EP0104961B1 - Verfahren zur Behandlung von Ton zur Entfernung von Verunreinigungen auf Titanbasis - Google Patents

Verfahren zur Behandlung von Ton zur Entfernung von Verunreinigungen auf Titanbasis Download PDF

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Publication number
EP0104961B1
EP0104961B1 EP83401617A EP83401617A EP0104961B1 EP 0104961 B1 EP0104961 B1 EP 0104961B1 EP 83401617 A EP83401617 A EP 83401617A EP 83401617 A EP83401617 A EP 83401617A EP 0104961 B1 EP0104961 B1 EP 0104961B1
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Prior art keywords
clay
activator
slurry
suspension
conditioning
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EP83401617A
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English (en)
French (fr)
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EP0104961A2 (de
EP0104961A3 (en
Inventor
Raymond H. Young
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BASF Catalysts LLC
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Engelhard Corp
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/002—Inorganic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/008—Organic compounds containing oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/005—Dispersants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/007—Modifying reagents for adjusting pH or conductivity
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/02—Ores
    • B03D2203/04—Non-sulfide ores

Definitions

  • the present invention relates to methods for treating clays such as kaolin, in order to give gloss to the clay and to make it more advantageous for use in industries such as the paper industry and coating industry and more particularly relates to methods for treating clay in which a suspension of clay is conditioned with activators and conditioning chemicals and then subjected to flotation in a flotation process air.
  • US Patent 3,072,255 describes the sulfurization of a dispersed clay using H 2 S or Na 2 S, followed by conditioning or flotation of the clay slip.
  • the procedure in this patent could result in the formation of a ferrous sulfide which is water-soluble and which decomposes in hot water and is not generally considered to be an activator which can be used to condition the clay before flotation.
  • the patent proposes neutralization and conditioning with oleic acid, followed by the addition of an alkaline material and of a particulate material such as graphite, a sulfide, carbon or equivalent, followed by additional conditioning. Means are not provided in the patent for maintaining the iron in the ferrous state during the conditioning of the slip.
  • US Patent 4186027 although not related to a flotation process, describes the reduction of the iron in the clay to its ferrous form using sodium hyposulfite, followed by filtration to separate the clay iron.
  • Calcium ion has been used for many years as an activator to condition clay suspensions for the elimination by flotation of kaolin impurities. However, it has been found that certain clays do not respond to activation by the calcium ion. In order to improve the response of the failed clays, a series of chemical salts containing ions other than the calcium ion have been tried as activators in the process according to the invention. Although some heavy metal ions improve the response of some clays, they are unacceptable due to their toxic nature.
  • ferrous ion which has already been suggested as an activator (U.S. Patent 3,979,282).
  • the use of the ferrous ion is complicated because of the ease with which it oxidizes during the conditioning phase. In this way, it is sometimes necessary to use excessive amounts which, in many cases, cause the flocculation of the suspension, which results in less good conditioning of the clay suspension.
  • ferrous ion activator under reducing conditions also greatly improves the response of clays which ordinarily cannot be activated by calcium ion.
  • the use of the ferrous ion / reducing agent system also improves the response of clays which are ordinarily activated by the calcium ion.
  • One method of improving the gloss applicable to clay consists in reducing the ferric ion usually present in variable amounts to a ferrous ion, by adding a chemical reducing compound.
  • a chemical reducing compound usually hyposulfite to effect this reduction of ferric ion.
  • the ferrous ion formed by the reduction is soluble in the aqueous phase of the suspension and can be removed by filtration; the iron content of the clay is thus lowered without flotation.
  • a quantity of the reducing agent is added which is sufficient to maintain the ferrous component which remains in the clay in a reduced form until the filtration phase and beyond this phase.
  • the iron present in a clay sample cannot be reduced entirely to its ferrous form. For this reason, a particular clay may have a high iron content, much of which may not be easily reducible to the ferrous form required for activation.
  • the total iron content of a clay therefore does not give adequate information on the fact that the clay may or may not supply in situ ferrous iron in sufficient quantity to ensure adequate activation nor on the fact that it is or not necessary to add an additional ferrous ion or another activator, for example a calcium ion. It has been found that the difference in gloss of a clay sample - before and after treatment with sodium hyposulfite - is a reliable measure of the amount of reducible iron present in a particular clay. These differences in gloss are illustrated in the following examples and are characterized in the following examples by low, medium or high levels of reducible iron.
  • the aqueous dispersion of the clay filler contains a solid content which is suitable and economical for the work, for example at least about 20% solids, preferably between about 20% and about 70% solids. A solids content of about 30% to about 40% can be used.
  • the filler is prepared in the conventional manner by stirring the clay with water and a dispersing agent, for example, a dispersing composition preferably formed from sodium silicate. Normally, 0.05 to 0.5% by weight of the dispersing agent is used, calculated on the basis of the weight of the dry charge.
  • the dispersion is then optionally treated with an oxidizing whitening agent such as sodium hypochlorite, ammonium persulfate or potassium persulfate, preferably potassium persulfate which can be obtained commercially under the trademark of “Oxone” factory from Dupont and Co.
  • an oxidizing whitening agent such as sodium hypochlorite, ammonium persulfate or potassium persulfate, preferably potassium persulfate which can be obtained commercially under the trademark of “Oxone” factory from Dupont and Co.
  • the amount of bleaching agent used is between 0.01% and 0.1% by weight calculated on the basis of the dry weight of the aqueous clay filler.
  • the pH of the dispersion is adjusted, by adding alkaline reagents, in the pH range of 4.5 to 7.0, with pH 6 to 7 being preferred.
  • the oxidizing whitening agent is allowed to react for at least about 15 hours, for example 15 to 24 hours, before continuing the treatment.
  • the resulting suspension is preferably sieved through a 0.043 mm mesh screen to remove impurities having a particle size greater than 44 micrometers (equivalent sphere diameter).
  • Other oxidizing whitening agents can be used, including water-soluble inorganic or organic compounds containing in their molecule readily available oxygen capable of bleaching, such as ammonium persulfate, potassium permanganate, hydrogen peroxide and the like.
  • the clay suspension is then mixed with a reducing agent capable of reducing at least some of the iron-based impurities contained in the clay suspension to their ferrous form.
  • the reducing agent also has the effect of preventing or delaying the re-transformation of the ferrous form into its more oxidized state.
  • suitable reducing agents available, including sodium hyposulfite, zinc hyosulfite, sulfur dioxide, sulfoxylates such as sodium formaldehyde sulfoxylate and the like.
  • the quantity of reducing agent used depends on its activity, on the severity of the oxidation conditions to which the suspension will be subsequently subjected and on the quantity of reducible iron available for transformation into the ferrous form. In general, an amount of 0.453 to 11.34 kg per tonne of reducing agent such as sodium or zinc hyposulfite is a satisfactory amount and an amount of 1.135 to 6.808 kg per tonne is preferred.
  • an additional activating ion can be added, for example, any of the alkaline earth ions, including magnesium, calcium, strontium or barium, or any of the "heavy metal" ions such as ferrous ion (preferred), cupric copper, manganese manganese and zinc, in the form a salt such as a chloride, nitrate, acetate, oxide or a mixture of salts, preferably a water-soluble ferrous salt, at a concentration of between 0.005% and 0.15% or more by weight of the dry load (or 0.045 to 1.361 kg per tonne of solids in the dispersion) preferably in the range of 0.01% to 0.075% by weight (0.090 to 0.681 kg per tonne of solids in the suspension).
  • any of the alkaline earth ions including magnesium, calcium, strontium or barium, or any of the "heavy metal" ions such as ferrous ion (preferred), cupric copper, manganese manganese and zinc, in the form a
  • An anionic oleophilic collecting agent is also added to the dispersion before packaging.
  • Collecting reagents of this kind include fatty acids having 8 to 20 carbon atoms, oleic acid, linoleic acid, lauric acid, tallow oil, red petroleum, fatty acids from coconut oil, and sulfooleic acid.
  • the preferred anionic collector is oleic acid.
  • the collecting reagent is usually added in an amount of 0.005% to 1.5% by weight of the dry charge (or 0.045 to 13.61 kg per tonne of suspension solids), the preferred range being 0.01% at 0.5% (or 0.090 to 4.53 kg per tonne of suspension solids).
  • the conditioning of the aqueous clay suspension is carried out after the addition of the reducing agent, activating ions, optionally, and the collector.
  • the conditioning is carried out by stirring the mixture of the suspension, the activating ions and the collecting reagent for a period of time ranging from 5 minutes to 180 minutes. A time of approximately 10 to 120 minutes is usually required.
  • a high mixing intensity is preferred, such as that obtained with an apparatus known as "Kady Mill", manufactured by Kinetic Dispersion Corporation., Buffalo, New York, E.U.A.
  • the packaging corresponds to an energy supply of around 25 to 1000 CV-h (horsepower-hours) per tonne of dry load.
  • a particularly satisfactory device is described and claimed in patent application EP-A-0 104 962 (83401618.0) entitled "Apparatus and method for conditioning high density clay”.
  • the conditioned aqueous suspension can be prepared for flotation by adding a dispersing agent belonging to the group of polycarboxylate salts.
  • the preferred dispersing agent is a water-soluble polyacrylate salt added in an amount of between 0.05% and 0.3% by weight of the dry load (or from 0.453 to 2.72 kg per tonne of suspension solids), 0 , 15% to 0.25% by weight of dry load (or 1.361 to 2.27 kg per tonne) being the preferred amount.
  • the lithium salt of polyacrylic acid is preferred, although the sodium and ammonium salts also give good results and the magnesium and potassium salts or mixtures of any of the salts mentioned above can also be used. used.
  • sodium silicate or polyphosphate salts may be substituted for a certain quantity or all of the deflocculating polyacrylate salts added after packaging and before or during flotation.
  • the acrylate salts having an average molecular weight of 500-10,000 (preferably 750-2400) can be used as dispersants in the process of this invention.
  • the conditioned suspension can be diluted for flotation, or not be at will.
  • the pH of the suspension conditioned with the dispersant added is adjusted for optimum foaming, which is in the range of 6.0 to 8; 0; a preferred range is 7.2 to 7.8 for most kaolins; however, the pH for flotation depends on the initial charge.
  • the preferred flotation process in the present invention does not require the addition of foaming aids such as the foaming agents used in the prior art.
  • the foaming is preferably carried out in a modified foaming cell having the constitution shown and described in patent application EP-A-0 104 099 (83 401 619.8) entitled "Apparatus and method of flotation by foaming".
  • the impurities based on titanium dioxide are removed with the foam and the resulting clay suspension is then recovered by flocculation, reducing bleaching, filtration and drying, or by some other recovery technique.
  • the clay suspension can be subjected to any desired subsequent treatment after flotation, for example, fractionation, reducing bleaching, flocculation, filtration and / or drying.
  • ppt means 0.4536 kg of reagent per tonne of clay solids.
  • the percentage of titanium dioxide was determined by X-ray fluorescence and the gloss was measured according to the TAPPI T-646 OX-75 standard. All other indications of parts and percentages are given on the basis of weight, unless otherwise specified. In addition, temperatures are given on the centigrade scale, unless otherwise indicated.
  • TREP means process for the elimination and extraction of titanium according to the invention.
  • a clay suspension was prepared from clay extracted in the Wilkinson County area or the Sandersville area of Georgia (E.U.A.).
  • the clay had a proportion of particles of 79% of less than 2 pm e.s.d. (equivalent spherical diameter) in the clay charge discharged by pump at the installation.
  • Oleic acid Food grade U.S.P.
  • N-grade sodium silicate approximately 37.7% solids (aqueous)
  • the clay suspension was treated with a 4.4 ppt "N" grade Na silicate dispersing agent, then passed through a 0.061 mm mesh screen to remove mica, sand and other coarse particles.
  • the feed suspension had a solids content of 32.5% and an initial pH of 6.7.
  • the suspension was combined with 1 ppt of Oxone (DuPont EI product comprising potassium persulfate) and the pH was adjusted to 6.5 to 6.0 using aqueous NaOH. The almost neutral suspension is then allowed to stand for approximately 15 to 24 hours before processing. This gave Oxone time to act on the possibly oxidizable material contained in the raw product.
  • the pH of the suspension was generally 6.5 to 6.8, the pH at which conditioning should begin. (Suspensions with a pH value as low as 6.1 can be treated satisfactorily by the TREP process according to the invention).
  • the conditioning of the feed suspension treated with Oxone was carried out using the amount of CaCl 2 and oleic acid indicated above. Percentage levels are based on the use of anhydrous reagents.
  • the conditioning was carried out in the Kinetic Dispersion apparatus (KADY), using 2500 ml of pretreated filler. The amount of chemicals to be used must be determined as well as the chemicals measured and prepared for addition.
  • the suspension is introduced into the cell of the KADY device and the rotor is lowered into the cell. After lowering the rotor, the KADY apparatus was turned on and the reagents were immediately added.
  • the suspension was allowed to condition for 20 minutes and the final temperature was about 82 ° C. After conditioning, the pH should be in the range of 6.1 to 6.3.
  • the 2500 ml of conditioned suspension was placed in a Denver cell and diluted to 4 liters with tap water.
  • the solids were generally in the range of 20-30%.
  • Sodium polyacrylate was added in an amount of 4 ppt as a post-conditioning dispersant. This dispersant was allowed to mix with the suspension for a few minutes before starting foaming.
  • dilute HCl was added to lower the pH to 6.2 to 6.5 and foaming started.
  • the Denver cell was operated at 1200 rpm for 45 minutes.
  • the pH was raised to a maximum value of 7.8, if it was necessary to improve the removal of impurities. All pH adjustments made during foaming were obtained by lowering with dilute HCI (4: 1) or by raising with dilute NH 4 OH (9: 1).
  • the suspension is flocculated by adding 10% H 2 S0 4 until a pH of 3 is obtained, it is bleached with 15 ppt of K-Brite (commercial form of hyposulfite sodium), filtered and dried.
  • K-Brite commercial form of hyposulfite sodium
  • the TAPPI gloss was measured on a Martin-Sweets gloss tester and the analysis of Ti0 2 was determined by X-ray fluorescence.
  • the acronym "GEB” means TAPPI gloss.
  • Fill means the clay suspension after dispersion using the sodium silicate dispersant.
  • No bl.” means unbleached.
  • BI means bleached using the sodium hyposulfite reducing whitener, as described above.
  • Diff. in GEB means the difference in brightness TAPPI of the load suspension bleached by reduction, compared to the unbleached charge suspension, and constitutes a measure of the quantity of reducible iron contained in said charge suspension.
  • Comparison A the charge suspension was conditioned with oleic acid and CaCl 2 , as described above, using the amounts and types of reagents listed below. Agitation in the KADY apparatus for 20 minutes-transfer to a Denver flotation cell and foaming with air as described above. The product was isolated by the method of flocculation, bleaching, filtration and drying described above. The product was subjected to a determination analysis of the percentage of Ti0 2 and of the GEB. The results are given in Table I, in comparison line A.
  • Example 1 A third batch was conditioned with another part of the charge suspension in the presence of 7.2 ppt of sodium hyposulfite - to reduce the ferric ions to ferrous ions - the level of oleic acid remained the same in all lots. No additional activator was used. The conditioned suspension was subjected to flotation and the product isolated by the procedure indicated above. The results are shown in Table I.
  • Example 1 illustrates the superiority of the in situ formation of iron, which resulted in the elimination of an amount of Ti0 2 three times greater than that which was eliminated when the Ca ++ activator was used. .
  • Comparison C - The suspension was conditioned using the types and amounts of reagents listed below as described above and subjected to flotation in a Denver cell to serve as a comparison sample. The product was isolated as described above.
  • Example 2 Another part of the charge described above was conditioned as described above but contained 7.5 ppt of sodium hyposulfite substituted for the reagent calcium chloride used in comparison C. The level of oleic acid remained constant. The results of these two operations are given in Table II.
  • Filler - a raw clay from the Sandersville area was dispersed with 2.1 ppt of "N" grade sodium silicate to give a suspension having a solids content of 37.6%.
  • Comparison D The charge suspension was conditioned as described above using the appropriate types and amounts of reagents to provide a comparison sample. This sample was isolated as described above by flocculation, bleaching, filtration and drying. The results are given in Table Ill.
  • Example 3 Another part of the charge identified above was conditioned as described above, by replacing the calcium chloride reagent with 7.5 ppt of sodium hyposulfite.
  • the packaging, flotation and isolation of the product were identical to the procedures described above. The results are given in Table III.
  • the examples given above show that it is possible to form, in a clay suspension, a reduced iron ion which acts as an activator for the strongly colored Ti0 2 impurity.
  • concentration of the reduced iron activator formed in situ is important and can be estimated by measuring the gloss (TAPPI) GEB of the charge before and after the reducing bleaching. The greater the difference in GEB, the more effective the reduced iron formed in situ as an activator.

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  • Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Silicates, Zeolites, And Molecular Sieves (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Emulsifying, Dispersing, Foam-Producing Or Wetting Agents (AREA)

Claims (17)

1. Verfahren zur Behandlung von Ton zur Entfernung von mineralischen Verunreinigungen auf Titanbasis, das die folgenden Stufen umfasst:
(a) Mischen des Tons in Form einer wässrigen Suspension mit einem Tonfeststoffgehalt von mindestens 25 Gew.-% mit einem Sammler für die mineralischen Verunreinigungen auf Titanbasis und einem Aktivator, der ein wasserlösliches Eisen(II)salz umfasst;
(b) Konditionieren der Mischung, die resultiert aus der wässrigen Suspension von Ton, Sammler und Aktivator mit einem Feststoffgehalt von mindestens 25 Gew.-%, für eine Zeitspanne, die ausreicht, um mindestens 18,387 Kw/h (25 PS-Dampf-Stunden) Energie pro Tonne Feststoffe zuzuführen;
(c) Durchführung einer Flotationsbehandlung mit der konditionierten Mischung zum Verschäumen und Eliminieren der Verunreinigungen auf Titanbasis mit dem Schaum; und
(d) Zurückgewinnen des Tons mit einem verminderten Gehalt an mineralischen Verunreinigungen auf Titanbasis, dadurch gekennzeichnet, dass man in der Stufe (a) zu der wässrigen Tonsuspension ein Reduktionsmittel zugibt.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass man vor dem Mischen der Tonsuspension mit dem Sammler, dem Reduktionsmittel und dem Aktivator die Tonsuspension mit einem oxidierenden Bleichmittel bei einem pH-Wert von etwa 6 bis etwa 7 bleicht.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Konditionierstufe (b) in einem Konditionierbehälter durchgeführt wird und dass die resultierende konditionierte Tonsuspension ohne Verdünnen in eine Flotationsvorrichtung durch Verschäumen überführt wird, in der die Stufen (c) und (d) durchgeführt werden.
4. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Ton mineralische Verunreinigungen auf Eisenbasis enthält, die zu einem Eisen (11)salz reduziert werden können, und dass der Aktivator ein Eisen(11)salz ist, das in situ durch Zugabe des Reduktionsmittels unter Ersatz eines bestimmten Anteils oder der Gesamtmenge des in der Phase (a) zugegebenen Aktivators gebildet worden ist.
5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass es sich bei dem Reduktionsmittel um Natriumhyposulfit handelt.
6. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass es sich bei dem oxidierenden Bleichmittel um Kaliummonopersulfat handelt.
7. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass das Reduktionsmittel in einer Menge von 1,135 bis 6,808 kg pro Tonne zugegeben wird.
8. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Ton eine ausreichende Menge an mineralischen Verunreinigungen auf Eisenbasis, die zu einem Eisen(11)salz reduziert werden können, enthält und dass kein weiterer Aktivator der Phase (a) zugegeben wird.
9. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass vor dem Bleichen durch das Oxidationsmittel die Tonsuspension mittels eines Dispergiermittels dispergiert wird.
10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, dass es sich bei dem Dispergiermittel um Natriumsilikat handelt.
11. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass es sich bei dem Sammler um Ölsäure handelt und dass der Aktivator auch Calciumchlorid umfasst.
12. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass es sich bei dem Sammler um Ölsäure handelt.
13. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Suspension nach der Flotation durch Verschäumen (c) ausgeflockt und mit Hilfe eines reduzierenden Bleichmittels gebleicht wird.
14. Verfahren nach Anspruch 13, dadurch gekennzeichnet, dass die Suspension mit Hilfe von Schwefelsäure ausgeflockt wird und dass es sich bei dem reduzierenden Bleichmittel um Natriumhyposulfit handelt.
15. Verfahren nach Anspruch 13, dadurch gekennzeichnet, dass man vor dem Ausflocken und Bleichen durch das Reduktionsmittel die Suspension sich absetzen lässt und sie durch Dekantation dehydratisiert.
16. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Konditionierstufe (b) bei einem pH-Wert von weniger als 7 durchgeführt wird.
17. Verfahren nach Anspruch 16, dadurch gekennzeichnet, dass die Flotationsstufe (d) anfänglich bei einem sauren pH-Wert und danach bei einem alkalischen pH-Wert durchgeführt wird.
EP83401617A 1982-08-25 1983-08-05 Verfahren zur Behandlung von Ton zur Entfernung von Verunreinigungen auf Titanbasis Expired EP0104961B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US411250 1982-08-25
US06/411,250 US4501658A (en) 1982-08-25 1982-08-25 Method of conditioning clay for flotation using in situ ferrous activator

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EP0104961A2 EP0104961A2 (de) 1984-04-04
EP0104961A3 EP0104961A3 (en) 1985-04-10
EP0104961B1 true EP0104961B1 (de) 1988-08-03

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EP (1) EP0104961B1 (de)
AU (1) AU566885B2 (de)
DE (1) DE3377569D1 (de)

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US4492628A (en) * 1982-08-25 1985-01-08 Freeport Kaolin Company Method of treating clay to improve its whiteness
DE3506808A1 (de) * 1985-02-27 1986-08-28 Henkel KGaA, 4000 Düsseldorf Verfahren zur aufbereitung von kaolinit durch flotation
US4935391A (en) * 1989-03-31 1990-06-19 Fmc Corporation Process for preparing a purified mineral coating
US6068693A (en) * 1997-06-16 2000-05-30 Ecc International Inc. Method for separating mixture of finely divided minerals and product thereof
AUPR820301A0 (en) * 2001-10-12 2001-11-01 Rmg Services Pty. Ltd. Treatment of a wide range of titanium oxide compounds
CN116393258B (zh) * 2023-05-26 2023-09-01 昆明理工大学 一种金红石的高效浮选方法

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US3353668A (en) * 1963-12-16 1967-11-21 Mineral & Chemicals Philipp Co Method for improving the brightness of clay
GB1103585A (en) * 1964-03-02 1968-02-14 English Clays Lovering Pochin Improvements in or relating to the processing of clay
US3462013A (en) * 1967-07-19 1969-08-19 Engelhard Min & Chem Method for beneficiating clay by flotation of colored impurities
US3979282A (en) * 1968-03-11 1976-09-07 English Clays Lovering Pochin & Company Limited Flotation of fine-grained materials
US3655038A (en) * 1970-02-12 1972-04-11 Engelhard Min & Chem Method for improving the brightness of gray sedimentary kaolin clay
US3701417A (en) * 1970-09-28 1972-10-31 Engelhard Min & Chem Purification of clay by selective flocculation
US3923647A (en) * 1972-05-08 1975-12-02 Vojislav Petrovich Froth flotation method for recovery of minerals
US3861934A (en) * 1972-06-13 1975-01-21 Engelhard Min & Chem Method for improving the brightness of kaolin clay
US4186027A (en) * 1976-10-07 1980-01-29 English Clays Lovering Pochin & Company Limited Processing of kaolinitic clays at high solids
US4343694A (en) * 1980-08-25 1982-08-10 Anglo-American Clays Corporation Magnetic beneficiation of clays utilizing magnetic seeding and flotation

Also Published As

Publication number Publication date
AU1836583A (en) 1984-03-01
AU566885B2 (en) 1987-11-05
EP0104961A2 (de) 1984-04-04
EP0104961A3 (en) 1985-04-10
US4501658A (en) 1985-02-26
DE3377569D1 (en) 1988-09-08

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