# US 11,110,421 B2 · Processing quarantined materials > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 11,110,421 B2 - Document ID: US11110421B2 - Status: Granted - Kind: B2 - Application number: 16/329,798 - Filed: 2017-09-01 - Published: 2019-08-08 - Granted: 2021-09-07 - Earliest claimed: 2016-09-01 - Assignees: The Crucible Group IP Pty Ltd - Applicants: The Crucible Group IP Pty Ltd - Inventors: Joseph George Herbertson; Lazar Strezov; Kannappar Mukunthan - Web page: https://patentgrep.com/patent/US11110421B2 ## CPC - B01J 6/008: {Pyrolysis reactions (of hydrocarbons C10G9/00)} - B01J 4/008: {Feed or outlet control devices} - B01J 6/004: {using hot gas streams in which the material is moved} - C10B 7/10: with conveyor-screws - C10B 49/04: while moving the solid material to be treated - C10B 53/02: of cellulose-containing material (production of pyroligneous acid C10C5/00) - C10B 57/10: Drying - C10C 5/00: Production of pyroligneous acid {distillation of wood, dry distillation of organic waste}(carbonisation of wood C10B) - B01J 2208/00769: Details of feeding or discharging - Y02E 50/10: Biofuels, e.g. bio-diesel - Y02P 20/145: the feedstock being materials of biological origin - B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS - C10B: DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS (cracking oils C10G; underground gasification of minerals E21B43/295) - C10C: WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID (compositions of bituminous materials C08L95/00; carbon filaments by decomposition of organic filaments D01F9/14) - Y02E: REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION - Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS ## Abstract A method and an apparatus for destroying biosecurity hazards in quarantined feed materials and producing valuable products that are safe and have economic value is disclosed. The apparatus includes a continuous converter (3) that has a reaction chamber (5) for producing a solid carbon-containing product, a gas product, and optionally an oil product and a separate water-based condensate product in the chamber, via pyrolysis or other reaction mechanisms. ## Claims ### Claim 1 A method for converting a feed material to a plurality of products in a continuous converter including a reaction chamber, an inlet for supplying the feed material to an upstream end of the reaction chamber, an assembly for moving the feed material through the reaction chamber from the upstream end towards a downstream end of the reaction chamber, and a plurality of outlets for discharging the products from the reaction chamber, the method including the steps of: (a) supplying the feed material to the upstream end of the reaction chamber via the inlet, the feed material comprising quarantined materials and biomass, the quarantined materials comprising between 25 wt % and 50 wt % of the total mass of the quarantined materials and the biomass; (b) moving the feed material through the reaction chamber from the upstream end to the downstream end and exposing the feed material within the reaction chamber to a time-temperature profile such that the feed material is heated from 200° C. to 600° C. over a period of 5-20 minutes which destroys biosecurity hazards in the feed material and dries and pyrolyses organic material in the feed material and releases water vapour and a volatile products gas phase from the feed material as the feed material moves through the reaction chamber; (c) moving the water vapour and the volatile products gas phase produced in step (b) through the reaction chamber in a direction counter to that of the feed material so that at least a part of the water vapour and condensable components of the volatile products gas phase condense in cooler upstream sections of the reaction chamber and form liquid water and liquid oil, at least the liquid oil being carried forward in the reaction chamber by the feed material to higher temperature regions of the reaction chamber and being progressively volatilised and cracked to a non-condensable gas; (d) discharging from the reaction chamber (i) a gas product via a gas product outlet and (ii) a dried and pyrolysed solid carbon-containing product from a solid product outlet; and (e) condensing water vapour from the gas product outside the chamber and forming a liquid water product. ### Claim 2 (depends on 1) The method defined in claim 1 wherein the feed material is less than 25 mm in size. ### Claim 3 (depends on 1) The method defined in claim 1 wherein less than 15 wt. % of the total mass of the feed material has a particle size of less than 1 mm. ### Claim 4 (depends on 1) The method defined in claim 1 wherein the amount of moisture in the feed material is less than 20 wt. % of the total mass of the feed material. ### Claim 5 (depends on 1) The method defined in claim 1 further comprising controlling the gas product composition by controlling the temperature profile in the reactor and therefore the residence time within a required temperature range. ### Claim 6 (depends on 1) The method defined in claim 1 further comprising maintaining a required temperature profile in the reaction chamber by supplying an oxygen-containing gas to the reaction chamber and at least partially combusting combustible gases in the reaction chamber. ### Claim 7 (depends on 1) The method defined in claim 1 further comprising establishing a temperature profile in the reaction chamber that includes the following zones extending successively along the length of the reaction chamber from the upstream end to the downstream end of the reaction chamber: (a) a drying zone for drying the feed material to form a dried feed material, (b) a pre-heating zone for heating the dried feed material to form a dried and heated feed material, and (c) a thermo-chemical reaction zone for thermally decomposing the dried and heated feed material and producing the solid carbon-containing product and gas. ### Claim 8 (depends on 1) The method defined in claim 1 further comprising supplying an oxygen-containing gas to the reaction chamber. ### Claim 9 (depends on 2) The method defined in claim 2, wherein the feed material is less than 20 mm in size. ### Claim 10 (depends on 3) The method defined in claim 3, wherein less than 10 wt. % of the total mass of the feed material has a particle size of less than 1 mm. ### Claim 11 (depends on 4) The method defined in claim 4 wherein the amount of moisture in the feed material is less than 15 wt. % of the total mass of the feed material. ### Claim 12 (depends on 6) The method defined in claim 6, wherein the oxygen-containing gas is air. ### Claim 13 (depends on 7) The method defined in claim 7, wherein the drying zone includes an end proximate the inlet having a temperature between 60-80° C. and wherein the upper temperature limit within the drying zone is between 100-150° C. ### Claim 14 (depends on 7) The method defined in claim 7, wherein the upper temperature limit of the drying zone is between 100-150° C. ### Claim 15 (depends on 1) The method defined in claim 1, wherein the solid-containing product comprises char. ### Claim 16 (depends on 8) The method defined in claim 8, wherein the oxygen-containing gas is air.