US3888194A - Method for incinerating industrial wastage - Google Patents

Method for incinerating industrial wastage Download PDF

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Publication number
US3888194A
US3888194A US44689574A US3888194A US 3888194 A US3888194 A US 3888194A US 44689574 A US44689574 A US 44689574A US 3888194 A US3888194 A US 3888194A
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Prior art keywords
wastage
fluidized bed
combustible
furnace
combustion
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Expired - Lifetime
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English (en)
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Kunio Kishigami
Hiroshi Kobayashi
Toru Sente
Koichi Sugiyama
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Mitsubishi Hitachi Power Systems Ltd
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Babcock Hitachi KK
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    • 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
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • This invention relates to a method for incinerating in a fluidized bed furnace the industrial wastage containing organic nitrogen compounds which produce, upon incineration, a great quantity of nitrogen oxide detri mental to the human body, and more particularly to a method for reducing and removing nitrogen oxide thus produced, by maintaining the interior of a fluidized bed in a reductive atmosphere. thereby minimizing the quantity of nitrogen oxide contained in the combustion waste-gas.
  • the fluidized incineration furnace air is blown from below through the incombustible fluidizing medium particles placed on a perforated plate provided in the furnace, to fluidize same, while the interior of the fluidized bed is preheated by means such as a burner to a temperature higher than combustion temperatures of the materials to be burnt, and the materials to be burnt are fed into the furnace from its top, whereby the materials to be burnt may be incinerated due to a combustion heat produced from the burning materials themselves.
  • the fluidized bed furnace as used herein is an incineration furnace using a fluidized bed.
  • Those elements are not present in the form ofa single substance but as complicated compounds. Those may be generally classified into biological compound such as protein and artificial compounds such as polyamide resin.
  • the organic nitrogen compounds contained in the industrial wastage such as for instance protein, polyamide resin, sewage sludge, acrylic resin, etc., are present in the form of a peptide bond (CO. NH), cyan radical (-CN), ammoniacal nitrogen (NH, nitric and nitrous nitrogens (NO;;, NO and the like, and the incineration of such organic nitrogen compounds would leads to the production of nitrogen oxides (NO which are detrimental to a human body and of a quantity which is commensurate to that of nitrogen contained in the materials to be burnt.
  • CO. NH peptide bond
  • -CN cyan radical
  • NO ammoniacal nitrogen
  • NO nitric and nitrous nitrogens
  • the nitrogen oxides (NO which are produced due to the oxidation of inorganic nitrogen contained in air during the combustion process in a general type industrial furnace such as a boiler are negligible in quantity in the case of a temperature being below l,()00C, whereas in the case of the temperature being over l,000C, the quantity of nitrogen oxides (NO,] produced is notably increased. This is because nitrogen (N and oxygen (0 in air react with each other at an elevated temperature such as above l,(l()()C according to the following formula, thereby producing NO:
  • nitrogen oxides produced from the combustion of organic nitrogen compounds contained in muddy wastage exhausted from various kinds of effluent treating apparatuses are not like those which are produced from the oxidation of nitrogen in air at an elevated temperature but those which are produced from the decomposition of organic nitrogen compounds contained in the muddy wastage. Accordingly, nitrogen oxide may be produced at any level of a lower temperature, as far as the muddy wastage is in the range of temperatures, at which it is combustible.
  • nitrogen oxides which are produced from the oxidation of nitrogen with oxygen in air during the combustion in the industrial furnaces of a general type may be prevented to some extent from being produced by lowering the combustion temperature to not more than l,000C.
  • nitrogen oxides which are produced from the combustion of organic nitrogen compounds may not be prevented from production simply by resorting to a measure to lower the temperature.
  • a method for incinerating industrial wastage in which air is blown into a furnace from below to fluidize incombustible fluidizing medium particles placed in the furnace, thereby forming a fluidized bed, while said industrial wastage is introduced in the fluidized bed from the top of the fluidized bed incineration furnace which has been preheated to a temperature above a combustion temperature of combustible industrial wastage to be burnt, and then the aforesaid wastage is burnt due to the combustion heat produced from the wastage itself, said method being characterized in that combustible materials abundant in carbon content is supplied together with the aforesaid wastage into the furnace, thereby maintaining the interior of the fluidized bed in a reductive atmosphere whereby the nitrogen oxides produced from the combustion of organic nitrogen contained in the aforesaid wastage may be reduced to an innocuous nitrogen and thus nitrogen oxide may be removed from the combustion waste gas.
  • FIG. I is a magnified view of a muddy particle within a fluidized bed incineration furnace, embodying the present invention.
  • FIGv 2 is a view illustrating the conditions within a fluidized bed incineration furnace embodying the present invention.
  • FIG. 3 is a schematic view illustrating an operational system and the cross section of a fluidized bed incineration furnace embodying the invention.
  • the present invention is directed to providing a method for incinerating industrial wastage containing organic nitrogen compounds, by using a fluidized bed furnace, in which industrial wastage together with ma terials containing a great amount of carbon, such as pulverized coal, heavy oil or the like is charged in a furnace to thereby fluidized the wastage and the carbon abundant material together with fluidizing medium with air, and then the industrial wastage is burnt, while the interior of the fluidized bed (or fluidized layer) is maintained in a reductive atmosphere, whereby the nitrogen oxides (NO,,.) produced from the organic nitrogen compounds contained in the wastage are reduced during the combustion of the wastage, to thereby obtain nitrogen gas (N thus preventing the production of nitrogen oxides.
  • a fluidized bed furnace in which industrial wastage together with ma terials containing a great amount of carbon, such as pulverized coal, heavy oil or the like is charged in a furnace to thereby fluidized the wastage and the carbon abundant material together with fluidizing medium with air, and then the industrial wastage
  • the fluidized bed is provided by blowing air or gas into a furnace from its bottom and fluidizing the fluidizing medium in the form of solid particle layer which is supported on a perforated plate within a furnace.
  • silica base particles primary constituent SiO such as river sand, which is chemically inactive, are used as a fluidizing medium of a solid particle layer, the particle size thereof being in the range from 0.1 to 2.0 mm.
  • sulfur and chlo rine are contained in the wastage and desired to be directly fixed and absorbed within the fluidized bed, it is preferable that chemically active cement clinker parti' cles be used as a fluidizing medium.
  • the composition of cement clinker particles is, for instance, 60 to 70% CaO, 6 to 8% Fe O and 3 to 6 SiO
  • the fluidized bed incineration furnace utilizes a fluidized bed for incineration.
  • the temperature of the fluidized bed is normally in the range from 750 to 850C. In the respect, such a temperature is extremely lower than the temperature (over 1,000C), at which nitrogen oxides are formed by the reaction of nitrogen with oxygen contained in air, as is the cases with industrial furnaces of a general type, such as a boiler. Furthermore, at such a low temperature, the quantity of nitro gen oxides produced according to the reaction of nitrogen with oxygen in air is neglisible.
  • Vigorous reaction may be achieved in the fluidized bed furnace, because the fluidizing solid particle layer consists of particles of a size from 0.l to 2.0 mm and thus presents extremely large contact surface area at the time when the particle layer stands still (e.g., the height of the layer is 500 to 1,000 mm). Accordingly,
  • the wastage particles are maldistributed microscopically to some extent, despite that muddy wastage has been dried. crushed and placed within the fluidized bed. Furthermore, the wastage particles are subjected to combustion at a very small ex cessive air ratio, such that a reductive atmosphere short of oxygen encircles around the small particles of crushed wastage.
  • FIG. 1 is a magnified view of a mud piece b, showing the condition within a fluidized a, microscopically. Mud pieces b float in the fluidizing medium particle group d forming a fluidized bed a, while a mud piece b containing a considerable amount of carbon components forms a reductive atmosphere in its surrounded zone c.
  • the fluidized bed itself has a strong catalytic action.
  • Fe O and AI O in the aforesaid active fluidizing medium particles or vanadium oxide (V 0 formed by vanadium (V) in the heavy oil in said medium particles, if heavy oil is used for auxiliary burning, and those compounds act as catalysts to accelerate the formation of carbon monoxide according to the following formulae:
  • Fe O (W MnO, A1 0 V 0 C11 0 and the like are considered to be catalysts adapted to accelerate the above reactions.
  • FIG. 2 showing the condition of the interior of a fluidized bed incineration furnace for use in muddy wastage incineration.
  • the primary air g of the combustion air is fed into the incineration furnace e from below for fluidizing the fluidizing medium within the furnace 0, thereby forming a fluidized bed k.
  • the fluidized bed It is preheated by means of a burners or the like. Materials abundant in carbon content such as pulverized coal or the like is supplied together with muddy wastage from the top of the furnace e into the fluidized bed It to be fluidized together with the fluidizing medium and incomplete combustion results, whereby the interior of the fluidized bed It is maintained in a reductive atmosphere.
  • the incineration is carried out in this manner.
  • there are present in the form of mixture CO, H CH 0 N and CO within the fluidized bed k such that the formation of the reductive atmosphere within the fluidized bed k may be accelerated.
  • An incineration furnace 1 includes a perforated plate 2 and an air chamber 3 in the lower portion thereof, while the dehydrated mud, which contains pulverized coal or fine granular coal. is supplied from the top portion of the incineration furnace 1 therein from a mud supply device 4.
  • the air which is required for fluidizing and combustion is supplied through a blower 8, damper l5 and duct 9 to the air chamber 3, thereby fluidizing by passing through the perforated plate 2 the fluidizing medium particles such as cement clinker and the like as well as the mud which contains pulverized coal and fine granular coal, said particles and mud being positioned on the perforated plate 2, and thus the fluidized bed is provided.
  • the operation of the incineration furnace begins with heating the fluidized bed by using a burner 6a. After which the incineration of the wastage proceeds due to the combustion of the pulverized coal (or fine granular coal) mixed with the muddy wastage. If the heat accruing from the combustion of the pulverized coal is insufficient. a burner 6a is used as an auxili ary means. The waste gas is discharged through a duct 7 out of the furnace.
  • the waste gas is introduced from duct 7. to thereby supply the waste gas through a damper l4 and blower 16 into the duct 9.
  • a signal 11 which represents the supplied amount of muddy wastage and is obtained in connection to R.P.M. of a rotary feeder of the muddy wastage supply device 4, and a temperature.
  • signal 18 from a thermometer 1 adapted to measure temperatures at the fluidized bed 5 are fed into a control box 10, whereby inlet dampers l5 and 14 of the blowers 8 and 16 are each controlled by means of signals 12a and 12b, while the control valves l9a and 19b for controlling the amount of oil for burners 6a and 6b are controlled by means of signals 13a and BI).
  • the burner 6a is primarily used for starting a furnace or for an auxiliary purpose, while the burner 6b is used for supplying combustible materials abundant in carbon content, such as heavy oil, to the fluidized bed 5 and is normally used in case the muddy wastage to be charged in the furnace 1 contains no pulverized coal or the like.
  • a damper 22 provided in the secondary air supply duct 21 is controlled by means of a signal 20.
  • the features of the present invention reside in that, for in cineration of combustible industrial wastage containing organic nitrogen, particularly muddy industrial wastage of a high water content; there is used a fluidizing bed which permits the incineration at an extremely low excessive air ratio (1.1 to L3); carbon components of no less than 20% by weight, based on the weight of the wastage, are mixed with the solid matter such as muddy wastage to thereby form a reductive atmosphere within the fluidized bed 5, while the temperature at the fluidized bed 5 is maintained to be not less than 500C to incinerate the wastage; nitrogen oxides produced are reduced by CO, H CH and the like which are thus produced; whereby nitrogen oxides may be removed from the waste combustion gas from the wastage in the form of nitrogen gas.
  • cement clinker particles containing a great amount of Fe O C50 MnO, A1 0 chrominum ore particles and manganese ore particles for the purpose of accelerating the aforesaid reductive reaction, thereby effectively reducing and removing nitrogen oxides.
  • the reactions which take place within the fluidized bed incineration furnace according to the present invention are summerized as follows: The following reactions take place for the combustible matter and the added carbon components, within the reductive fluidized bed which is maintained at a temperature of not less than 500C:
  • C H represents hydrocarbon groups contained in the combustible matters, part of which is subjected to dry destillation and decomposition within the fluidized bed under a reductive atmosphere to thereby produce methane (CH and the like.
  • a method for incinerating industrial wastage as de fined in claim I wherein the resultant combustion gases obtained from the prior steps are mixed with air and maintained at a temperature above the combustion temperature of the combustible gases and below l,000 C for completing the combustion of the combustible gases without producing nitrogen oxides from the nitrogen gas.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Regulation And Control Of Combustion (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Treatment Of Sludge (AREA)
  • Incineration Of Waste (AREA)
US44689574 1973-11-21 1974-02-28 Method for incinerating industrial wastage Expired - Lifetime US3888194A (en)

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JP13018773A JPS5227467B2 (it) 1973-11-21 1973-11-21

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Cited By (33)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3974783A (en) * 1975-08-22 1976-08-17 Nalco Chemical Company Method for improving sewage sludge incineration
FR2376364A1 (fr) * 1977-01-03 1978-07-28 Dorr Oliver Inc Procede d'incineration, a l'aide d'un combustible a forte teneur en soufre, d'une boue d'eau d'egout traitee par de la chaux
US4168670A (en) * 1977-01-03 1979-09-25 Dorr-Oliver Incorporated Incineration of lime-conditioned sewage sludge with high sulfur fuel
US4171945A (en) * 1976-08-26 1979-10-23 The British Petroleum Company Limited Fluidized bed
US4241672A (en) * 1978-12-04 1980-12-30 The United States Of America As Represented By The United States Department Of Energy Method of regulating the amount of underfire air for combustion of wood fuels in spreader-stroke boilers
US4308806A (en) * 1978-04-05 1982-01-05 Babcock-Hitachi Kabushiki Kaisha Incinerator for burning waste and a method of utilizing same
US4335683A (en) * 1981-04-09 1982-06-22 Foster Wheeler Energy Corporation Fluidized bed heat exchanger with control to respond to changes in demand
US4340433A (en) * 1976-09-16 1982-07-20 Can-Eng Holdings Limited Method of heat treating articles
US4343246A (en) * 1980-04-07 1982-08-10 Dorr-Oliver Incorporated Slurry coal feed system for fluidized bed reactor
US4409909A (en) * 1980-03-20 1983-10-18 Kabushiki Kaisha Okawara Seisakusho Process of combustion in a fluidized-bed incinerator
US4436037A (en) 1982-04-21 1984-03-13 General Motors Corporation Continuous ignition source for controlled disposal of combustible polymer waste in a fluidized bed reactor
US4708068A (en) * 1986-08-20 1987-11-24 Kabushiki Kaisha Komatsu Seisakusho Fluidized-bed incineration equipment for removing organic substances
US4961391A (en) * 1989-03-29 1990-10-09 International Technology Corporation Thermal treatment process for organically contaminated material
US5530176A (en) * 1994-12-01 1996-06-25 Pneu-Mech Systems Mfg., Inc. Method and apparatus for disposing of hazardous waste material in a cement-producing kiln
US6083296A (en) * 1995-04-07 2000-07-04 Technological Resources Pty. Limited Method of producing metals and metal alloys
US6143054A (en) * 1997-09-26 2000-11-07 Technological Resources Pty Ltd. Process of producing molten metals
US6270553B1 (en) 1996-12-18 2001-08-07 Technological Resources Pty. Ltd. Direct reduction of metal oxide agglomerates
US6289034B1 (en) 1998-08-28 2001-09-11 Technologies Resources Pty. Ltd. Process and an apparatus for producing metals and metal alloys
US6322745B1 (en) 1998-07-01 2001-11-27 Technological Resources Pty. Ltd. Direct smelting vessel and direct smelting process
US6328783B1 (en) 1996-12-18 2001-12-11 Technological Resources Pty Ltd Producing iron from solid iron carbide
US6379424B1 (en) 1999-10-26 2002-04-30 Technological Resources Pty. Ltd. Direct smelting apparatus and process
US6379422B1 (en) 1999-08-05 2002-04-30 Technological Resources Pty. Ltd. Direct smelting process
US6387153B1 (en) 1999-10-15 2002-05-14 Technological Resources Pty Ltd Stable idle procedure
US6402808B1 (en) 1998-07-24 2002-06-11 Technological Resources Pty. Ltd. Direct smelting process
US6423114B1 (en) 1999-08-10 2002-07-23 Technological Resources Pty. Ltd. Pressure control
US6423115B1 (en) 1999-01-08 2002-07-23 Technological Resources Pty Ltd Direct smelting process
US6428603B1 (en) 1999-09-27 2002-08-06 Technological Resources Pty., Ltd. Direct smelting process
US6440195B1 (en) 1998-10-14 2002-08-27 Technological Resources Pty. Ltd. Process and an apparatus for producing metals and metal alloys
US6475264B1 (en) 1998-07-24 2002-11-05 Technological Resources Pty Ltd Direct smelting process
US6478848B1 (en) 1998-09-04 2002-11-12 Technological Resources Pty Ltd Direct smelting process
US6517605B1 (en) 1999-07-09 2003-02-11 Technological Resources Pty. Ltd. Start-up procedure for direct smelting process
US6585929B1 (en) 1999-06-08 2003-07-01 Technological Resources Pty Ltd Direct smelting vessel
US6602321B2 (en) 2000-09-26 2003-08-05 Technological Resources Pty. Ltd. Direct smelting process

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS52128879A (en) * 1976-04-23 1977-10-28 Daiichi Nenryo Kogyo Method of nonnpolluting sludge containing chromium
JPS5334374A (en) * 1976-09-10 1978-03-30 Babcock Hitachi Kk Method and device for burning shells
JPS5389281A (en) * 1977-01-14 1978-08-05 Ishigaki Mech Ind Control of nox emission in fluidized bed incinerator
JPS5389280A (en) * 1977-01-14 1978-08-05 Ishigaki Mech Ind Removal of nitrogen oxides in fluidized bed incinerator
SE7712262L (sv) * 1977-06-20 1978-12-21 Energy Products Of Idaho Anordning for forbrenning, pyrolys eller forgasning av avfall
JPS5832285B2 (ja) * 1977-11-25 1983-07-12 三井造船株式会社 含窒素可燃物の流動燃焼法
JPS57101215A (en) * 1980-12-15 1982-06-23 Okawara Mfg Co Ltd Low nox combustion in fluidized bed type incinerator
JPS56133521A (en) * 1980-03-20 1981-10-19 Okawara Mfg Co Ltd Adjusting method for combustion air in fluidizing bed incinerator
JPS60251309A (ja) * 1984-05-25 1985-12-12 Kunio Watabe 流動層焼却炉の操業方法
JP6063307B2 (ja) * 2013-03-12 2017-01-18 メタウォーター株式会社 汚泥燃焼装置及び汚泥燃焼方法

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US2729428A (en) * 1953-04-20 1956-01-03 Shell Dev Fluidized bed temperature conditioner and method of controlling temperatures of fluid streams
US3306236A (en) * 1964-09-11 1967-02-28 Exxon Research Engineering Co Burner for waste materials and method of burning waste materials
US3515381A (en) * 1965-06-16 1970-06-02 Charbonnages De France Method of heat treatment of sludges
US3589313A (en) * 1968-08-30 1971-06-29 Us Health Education & Welfare Solid waste disposal method and apparatus
US3772998A (en) * 1970-07-29 1973-11-20 Mettalges Ag Method of and apparatus for the combustion of sludge
US3776150A (en) * 1972-03-06 1973-12-04 Awt Systems Inc Fluidized bed system for solid wastes

Patent Citations (6)

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US2729428A (en) * 1953-04-20 1956-01-03 Shell Dev Fluidized bed temperature conditioner and method of controlling temperatures of fluid streams
US3306236A (en) * 1964-09-11 1967-02-28 Exxon Research Engineering Co Burner for waste materials and method of burning waste materials
US3515381A (en) * 1965-06-16 1970-06-02 Charbonnages De France Method of heat treatment of sludges
US3589313A (en) * 1968-08-30 1971-06-29 Us Health Education & Welfare Solid waste disposal method and apparatus
US3772998A (en) * 1970-07-29 1973-11-20 Mettalges Ag Method of and apparatus for the combustion of sludge
US3776150A (en) * 1972-03-06 1973-12-04 Awt Systems Inc Fluidized bed system for solid wastes

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3974783A (en) * 1975-08-22 1976-08-17 Nalco Chemical Company Method for improving sewage sludge incineration
US4171945A (en) * 1976-08-26 1979-10-23 The British Petroleum Company Limited Fluidized bed
US4340433A (en) * 1976-09-16 1982-07-20 Can-Eng Holdings Limited Method of heat treating articles
FR2376364A1 (fr) * 1977-01-03 1978-07-28 Dorr Oliver Inc Procede d'incineration, a l'aide d'un combustible a forte teneur en soufre, d'une boue d'eau d'egout traitee par de la chaux
US4168670A (en) * 1977-01-03 1979-09-25 Dorr-Oliver Incorporated Incineration of lime-conditioned sewage sludge with high sulfur fuel
US4308806A (en) * 1978-04-05 1982-01-05 Babcock-Hitachi Kabushiki Kaisha Incinerator for burning waste and a method of utilizing same
US4241672A (en) * 1978-12-04 1980-12-30 The United States Of America As Represented By The United States Department Of Energy Method of regulating the amount of underfire air for combustion of wood fuels in spreader-stroke boilers
US4409909A (en) * 1980-03-20 1983-10-18 Kabushiki Kaisha Okawara Seisakusho Process of combustion in a fluidized-bed incinerator
US4343246A (en) * 1980-04-07 1982-08-10 Dorr-Oliver Incorporated Slurry coal feed system for fluidized bed reactor
US4335683A (en) * 1981-04-09 1982-06-22 Foster Wheeler Energy Corporation Fluidized bed heat exchanger with control to respond to changes in demand
US4436037A (en) 1982-04-21 1984-03-13 General Motors Corporation Continuous ignition source for controlled disposal of combustible polymer waste in a fluidized bed reactor
US4708068A (en) * 1986-08-20 1987-11-24 Kabushiki Kaisha Komatsu Seisakusho Fluidized-bed incineration equipment for removing organic substances
US4961391A (en) * 1989-03-29 1990-10-09 International Technology Corporation Thermal treatment process for organically contaminated material
US5530176A (en) * 1994-12-01 1996-06-25 Pneu-Mech Systems Mfg., Inc. Method and apparatus for disposing of hazardous waste material in a cement-producing kiln
US6267799B1 (en) 1995-04-07 2001-07-31 Technological Resources Pty. Ltd. Method of producing metals and metal alloys
US6083296A (en) * 1995-04-07 2000-07-04 Technological Resources Pty. Limited Method of producing metals and metal alloys
US6270553B1 (en) 1996-12-18 2001-08-07 Technological Resources Pty. Ltd. Direct reduction of metal oxide agglomerates
US6328783B1 (en) 1996-12-18 2001-12-11 Technological Resources Pty Ltd Producing iron from solid iron carbide
US6143054A (en) * 1997-09-26 2000-11-07 Technological Resources Pty Ltd. Process of producing molten metals
US6322745B1 (en) 1998-07-01 2001-11-27 Technological Resources Pty. Ltd. Direct smelting vessel and direct smelting process
US6402808B1 (en) 1998-07-24 2002-06-11 Technological Resources Pty. Ltd. Direct smelting process
US6475264B1 (en) 1998-07-24 2002-11-05 Technological Resources Pty Ltd Direct smelting process
US6289034B1 (en) 1998-08-28 2001-09-11 Technologies Resources Pty. Ltd. Process and an apparatus for producing metals and metal alloys
US6478848B1 (en) 1998-09-04 2002-11-12 Technological Resources Pty Ltd Direct smelting process
US6440195B1 (en) 1998-10-14 2002-08-27 Technological Resources Pty. Ltd. Process and an apparatus for producing metals and metal alloys
US6423115B1 (en) 1999-01-08 2002-07-23 Technological Resources Pty Ltd Direct smelting process
US6585929B1 (en) 1999-06-08 2003-07-01 Technological Resources Pty Ltd Direct smelting vessel
US6517605B1 (en) 1999-07-09 2003-02-11 Technological Resources Pty. Ltd. Start-up procedure for direct smelting process
US6379422B1 (en) 1999-08-05 2002-04-30 Technological Resources Pty. Ltd. Direct smelting process
US6423114B1 (en) 1999-08-10 2002-07-23 Technological Resources Pty. Ltd. Pressure control
US6428603B1 (en) 1999-09-27 2002-08-06 Technological Resources Pty., Ltd. Direct smelting process
US6387153B1 (en) 1999-10-15 2002-05-14 Technological Resources Pty Ltd Stable idle procedure
US6379424B1 (en) 1999-10-26 2002-04-30 Technological Resources Pty. Ltd. Direct smelting apparatus and process
US6602321B2 (en) 2000-09-26 2003-08-05 Technological Resources Pty. Ltd. Direct smelting process

Also Published As

Publication number Publication date
JPS5227467B2 (it) 1977-07-20
DE2410477A1 (de) 1975-05-22
JPS5080674A (it) 1975-06-30
DE2410477B2 (de) 1977-03-24

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