WO2013183037A2 - Système de gazéification en traitement des déchets - Google Patents

Système de gazéification en traitement des déchets Download PDF

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Publication number
WO2013183037A2
WO2013183037A2 PCT/IB2013/054736 IB2013054736W WO2013183037A2 WO 2013183037 A2 WO2013183037 A2 WO 2013183037A2 IB 2013054736 W IB2013054736 W IB 2013054736W WO 2013183037 A2 WO2013183037 A2 WO 2013183037A2
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WO
WIPO (PCT)
Prior art keywords
molten metal
vessel
molten
air
feed
Prior art date
Application number
PCT/IB2013/054736
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English (en)
Other versions
WO2013183037A3 (fr
Inventor
Ivan TAN THIAM LYE
Furuta KOHJI
Xin Yi ONG
Ruyi JAN LEONG
Edwin WONG PENG SOON
Kil KYEONG HWAN
Original Assignee
Strategic Petroleum Co Pte Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Strategic Petroleum Co Pte Ltd filed Critical Strategic Petroleum Co Pte Ltd
Priority to US14/406,253 priority Critical patent/US20150184090A1/en
Publication of WO2013183037A2 publication Critical patent/WO2013183037A2/fr
Publication of WO2013183037A3 publication Critical patent/WO2013183037A3/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/57—Gasification using molten salts or metals
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/348—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents by direct contact with heat accumulating liquids, e.g. molten metals, molten salts
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1665—Conversion of synthesis gas to chemicals to alcohols, e.g. methanol or ethanol
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1668—Conversion of synthesis gas to chemicals to urea; to ammonia
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/301—Treating pyrogases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present specification relates to a hazardous, garbage, industrial waste treatment system and a novel method of gasification, treatment and or treating hazardous, medical waste.
  • wastes include organic materials, such as pesticides, polychlorinated biphenyls (PCBs), and organic materials.
  • PCBs polychlorinated biphenyls
  • PBBs polybrominated biphenyls
  • other wastes include inorganic material, such as the oxides of iron, zinc, aluminum, copper and magnesium and the salts of ferric chloride, ferrous chloride, aluminum chloride, etc.
  • Medical and biohazardous waste is often a special problem since it is usually non- homogeneous waste; i.e. it may include liquids and/or solids such as paper, plastic, fabric, biological tissues, metal, glass, and the like. Many incinerators do not fully burn such mixed composition waste.
  • Solid waste treatment is also shown in a fiuidized bed environment in U.S. Pat. No. 3,776, 150 issued Dec. 4, 1973.
  • the latter device conveys solid waste through an auger system into a pair of separate fiuidized beds.
  • Baston patent No. 4,359,005, issued Nov. 16, 1982 also discloses a fiuidized bed incineration of waste products, wherein a limestone bed is used to prevent phosphorus contamination.
  • Koyanagi patent No. 3.861 ,336 depicts an incinerator of the rotary kiln type. Refuse separation and sorting is seen in U.S. Pat. No. 3,650,396. Solid waste is transferred through a plurality of individual processing stages, including pulverization, fluidized bed reaction, and magnetic separation. Certain constituent byproducts are recovered.
  • U.S. Pat. No. 682,313 patented Sept. 10, 1901 by B. Zwillinger, provided an apparatus for carbonizing material.
  • the apparatus included hollow internal walls, a chimney leading from one end of the flue, and a superheating-furnace discharging its waste gases into the opposite end of the flue, and means for passing gas through such superheating-furnace and into the carbonizing-chamber.
  • U.S. Pat. No. 1 ,747,816 patented Feb. 18, 1930 by W. H. Carrington provided a garbage furnace comprising a fuel chamber and a combustion chamber for the garbage separated by a partition wail, a fuel grate in the fuel chamber, and a garbage grate at a higher level in the combustion chamber.
  • the partition wall was provided with a port above the grates.
  • a secondary grate was provided in such combustion chamber for guarding such port against obstruction.
  • U.S. Pat. No. 1 ,906,023 patented Apr. 25, 1933 by K. J. Tobin provided an incinerator appliance including a combustion chamber provided with a heat emitting source. A substantially-closed receptacle was mounted in the chamber above such heat source. The receptacle and the heat emitting source constituted the incinerator.
  • the apparatus included an outer insulated wall section, and an inner casing mounted on the base adjacent to the inner edge of the annular passageway and in spaced relation with the outer wail section.
  • a retort was disposed within the inner casing and was spaced from the inner surface thereof, A pipe carried off liquid from the retort, Means were provided for condensing vapours rising from the retort.
  • U.S. Pat. No. 2,812,291 patented Nov. 5, 1957 by C. H. Hughes provided a broad oven including an elongated rectangular coking oven having a flat floor and capable of being sealed against air, and a heating flue system associated with such oven to supply heat.
  • the heating system included a plurality of heating flues located directly under the floor of the oven, and side heating flues located in each side wall of the oven.
  • a heat exchanger unit was associated with such heating flues to transfer heat from outgoing hot burnt products of combustion to incoming air.
  • a vaulted arch was disposed over the entire upper part of the oven, and a vaulted roof was located directly over such arch and spaced therefrom to provide a fume chamber.
  • a plurality of ports was provided in such arch directly to connect the oven to the fume chamber. At least one burner and associated air port communicated with the fume chamber to produce burnt products of combustion. An outlet port was associated with such fume chamber for the withdrawal of gases and vapours and burnt products of combustion.
  • U.S. Pat. No. 580,594 patented Aug. 4, 1959 by M. A. Naulin, provided an incinerator wall construction. That wall construction included a substantiaily-channei- shaped metal outer wall member and a cementitious refractory liner. Such liner was formed by interlocking sections.
  • U.S. Pat. No. 2,959, 140 patented Nov. 8, 1960 by H. Friedberg provided a smokeless and odourless incinerator having walls forming a furnace chamber, and a casing surrounding such chamber on all sides and spaced outwardly therefrom. An opening was provided in the upper end of the casing for the introduction of the charge to be consumed,
  • a hollow combined burner shield and duct was disposed in the furnace chamber.
  • An ash trap was also provided in the furnace chamber.
  • Baffle means supported in the trap permitted only non-linear gaseous to flow through such baffle means.
  • a secondary combustion device was positioned at the flue connection near the top of the upwardly-extending burner shield and duct, A maze of ceramic material was provided through which products of combustion had to pass from the furnace chamber to the flue connection, A small opening was provided for supplying combustion air to the secondary combustion device.
  • U.S. Pat. No. 3,098,458 patented July 23, 1983 by D. C. Lanty, Jr. provided a rotary refuse converter including the combination of a housing, a rotary converter extending longitudinally of the housing, burner means in the housing for heating the converter, means for rotating the converter, a fixed refuse inlet tube structure at one end of the converter, a fixed discharge receptacle and a charred refuse outlet tube at the other end of the converter, sealing means between the rotary converter and the discharge receptacle and sealing means between the rotary converter and the inlet tube structure to preclude escape of gases from the converter.
  • An outlet pipe for recovered combustible gases from the converter extended from the discharge receptacle to the burner means. Sealing means were provided for the refuse inlet tube, and for the charred refuse outlet tube. Valves in the outlet pipe selectively directed a portion of the recovered combustible gases to the burner.
  • That incinerator included means defining a combustion chamber, and a charging door defining an access means to the combustion chamber, and means operatively connected to the combustion chamber to exhaust the waste gases.
  • Means were disposed above the charge of waste material for controlling the temperature of the portion of the charge on top of the burning portion of the pile of burning combustibles, the control means including a water spray nozzle extending into the chamber and above the burning charge of waste materials for modulating initial combustion of a new charge of waste combustibles.
  • Means were responsive to the opening of the door for activating the spray nozzle. Means were provided for indicating when the temperature in the combustion chamber exceeded the distillation temperature of the combustibles.
  • Canadian Patent Number 688,561 patented June 9, 1989 by F. A. Lee et al provided a fired heater. That heater included a pair of refractory faced side walls oppositely disposed each relative the other and embracing a chamber therebetween. Heating means were operatively associated with each of the side wails for heating the refractory so that radiation was emitted therefrom. A tube was disposed in the chamber, and means were provided for circulating a process fluid through the tube.
  • the patented incinerator included a refractory-lined, substantially cylindrical combustion chamber having a flue outlet coupled to one end thereof. Means were provided for feeding combustible material into the chamber. Means were provided for introducing forced air into the chamber.
  • Means were provided for causing a stream of air to impinge upon the combustible material while entering the chamber. Means were also provided for controlling the flow of air into the chamber so that the rate of supply of air sufficed but did not substantially exceed that which was required for complete combustion of the combustible material within the combustion chamber.
  • combustion chamber and an adjustable heat source for supplying heat thereto.
  • the furnace also had a refractory lining with means thereon for receiving the heat source.
  • the combustion chamber was provided, in the region of the heat source, with a particularly defined inner sheet metal mantle.
  • the refractory lining was provided with passages for the supply of combustion air, and the mantle had slots therein in communication with the passages.
  • U.S. Pat. No. 4,230,451 patented Oct. 28, 1980 by M. Chambe provided an apparatus for the thermal treatment of a mass of organic materials. That apparatus included a horizontally elongated tank having a generally cyiindricai bottom and formed with an inner wail of thermally-conductive material spaced from an outer wall of thermally-insulating material. A roof was hermetically sealed to the tank, the roof was provided with a sealabie opening through which the mass could be introduced into the chamber.
  • the tank was formed along the bottom thereof with a sealabie outlet for discharging the thermally treated mass.
  • a burner opened into the passage and sustained a flame adapted to generate hot air which traverses the passage along the inner wall to heat the mass.
  • a duct was provided for feeding vapour evolved in the chamber to the burner and to supply the flame with the vapour.
  • Temperature-sensing means responsive to the temperature in the chamber were provided for controlling the flame.
  • Swistun provided a sawdust burning furnace which included an inner shell, an outer shell disposed concentrically around the inner shell, a bottom member, a cover member, a lower horizontal channel interconnected therewith, and an exhaust aperture defined in the outer shell adapted for interconnection to a flue connector.
  • a firebox was disposed inside the inner shell and was provided with air intake means.
  • a bieeder tube interconnected the firebox through the walls of the inner and outer shells to the outside of the outer shell, and has air vent means disposed between the inner and outer shells, and means to provide air to the bleeder tube.
  • U.S. Pat. No. 4,495,873 patented Jan. 9, 1985 by E. B. Blankenship provided an incinerator for burning odour-forming materials.
  • the incinerator was made up of an inner housing located within an outer housing and which had spaced-apart walls forming an interior space therebetween.
  • the inner and outer housings had aligned upper openings with insulated closure members.
  • a central chamber extended from the upper opening of the inner housing to a lower position for receiving material to be burned.
  • a gas collection chamber surrounded the upper chamber and an exhaust blower was provided for drawing gas from the central chamber to the interior space by way of the heat activated odour reducing catalyst and the collection chamber,
  • a heater was provided for preheating the heat activated odour reducing catalyst.
  • a second exhaust blower was provided for drawing gas from the interior space to the atmosphere.
  • a main heater was located within the lower portion of the central chamber for burning the material deposited therein.
  • An air inlet extended through the wail of the inner housing to the central chamber and a blower was provided for drawing air from the interior space into the central chamber.
  • Air ducts extended into the interior space for providing air to support combustion and for cooling purposes.
  • Canadian Patent Number 1 ,205,683 patented June 10, 1986 by E. H. Benedick, provided a vertical flow incinerator having regenerative heat exchange. That thermal recovery incinerator included a plurality of adjacent, substantially-vertical gas- processing sections, each of which included heat exchange means and a cover for the section with apertures formed therein.
  • a high temperature combustion chamber was disposed above the sections, and was in gas-flow communication therewith through the apertures.
  • the hazardous waste disposal system included a hollow high temperature cylindrical core defining a central reaction zone, a shell about the core and defining an annular space thereabout communicating with the reaction zone interior, and means for heating the core.
  • Means directed a carrier gas in a flow through the annular space for preheating the gas and then through the reaction zone.
  • Means were provided for continuously- inserting hazardous waste into the reaction zone and means were provided for removing reaction product from a bottom end of the reaction zone.
  • U.S. Pat. No. 4, 140,066 patented Feb. 20, 1979 by H. Rathjen et al provided a process for the thermal decomposition of poiychlorinated organic compounds, e.g., polych!orinated phenyls and biphenyls (PCB's).
  • the process comprised heat treating the poiychlorinated organic compounds in a flame, in a particularly-defined high- turbulence, combustion chamber.
  • Canadian Patent Number 1 ,164,631 patented Apr. 3, 1984 by O. D. Jorden provided a system and apparatus for the continuous destruction and removal of
  • That system included a mixing chamber, an agitator in the mixing chamber, a pump for feeding the fluid containing
  • a reaction chamber was operatively-connected to the mixing chamber for receiving the fluid containing the poiychlorinated biphenyl and reagent from the mixing chamber.
  • a separator separated the products of reaction between the
  • the apparatus included a plasma generator for producing a high temperature plasma, means for feeding hazardous waste to and through the plasma generator, means for feeding sufficient oxidizing agents to the hazardous waste to permit the complete decomposition of the hazardous waste to stable products, and means for controlling the temperature of the plasma and the flow of hazardous waste through the plasma generator.
  • Canadian Patent Number 1 ,225,775 patented Aug. 18, 1987 by W. C. eenan provided a method for treating poiychlorinated biphenyl contaminated sludge.
  • the method included the steps of heating the material by exposure to hot gas in a heating means thereby separating the poiychlorinated biphenyls from the material, and then conveying the separated poiychlorinated biphenyls out of the heating means for further treatment.
  • Canadian Patent Number 1 ,230,816 patented Dec. 22, 1987 by Y. Kilamira provided an apparatus for rendering poiychlorinated biphenyl toxic free.
  • the apparatus included a combustion furnace, a combustion vessel disposed in the combustion furnace, and a grid in the combustion vessel which divided the interior thereof into an upper and lower section.
  • a PCB tank communicated with the lower section of the combustion vessel, for filling the combustion vessel.
  • a burner and a fan were movable so as to be selectively placed in a position in opposition to an opening of the combustion furnace.
  • a gas treatment tank communicated with the combustion furnace via an exhaust duct.
  • Molten metal reactors may be used to treat a wide variety of waste materials including wastes which include haiogenated hydrocarbons, biomedical waste, and radioactive wastes.
  • Molten metal reactors utilize a bath of molten reactant metal which may include aluminum, magnesium, and/or lithium, for example, along with other metals.
  • the atmosphere above the bath Is preferably purged of oxygen.
  • waste material is placed in contact with the molten reactant metal the metal reacts with the organic molecules in the waste material to strip halogen atoms and form metal salts.
  • the reaction also liberates carbon along with other elements such as hydrogen and nitrogen. Carbon, hydrogen, nitrogen, and some metal salts may be removed from the molten metal reactor in a gaseous form. Metals which may be included in the waste material, or are liberated from the waste material, may alloy with the bath, Other reaction products or liberated materials collect at the surface or bottom of the bath and may be removed by suitable means.
  • Molten metal reactors require a heating arrangement to heat the reactant metal to a molten state and then maintain the reactant metai in a moiten state at a pre- determined temperature as waste material is added to the bath.
  • U.S. Pat. No. 6,195,382 to Wagner shows a moiten metai reactor having an induction heater for heating the reactant metai.
  • U.S. Pat. No. 5,271 ,341 to Wagner discloses a two-chamber molten metal reactor having a hydrocarbon-fired heater in one of the chambers. This two-chamber arrangement allows the reactant metai to be heated with hydrocarbon-fired burners while maintaining a separate area in which reaction products may collect for removal.
  • Tyrer in U.S. Pat. No. 1 ,803,221
  • Nixon in U.K. Patent 1 , 187,782
  • two-zone gasifie processes that have the potential to produce a high- purity hydrogen-rich gas by introducing the hydrocarbon feed below the surface of the molten iron, thereby minimizing the production of cracked products.
  • these molten- metal gasifier processes produce hydrogen-rich and carbon monoxide-rich gases at atmospheric pressure, when in fact most industrial processes require that such gases be available at higher pressures, such as 5 to 100 atmospheres absolute or higher.
  • it is necessary to compress the gases prior to industrial use, which is very expensive.
  • Molten metal, especially molten iron, baths are well known and widely used as gasifiers.
  • the light temperatures in such baths rapidly decompose, by thermal action, a variety of solid, liquid and gaseous feeds into hydrogen and/or carbon oxides.
  • Such processes are well known, e.g., U.S. Pat. Nos. 4,574,714 and 4,602,574 to Bach teach a molten iron gasifier.
  • Another, and preferred, molten metal reactor is disclosed in U.S. Pat. No. 5,435,814, MOLTEN METAL DECOMPOSITION
  • U.S. Pat. No. 4,062,657 issued to Knuppel et al. is directed to a process and an apparatus for gasifying sulphur-bearing coal in a molten iron bath. Reportedly, hot liquid slag is transferred from the iron bath to a second vessel in which the slag is desulfurized by contact with an oxygen containing gas, and then returned to the iron bath for reuse.
  • U.S. Pat. No. 4,406,666, issued to Paschen et al, is directed to a device for the gasification of carbon-containing material in a molten metal bath process to obtain the continuous production of a gas composed of carbon monoxide and hydrogen.
  • the '666 Patent states that gaseous carbon materials as well as gases containing oxygen can be introduced into the reactor below the surface of the molten metal bath.
  • the molten metal reportedly consists of molten iron, silicon, chromium, copper, or lead.
  • a method for converting carbon-containing feed, such as municipal garbage or a hydrocarbon gas, to carbon dioxide is described in U.S. Pat. No. 5, 177,304 issued to Nagei.
  • the carbon-containing feed and oxygen are introduced to a molten metal bath having immiscible first and second molten metal phases.
  • the '304 Patent states that the feed is converted to atomic carbon in the bath, with the first metal phase oxidizing atomic carbon to carbon monoxide and the second metal phase oxidizing carbon monoxide to carbon dioxide.
  • Heat released by exothermic reactions within the molten bath can reportedly be transferred out of the molten system to power generating means, such as a steam turbine.
  • Hydrocarbon-fired heaters are desirable for many molten metal reactor applications.
  • other applications for molten metal reactors cannot accommodate heating using hydrocarbon-fired burners.
  • a molten metal reactor may be highly desirable for treating biomedical wastes and other wastes generated aboard a ship.
  • a sufficient hydrocarbon supply may not be readily available aboard the ship to provide the required heating.
  • induction heaters are well-suited for fixed plants which have access to a suitable electric power supply.
  • the electromagnetic field produced by induction heaters may limit the temperatures at which the molten metal reactor could be operated. This temperature limitation arose from the fact that portions of the electromagnetic field extended beyond the molten reactant metal and passed through the reactor vessel and related equipment.
  • Fig. 1 shows a cross section view of a first reactor vessel in connection with a
  • Fig. 2 shows a top view of a reactor vessel according to a second embodiment
  • Fig. 3 shows a cross sectional view of a first measuring lance
  • Fig. 4 shows a cross sectional view of a second measuring lance
  • Fig. 5 shows a cross sectional view of a third measuring lance
  • Fig. 6 shows an ash removal section of a molten metal gasification system
  • Fig. 7 shows a molten metal gasification system according to a further embodiment.
  • industrial waste treatment system which comprises a refractory-lined crucible vessel for holding a melt (molten metal) and a inlet tubular conduit for directing the flow of a stream of industrial waste material or feed such as carbonaceous feedstock to be dropped into contact with the said melt disposed within the refractory-lined crucible, an outlet exhaust conduit for directing the flow of exhaust gases evolving from the melt to a gas treatment unit (in a second vessel) for reducing the Sulphur and particulate content of said exhaust gases.
  • the moiten metal comprises the following melt composition:
  • a slag-oxide layer formed subsequently during the operation of the present specification is periodically drained and removed from the refractory-lined vessel.
  • a typical reference composition of the molten slag layer is exemplified as follows:
  • industrial waste is first loaded onto a compactor unit/train, compacted into a dense, compacted paste-form and pumped by means of an auger drive through a conduit that is adapted to direct the compacted waste into contact with a molten metal disposed within a refractory- lined treatment vessel (first reactor).
  • a lance device positioned above the surface of the molten metal ejects an air jet to cause contact with the molten metal to cause partial oxidation of the molten metal and to form a slag layer thereon.
  • Evolving gases are directed via one or more exhaust gas passageway to a second reactor where additional heat is supplied to further reduce dioxins otherwise not treated in the first reactor.
  • At least a jet of air in ejected from a iance device positioned above the molten metal and molten slag-oxide layer in the manner as follows: a) ejecting at least one primary jet of air from a Iance positioned above the molten metal into the molten metal to react with impurities therein and to form a layer of molten slag; b) continuing to eject the primary jet of air from the Iance and thereby causing the primary jet of air to pass through the slag layer into the molten metal; c) ejecting a plurality of secondary jets of air from the lance, the secondary jet of air travelling for a distance separately from the primary jet of air; and d) entraining the secondary jets of air into the primary jet of air upstream of the entry of the primary jet of air into the volume of the molten metal.
  • the said primary jet of air is desirably ejected from the iance in both step (a) and step (b) of the method according to the specification at an axial velocity that is supersonic.
  • a supersonic velocity in the range of achl .5 to ach 3 may be used.
  • the longitudinal axis of each secondary jet diverges from the longitudinal axis of its associated primary jet in the direction of travel at an angle of up to 45°.
  • the preferred angle of divergence of each secondary air jet from its associated primary air jet is in the range of 5° to 25° depending on the absolute velocity of the second air jet and its velocity relative to the first air jet. Particularly preferred angles of divergence are in the range of 10° to 20°.
  • FIG. 1 shows an example for a gasification system according to the present specification.
  • a gasifier 100 comprises a first reactor vessel 101 that is covered by a cover 102.
  • the gasifier 100 is connected to a second reactor vessel 103 via a gas passage conduit 104.
  • the reactor vessel 101 contains a molten metal layer 107 and a molten siag-oxyde layer 108 which floats on top of the molten metal layer 107.
  • the gasifier comprises injection tubes 105, 108 for injecting air jets into the molten slag-oxyde layer 108 and through the slag-oxyde layer into the molten metal layer 107.
  • an overhead lance 1 16 is provided in the cover 102 and feed conduits 109, 1 10 are provided in a bottom wall of the reactor vessel 101. In other embodiments, further feed conduits may be provided in side walls of the reactor vessel 101.
  • the overhead lance provides an example of a tubular conduit according to the specification.
  • the injection tubes 105, 106 are connected to an air reservoir 1 1 1 via a compressor 112.
  • the overhead lance 1 16 is connected to a reservoir 1 13 of a feed fuel via a feeder pump 1 14.
  • a tilting mechanism 1 15 is provided for tilting the first reactor vessel 101 at a tilt angle alpha, in one embodiment, the tilt angle can be adjusted between 0 and 60 degrees.
  • Tables 1-5 are exemplary operation design parameters that may be used with the waste treatment system. However, other operations and/or configurations may be realized.
  • Tables 8-7 includes the bill of materials which may be varied. TABLE 1
  • thai sodium hydroxide is an optional additive and may not be applied depending on waste composition, operating condition and melt temperature.
  • sodium oxide and or CaC03 is deployed by admixing a pre-determined amount to the industrial waste prior to being pumped into contact with the molten slag-oxide layer in the first vessel of the present specification to control the basicity of the slag-oxide layer during the treatment of the waste material.
  • composition of slag varies with the type of melting process used and the type of iron or steel being melted in the first vessel, additional oxides or nonmetai!ic compounds are formed when molten metal is treated with industrial waste material that changes the chemistry of the system, and because these oxides and
  • nonmetaliics are not soluble in iron, they float in the liquid metal as an emulsion, and eventually these nonmetaliics coalesce into the molten slag-oxide layer on the top surface of the molten metal.
  • a readiiy castable, water-free refractory material for the working liner comprising 60% Al 2 O 3 , 38% SiO 2 , and 2% TiO 2.
  • the lance device (positioned above the molten metal), and or parts of the first vessel adapted to contain the molten metal can be made from alumina refractory containing at least 88 wt.
  • % alumina % alumina and being non-porous with a porosity of up to 20%
  • the terms non-porous and substantially non-porous are used herein to describe a refractory with a porosity of up to 20%. in one non-limiting sample, the refractory composition and specifications are herein disclosed:
  • Biomedical wastes including infectious, pathological, chemo
  • Incinerator fly ash it is noted above in Table 2 that the waste streams need not be separated and can be directed as a waste mixture thus making waste treatment significantly more cost effective.
  • the refractory-lined vessel is configured to hold between 1 to 15 metric tons of melt, and the refractory-lined vessel further operable to be adapted onto a skid-mount rail.
  • the present specification may be mounted on a trailer truck and the first vessel configured to be held in a 20-foot or 40-foot freight container unit (shipping TEU), and be adapted such that the trailer is divided into two sections, each section having means for connection with the respective ends of the skid members and each section having means for raising one end of the trailer into the connection means at the required level for travel, and each section having adjustable stabilizing equipment for maintaining the tanks in position on the trailer as if is transported.
  • the refractory-lined vessel is configured to hold between 500Kg to 1 ,5 tons of molten metal (melt).
  • generated - ail of the feedstock may be 100% waste
  • industrial waste is first compacted prior to being pumped into the flow conduit tubular apparatus that directs the compacted industrial waste into contact with the moiten metal, the compaction is further operated by means of a compaction power unit.
  • a power unit of this aspect is of the type which moves a compaction head along between the ends of a refuse container for packing the refuse and for removing the compacted refuse from the refuse container.
  • the power unit is attached to the interior of the refuse container and to the compaction head.
  • the power unit of this aspect comprises a housing provided with a chamber therein.
  • a first piston of a given transverse dimension is positioned within the chamber. Attached to the first piston and coaxial therewith are spaced-apart coaxial cylinders.
  • a second piston which has a smaller transverse dimension than the first piston is also within the chamber and is coaxial with the first cylinder and is between the cylinders which are attached to the first piston.
  • Fluid is introduced through a main passage of the housing for operation of the pistons.
  • a valve mechanism is located within the main passage.
  • the fluid is conducted into the main passage and then through an auxiliary passage into a space between the cylinders which are attached to the first piston, for movement of the second piston or smaller piston, for initial operation of the power unit and for initial movement of a compaction head which is attached to the power unit.
  • Fluid which moves the first piston or smaller piston is of a given initial pressure. This fluid of the given pressure moves the smaller piston until this fluid pressure is unable to move the smaller piston farther. Then the pressure of fluid flowing into the main passage increases, This increase in fluid pressure causes valve operation in the main passage which closes the auxiliary passage and closes fluid between the main passage and to the smaller piston.
  • a fixed hopper bin having a bottom outlet opening which registers with an opening in the underlying compactor unit ahead of the horizontal ram thereof; and a vertically swingable dumping bin which is raised to a steep angle above the compactor unit base to feed large volumes of waste by gravity action into the fixed hopper bin.
  • the side walls of the hopper and dumping bins at one side of the apparatus are cut downwardly to allow side loading of refuse by front end loaders and the like when the dumping bin is in a level position on the compactor unit base.
  • the dumping bin is raised and lowered by power cylinder means on opposite sides of the compactor unit base.
  • a load cell device is configured to read and record the mass weight of the industrial waste material and transmits the recorded data signal to a remote processor for calculating the quantity of CaC03 to be admixed during the stage of waste compaction so as to adjust and control the chemical composition of the molten slag layer that is formed during operation of the molten metal disposed in the first reaction vessel.
  • a remote processor calculates the quantity of CaC03 to be admixed into the industrial waste based on the function of the total mass weight of the molten metal in the first reactor vessel, the mass weight of the industrial waste material loaded into the hopper unit, or a combination thereof.
  • reaction dynamics Based on a iron melt, substantially molten at a temperature of between 1 100 to 1300 degrees C, the reaction dynamics are as follows:
  • MgO.AI203(l) ⁇ Mg (I) + 2AI (I) + 40 Mg(s)+CO(g) ⁇ MgO(l)+C(l) in some cast irons the silicon and manganese levels present in its solid phase may range from Si 1.5 to 2.0% wt and n from 0.5 to 1.0%, and while energy fuel expenditure for such cast iron charge materials are lower during reactor start-up, the formation of the molten iron bath and in combination with the stirring action of the oxidizer gas will cause formation of SiO and MnO in the slag layer right above the molten iron bath surface, contributing to limited but severe erosion of the refractory lining in the reactor.
  • the heat of reaction ( ⁇ ), or enthalpy determines the energy cost of the process.
  • thermodynamic driving force that makes a reaction occur A negative value for ⁇ indicates that a reaction can proceed spontaneously without external inputs, while a positive value indicates that it will not.
  • the enthalpy change ( ⁇ ) is a measure of the actual energy that is liberated when the reaction occurs (the "heat of reaction”), if it is negative, then the reaction gives off energy, while if it is positive the reaction requires energy.
  • the entropy change (AS) is a measure of the change in the possibilities for disorder in the products compared to the reactants.
  • An EiSingham diagram is a plot of AG versus temperature. Since ⁇ and AS are essentially constant with temperature unless a phase change occurs, the free energy versus temperature plot can be drawn as a series of straight lines, where AS is the slope and ⁇ is the y-intercept. The slope of the line changes when any of the materials involved melt or vaporize, (note that free energy of formation is negative for most metal oxides).
  • the position of the line for a given reaction on the ES!ingham diagram shows the stability of the oxide as a function of temperature. Reactions closer to the top of the diagram are the most "noble" metals (for example, gold and platinum), and their oxides are unstable and easily reduced. As we move down toward the bottom of the diagram, the metals become progressively more reactive and their oxides become harder to reduce.
  • the most "noble" metals for example, gold and platinum
  • Typical composition of the exhaust gas produced may be as follows:
  • the molten metal is inductively heated in the vessel to at least 1300 degrees C, and industrial waste material is pumped via a tubular conduit into contact with the slag oxide layer that is formed on the top surface of the molten metal.
  • the molten metal is inductively heated and further exothermicaily oxidized to a temperature in the range of between 1400 ⁇ 1500 degrees C, and between 0.5% to 10.7% mass weight of the industrial waste is admixed with CaC03 (CaC0.sub,3) to control the basicity of the molten slag layer that forms on the top surface of the molten metal in the first reactor vessel.
  • the vessel is refractory-lined and may be made up of the following refractory material having the chemical composition:
  • the chemical composition of the molten metal or molten slag-oxide layer would be monitored by using a measuring lance device to be inserted into the molten metal which comprises an expendable body, a protected first thermocouple mounted on one end of said lance, a receptacle chamber for receiving the molten metal, a protected second thermocouple mounted inside said chamber, and a path for the molten metal leading to said chamber, characterized in that an opening through which air can be discharged is provided in a part of a protecting tube for the second thermocouple, said part not positioned in said receptacle chamber.
  • Figures 3, 4 and 5 show examples of measurement lances.
  • a lance body 10 is provided with a deoxidation chamber 1 ' and a receptacle chamber 1 .
  • the deoxidation chamber 1 ' is made of steel and the receptacle chamber is made of steel or cast iron.
  • the lance body 10 is dipped into a molten steel contained in a converter which is being refined by means of a sub-lance not shown.
  • the temperature of the molten steel can be measured by a thermocouple 2' provided at the tip end of lance body 10.
  • the molten steel enters deoxidation chamber 1 ' through a path or mouth 9 thereof, where the steel comes Into contact with a deoxidation agent 14 such as A!, Ti, etc. which has previously been placed in chamber 1 '.
  • the molten steel thus deoxidized enters receptacle chamber 1 through an outlet 15 where the solidification temperature of the molten steel is measured by another thermocouple 2 to determine the amount of carbon in the steel.
  • the lance which has thus received the moiten steel is withdrawn from the bath, and the steel in the receptacle chamber 1 can be measured with respect to its composition such as M , S, P, etc. by the use of a Count VAC analyzer.
  • deoxidation chamber 1 ' is made of steel as above, there is hardly any adverse effect which would otherwise have been encountered by the through melting loss of a part of the deoxidation chamber 1 ' such as a corner of the mouth 9, the outlet 15 and the like.
  • a spray nozzle can be provided in the upper part of the connector.
  • a lance is shown wherein a receptacle chamber 1 for receiving a sampled molten steel surrounded by a lance body 10 made of refractory paper, which is connected to a connector 18, which is in turn connected to a sub-lance 18 via a holder 17.
  • a spray nozzle 19 is provided at the sub-lance 18 in the upper part of the connector 16.
  • a gas such as oxygen, nitrogen and the like is sprayed to cool lead wires 13 and the connector 16, while water vapor or tar, etc. in the holder 17 and the sub-lance 18 can be purged from a hole 20.
  • numeral V refers to a deoxidation chamber
  • 14 refers to a deoxidaiion agent
  • 9 refers to a path or mouth for receiving the molten steel.
  • the present specification discloses a method for operating a waste treatment system for treating a feed, such as an industrial waste material, by contacting the feed into a molten metal in a first vessel, wherein the first vessel contains a volume of the molten metal.
  • a jet of air is ejected from a lance positioned above the molten metal into the molten metal to react with the molten metal to form a layer of molten slag-oxide.
  • the jet of air is continued to be injected from the lance at least until the jet of air passes through the molten slag-oxide layer into the molten metal.
  • the feed is pumped from a tubular conduit positioned above the molten slag-oxide layer to cause contact between the feed and the molten slag-oxide layer, wherein the feed is selected from coal, coal-liquid slurry, biomass, waste-derived material, crude oil, tar sands, shale-derived material, or a combination thereof.
  • the molten metal bath material has the following composition:
  • Aluminum in the range of 0.005 to 0.1 mass weight percent, Titanium in the range of 0.015 to 0.05 mass weight percent;
  • Exhaust gases evolving from the molten metal and molten slag-oxide layer are directed to a second vessel to treat the exhaust gases to a pre-determined proximate gas molar composition.
  • a product syngas flowing from the molten metal is directed by one or more gas passage conduit configured in operational communication with the second vessel and with a powerplant for electric power generation, a first chemical catalytic reactor to chemically reform product syngas into a pre-determined hydrocarbon product, a second chemical catalytic reactor to chemically reform product syngas into anhydrous ammonia product, a third chemical catalytic reactor to chemically reform product syngas into methanol product, or a combination thereof.
  • the abovementioned composition of the molten metal bath leads to a high efficiency of syngas production for the abovementioned types of feed materials. This efficiency is further enhanced by blowing air through the slag layer into the molten metal and thereby increasing the amount of metal in the slag layer.
  • the injection of air may be made even more effective by using a Laval nozzle, also known as "convergent-divergent nozzle", to produce a supersonic air jet and by using a first and second jet of air which are inclined to each other, thereby entraining the second jet of air into the first jet of air.
  • the air speed is controlled by a processor, for example adjusting an air pressure or a shape of a Laval nozzle.
  • a device for operating a waste treatment system for treating a feed such as industrial waste material, by bringing the feed into a molten metal in a first vessel, wherein the first vessel contains a volume of the molten metal.
  • the device comprises ejection means, such as an ejection nozzle, for ejecting at least one jet of air from a lance positioned above the molten metal into the molten metal to react with the molten metal to form a layer of molten slag-oxide and for continuing to eject at least one jet of air from the lance and thereby causing at least one jet of air to pass through from the molten slag-oxide layer into the molten metal.
  • ejection means such as an ejection nozzle
  • the device comprises a tubular conduit for connection to a feeder pump and for causing a contact between the feed and the molten slag-oxide layer, the tubular conduit being positioned above the vessel.
  • the device comprises one or more gas passage conduits configured in operational communication with the first vessel.
  • the gas passage conduits comprise a first gas passage conduit for directing exhaust gases evolving from the molten metal and molten slag-oxide layer to a second vessel to treat the exhaust gases to a pre-determined proximate gas molar composition.
  • the one or more gas passage conduits comprise a second gas passage conduit for directing syngas from the first vessel to a syngas consumer.
  • the first and the second gas passage conduit may also be identical.
  • the syngas consumer may be provided by a powerplant for electric power generation, a first chemical catalytic reactor to chemically reform product syngas into a pre-determined hydrocarbon product, a second chemical catalytic reactor to chemically reform product syngas into anhydrous ammonia product, a third chemical catalytic reactor to chemically reform product syngas into methanol product, or a combination thereof.
  • the second vessel is located within the syngas consumer.
  • the second vessel is located between the first vessel and the syngas consumer.
  • a device is capable of generating a high yield of syngas by providing a high metal content in the slag layer and thereby an effective heat transfer to the feed.
  • the metal content in the slag layer is increased by providing suitable ejection means for blowing air through the slag layer into the molten metal.
  • Experiments on direct-contact heat exchange between molten metal and water for steam production were conducted. These experiments involved the injection of water into molten lead-bismuth eutectic for heat transfer measurements. Based on the initial results of the experiments, the effects of the water flow rate and the molten metal superheat temperature difference between molten metal and saturated water on the volumetric heat transfer coefficient were discussed. Molten lead-bismuth was chosen to obtain text data. The experiments were performed with lead to
  • a steam production according to the further embodiment may be used in combination with a gasification method or with a gasification apparatus according to any of the other embodiments.
  • the experimental apparatus consists of a test section and associated components.
  • Water is pumped from a supply tank to the injector through a set of filters
  • the filters were reused from a previous project WATERMUSIC.
  • the water flow rate is metered by valves and measured by flow meters with ranges of 14 to 100 ml/min and 50 to 500 ml/min.
  • the present specification discloses a water injector for a gasifier having a supply means for an inert gas, such as argon, and a step of injecting water onto molten metal through an injector and injecting an inert gas into the injector.
  • an air supply into the containment vessel is turned on to freeze metal in the transfer tube and prevent inadvertent transfer back to the melt vessel.
  • a pump is provided that would remove any water that condensed inside the containment vessel. However, this should not happen since the steam is exhausted into a condenser outside of the containment vessel.
  • step (a) at least one jet of air is
  • step (b) at least one jet of air is ejected at a supersonic axial velocity in the range of between Mach 1 to Mach 3.5.
  • step (b) at least one jet of air is ejected at a supersonic axial velocity in the range of between Mach 1 to Mach 3.5.
  • the molten metal is inductively heated in the first vessel by one or more electromagnetic induction coil field.
  • the supersonic axial velocity of at least one jet of air ejected from the lance is controlled by a remote processor.
  • the method according to item 10 wherein the refractory-lined inner layer of the second vessel further comprises alumina Al.sub.2.0.sub.3 of at least 35 mass weight percent.
  • the method according to item 10 or item 1 1 wherein refractory-lined material has a material density of 3.5 Mg/m.sup.3. 13.
  • a method for controlling chemical reaction of a feed to generate product syngas therefrom comprising the steps of: a) directing the feed into a reactor within which a molten metal bath material is disposed; the temperature of molten metal bath material inductively heated to at least 1300 degrees Celsius by one or more induction coil apparatus energized with one or more alternating current "AC" power waveform; b) pressurizing the reactor to a pressure of at least 1 bar pressure absolute.
  • a method for controlling chemical reaction of a feed to generate product syngas therefrom comprising the steps of: a) directing the feed into a reactor within which a molten metal bath material is disposed; the temperature of molten metal bath material inductively heated to at least 1500 degrees Celsius by one or more induction coil apparatus energized with one or more AC (alternating current) power waveform; b) pressurizing the reactor to a pressure of at least 1.2 bar pressure absolute.
  • the method according to one of the items 19 to 21 wherein at least a portion of the molten metal bath is oxidized to cause formation of a molten slag-oxide layer on the surface of the molten metal bath.
  • the feed is selected from coal, coal-liquid slurry, biomass, waste-derived material, crude oil, tar sands, shale-derived material, or a combination thereof.
  • flowing from molten metal is directed by one or more gas passage conduit configured in operational communication with a powerplant for electric power generation, a chemical catalytic reactor to chemically reform product syngas into a pre-determined hydrocarbon product, a chemical catalytic reactor to chemically reform product syngas into anhydrous ammonia product, a chemical catalytic reactor to chemically reform product syngas into methanol product, or a combination thereof.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention porte sur le fonctionnement d'un système de traitement des déchets pour le traitement d'une charge par la mise en contact de la charge avec un métal en fusion dans une première cuve. Un jet d'air est éjecté à partir d'une lance dans le métal en fusion pour réagir avec le métal en fusion pour former une couche d'oxyde-laitier en fusion. La charge est choisie parmi du charbon, de la boue liquide de charbon, de la biomasse, de la matière issue de déchets, du pétrole brut, des sables bitumineux, de la matière issue de schiste, ou une association de ceux-ci. La matière de bain métallique en fusion comprend du carbone, du silicium, du manganèse, du chrome, du soufre, du phosphore, de l'aluminium et du titane. Les gaz de combustion qui se dégagent du métal en fusion et de la couche d'oxyde-laitier en fusion sont envoyés vers une seconde cuve pour traiter les gaz de combustion à une composition molaire gazeuse proche d'une valeur prédéfinie.
PCT/IB2013/054736 2012-06-08 2013-06-10 Système de gazéification en traitement des déchets WO2013183037A2 (fr)

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US14/406,253 US20150184090A1 (en) 2012-06-08 2013-06-10 Waste treatment gasification system

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IB2012052893 2012-06-08
IBPCT/IB2012/052893 2012-06-08

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Cited By (3)

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EP3009495A1 (fr) * 2014-10-15 2016-04-20 Commissariat à l'Énergie Atomique et aux Énergies Alternatives Procédé et dispositif pour la pyro-gazéification d'une matière carbonée comprenant un bain de cendres en fusion
RU2773469C1 (ru) * 2021-06-18 2022-06-06 Общество с ограниченной ответственностью "Чистая энергия" Способ переработки отходов из полимерных, композитных и резинотехнических материалов и устройство для его осуществления
WO2022265538A1 (fr) * 2021-06-18 2022-12-22 Общество с ограниченной ответственностью "Чистая энергия" Procédé de retraitement de matériaux polymères, composites et caoutchouteux techniques

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CN107243500B (zh) * 2017-06-28 2019-05-21 河南科技大学 一种高温旋风熔融式铬渣解毒装置及其解毒方法
US11638331B2 (en) 2018-05-29 2023-04-25 Kontak LLC Multi-frequency controllers for inductive heating and associated systems and methods
US11555473B2 (en) 2018-05-29 2023-01-17 Kontak LLC Dual bladder fuel tank
US11512260B2 (en) 2018-06-11 2022-11-29 Donald Gene Taylor Pulse detonation shockwave gasifier

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US3897739A (en) * 1974-10-30 1975-08-05 Us Health Fluid bed combustor for operation at ash fusing temperatures
US4574714A (en) * 1984-11-08 1986-03-11 United States Steel Corporation Destruction of toxic chemicals
US6069290A (en) * 1990-05-16 2000-05-30 Clean Technologies International Corporation Waste treatment process and reactant metal alloy
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3009495A1 (fr) * 2014-10-15 2016-04-20 Commissariat à l'Énergie Atomique et aux Énergies Alternatives Procédé et dispositif pour la pyro-gazéification d'une matière carbonée comprenant un bain de cendres en fusion
FR3027311A1 (fr) * 2014-10-15 2016-04-22 Commissariat Energie Atomique Procede et dispositif pour la pyro-gazeification d'une matiere carbonee comprenant un bain de cendres en fusion
RU2773469C1 (ru) * 2021-06-18 2022-06-06 Общество с ограниченной ответственностью "Чистая энергия" Способ переработки отходов из полимерных, композитных и резинотехнических материалов и устройство для его осуществления
WO2022265538A1 (fr) * 2021-06-18 2022-12-22 Общество с ограниченной ответственностью "Чистая энергия" Procédé de retraitement de matériaux polymères, composites et caoutchouteux techniques

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WO2013183037A3 (fr) 2014-02-20

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