EP0717783A1 - Ennoblissement de materiaux titaniferes - Google Patents

Ennoblissement de materiaux titaniferes

Info

Publication number
EP0717783A1
EP0717783A1 EP94926722A EP94926722A EP0717783A1 EP 0717783 A1 EP0717783 A1 EP 0717783A1 EP 94926722 A EP94926722 A EP 94926722A EP 94926722 A EP94926722 A EP 94926722A EP 0717783 A1 EP0717783 A1 EP 0717783A1
Authority
EP
European Patent Office
Prior art keywords
leach
caustic
leaching
caustic leach
titaniferous
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP94926722A
Other languages
German (de)
English (en)
Other versions
EP0717783A4 (fr
Inventor
Ross Alexander Mcclelland
Michael John Hollitt
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Technological Resources Pty Ltd
Original Assignee
Technological Resources Pty 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 Technological Resources Pty Ltd filed Critical Technological Resources Pty Ltd
Publication of EP0717783A1 publication Critical patent/EP0717783A1/fr
Publication of EP0717783A4 publication Critical patent/EP0717783A4/fr
Withdrawn legal-status Critical Current

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
    • 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
    • C22B34/1236—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 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching
    • C22B34/1254—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 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching using basic solutions or liquors
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • 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
    • C22B34/1236—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 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching
    • C22B34/124—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 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching using acidic solutions or liquors
    • C22B34/125—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 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching using acidic solutions or liquors containing a sulfur ion as active agent
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • This invention relates to the removal of impurities from naturally occurring and synthetic titaniferous materials.
  • the invention is particularly suited to the enhancement of titaniferous materials used in the production of titanium metal and titanium dioxide pigments by means of industrial chlorination systems.
  • Embodiments of the present invention have the common features of the use of caustic leaching and pressure sulphuric acid leaching for the upgrading of titaniferous materials, e.g. titaniferous slags, derived from hard rock ilmenites. Additional steps may be employed as will be described below.
  • titanium dioxide bearing feedstocks are fed with coke to chlorinators of various designs (fluidised bed, shaft, molten salt), operated to a maximum temperature in the range 700 - 1200°C.
  • chlorinators of various designs (fluidised bed, shaft, molten salt), operated to a maximum temperature in the range 700 - 1200°C.
  • the most common type of industrial chlorinator is of the fluidised bed design.
  • Gaseous chlorine is passed through the titania and carbon bearing charge, converting titanium dioxide to titanium tetrachloride gas, which is then removed in the exit gas stream and condensed to liquid titanium tetrachloride for further purification and processing.
  • the chlorination process as conducted in industrial chlorinators is well suited to the conversion of pure titanium dioxide feedstocks to titanium tetrachloride.
  • most other inputs i.e. impurities in feedstocks
  • the attached table provides an indication of the types of problems encountered.
  • each unit of inputs which does not enter products contributes substantially to the generation of wastes for treatment and disposal.
  • Some inputs e.g. particular metals, radioactives
  • Preferred inputs to chlorination are therefore high grade materials, with the mineral rutile (at 95-96% Ti0 2 ) the most suitable of present feeds. Shortages of rutile have led to the development of other feedstocks formed by upgrading naturally occurring ilmenite (at 40-60% Ti0 2 ), such as titaniferous slag (approximately 86% Ti0 2 ) and synthetic rutile (variously 92-95% Ti0 2 ) . These upgrading processes have had iron removal as a primary focus, but have extended to removal of magnesium, manganese and alkali earth impurities, as well as some aluminium.
  • Si Accumulates Can May require i ne ncourage distillat ion chlorinator, d u c t from product r e d u c i n gb lockage . c a m p a i g n Condenses in life. part with
  • titaniferous minerals e.g. ilmenite
  • the titaniferous mineral is reduced with coal or char in a rotary kiln, at temperatures in excess of 1100°C.
  • the iron content of the mineral is substantially metallised.
  • Sulphur additions are also made to convert manganese impurities partially to sulphides.
  • the metallised product is cooled, separated from associated char, and then subjected to aqueous aeration for removal of virtually all contained metallic iron as a separable fine iron oxide.
  • the titaniferous product of separation is treated with 2-5% aqueous sulphuric acid for dissolution of manganese and some residual iron.
  • aqueous sulphuric acid for dissolution of manganese and some residual iron.
  • Recent disclosures have provided a process which operates reduction at lower temperatures and provides for hydrochloric acid leaching after the aqueous aeration and iron oxide separation steps. According to these disclosures the process is effective in removing iron, manganese, alkali and alkaline earth impurities, a substantial proportion of aluminium inputs and some vanadium as well as thorium.
  • the process may be operated as a retrofit on existing kiln based installations. However, the process is ineffective in full vanadium removal and has little chemical impact on silicon.
  • ilmenite is first thermally reduced to substantially complete reduction of its ferric oxide content (i.e. without substantial metallisation), normally in a rotary kiln.
  • the cooled, reduced product is then leached under 35 psi pressure at 140-150°C with excess 20% hydrochloric acid for removal of iron, magnesium, aluminium and manganese.
  • the leach liquors are spray roasted for regeneration of hydrogen chloride, which is recirculated to the leaching step.
  • the ilmenite undergoes grain refinement by thermal oxidation followed by thermal reduction (either in a fluidised bed or a rotary kiln) .
  • the cooled, reduced product is then subjected to atmospheric leaching with excess 20% hydrochloric acid, for removal of the deleterious impurities. Acid regeneration is also performed by spray roasting in this process.
  • ilmenite is thermally reduced (without metallisation) with carbon in a rotary kiln, followed by cooling in a non-oxidising atmosphere.
  • the cooled, reduced product is leached under 20 - 30 psi gauge pressure at 130°C with 10 - 60% (typically 18 - 25%) sulphuric acid, in the presence of a seed material which assists hydrolysis of dissolved titania, and consequently assists leaching of impurities.
  • Hydrochloric acid usage in place of sulphuric acid has been claimed for this process. Under such circumstances similar impurity removal to that achieved with other hydrochloric acid based systems is to be expected. Where sulphuric acid is used radioactivity removal will not be complete.
  • a commonly adopted method for upgrading of ilmenite to higher grade products is to smelt ilmenite at temperatures in excess of 1500°C with coke addition in an electric furnace, producing a molten titaniferous slag (for casting and crushing) and a pig iron product.
  • molten titaniferous slag for casting and crushing
  • pig iron product Of the problem impurities only iron is removed in this manner, and then only incompletely as a result of compositional limitations of the process.
  • a titaniferous ore is treated by alternate leaching with an aqueous solution of alkali metal compound and an aqueous solution of a non-sulphuric mineral acid (US Patent No. 5,085,837).
  • the process is specifically limited to ores and concentrates and does not contemplate prior processing aimed at artificially altering phase structures. Consequently the process requires the application of excessive reagent and harsh processing conditions to be even partially effective and is unlikely to be economically implemented to produce a feedstock for the chloride pigment process.
  • a wide range of potential feedstocks is available for upgrading to high titania content materials suited to chlorination.
  • Examples of primary titania sources which cannot be satisfactorily upgraded by prior art processes for the purposes of production of a material suited to chlorination include hard rock (non detrital) ilmenites, siliceous leucoxenes, many primary (unweathered) ilmenites and large anatase resources.
  • Many such secondary sources e.g. titania bearing slags also exist.
  • titania reserves A large portion of the world's identified titania reserves is in the form of hard rock ilmenites.
  • the present invention provides a combination of processing steps which may be incorporated into more general processes for the upgrading of titaniferous materials, rendering such processes applicable to the treatment of a wider range of feeds and producing higher quality products than would otherwise be achievable.
  • the present invention provides a process for upgrading a titaniferous material by removal of impurities, which process involves alternately leaching of the material in a caustic leach and a pressure sulphuric acid leach.
  • the present invention ensures that caustic leaching can be conducted economically and effectively despite the need for the use of excess caustic in the leach by circulation of caustic leach liquors after solid/liquid separation through a caustic regeneration step using lime addition to precipitate complex aluminosilicates and regenerate caustic solution.
  • the complex aluminosilicates are then separated from the regenerated caustic solution which is recycled to the leach.
  • titaniferous materials containing both alumina and silica in such a manner has not previously been disclosed, and it is herein revealed that only under specific operating conditions can such a process be operated without precipitation of complex aluminosilicates in the caustic leach.
  • the process of the invention can remove iron, magnesium, aluminium, silicon, calcium, magnesium, manganese, phosphorus, chromium and vanadium, which impurities form an almost comprehensive list of impurities in hard rock ilmenite sources of titania.
  • the titaniferous material may be roasted in any suitable device and to any temperature under reducing or oxidising conditions prior to leaching. Such roasting may be conducted in order to enhance the response of the material to the leaching steps or to reduce the production of sulphur dioxide in the leach by oxidation of any trivalent titania in the titaniferous material.
  • Additives may be made to the titaniferous material prior to such a roasting step in order to enhance the response of the material to the leaching steps, or for any other purpose.
  • the titaniferous material may be preground prior to roasting or leaching in order to enhance reaction rates or in preparation for agglomeration steps which are improved by generation of a broad particle size distribution in the material to be agglomerated.
  • the final titaniferous product may be agglomerated by any suitable technique to produce a size consist which is suitable to the market for synthetic rutile. After agglomeration the product may be fired at temperatures sufficient to produce sintered bonds, thereby removing from dusting losses in fluidised bed chlorinators.
  • the final product may be calcined in order to remove volatile matter (e.g. water, sulphur dioxide and sulphur trioxide) .
  • volatile matter e.g. water, sulphur dioxide and sulphur trioxide
  • a caustic solution bleed or caustic solution evaporation step (for wash water removal) may be operated.
  • the sulphuric acid leach exit liquor may be neutralised to produce solid sulphates and hydroxides for disposal.
  • the sulphuric acid leach exit liquor may be treated for regeneration of sulphuric acid from the aqueous sulphate solutions formed in the process.
  • leach steps may be incorporated into the process as desired.
  • a hydrochloric acid leach may; be conducted to assist in the removal of trace levels of radioactivity.
  • Pressure filtration of the complex aluminosilicate precipitated in caustic recovery may be operated to assist solid/liquid separation.
  • Flocculants and other aids may be used to assist solid/liquid separation.
  • This example is to demonstrate the ineffectiveness of treatments found to be effective for upgrading other titaniferous materials on materials such as titaniferous slags produced from hard rock ilmenites.
  • titaniferous slag having the composition indicated in Table 1 was subjected to oxidation roasting in air at 750°C for 30 minutes, followed by reduction roasting in a 1:3 hydrogen to carbon dioxide (volumetric basis) gas mixture at 680°C for one hour.
  • the cooled product of this thermal treatment contained no ferric iron and no trivalent titania.
  • the phase composition of the material was indicated by X-ray diffraction as pseudobrookite.
  • the thermally treated material was leached in refluxing 10% caustic soda solution at 10% slurry density. After filtration and washing the solid residue had a composition as indicated in Table 2.
  • the residue of the caustic leach was subjected to a leach with refluxing 20% hydrochloric acid at 30% slurry density for 6 hours. After filtration and washing the solid residue had the composition which is also indicated in Table 2.
  • Example 1 The treatment indicated in Example 1 was repeated with the exception that the caustic leach was conducted under pressure at 165°C.
  • compositions of the caustic and acid leached products are indicated in Table 3. It is clear that the caustic leach had no appreciable effect on the silica or alumina contents of the material.
  • the acid leach despite being largely ineffective in producing an upgrade which might be suitable for the chloride pigment process did have a substantial effect on the silica and alumina contents. There was no such effect on a sample of slag submitted directly to hydrochloric acid leaching.
  • a sample of the slag whose composition is indicated in Table 1 was mixed with 2% borax, formed into pellets and subjected to reduction roasting in a 19:1 hydrogen to carbon dioxide (volumetric basis) gas mixture at 1000°C for 2 hours.
  • the phase composition of the cooled product of this thermal treatment was indicated by X-ray diffraction as pseudobrookite.
  • the residue of the caustic leach was subjected to a pressure leach at 150°C with 20% sulphuric acid at 5% slurry density for 6 hours. After filtration and washing the solid residue had the composition which is also indicated in Table 4.
  • the leach liquor from the above caustic leach was preserved and after analysis was treated with micronised lime at the weight ratio of 1.3 units of lime per unit of dissolved silica.
  • the resulting complex aluminosilicate precipitate and any excess lime were removed by filtration and the "regenerated" caustic solution was preserved for reuse in leaching.
  • This example is to demonstrate the ineffectiveness of acid leaching alone in the removal of silica from titaniferous materials such as titaniferous slags produced from hard rock ilmenites.
  • titaniferous slag having the composition shown in Table 1 was subjected to roasting for two hours in an atmosphere of 1:19 (volumetric basis) of hydrogen to carbon dioxide at 1000°C. After cooling in the roasting atmosphere the roasted slag was pressure leached at 135°C in 20% sulphuric acid at 25% w/w slurry density for six hours.
  • composition of the leach residue is given in Table 5.
  • Such direct acid leach treatment of a roasted titaniferous material may be anticipated to result in little improvement of product quality by leaching, and no removal of Si0 2 .
  • Example 5 A sample of slag to which no addition of additive had been made and which was not subjected to any thermal treatment was treated by the same leaching steps as indicated in Example 3.
  • composition of the final product was as recorded in Table 6. Substantial removal of impurities have been achieved without thermal treatment.

Landscapes

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

Abstract

L'invention concerne un procédé d'ennoblissement d'un matériau titanifère par enlèvement des impuretés dudit matériau. Ce procédé comprend un affinage alternatif du matériau titanifère dans un bain caustique et dans un bain d'acide sulfurique sous pression.
EP94926722A 1993-09-07 1994-09-07 Ennoblissement de materiaux titaniferes Withdrawn EP0717783A4 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
AUPM1051/93 1993-09-07
AUPM105193 1993-09-07
PCT/AU1994/000528 WO1995007366A1 (fr) 1993-09-07 1994-09-07 Ennoblissement de materiaux titaniferes

Publications (2)

Publication Number Publication Date
EP0717783A1 true EP0717783A1 (fr) 1996-06-26
EP0717783A4 EP0717783A4 (fr) 1997-04-23

Family

ID=3777178

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94926722A Withdrawn EP0717783A4 (fr) 1993-09-07 1994-09-07 Ennoblissement de materiaux titaniferes

Country Status (7)

Country Link
EP (1) EP0717783A4 (fr)
JP (1) JPH09504828A (fr)
CN (1) CN1042349C (fr)
CA (1) CA2171185A1 (fr)
NO (1) NO317932B1 (fr)
WO (1) WO1995007366A1 (fr)
ZA (1) ZA946864B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2592655C2 (ru) * 2014-12-24 2016-07-27 Федеральное государственное бюджетное учреждение науки Объединенный институт высоких температур Российской академии наук (ОИВТ РАН) Способ термохимической переработки редкометального сырья
RU2623564C1 (ru) * 2016-04-25 2017-06-27 Федеральное государственное бюджетное учреждение науки Институт металлургии и материаловедения им. А.А. Байкова Российской академии наук (ИМЕТ РАН) Способ переработки лейкоксенового концентрата

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AUPM511994A0 (en) * 1994-04-15 1994-05-12 Technological Resources Pty Limited Leaching of a titaniferous material
US6627165B2 (en) * 1994-04-15 2003-09-30 Technological Resources Pty Ltd Process for upgrading a titaniferous material containing silica
AUPM511894A0 (en) * 1994-04-15 1994-05-12 Technological Resources Pty Limited Treatment of leach liquors for upgrading a titaniferous material
CN1060817C (zh) * 1997-08-08 2001-01-17 杨道光 钛铁矿电解渗析分离法
WO2005024074A1 (fr) * 2003-09-05 2005-03-17 Promet Engineers Pty Ltd Procede destine a extraire des oxydes de titane cristallins
WO2007052801A1 (fr) * 2005-11-07 2007-05-10 Tohoku University Procede d’extraction du rutile
CN103834798B (zh) * 2012-11-26 2015-11-18 贵阳铝镁设计研究院有限公司 由低品位TiO2炉渣制备富钛料的方法
CN103952533B (zh) * 2014-04-23 2016-01-20 鞍钢集团矿业公司 利用煅烧、碱浸及脱泥再选钒钛磁铁精矿的方法
CN103966423B (zh) * 2014-04-23 2016-02-03 鞍钢集团矿业公司 利用碱浸、酸洗及重选再选钒钛磁铁精矿的方法
CN104828864B (zh) * 2015-05-26 2017-07-21 昆明冶金研究院 一种钛铁矿盐酸浸出制备人造金红石的工艺

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE276025C (fr) *
GB711833A (en) * 1949-03-03 1954-07-14 Nat Titanium Pigments Ltd Improved manufacture of titanium compounds
WO1991013180A1 (fr) * 1990-03-02 1991-09-05 Wimmera Industrial Minerals Pty. Ltd. Fabrication de rutile synthetique
EP0460319A1 (fr) * 1990-03-27 1991-12-11 Qit-Fer Et Titane Inc. Procédé de préparation de rutile synthétique à partir de scories titanifères contenant du magnésium

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT1030645B (it) * 1974-10-04 1979-04-10 Sir Soc Italiana Resine Spa Procedimento per la produzione di biossido di titanio
US4176159A (en) * 1976-11-15 1979-11-27 Mendonca Paulo Ayres Falcao De Process for concentration of titanium containing anatase ore
ZA781126B (en) * 1977-03-09 1979-01-31 Mineracao Vale Paranaiba Sa Va Method for obtaining high tio2 grade anatase concentrates from lower tio2 grade anatase concentrates
JPH01301518A (ja) * 1988-05-28 1989-12-05 Sakai Chem Ind Co Ltd 酸化チタンの製造方法
US5011666A (en) * 1988-07-28 1991-04-30 E. I. Du Pont De Nemours And Company Method for purifying TiO2 ore
DE3912554C1 (fr) * 1989-04-17 1990-07-12 Bayer Ag, 5090 Leverkusen, De
AU1498092A (en) * 1991-04-19 1992-10-22 Rgc Mineral Sands Limited Removal of radionuclides from titaniferous material
AU639390B2 (en) * 1991-04-19 1993-07-22 Rgc Mineral Sands Limited Removal of radionuclides from titaniferous material

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE276025C (fr) *
GB711833A (en) * 1949-03-03 1954-07-14 Nat Titanium Pigments Ltd Improved manufacture of titanium compounds
WO1991013180A1 (fr) * 1990-03-02 1991-09-05 Wimmera Industrial Minerals Pty. Ltd. Fabrication de rutile synthetique
EP0460319A1 (fr) * 1990-03-27 1991-12-11 Qit-Fer Et Titane Inc. Procédé de préparation de rutile synthétique à partir de scories titanifères contenant du magnésium

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
ERZMETALL, STUTGART, DE, vol. 33, no. 6, June 1980, pages 308-314, XP002025565 E. GOCK, K.-H. JACOB : "Direkter Aufschluss von Rutil mit Schwefels{ure" *
See also references of WO9507366A1 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2592655C2 (ru) * 2014-12-24 2016-07-27 Федеральное государственное бюджетное учреждение науки Объединенный институт высоких температур Российской академии наук (ОИВТ РАН) Способ термохимической переработки редкометального сырья
RU2623564C1 (ru) * 2016-04-25 2017-06-27 Федеральное государственное бюджетное учреждение науки Институт металлургии и материаловедения им. А.А. Байкова Российской академии наук (ИМЕТ РАН) Способ переработки лейкоксенового концентрата

Also Published As

Publication number Publication date
JPH09504828A (ja) 1997-05-13
CA2171185A1 (fr) 1995-03-16
WO1995007366A1 (fr) 1995-03-16
CN1134730A (zh) 1996-10-30
CN1042349C (zh) 1999-03-03
NO960917D0 (no) 1996-03-06
ZA946864B (en) 1995-09-04
NO960917L (no) 1996-04-25
EP0717783A4 (fr) 1997-04-23
NO317932B1 (no) 2005-01-10

Similar Documents

Publication Publication Date Title
US8834600B2 (en) Extraction process for reactive metal oxides
US6500396B1 (en) Separation of titanium halides from aqueous solutions
JP5171631B2 (ja) チタン鉱石の選鉱
US20020104406A1 (en) Upgrading titaniferous materials
US5730774A (en) Process for upgrading titaniferous materials
US5885536A (en) Process for alkaline leaching a titaniferous material
EP0717783A1 (fr) Ennoblissement de materiaux titaniferes
US7494631B2 (en) Titaniferous ore beneficiation
AU749393C (en) Beneficiation of titania slag by oxidation and reduction treatment
WO1995028502A1 (fr) Lessivage d'un materiau titanifere
US6627165B2 (en) Process for upgrading a titaniferous material containing silica
AU700536B2 (en) Leaching of a titaniferous material
AU697952B2 (en) Upgrading titaniferous materials
AU2005200649A1 (en) Upgrading titaniferous materials
AU678375C (en) Upgrading titaniferous materials
CA2137812C (fr) Enrichissement de materiaux titaniferes
AU690977B2 (en) Treatment of leach liquors for upgrading a titaniferous material
AU2387799A (en) Upgrading titaniferous materials
Mukherjee et al. Status of Waste Treatment in Titanium Mineral Industries
AU2008201905A1 (en) Upgrading titaniferous materials
AU687054B2 (en) Process for upgrading titaniferous materials
GENERAL LEACHING WITH ACIDS

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19960404

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

A4 Supplementary search report drawn up and despatched

Effective date: 19970307

AK Designated contracting states

Kind code of ref document: A4

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

17Q First examination report despatched

Effective date: 19980507

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 19991218