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WO2006048283A1 - Procede et installation pour produire du laitier d'oxyde de titane a partir d'ilmenite - Google Patents

Procede et installation pour produire du laitier d'oxyde de titane a partir d'ilmenite Download PDF

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Publication number
WO2006048283A1
WO2006048283A1 PCT/EP2005/011761 EP2005011761W WO2006048283A1 WO 2006048283 A1 WO2006048283 A1 WO 2006048283A1 EP 2005011761 W EP2005011761 W EP 2005011761W WO 2006048283 A1 WO2006048283 A1 WO 2006048283A1
Authority
WO
WIPO (PCT)
Prior art keywords
ilmenite
reactor
gas
electric furnace
reduction
Prior art date
Application number
PCT/EP2005/011761
Other languages
English (en)
Inventor
Petri Jokinen
Ali-Naghi Beyzavi
Lothar Formanek
Original Assignee
Outotec Oyj
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 Outotec Oyj filed Critical Outotec Oyj
Priority to CA2583359A priority Critical patent/CA2583359C/fr
Priority to AU2005300680A priority patent/AU2005300680B2/en
Publication of WO2006048283A1 publication Critical patent/WO2006048283A1/fr
Priority to NO20072742A priority patent/NO343430B1/no

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B4/00—Electrothermal treatment of ores or metallurgical products for obtaining metals or alloys
    • C22B4/08—Apparatus
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1204—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 preliminary treatment of ores or scrap to eliminate non- titanium constituents, e.g. iron, without attacking the titanium constituent
    • C22B34/1209—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 preliminary treatment of ores or scrap to eliminate non- titanium constituents, e.g. iron, without attacking the titanium constituent by dry processes, e.g. with selective chlorination of iron or with formation of a titanium bearing slag
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/10—Dry methods smelting of sulfides or formation of mattes by solid carbonaceous reducing agents
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
    • C22B5/14—Dry methods smelting of sulfides or formation of mattes by gases fluidised material
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/18—Reducing step-by-step

Definitions

  • the present invention relates to a process for producing titania slag from ilmenite, and to a corresponding plant.
  • Ilmenite which beside titanium dioxide contains large amounts of iron oxides (X-TiO 2 + y-FeO + Z-Fe 2 O 3 ), is one of the most important starting materials, apart from rutile, for recovering metallic titanium and titanium compounds, such as tita ⁇ nium dioxide used for pigment production. Separating the iron from the ore usually is effected by electric melting of ilmenite in a metallurgical furnace, the iron oxides being reduced to metallic iron, which is precipitated from the slag containing tita ⁇ nium dioxide.
  • a disadvantage of this process is the very high demand for electric energy, which is about 2,200 kWh per ton of titania slag and represents the main part of the production costs.
  • the demand for energy for producing titania slag from ilmenite can be reduced by 40 to 50% as compared with the processes known so far, when the ilmenite is prereduced prior to electric melting and is introduced into the electric furnace in the hot condition, i.e. without cooling or upon being cooled only little after the partial reduction.
  • Another advantage of this procedure consists in the increase of the magnetic susceptibility of the ilmenite with respect to the impurities, such as chromium, contained in the starting ore, so that in the case of a magnetic separa ⁇ tion a reliable separation between fractions containing titanium dioxide and frac ⁇ tions free from titanium can be achieved.
  • the partial reduction a) can be effected in any apparatus known to those skilled in the art for this purpose, for instance in a rotary kiln. Particularly good results are obtained, however, when the partial reduction a) of the ilmenite is performed in a fluidized bed, preferably in a circulating fluidized bed, namely either in a one-stage or multi-stage operation. Due to the high mass and heat transfer in fluidized beds, a uniform reduction of the material used is thereby achieved with a minimum expenditure of energy.
  • the grain size of the granular ilmenite used is less than 1 mm and particularly preferably less than 400 ⁇ m.
  • reducing agent for the partial reduction a) of the ilmenite all substances known to those skilled in the art for this purpose can be used in principle, and in particular coal, char, molecular hydrogen, gas mixtures containing molecular hydrogen, carbon monoxide and gas mixtures containing carbon monoxide, for instance reformed gas, turned out to be useful.
  • reducing agent there is preferably used a gas mixture containing carbon monoxide and molecular hydrogen, particularly preferably a gas mixture of 60 to 80 vol-% carbon monoxide and 40 to 20 vol-% molecular hydrogen, and quite particularly preferably a gas mixture of 70 vol-% carbon monoxide and 30 vol-% hydrogen in combination with char.
  • the partial reduction is performed in a circulating fluidized bed, this can for instance easily be realized in that ilmenite to be partially reduced and char are continuously supplied to the fluidized-bed reactor via a solids supply conduit, and the solids in the reactor are fluidized by a gas mixture containing carbon monoxide and molecular hydro ⁇ gen.
  • the process conditions preferably are adjusted such that the degree of metallization of the product obtained by this process step is 50 to 95% and particularly preferably 70 to 80%, based on its iron content.
  • the produc ⁇ tion of the char used as reducing agent is effected in one process step with the heating of the ilmenite in a stationary fluidized-bed reactor.
  • the preheated ilmenite together with coal preferably coal with a grain size of less than 5 mm, and molecular oxygen or a gas mixture containing molecular oxygen, is introduced into a fluidized-bed reactor and heated there to a temperature of pref ⁇ erably more than 900 0 C and particularly preferably more than 1 ,000 0 C.
  • the fluidization of the solids preferably is effected by means of the gas mixture used as reducing agent in the succeeding step of partial reduction, the degree of carbonization being adjustable by adjusting the retention time to a suit ⁇ able value.
  • the off gas from the reduction reactor is passed through the heat exchanger(s) used for preheating the ilmenite, subsequently the off gas possibly is passed through a waste heat boiler by generating steam, in which steam is generated, before dust is removed from the cooled waste gas and the same possibly is further cooled, in a CO 2 absorber possibly is separated from the carbon dioxide obtained during the partial reduction of ilmenite, is heated in a succeeding gas heater and finally again supplied to the reduction reactor and possibly the carbonization reactor as fluidizing gas.
  • the crude ilmenite used has a comparatively high content of FeO, it was found to be expedient to subject the same to an oxidative pretreatment prior to the partial reduction a), in order to rather completely oxidize the FeO to obtain F ⁇ 2 ⁇ 3 .
  • This is advantageous because FeO is present in a crystal lattice structure, which largely resists the attack of reducing gases, whereas the lattice structure of Fe 2 O 3 result ⁇ ing from the oxidation of FeO allows an efficient diffusion of gas into the pores of the material.
  • the oxidation is performed such that the FeO content of the treated material after the oxidation is less than 5 wt-%, and particularly pref- erably less than 3 wt-%.
  • the temperature of the partially reduced material used during the magnetic separation preferably is at least 600 0 C, particularly preferably at least 675°C, and quite particularly preferably about 700 0 C.
  • the magnetic fraction subsequently is trans ⁇ ferred into the electric furnace without cooling or heating.
  • the energy required for cooling the partially reduced material after the partial reduction on the one hand and the energy required for heating the material supplied to the electric furnace to the operating temperatures in the furnace on the other hand thus is minimized without a substantial reoxidation of the partially reduced material taking place before entrance into the electric furnace.
  • the non magnetic fraction can be further processed and the char in this non magnetic fraction can be reused in the process, e.g. as a feed material.
  • the titania slag withdrawn from the electric furnace contains 75 to 90 wt-% and particularly preferably about 85 wt-% titanium dioxide, and the liquid pig iron contains more than 94 wt-% metallic iron.
  • a plant in accordance with the invention which can be used in particular for per ⁇ forming the process described above, comprises a carbonization reactor constitut ⁇ ing a stationary fluidized-bed reactor for carbonizing coal by heating ilmenite at the same time, a reduction reactor constituting a circulating fluidized-bed reactor for the partial reduction of ilmenite, and an electric furnace.
  • the carbonization reactor is connected with the reduction reactor via a connecting passage such that the solids/gas suspension can pass from the upper part of the carbonization reactor into the lower part of the reduction reactor, and downstream of the reduction reactor a cyclone is provided for separating the solids from the solids/gas suspension, a solids return conduit extending from the cyclone to the carbonization reactor.
  • At least one preheating stage including a solids/gas suspension heat exchanger and a downstream cyclone upstream of the carbonization reactor, in which the ilmenite is preheated to temperatures of 500 to 900 0 C, particularly preferably 600 to 850 0 C and quite particularly preferably about 800 0 C, before being charged into the car ⁇ bonization reactor.
  • a means for circulating the fluidizing gas in the plant in accordance with an embodiment of the invention.
  • the plant in addition comprises a magnetic separator.
  • Fig. 1 shows a process diagram of a process and a plant in accordance with a first embodiment of the present invention
  • Fig. 2 shows a process diagram of a process and a plant in accordance with a second embodiment of the present invention.
  • a mixture of char and ilmenite which previously were withdrawn from the bins 2, 3 and were mixed with each other in the mixing tank 4, is continuously charged via the solids supply conduit 1 into the suspension heat exchanger 5 of a first preheating stage, in which the material preferably is suspended and preheated by the off gas with ⁇ drawn from a second preheating stage. Subsequently, the suspension is con ⁇ ducted by the gas stream into a cyclone 6, in which the solids are separated from the gas.
  • the separated solids then are delivered through conduit 7 into a second Venturi-type suspension heat exchanger 8, where they are further preheated to a temperature of about 800 0 C, and in a downstream cyclone 9 are again separated from the gas stream.
  • the ore thus preheated is delivered through the solids conduit T into the carboni ⁇ zation reactor 10, to which coal with a grain size of less than 5 mm as well as oxygen are supplied via the solids conduit 7".
  • a fluidizing gas con ⁇ sisting of 70 vol-% carbon monoxide and 30 vol-% molecular hydrogen with a temperature of about 600 0 C is supplied to the carbonization reactor 10 via the gas conduit 11 for fluidizing the solids in the reactor 10 by forming a stationary fluidized bed.
  • the oxygen and fluidizing gas supply rate as well as the retention time of the solids in the carbonization reactor 10 are adjusted such that a temperature of about 1 ,050 0 C is obtained in the fluidized bed and a sufficient carbonization of the coal is achieved.
  • the coal supplied in conduit 7" can be externally predried and/or precarbonized before entering the reactor 10.
  • the gas-solids mixture is continuously passed from the carbonization reactor 10 via the connecting passage 12 into the reduction reactor 13, in which the solids are fluidized by the fluidizing gas supplied via the gas conduit 11' by forming a circulating fluidized bed, and the ilmenite is reduced by the reducing agents, in particular by carbon monoxide, to a degree of metallization of about 70%, based on its iron content.
  • the suspension is conducted by the gas stream into the cyclone 14 downstream of the reduction reactor 13, in which cyclone the solids are separated from the gas.
  • the separated solids are recirculated through the return conduit 15 into the carbonization reactor 10, whereas the off gas containing CO 1 H 2 and CO 2 with a temperature of about 1 ,000 0 C is transferred via the gas conduit 16 first into the suspension heat exchanger 8 of the second preheating stage and from there via the cyclone 9 and the gas conduit 16' into the suspension heat exchanger 5 of the first preheating stage, in which the same is cooled to about 500 0 C.
  • the off gas separated in the cyclone 6 downstream of the suspension heat exchanger 5 is first conducted through a waste heat boiler (not shown), in which the off gas is cooled to approximately 200 0 C by generating steam (4 bar), before it is separated from dust in a scrubber 17 and cooled further to about 30 0 C.
  • the solid/sludge outlet of the scrubber (fines of ore and carbon) can be further used in the process, e.g. after pelletizing as feed material to mixing tank 4 and/or to the reactor 10 and/or 13 and/or furnace 22.
  • carbon dioxide is removed from the off gas in the CO2 absorber 18, and the gas mixture thus purified can be preheated in a heat exchanger, e.g.
  • the value of hydrogen and/or water and/or water vapour in the circulating gas flow may be controlled e.g. by a hydrogen permeable membrane or a water condenser/absorber or water evaporator.
  • a mixture of partially reduced ilmenite and char with a temperature of about 1 ,000 0 C is continuously withdrawn via the pneumatic product discharge conduit 20, is cooled to about 700 0 C in a heat exchanger (not shown), and with this temperature is charged to the magnetic separator 21 , where a fraction rich in titanium dioxide is separated as magnetic product from a non- magnetic fraction, which substantially comprises chromite, ash and char, before the magnetic fraction is charged into the electric furnace 22.
  • titania slag with 75 to 90 wt-% titanium dioxide and liquid pig iron with more than 94 wt-% metallic iron are ob- tained as products.
  • the off gas from the electric furnace contains more than 90 vol-% carbon monoxide and, after dedusting, is burnt in an afterburning chamber (not shown), and the hot flue gas is supplied to the gas heater 19 for heating the fluidizing gas. Also a part of the circulation gas flow can be burnt and supplied to the gas heater 19.
  • the plant shown in Fig. 2 additionally includes an oxidation reactor 23 upstream of the carbonization reactor 10.
  • Ore preheated in the suspension heat exchangers 5, 8 is introduced into the oxidation reactor 23 via the solids conduit T and is fluidized with fluidizing gas supplied via the gas conduit 11", which before was preheated in the heat exchanger 24 with the waste gas from the cyclone 14 downstream of the reduction reactor 13, by forming a circulating fluidized bed.
  • fuel is supplied to the oxidation reactor 23 via conduit 16'".
  • the suspension is conducted by the gas stream into the cyclone 25 downstream of the oxidation reactor 23, in which the solids are separated from the gas.
  • One part of the solids is recirculated to the oxidation reactor 23, while the other part is introduced into the carbonization reactor 10 via the solids conduit 7'".
  • Off gas withdrawn from the cyclone 25 is transferred via the gas conduit 26 into the suspension heat exchanger of the second preheating stage 8 and from there via the cyclone 9, the suspension heat exchanger of the first preheating stage 5 and the cyclone 6 to a waste gas cleaning unit (not shown).
  • the suspension heat exchanger 5 was charged via the solids supply conduit 1 with raw ilmenite (12 kg/h) having a grain size of less than 1 mm with the following composition:
  • F ⁇ total 34.90 wt-% After passage through the first and second preheating stages, the preheated ore was introduced into the oxidation reactor 23 via conduit 7', in order to almost com ⁇ pletely oxidize the FeO to form F ⁇ 2 ⁇ 3 . Furthermore, fuel and fluidizing gas were supplied to the oxidation reactor 23 via conduit 11". After separating the solids from the gas in the cyclone 25 downstream of the oxidation reactor 23, the solids were introduced into the carbonization reactor 10 via the solids conduit 7'". The oxygen content of the waste gas from the cyclone 25 was 6 vol-%.
  • Solids withdrawn from the reduction reactor 13 via conduit 20 were first of all separated magnetically in the magnetic separator 21 , and the magnetic fraction obtained thereby was charged into an electric furnace 22.
  • the installed trans ⁇ former capacity of the furnace 22 was 2 MVA.
  • the titania slag was tapped every 2 hours, and the sponge iron was tapped twice per day.
  • the titania slag and the sponge iron thus obtained had the compositions as shown in Table 1.
  • the calculated electric energy consumption for the process was 1.004 kWh per ton of slag. Comparative Example
  • compositions of the titania slag and the sponge iron thus obtained are set forth in Table 1.
  • the calculated electric energy consumption for the process was 2,050 kWh per ton of slag.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Furnace Details (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)

Abstract

Dans le cadre d'un procédé pour produire du laitier d'oxyde de titane à partir d'ilménite, de l'ilménite granulaire est tout d'abord réduit partiellement au moyen d'un agent réducteur dans un réacteur de réduction, puis la matière chaude à une température d'entrée d'au moins 550 °C, est transférée dans un four électrique dans lequel elle est fondue en la présence d'un agent réducteur par formation de fonte brute liquide et de laitier d'oxyde de titane. Le réacteur de réduction est un réacteur à lit fluidisé mobile.
PCT/EP2005/011761 2004-11-03 2005-11-03 Procede et installation pour produire du laitier d'oxyde de titane a partir d'ilmenite WO2006048283A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CA2583359A CA2583359C (fr) 2004-11-03 2005-11-03 Procede et installation pour produire du laitier d'oxyde de titane a partir d'ilmenite
AU2005300680A AU2005300680B2 (en) 2004-11-03 2005-11-03 Process and plant for producing titania slag from ilmenite
NO20072742A NO343430B1 (no) 2004-11-03 2007-05-30 Fremgangsmåte og anlegg for fremstilling av titaniaslagg fra ilmenitt

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE200410053676 DE102004053676B4 (de) 2004-11-03 2004-11-03 Verfahren und Anlage zur Herstellung von Titanschlacke aus Ilmenit
DE102004053676.7 2004-11-03

Publications (1)

Publication Number Publication Date
WO2006048283A1 true WO2006048283A1 (fr) 2006-05-11

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2005/011761 WO2006048283A1 (fr) 2004-11-03 2005-11-03 Procede et installation pour produire du laitier d'oxyde de titane a partir d'ilmenite

Country Status (8)

Country Link
CN (1) CN100540698C (fr)
AU (1) AU2005300680B2 (fr)
CA (1) CA2583359C (fr)
DE (1) DE102004053676B4 (fr)
NO (1) NO343430B1 (fr)
UA (1) UA92729C2 (fr)
WO (1) WO2006048283A1 (fr)
ZA (1) ZA200704343B (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009006958A1 (fr) 2007-07-09 2009-01-15 Outotec Oyj Réacteur à lit fluidisé pour le traitement de substances fluidisables et procédé correspondant
WO2014146682A1 (fr) 2013-03-18 2014-09-25 Outotec (Finland) Oy Procédé et installation pour produire du laitier de titane à partir d'ilménite
US8926728B2 (en) 2010-06-04 2015-01-06 Outotec Oyj Process and plant for producing hot metal
WO2016120529A1 (fr) 2015-01-30 2016-08-04 Outotec (Finland) Oy Procédé de production de laitier contenant de l'oxyde de titane et de la fonte brute en provenance d'ilménite et installation
WO2020151034A1 (fr) * 2019-01-24 2020-07-30 东北大学 Procédé pour la séparation et l'enrichissement de constituants de valeur à partir de minerai de fer contenant du titane

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009038052B4 (de) * 2009-08-19 2012-09-27 Wolfgang Krumm Verhüttungsverfahren durch Einsatz eines vorreduzierten Ilmeniterzstromes und/oder Hämatiterzstromes
CN102399998B (zh) * 2011-11-18 2014-03-26 攀钢集团攀枝花钢铁研究院有限公司 一种利用钒钛铁精矿融态还原冶炼酸溶性钛渣的方法
CN103421925B (zh) * 2013-08-26 2015-04-22 江苏大学 一种制备氯化钛渣的方法
EP3106531A1 (fr) * 2015-06-15 2016-12-21 Improbed AB Utilisation d'ilménite pré-oxydée dans des chaudières à lit fluidisé

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US3713781A (en) * 1970-10-21 1973-01-30 W Dunn Cross-flow fluid bed reactor
US3765868A (en) * 1971-07-07 1973-10-16 Nl Industries Inc Method for the selective recovery of metallic iron and titanium oxide values from ilmenites
JPS5031526B1 (fr) * 1969-05-12 1975-10-13
US4359212A (en) * 1979-05-29 1982-11-16 Stora Kopparbergs Bergslags Ab Apparatus for reducing finely divided iron oxide material
DE10260737A1 (de) * 2002-12-23 2004-07-15 Outokumpu Oyj Verfahren und Anlage zur Wärmebehandlung von titanhaltigen Feststoffen

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DE810156C (de) * 1946-11-18 1951-08-06 Titan Co As Verfahren zur Gewinnung von Eisen und titanhaltiger Schlacke aus titanhaltigen Eisenerzen
DE2234843A1 (de) * 1972-07-15 1974-01-31 Bayer Ag Verfahren zur herstellung von titandioxidkonzentraten
DE10260767A1 (de) * 2002-12-23 2004-07-01 Koenig & Bauer Ag Einrichtung zur Formatverstellung an bogenführenden Trommeln von Bogendruckmaschinen
CN1233560C (zh) * 2003-02-21 2005-12-28 中南大学 制备金红石型二氧化钛的方法

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JPS5031526B1 (fr) * 1969-05-12 1975-10-13
US3713781A (en) * 1970-10-21 1973-01-30 W Dunn Cross-flow fluid bed reactor
US3765868A (en) * 1971-07-07 1973-10-16 Nl Industries Inc Method for the selective recovery of metallic iron and titanium oxide values from ilmenites
US4359212A (en) * 1979-05-29 1982-11-16 Stora Kopparbergs Bergslags Ab Apparatus for reducing finely divided iron oxide material
DE10260737A1 (de) * 2002-12-23 2004-07-15 Outokumpu Oyj Verfahren und Anlage zur Wärmebehandlung von titanhaltigen Feststoffen

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DATABASE WPI Section Ch Week 197545, Derwent World Patents Index; Class M24, AN 1975-74991W, XP002364193 *
VIJAY P L ET AL: "PREOXIDATION AND HYDROGEN REDUCTION OF ILMENITE IN A FLUIDIZED BED REACTOR", METALLURGICAL AND MATERIALS TRANSACTIONS B: PROCESS METALLURGY & MATERIALS PROCESSING SCIENCE, TMS, WARRENDALE, PA, US, vol. 27B, no. 5, October 1996 (1996-10-01), pages 731 - 738, XP000632260, ISSN: 1073-5623 *

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009006958A1 (fr) 2007-07-09 2009-01-15 Outotec Oyj Réacteur à lit fluidisé pour le traitement de substances fluidisables et procédé correspondant
EA015592B1 (ru) * 2007-07-09 2011-10-31 Оутотек Ойй Реактор с псевдоожиженным слоем для обработки псевдоожижаемых материалов и способ обработки псевдоожижаемых материалов в этом реакторе
AU2008274669B2 (en) * 2007-07-09 2012-08-23 Metso Metals Oy Fluidized-bed reactor for the treatment of fluidizable substances and process herefor
US8926728B2 (en) 2010-06-04 2015-01-06 Outotec Oyj Process and plant for producing hot metal
WO2014146682A1 (fr) 2013-03-18 2014-09-25 Outotec (Finland) Oy Procédé et installation pour produire du laitier de titane à partir d'ilménite
AU2013383015B2 (en) * 2013-03-18 2016-09-08 Outotec (Finland) Oy Process and plant for producing titanium slag from ilmenite
WO2016120529A1 (fr) 2015-01-30 2016-08-04 Outotec (Finland) Oy Procédé de production de laitier contenant de l'oxyde de titane et de la fonte brute en provenance d'ilménite et installation
WO2020151034A1 (fr) * 2019-01-24 2020-07-30 东北大学 Procédé pour la séparation et l'enrichissement de constituants de valeur à partir de minerai de fer contenant du titane

Also Published As

Publication number Publication date
UA92729C2 (uk) 2010-12-10
AU2005300680A1 (en) 2006-05-11
CA2583359A1 (fr) 2006-05-11
ZA200704343B (en) 2008-08-27
DE102004053676B4 (de) 2010-02-25
CN100540698C (zh) 2009-09-16
AU2005300680B2 (en) 2010-02-25
CA2583359C (fr) 2013-10-08
NO20072742L (no) 2007-07-19
DE102004053676A1 (de) 2006-05-04
CN101052732A (zh) 2007-10-10
NO343430B1 (no) 2019-03-04

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