WO2005090619A1 - Production d'oxyde de titane - Google Patents

Production d'oxyde de titane Download PDF

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Publication number
WO2005090619A1
WO2005090619A1 PCT/AU2005/000387 AU2005000387W WO2005090619A1 WO 2005090619 A1 WO2005090619 A1 WO 2005090619A1 AU 2005000387 W AU2005000387 W AU 2005000387W WO 2005090619 A1 WO2005090619 A1 WO 2005090619A1
Authority
WO
WIPO (PCT)
Prior art keywords
process defined
reducing gas
leaching
titaniferous material
iron
Prior art date
Application number
PCT/AU2005/000387
Other languages
English (en)
Inventor
Alan David Stuart
Graham Andrew Reynolds
John Andrew Lawson
Original Assignee
Bhp Billiton Innovation 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
Priority claimed from AU2004901444A external-priority patent/AU2004901444A0/en
Application filed by Bhp Billiton Innovation Pty Ltd filed Critical Bhp Billiton Innovation Pty Ltd
Priority to EP05714259A priority Critical patent/EP1733063A4/fr
Priority to BRPI0508889-5A priority patent/BRPI0508889A/pt
Priority to AU2005224285A priority patent/AU2005224285A1/en
Priority to EA200601725A priority patent/EA010600B1/ru
Publication of WO2005090619A1 publication Critical patent/WO2005090619A1/fr
Priority to US11/522,651 priority patent/US20070122325A1/en

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
    • 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
    • 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
    • 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
    • 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

Definitions

  • the present invention relates to a process for producing titania from a titaniferous material.
  • titanium material is understood herein to mean any titanium-containing material, including by way of example, ores, ore concentrates, and titaniferous slags .
  • the present invention relates particularly to a process for producing titania from a solid titaniferous material that can be described in general terms as a sulfate process .
  • sulfate process is understood herein to mean a process for producing titania from a titaniferous material that comprises treating a solid feed material and at least substantially dissolving the feed material into solution and thereafter recovering titania from solution.
  • the applicant has been carrying out research and development work in relation to the sulfate process .
  • the work has resulted in two options for the sulfate process .
  • Both process options include the steps of:
  • the research and development work included leaching ilmenite in 400-750 g/1 sulfuric acid.
  • the work included adding iron in the form of scrap iron during the leaching step (a) .
  • the main advantage of adding iron is to accelerate the rate of leaching.
  • the disadvantages of adding iron include increased amounts of iron sulfate as a by-product and increased process complexity (such that an industrial plant would need equipment for handling scrap iron and for dealing with hydrogen gas that is evolved as a consequence of iron addition) .
  • scrap iron although not expensive currently, introduces an additional operating cost to the process.
  • the leaching rate is such, even with the addition of iron, that it may still be necessary to grind ilmenite prior to the leaching step to improve the rate.
  • the present invention provides a process for producing titania from a solid, iron- containing titaniferous material (such as ilmenite) which includes the steps of:
  • step (a) comprises treating titaniferous material under conditions that result in ferrous ions being a predominant form of iron in the titaniferous material.
  • step (a) comprises treating titaniferous material under conditions that do not result in substantial formation of rutile that is unleachable under the conditions of leaching step (b) .
  • step (a) comprises treating titaniferous material under conditions so that there is either no metallic iron formed in the step or a selected relatively small amount of metallic iron formed in the step.
  • Step (a) may be carried out in any suitable treatment apparatus such as a fluidized bed or a kiln.
  • step (a) comprises treating titaniferous material by contacting titaniferous material with the reducing gas in a fluidized bed.
  • step (a) includes by way of example the selection of (i) the composition of the reducing gas, (ii) the temperature of the reducing gas, and (iii) the contact time of the reducing gas and the titani erous material .
  • the reducing gas may be any suitable gas, such as hydrogen, carbon monoxide, and mixtures thereof.
  • the reducing gas is a mixture of (a) hydrogen and/or carbon monoxide and/or methane and (b) another suitable gas such as an inert gas and/or carbon dioxide.
  • the inert gas is nitrogen.
  • the hydrogen comprises up to 25%, more preferably 3-25%, by volume of the reducing gas.
  • the temperature of the reducing gas is less than 700°C to avoid substantial formation of rutile that is unleachable under the conditions of leaching step (b) .
  • the temperature of the reducing gas is 450-550°C.
  • the carbon monoxide comprises up to 60%, more preferably 30-60%, by volume of the reducing gas.
  • the temperature of the reducing gas is less than 700°C, more preferably less than 650°C.
  • the temperature of the gas be 600°C.
  • the average contact time of the material and the reducing gas is less than 120 minutes, more preferably 20-120 minutes.
  • Steps (b) and (c) may be as described in International application PCT/AU03/01386 and International application PCT/AU2004/001421.
  • the leaching step (b) may comprise a multiple leaching step involving (i) a first step of leaching the titaniferous material with the leach liquor and forming a process solution that includes an acidic solution of titanyl sulfate; (ii) separating the process solution and a residual solid phase; (iii) leaching the residual solid phase in a subsequent leach step with a leach liquor and forming a further process solution that includes an acidic solution of titanyl sulfate and iron sulfate; (iv) separating the process solution and a residual solid phase; and (v) supplying the separated process solution to the first leach step and/or mixing the separated process solution with the process solution from the first leach step for subsequent processing in reducing step (c) .
  • the leaching step (b) includes selecting and/or controlling the leaching conditions to avoid undesirable amounts of premature hydrolysis and undesirable amounts of premature precipitation.
  • the acid concentration in the leaching step (b) should be at least 350 g/1 sulfuric acid throughout the leaching step when operating at a leach temperature in the range of from 95°C to the boiling point in order to avoid premature hydrolysis .
  • the acid concentration at the end of the leaching step (b) should be less than 450 g/1 when operating at a leach temperature in the range from 95°C to the boiling point in order to avoid an undesirable amount of premature precipitation of titanyl sulfate.
  • the acid concentration at the start of the leaching step (b) may be higher than the above desirable concentrations, typically as high as 700 g/1.
  • step (c) of recovering titania from the leach liquor may comprise the steps of (i) separating iron sulfate from the leach liquor, (ii) separating titanyl sulfate from the leach liquor either after or before step (i) , and (iii) recovering titania from the titanyl sulfate.
  • step (ii) of separating titanyl sulfate from the leach liquor may comprise solvent extraction of titanyl sulfate from the leach liquor, as described in International application PCT/AU03/01386.
  • step (ii) of separating titanyl sulfate from the leach liquor comprises precipitating titanyl sulfate from the leach liquor, as described in International application PCT/AU2004/001421.
  • Steps (b) and (c) are not confined to the steps described in International application PCT/AU03/01386 and International application PCT/AU2004/001421.
  • the leaching step (b) may be in accordance with the standard sulfate process , which includes a 2-stage step with a first stage involving solid state sulfation of pre-treated titaniferous material from step (a) with concentrated sulfuric acid and a second stage involving dissolving the sulfated product in wate /dilute acid and forming an acidic solution of titanyl sulfate and iron sulfate.
  • the research and development work carried out by the applicant in relation to treatment of ilmenite has focussed on the use of hydrogen gas and carbon monoxide. The following description relates to the research and development work carried out at the Newcastle Technology Centre of the applicant.
  • a first set of treatment experiments involving reducing gases containing H 2 was carried out on Beenup ilmenite.
  • the experiments on Beenup ilmenite are not discussed in detail herein.
  • Table 1 sets out the particle size distribution of the first batch of Stradbroke ilmenite.
  • Table 2 sets out the particle size distribution of the second batch of Stradbroke ilmenite.
  • the first and second batches of the Stradbroke ilmenite had similar particle size distributions and were finer in particle size than the Beenup ilmenite. Specifically, whilst the top size was smaller, the bottom size was the same as that of Beenup ilmenite.
  • TGA thermogravimetric analysis apparatus
  • the full size fraction of the first batch of the Stradbroke ilmenite as set out in Table 1 above was selected for use in the TGA experiments, as the finest fraction was large enough to resist terminal velocity at 12 1/min gas flow.
  • the use of the "as received" size fraction also had a benefit of minimising further beneficiation through sizing or crushing at either a mine site or plant scale production.
  • the experiments monitored the weight loss of the samples during the course of the experiments .
  • FIG. 1 An example of the results in this regard is shown in Figure 1.
  • the figure shows that there was substantial weight loss in the first 20 minutes of the experiment and that thereafter the weight loss was at a constant, relatively shallow, gradient to the time that the experiment was stopped.
  • the constant gradient weight loss is consistent with what would be expected with reduction of ferric ions to ferrous ions . If reduction had been completed, ie with formation of 100% metallic iron, it would have been expected that the weight loss plot would have plateaued at a lower level .
  • the treated ilmenite was removed from the TGA and thereafter leached (on the same day) in 431 g/1 sulfuric acid at or just below 100°C.
  • the leach stage lasted 5 hours total.
  • the solids and liquids were separated by filtration and the filtrate was tested for free acid and titanium.
  • Extraction was determined as the mass of titanium present in the liquid phase after leaching, with respect to the mass available from the solid phase at the commencement of the experiment.
  • Sample STR-IR13- LI is a repeat of sample STR- IR7- LI (550°C, 20% H 2 in N 2 for 45 minutes) because the original result, ie sample STR-IR7- LI, was much lower than expected.
  • the results of sample STR-IR7-L1 are not presented here. There were two faults noted in the original experiment - the sample when removed from the TGA was hotter than expected (possibly causing reoxidation) and secondly the level of the water bath dropped significantly during the leach due to a poor seal between the water bath and the lid.
  • Hot Reduction Rig Test and Subsequent Leaching Test of Treated Material The impact of treatment of the first batch of the Stradbroke ilmenite in accordance with the invention was also evaluated in a Hot Reduction Rig (HRR) .
  • HRR Hot Reduction Rig
  • the HRR is a tube furnace that comprises a tube passing through the centre of a Kanthal split furnace.
  • the tube furnace has three main sections .
  • the upper section has a cyclone to decelerate and remove particulates from the gas phase.
  • a dip leg returns these solids to the bed.
  • the sample section has a perforated plate that allows the solids bed to be fluidised by the flow of reaction gas .
  • the sample size is usually around 500 g mass .
  • the lower section below the sample is filled with stainless steel turnings . This area is designed to act as a heat exchanger to heat the reaction gas quickly to the required reaction temperature.
  • the HRR differs from the TGA as the entire sample is evenly exposed to a steady stream of reaction gas .
  • the fluidised bed avoids mass transfer effects seen in the latter stages of TGA tests. Consequently, comparisons between the TGA tests and HRR tests can be difficult, as the time required to reach a certain reduction point in the HRR should be less than the required in the TGA.
  • 500g of the first batch of the unground Stradbroke ilmenite was treated in accordance with the invention for 90 minutes under 20% H 2 in N 2 at 550°C in the HRR.
  • the treated sample was cooled under nitrogen to 40°C, removed and thereafter leached in sulfuric acid for 5 hours on the same day in a two-litre reactor kettle.
  • the acid concentration was maintained at 400 g/1.
  • the kettle was maintained at a temperature of 110°C.
  • the solids loading was 400 g/1 at the start of the leach.
  • the rate of titanium and iron dissolution exceeded any other bench test result of the applicant to that date.
  • the speed at which the initial reaction occurred caused the acid levels to drop below the target acidity.
  • the final solution containing 49 g/1 titanium exceeds almost all tests thus far for concentration of titanium in solution with respects to solids loading, time and acid concentration. Extraction of titanium from the solids was 34% (42% when adjusted for sampling) .
  • a 500g sample of the second batch of the Stradbroke ilmenite was treated for 20 minutes under 20% H 2 at 550°C in the HRR. At the end of the 20 minute treatment period, the treated sample was cooled under nitrogen to 40°C, removed and thereafter a 50g sample was leached in sulfuric acid for 5 hours in a two-litre reaction kettle. The kettle was maintained at a temperature of 110°C. The acid concentration was maintained at 450 g/1. The solids loading at the start of the leach was 50 g/1.
  • a 50g sample of the second batch of the Stradbroke ilmenite in the as-received form and a 50g sample of the second batch of the Stradbroke ilmenite in a ground form were also leached in two-litre reaction kettles under the same conditions described in the preceding paragraph. In both cases, iron rods were added to the kettles .
  • 500g samples of Cruzor ilmenite were fluidised with N 2 in a fluid bed reactor.
  • the reactor was heated to a target temperature and the N 2 atmosphere was replaced by reducing gas (combinations of CO, C0 2 , H 2 and CH 4 ) . After a specified time the reducing gas was replaced with N 2 and the reactor was allowed to cool.
  • the product from the reactor was leached immediately in 450 g/1 sulfuric acid for 48 hours at 110°C. Samples were taken at specific intervals for analysis to determine leaching rate and extraction.
  • Figure 3 is a plot of titanium extraction (%) versus leach time (hrs) for experiments on 4 samples that were reduced under different temperature conditions. The purpose of the Figure is to illustrate the impact of reduction temperature on titanium extraction.
  • Figure 3 shows that optimum titanium extraction on leaching was obtained with the sample that was reduced at 600°C.
  • Figure 4 is a plot of titanium extraction (%) versus leach time (hrs) for experiments on 4 samples reduced under different partial pressures of CO in the reducing gas. The purpose of the Figure is to illustrate the impact of the partial pressure of CO on titanium extraction.
  • Figure 4 shows that titanium extraction increased with partial pressure of CO in the reducing gas with the sample reduced with a CO partial pressure of 0.6 in the reducing gas achieved the highest titanium extraction.

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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)
  • Inorganic Compounds Of Heavy Metals (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L'invention concerne un procédé de production d'oxyde de titane à partir d'un matériau titanifère solide contenant du fer (par exemple l'ilménite). Ledit procédé consiste notamment à traiter le matériau titanifère contenant du fer dans des conditions qui permettent de réduire les ions ferriques en ions ferreux dans ledit matériau, puis à lixivier le matériau titanifère traité et former une liqueur lixiviante qui comprend une solution acide de sulfate de titane et un sulfate de fer et à récupérer l'oxyde de titane à partir de la liqueur lixiviante.
PCT/AU2005/000387 2004-03-18 2005-03-17 Production d'oxyde de titane WO2005090619A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP05714259A EP1733063A4 (fr) 2004-03-18 2005-03-17 Production d'oxyde de titane
BRPI0508889-5A BRPI0508889A (pt) 2004-03-18 2005-03-17 processo para produzir titánia a partir de um material titanìfero sólido que contém ferro
AU2005224285A AU2005224285A1 (en) 2004-03-18 2005-03-17 Production of titania
EA200601725A EA010600B1 (ru) 2004-03-18 2005-03-17 Производство диоксида титана
US11/522,651 US20070122325A1 (en) 2004-03-18 2006-09-18 Production of titania

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2004901444 2004-03-18
AU2004901444A AU2004901444A0 (en) 2004-03-18 Production of titania

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US11/522,651 Continuation-In-Part US20070122325A1 (en) 2004-03-18 2006-09-18 Production of titania

Publications (1)

Publication Number Publication Date
WO2005090619A1 true WO2005090619A1 (fr) 2005-09-29

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ID=34993722

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU2005/000387 WO2005090619A1 (fr) 2004-03-18 2005-03-17 Production d'oxyde de titane

Country Status (8)

Country Link
US (1) US20070122325A1 (fr)
EP (1) EP1733063A4 (fr)
CN (1) CN1961086A (fr)
BR (1) BRPI0508889A (fr)
EA (1) EA010600B1 (fr)
TW (1) TW200538397A (fr)
WO (1) WO2005090619A1 (fr)
ZA (1) ZA200607893B (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008028245A1 (fr) 2006-09-06 2008-03-13 Bhp Billiton Innovation Pty Ltd Procédé au sulfate
WO2008028244A1 (fr) * 2006-09-06 2008-03-13 Bhp Billiton Innovation Pty Ltd Procédé au sulfate
WO2010034083A1 (fr) * 2008-09-29 2010-04-01 Bhp Billiton Innovation Pty Ltd Procédé de préparation de pâte au sulfate
RU2571904C1 (ru) * 2014-11-06 2015-12-27 Федеральное государственное бюджетное учреждение науки Институт химии и технологии редких элементов и минерального сырья им. И.В. Тананаева Кольского научного центра Российской академии наук (ИХТРЭМС КНЦ РАН) Способ переработки титансодержащего материала

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10407316B2 (en) 2014-07-08 2019-09-10 Avertana Limited Extraction of products from titanium-bearing minerals
CN107723480A (zh) * 2017-08-23 2018-02-23 成都圻坊生物科技有限公司 一种精选钛矿的处理方法

Citations (6)

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Publication number Priority date Publication date Assignee Title
US4206021A (en) * 1978-03-02 1980-06-03 Thann Et Mulhouse S.A. Process for the production of pigmentary titanium dioxide by the sulphuric acid method
US4986742A (en) * 1985-07-05 1991-01-22 Bayer Aktiengesellschaft Process for the production of high-grade titanium dioxide by sulfate method
WO1994026944A1 (fr) * 1993-05-07 1994-11-24 Technological Resources Pty Ltd Procede d'amelioration de materiaux titaniferes
EP0801030A2 (fr) * 1996-04-13 1997-10-15 Tioxide Group Services Limited Production d'oxyde de titane
EP0869194A1 (fr) * 1997-04-03 1998-10-07 Kemira Pigments Oy Procédé de préparation du bioxyde de titane
WO2000048944A1 (fr) * 1999-02-19 2000-08-24 Mbx Systems, Inc. Procedes ameliores de lixiviation de minerais

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GB1282324A (en) * 1969-07-31 1972-07-19 British Titan Ltd Process for the benification of iron-containing titaniferous materials
US3877929A (en) * 1969-07-31 1975-04-15 Jack Whitehead Process for reducing iron content of titaniferous material
GB1312765A (en) * 1971-03-12 1973-04-04 British Titan Ltd Benefication process for iron-containing titaniferous material
US4288418A (en) * 1979-08-10 1981-09-08 Nl Industries, Inc. Process for manufacturing titanium dioxide
US5389355A (en) * 1987-12-09 1995-02-14 Qit-Fer Et Titane, Inc. Method of preparing a synthetic rutile from a titaniferous slag containing alkaline earth metals
JPH04119919A (ja) * 1990-09-12 1992-04-21 Chiyuushitsu Kenkyusho:Kk 二酸化チタンの製造方法
US6471743B1 (en) * 1999-02-19 2002-10-29 Mbx Systems, Inc. Methods for leaching of ores

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Publication number Priority date Publication date Assignee Title
US4206021A (en) * 1978-03-02 1980-06-03 Thann Et Mulhouse S.A. Process for the production of pigmentary titanium dioxide by the sulphuric acid method
US4986742A (en) * 1985-07-05 1991-01-22 Bayer Aktiengesellschaft Process for the production of high-grade titanium dioxide by sulfate method
WO1994026944A1 (fr) * 1993-05-07 1994-11-24 Technological Resources Pty Ltd Procede d'amelioration de materiaux titaniferes
EP0801030A2 (fr) * 1996-04-13 1997-10-15 Tioxide Group Services Limited Production d'oxyde de titane
EP0869194A1 (fr) * 1997-04-03 1998-10-07 Kemira Pigments Oy Procédé de préparation du bioxyde de titane
WO2000048944A1 (fr) * 1999-02-19 2000-08-24 Mbx Systems, Inc. Procedes ameliores de lixiviation de minerais

Non-Patent Citations (1)

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Title
See also references of EP1733063A4 *

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008028245A1 (fr) 2006-09-06 2008-03-13 Bhp Billiton Innovation Pty Ltd Procédé au sulfate
WO2008028244A1 (fr) * 2006-09-06 2008-03-13 Bhp Billiton Innovation Pty Ltd Procédé au sulfate
US8021634B2 (en) 2006-09-06 2011-09-20 Bhp Billiton Innovation Pty. Ltd. Sulfate process
US8273322B2 (en) 2006-09-06 2012-09-25 Bhp Billiton Innovation Pty. Ltd. Sulfate process
WO2010034083A1 (fr) * 2008-09-29 2010-04-01 Bhp Billiton Innovation Pty Ltd Procédé de préparation de pâte au sulfate
US8728437B2 (en) 2008-09-29 2014-05-20 Bhp Billiton Innovation Pty Ltd Sulfate process
RU2571904C1 (ru) * 2014-11-06 2015-12-27 Федеральное государственное бюджетное учреждение науки Институт химии и технологии редких элементов и минерального сырья им. И.В. Тананаева Кольского научного центра Российской академии наук (ИХТРЭМС КНЦ РАН) Способ переработки титансодержащего материала

Also Published As

Publication number Publication date
EA010600B1 (ru) 2008-10-30
ZA200607893B (en) 2008-02-27
US20070122325A1 (en) 2007-05-31
EA200601725A1 (ru) 2007-02-27
BRPI0508889A (pt) 2007-09-11
EP1733063A4 (fr) 2008-10-01
EP1733063A1 (fr) 2006-12-20
TW200538397A (en) 2005-12-01
CN1961086A (zh) 2007-05-09

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