating syngas. Preferably, a part of the thermal energy of the syngas is used in an evaporator 9 and/or a superheater 13 to heat water and/or steam and/or to evaporate water. The evaporated water is preferably guided to a steam space 22 of the steam drum 11 and can, thus, be used to heat the heat transfer fluid 16. The partial oxidation reactor 23 and the temperature of the heat transfer fluid 16 can be controlled independently allowing to one single partial oxidation reactor 23 for at least two multiple hearth furnaces 2.

The torrefaction unit 1 comprises at least one multiple hearth furnace 2 which is heated by a heat transfer fluid 16 comprising hot water taken form a water space 21 of a steam drum 11. The heat transfer fluid 16 is guided through a water circuit 20 to a heating system 19 of the at least one multiple hearth furnace 2. This means the multiple hearth furnace 2 is heated to a torrefaction temperature indirectly by the use of hot water as heat transfer fluid 16. This is environmentally advantageous. The torrefaction gas 3 created by the torrefaction of material comprising biomass such as municipal solid waste is preferably partially oxidized in a partial oxidation reactor 23 for creating syngas. Preferably, a part of the thermal energy of the syngas is used in an evaporator 9 and/or a superheater 13 to heat water and/or steam and/or to evaporate water. The evaporated water is preferably guided to a steam space 22 of the steam drum 11 and can, thus, be used to heat the heat transfer fluid 16. The partial oxidation reactor 23 and the temperature of the heat transfer fluid 16 can be controlled independently allowing to one single partial oxidation reactor 23 for at least two multiple hearth furnaces 2.

A method for pyrolysis of polycarbonate-containing material in order to recover raw materials is provided. The method comprises at least the following steps: (a) introducing material intended for the pyrolysis, at least comprising material that contains a mixture of a polycarbonate-containing compound and a polystyrene-containing compound, into a reactor; (b) decomposing, at a temperature of 300 C. to 700 C., at least the material intended for pyrolysis introduced into the reactor in step (a) and obtaining a product that is present in the gaseous phase as the pyrolysate and of pyrolysis residues that are present in a non-gaseous phase; and (c) cooling the removed pyrolysate to a temperature of less than 300 C. while obtaining a pyrolysis product, selected from pyrolysis condensate, pyrolysis sublimate or a mixture thereof.