WO2007088010A1 - Monodisperse , makroporöse chelatharze in der metallgewinnung - Google Patents
Monodisperse , makroporöse chelatharze in der metallgewinnung Download PDFInfo
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- WO2007088010A1 WO2007088010A1 PCT/EP2007/000678 EP2007000678W WO2007088010A1 WO 2007088010 A1 WO2007088010 A1 WO 2007088010A1 EP 2007000678 W EP2007000678 W EP 2007000678W WO 2007088010 A1 WO2007088010 A1 WO 2007088010A1
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- Prior art keywords
- monodisperse
- macroporous
- groups
- bead polymer
- metals
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- 0 C*Cc(ccc1cccnc11)c1O Chemical compound C*Cc(ccc1cccnc11)c1O 0.000 description 2
Classifications
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- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J45/00—Ion-exchange in which a complex or a chelate is formed; Use of material as complex or chelate forming ion-exchangers; Treatment of material for improving the complex or chelate forming ion-exchange properties
-
- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
-
- 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
- the present invention relates to the use of monodisperse, macroporous ion exchangers with conjugating groups, also referred to below as monodisperse, macroporous chelating resins, in metal extraction in hydrometallurgy processes, in particular in so-called resin in PuIp processes (R.I.P processes).
- the metals of value relevant for industrial use are found in ore minerals, which are mined by mining. The ore then in larger chunks is ground into small particles. From these rock particles, the recyclables can be removed by several methods.
- the common technique is hydrometallurgy, also known as wet metallurgy.
- a distinction is made between two stages, namely the conversion of the compounds into aqueous metal salt solutions with the aid of acids or alkalis, optionally after pretreatment of the ores, to produce soluble compounds (roasting, pyrogenic digestion).
- the choice of the solvent is determined by the type of metal, its binding present in the ore, the type of ore companion (gait) and the price.
- the most widely used solvent is sulfuric acid, besides hydrochloric acid, nitric acid and hot concentrated saline solutions.
- ammoniacal solutions can also be used, sometimes even at high pressure and elevated temperature (pressure leaching).
- Sodium hydroxide is used for the extraction of alumina, for precious metals alkali cyanide solutions are used.
- the recovery of metals in hydrometallurgy may be by precipitation by means of a less noble metal (cementation), by reduction with hydrogen or carbon monoxide at high pressure (pressure precipitation) or by electrolysis using insoluble electrodes or by crystallization (sulphates of copper, Zinc, nickel or thallium) by conversion (precipitation) into sparingly soluble compounds such as hydroxides, carbonates or basic salts by means of chalk, milk of lime or soda solution.
- the extraction of the metals from the rock can also be carried out by other methods.
- the type of process used depends on several factors, such as the ore content of the ore, the particle size at which the crushed ore was ground, or the equipment conditions, to name but a few.
- the so-called heap leach method uses relatively coarse ore particles with a low metal content.
- the agitation leach process uses finer ore particles (about 200 ⁇ m) with high metals content in the leach process.
- the size of the milled ore particles to be used in these methods is in the range of about 30 - about 250 microns. Because of the small size of the particles and the large amount of rock, a classic filtration of the particles from the liquid phase to nutsche is very expensive. In most cases a separation according to the gravitational principle in decanters is applied by settling the solid phase in very large agitator vessels. In order to obtain a good separation with a particle-free material solution as possible, stirred vessels with a diameter of 50 meters and more are used, several of them in series. Large amounts of water are needed, which are very expensive, as many mines are located in arid areas (deserts). In addition, for better separation of the particles often filtration media that are expensive and polluting the environment, are used.
- Valuable metals are operated, process steps of filtration and clarification represent a high proportion of the capital costs of the plant and the current operating costs.
- New processes of this type are carbon in PuIp processes for silver and gold and resin in PuIp (RIP) process for gold, cobalt, nickel and manganese.
- the RIP process for gold recovery using ion exchangers is described, for example, in CA. Fleming, Recovery of gold by Resin in Pulp at the Golden Jubilee Mine, Precious Metals 89, edited by MCJha and SD Hill, TMS, Warrendale, Pa., 1988, 105-119 and in CA. Fleming, Resin in pulp as to an alternative process for cyanide leach slurries, Proceedings of 23 Canadian Mineral Processors Conference, Ottawa, January 1991.
- resins are used in US Pat. No. 6,350,420, which are described in US Pat. Nos. 4,098,867 and 5,141,965. Accordingly, suitable resins are Rohm & Haas ER 904, a strongly basic macroporous anion exchanger, Amberlite XE 318, Dow XFS-43084, Dow XFS-4195 and Dow XFS-4196.
- the ion exchangers described in US 4,098,867 and US 5,141,965 contain differently substituted aminopyridine, in particular 2-picolylamine groups. All ion exchangers described there have a heterodisperse bead diameter distribution. In US Pat. No. 5,141,965, the ion exchanger shows bead diameters in the range 0.1-1.5 mm, preferably 0.15-0.7 mm, most preferably 0.2-0.6 mm. The ion exchangers described in US Pat. No. 4,098,867 have bead diameters between 20-50 mesh (0.3 mm-0.850 mm), or larger diameters.
- Rohm & Haas IR 904, a strongly basic macroporous anion exchanger and Amberlite XE 318 are also heterodisperse ion exchangers with bead diameters in the range of 0.3 - 1.2 mm.
- the methods discussed in the above prior art have several disadvantages. Thus, it is found that the loading of the ion exchange beads with the metals, eg cobalt and nickel, in the RIP process is uneven, resulting in significant losses of the metals to be recovered.
- the ion exchangers loaded with the metals to be recovered are separated via sieves from the fine ore particles and the exhausted solution.
- the mesh size of the sieves must be such that the loaded ion exchange beads remain on the sieve, but the ore particles and the solution can flow through unhindered.
- the chelate resins to be used in accordance with US Pat. No. 6,350,420 have bead diameters in the range 0.1-1.5 mm and are thus of almost the same order of magnitude as the ore particles to be extracted with a size distribution in the range between 30 ⁇ and 250 ⁇ . It has been shown that this leads to blockages in the screening and to a poor separation of the ion exchanger from the particles.
- the separation process is slowed down, larger amounts of water are necessary in order to slurry the particle / ion exchange material and thus be able to better sieve it.
- the separation process is worsened and can only be operated economically by the use of additional separation gate.
- the object of the present invention was therefore to improve the RIP process to the extent that the disadvantages of the prior art described above are avoided and thus to a higher yield of valuable metals, less water consumption, less equipment and ultimately leads to an economically improved process.
- the solution of the problem and thus the subject of the present invention is the use of monodisperse ion exchangers, preferably monodisperse, macroporous chelating resins in the R.I.P. process for the extraction of metals from their ores.
- the monodisperse, macroporous chelate exchangers to be used according to the invention contain functional groups of the series aminoacetic acid and / or iminodiacetic acid, aminomethylphosphonic acid, thiourea, mercapto, picolinamino or optionally weakly acidic groups, preferably carobxyl groups, in addition to the chelating group.
- the monodisperse, macroporous chelating resins to be used in accordance with the invention in R.I.P. processes show significantly higher yields of metals to be recovered with reduced water requirement, reduced apparatus expenditure and fewer losses of ion exchanger than a R.I.P. Process operated according to the prior art with heterodisperse ion exchangers.
- the monodisperse, macroporous chelate exchangers to be used in the RIP process according to the invention also have the advantages of lower pressure loss, higher loading rates, equally long diffusion paths through the beads but with better kinetics, higher separation capacity, sharper separation zones, lower chemical use during elution and higher Perlstabiltician.
- the advantage of using monodisperse, macroporous chelating resins in the RIP process is also the fact that due to the jetting process or seed-feed process in the preparation of the ion exchanger precursor, the monodisperse, macroporous bead polymers, the average bead diameter of the ion exchange beads Already during their production can be matched exactly to the particle size of the ore and the mesh size of the sieves.
- monodisperse, macroporous chelating resins The preparation of monodisperse, macroporous chelating resins is known in principle to a person skilled in the art.
- a monodisperse feed is used, which in turn can be produced, for example, by sieving or by jetting.
- monodisperse chelate resins prepared by seed-feed or jetting processes are used.
- D 60 describes the diameter at which 60% by mass is smaller or equal to 40% in the distribution curve.
- D 10 denotes the diameter at which 10% by mass is smaller in the distribution curve and 90% by mass larger are the same.
- the monodisperse bead polymer the precursor of the ion exchanger
- monodisperse optionally encapsulated monomer droplets comprising a monovinylaromatic compound, a polyvinylaromatic compound and an initiator or initiator mixture and optionally a porogen in aqueous suspension.
- the optionally encapsulated monomer droplets are doped with a (meth) acrylic compound and then polymerized.
- microencapsulated monomer droplets are used for the synthesis of the monodisperse bead polymer.
- the person skilled in the art is aware of the various preparation processes of monodisperse bead polymers both according to the jetting principle and according to the seed-feed principle known from the prior art. Reference may be made to US Pat. No. 4,444,961, EP-A 0 046 535, US Pat. No. 4,419,245 and WO 93/12167.
- EP-A 1078690 describes a process for the preparation of monodisperse ion exchangers with chelating functional groups by the so-called phthalimide process by
- the monodisperse, macroporous chelate exchangers prepared according to EP-A 1078690 carry the chelating groups which form during process step d)
- Rl is hydrogen or a radical CH 2 -COOH or CH 2 P (O) (OH) 2
- R 2 is a radical CH 2 COOH or CH 2 P (O) (OH) 2 and
- n stands for an integer between 1 and 4.
- such chelating resins are referred to as resins having aminoacetic acid groups and / or with iminodiacetic acid groups or with aminomethylphosphonic acid groups.
- Chelate exchangers with SH groups are likewise suitable for the R.I.P. process in the context of the present invention. These resins are readily accessible by hydrolysis of the latter chelating thiourea group exchangers.
- Groups contain by reacting monomer droplets from a mixture of a monovinylaromatic compound, a polyvinyl aromatic compound, a (meth) acrylic compound, an initiator or an initiator combination and optionally a porogen to a crosslinked bead polymer, the resulting bead polymer with chelating
- n 1 to 4
- R 1 is hydrogen or a radical CH 2 -COOR 3 or CH 2 P (O) (OR 3 ) 2 or -CH 2 -S-CH 2 COOR 3 or -CH 2 -SC j -C 4 -alkyl or
- R 2 is a radical CH 2 COOR 3 or CH 2 P (O) (OR 3 ⁇ or -CH 2 -S-CH 2 COOR 3 or -CH 2 -SC! C 4 alkyl or -CH 2 -S-CH 2 CH (NH 2 ) COOR 3 or
- R 3 is H or Na or K.
- picolinamine resins New and not yet described are monodisperse, macroporous chelating resins with weakly basic groups, so-called picolinamine resins.
- the subject of the present application is therefore also a process for the preparation of choline resins containing picolinamino groups, characterized in that
- a) produces a monodisperse, macroporous bead polymer based on styrene, divinylbenzene and ethylstyrene according to the above-described prior art either by jetting or by a seed-feed process,
- this new chelating resin can according to the invention in R.I.P. Process, which is also the subject of the present invention, as well as the monodisperse, macroporous chelating resins with picolinamino groups themselves, are the subject of the present invention. These are available through
- this new chelate resin may be macroporous or gelatinous.
- the macroporous, monodisperse picolinamino group-containing chelating resins are the macroporous, monodisperse picolinamino group-containing chelating resins to prefer.
- the monodisperse, macroporous chelate resins to be used according to the invention in the R.I.P. process can be adapted in terms of process engineering with their bead diameter to the mesh size of the sieves to be used in the R.I.P. process.
- the mesh size of the sieves is usually in the range of about 300 ⁇ - 600 ⁇ .
- the size of the ore particles themselves should be smaller than the mesh size of the sieves, which on the one hand requires a corresponding pretreatment of the ores by grinding or acid treatment.
- the size of the ground ore particles for use in the R.I.P. process is usually in the range of about 30 to about 250 microns.
- monodisperse, macroporous chelating resins having an average bead diameter in the range from 0.35-1.5 mm, preferably 0.45-1.2 mm, particularly preferably 0.55-1.0 mm, are most suitable.
- the specified bead diameters refer to the commercial or delivery form.
- the bead diameter decreases slightly, in many cases by about 4-10%.
- the monodisperse, macroporous chelate exchangers to be used according to the invention are metered in the R.I.P. process, preferably under atmospheric pressure, to the ore particle suspension obtained after the acid treatment. After completion of the metered addition, the resulting chelate exchanger-containing suspension is stirred for 5 minutes to 10 hours, preferably between 15 minutes and 3 hours, as the reaction time.
- the temperature at which the ion exchangers in the RIP process are brought into contact with the ore particle suspension obtained after the acid treatment can be freely selected over a wide range. It is in the range between ambient temperature and 160 0 C. Preference is given to temperatures in the range 60 - 9O 0 C. In general, working is carried out without pressure. However, it has been found that the higher the temperature selected during the treatment, the faster the loading of the chelating agent with the metals to be recovered takes place.
- the pH of the suspension is increased by the addition of neutralizing agents.
- the optimum pH is generally at pH 1 to 6, preferably 2.5 to 4.5 and can be easily determined by simple preliminary tests.
- Suitable neutralizing agents are e.g. Lime (lime), magnesium hydroxide or caustic soda.
- the contacting of suspension and chelate resin can be carried out in one stage.
- a multi-step process for. B. in the form of a cascade method apply.
- the cascade process can be done in cocurrent or counter current.
- cocurrent or counter current By this is meant that the ion exchanger and the metal-containing suspension in the same direction or in the opposite direction is passed through the system. Erf ⁇ ndungshunt the countercurrent process is preferred because it leads to a particularly effective utilization of the metal contents in the ore.
- the eluted chelate resin can be used for other loading / unloading cycles. In the case of the countercurrent cascade process, it is returned directly to the circulation.
- the metal to be recovered is separated by elution from the loaded chelate exchanger by elution with mineral acids such as sulfuric acid or hydrochloric acid.
- concentration of the mineral acids is in the range of 1-30 wt.%, Preferably 6 to 15 wt.%.
- the separation of the metal from the chelating resin can also be carried out with complexing solutions, such as ammoniacal solutions.
- the recovered metal-containing solution is usually subjected to further purification processes, as they are commonly used in metal extraction.
- macroporous chelating resins in the R.I.P. process metals include IE. To VI. Main group and the 5th to 12th subgroup of the Periodic Table of the Elements.
- Preferred metals to be obtained by the RIP process according to the invention with monodisperse, macroporous chelate exchangers are mercury, iron, titanium, chromium, tin, cobalt, nickel, copper, zinc, lead, cadmium, manganese, uranium, bismuth, vanadium, and platinum group elements Ruthenium, osmium, iridium, rhodium, palladium, platinum and the precious metals gold and silver. Particular preference is given to obtaining cobalt, nickel, copper, zinc, rhodium, gold and silver in this manner.
- the present invention also relates to a method for recovering metals from their ores according to the principle of resin in PuIp, characterized in that
- a metal-containing optionally previously by roasting or by pyrogenic digestion, processed ore into particles of size smaller than 0.5 mm and the milled ore with acids, preferably sulfuric acid, hydrochloric acid, nitric acid or mixtures thereof with each other, for dissolving out the metals to be recovered offset
- the metal-loaded chelate resin is filtered off from the accompanying material by means of a sieve and optionally washed to remove residual particles,
- Ores to be used according to the invention are lateritic ores, limonite ores, pyrrothin, smaltine, cobaltine, linseed, magnetic gravel and other iron, nickel, cobalt, copper, zinc, silver, gold, titanium, chromium, tin, magnesium, arsenic, manganese, aluminum, other platinum , Precious metals, heavy metals and ores containing alkaline earth metals. Examples
- the microcapsule consists of a formaldehyde-cured complex coacervate of gelatin and a copolymer of acrylamide and acrylic acid. Finally, 3200 g of aqueous phase with a pH of 12 are added. The average particle size of the monomer pots is 460 microns.
- the mixture is polymerized while stirring by increasing the temperature according to a temperature program at 25 0 C and ending at 95 ° C.
- the mixture is cooled, washed through a 32 micron sieve and then dried in vacuo at 80 0 C. This gives 1893 g of a spherical bead polymer having an average particle size of 440 .mu.m, narrow particle size distribution and smooth surface.
- the bead polymer is chalky white in the plan and has a bulk density of about 370 g / l.
- Elemental Analytical Composition Carbon: 75.3 wt%; Hydrogen: 4.6% by weight; Nitrogen: 5.75% by weight;
- amidomethylated polymer beads from Example Ib 851 g of 50 wt .-% sodium hydroxide solution and 1470 ml of deionized water are added at room temperature. The suspension is heated to 180 ° C. and stirred for 8 hours at this temperature.
- the resulting bead polymer is washed with demineralized water.
- Elemental Analytical Composition Carbon: 78.2 wt%; Nitrogen: 12.25% by weight; Hydrogen: 8.4% by weight.
- a mixture of 3200 g of microencapsulated monomer droplets with a narrow particle size distribution prepared from a monomer mixture of 3.6% by weight of divinylbenzene and 0.9% by weight of ethylstyrene (used as a commercially available isomer mixture of divinylbenzene and ethylstyrene with 80% divinylbenzene ), 0.5% by weight of dibenzoyl peroxide, 56.2% by weight of styrene and 38.8% by weight of isododecane (technical mixture of isomers with a high proportion of pentamethylheptane) are added.
- the microcapsule itself consists of a formaldehyde-cured complex coacervate of gelatin and a copolymer of acrylamide and acrylic acid. Finally, 3200 g of aqueous phase with a pH of 12 are added. The average particle size of the monomer droplets is 460 ⁇ m.
- the mixture is polymerized while stirring by increasing the temperature according to a temperature program at 25 0 C and ending at 95 ° C.
- the mixture is cooled, washed through a 32 micron sieve and then dried in vacuo at 80 0 C. This gives 1893 g - i ⁇ - a spherical bead polymer having an average particle size of 440 microns, narrow particle size distribution and smooth surface.
- the bead polymer is chalky white in the plan and has a bulk density of about 370 g / l.
- the resulting bead polymer is washed with demineralized water.
- Elemental analytical composition Carbon: 82.2% by weight
- 1520 ml of aminomethylated bead polymer from Example 2c) are added at room temperature to 1520 ml of demineralized water.
- the suspension is heated to 9O 0 C.
- 713.3 g of monochloroacetic acid are metered in at 90 0 C.
- the pH is maintained by metering of 50 wt .-% sodium hydroxide solution at pH 9.2.
- the suspension is heated to 95 ° C and the pH adjusted to 10.5. It is stirred for a further 6 hours at this temperature.
- the mean bead diameter is 602 ⁇ .
- the equality coefficient is 1.04.
- the unit coefficient is 0.586.
- the suspension is heated to 7O 0 C and stirred for a further 6 hours at this temperature.
- the reaction broth is drawn off, demineralized water is metered in, and residual amounts of dichloroethane are removed by distillation.
- the resulting bead polymer is washed with demineralized water.
- 1,500 ml of aminomethylated bead polymer from Example 3c) are added at room temperature to 1500 ml of demineralized water.
- the suspension is heated to 90 0 C. 705 g of monochloroacetic acid are metered in at 90 ° C. in the course of 4 hours.
- the pH is maintained at pH 9.2 by metering in 50% strength by weight sodium hydroxide solution.
- the suspension is heated to 95 ° C. and the pH is adjusted to 10.5. It is stirred for a further 6 hours at this temperature. Thereafter, the suspension is cooled.
- the resin is washed free of chloride with demineralized water.
- the ion exchanger is separated from the suspension.
- concentration of nickel and cobalt ions in the suspension before and after treatment with the ion exchanger are measured - see Table 1.
- Example 2 Sodium hydroxide solution, the pH of the suspension is adjusted to pH 2.5. Subsequently, 25 ml of a monodisperse, macroporous chelate resin with iminoacetic acid groups (see Example 2) are metered. The suspension is stirred for 5 hours at room temperature.
- the ion exchanger is separated from the suspension.
- concentration of nickel and cobalt ions in the suspension before and after treatment with the ion exchanger are measured - see Table 1.
- the results from Table 1 show surprisingly clearly that a monodisperse chelate resin is able to remove nickel and / or cobalt ions in larger quantities from a leach suspension, as a heterodisperse chelate resin according to the prior art.
- the resin is again transferred to the column. 1000 ml of 2% strength by weight sodium hydroxide solution are filtered over. Subsequently, the resin is washed alkali-free with demineralized water to a pH value of 8 in the eluate. The resin is rinsed in a tamping volumeter under demineralised water and shaken to volume consistency - volume V2 of the resin in the free base form (OH - form).
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Abstract
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Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BRPI0707473-5A BRPI0707473A2 (pt) | 2006-02-01 | 2007-01-26 | uso de trocador de quelação, processo para produção de metais de seus minérios, processo para produção de grupos picolinamino contendo resina de quelação e grupo picolinamino contendo resina de quelação |
AU2007211680A AU2007211680A1 (en) | 2006-02-01 | 2007-01-26 | Monodisperse, macroporous chelating resins in metal winning |
CA002640479A CA2640479A1 (en) | 2006-02-01 | 2007-01-26 | Chelating resins in metal recovery |
US12/087,632 US20090158896A1 (en) | 2006-02-01 | 2007-01-26 | Monodisperse, Macroporous Chelating Resins in Metal Winning |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DE102006004953A DE102006004953A1 (de) | 2006-02-01 | 2006-02-01 | Chelatharze in der Metallgewinnung |
DE102006004953.5 | 2006-02-01 |
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WO2007088010A1 true WO2007088010A1 (de) | 2007-08-09 |
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PCT/EP2007/000678 WO2007088010A1 (de) | 2006-02-01 | 2007-01-26 | Monodisperse , makroporöse chelatharze in der metallgewinnung |
Country Status (8)
Country | Link |
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US (1) | US20090158896A1 (de) |
AU (1) | AU2007211680A1 (de) |
BR (1) | BRPI0707473A2 (de) |
CA (1) | CA2640479A1 (de) |
DE (1) | DE102006004953A1 (de) |
RU (1) | RU2434062C2 (de) |
WO (1) | WO2007088010A1 (de) |
ZA (1) | ZA200806595B (de) |
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WO2009013142A2 (de) * | 2007-07-23 | 2009-01-29 | Lanxess Deutschland Gmbh | Chelatharze |
EP2025387A1 (de) * | 2007-07-23 | 2009-02-18 | LANXESS Deutschland GmbH | Verfahren zur Herstellung monodisperser Chelatharze |
WO2009109520A1 (de) | 2008-03-03 | 2009-09-11 | Lanxess Deutschland Gmbh | Picolylaminharze |
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US20100252506A1 (en) * | 2007-07-23 | 2010-10-07 | Lanxess Deutschland Gmbh | Method for producing chelate resins |
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- 2007-01-26 RU RU2008134862/02A patent/RU2434062C2/ru not_active IP Right Cessation
- 2007-01-26 CA CA002640479A patent/CA2640479A1/en not_active Abandoned
- 2007-01-26 US US12/087,632 patent/US20090158896A1/en not_active Abandoned
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US8177982B2 (en) | 2007-07-23 | 2012-05-15 | Lanxess Deutschland Gmbh | Method of producing monodisperse chelate resins |
EP2025387A1 (de) * | 2007-07-23 | 2009-02-18 | LANXESS Deutschland GmbH | Verfahren zur Herstellung monodisperser Chelatharze |
WO2009013142A3 (de) * | 2007-07-23 | 2009-06-25 | Lanxess Deutschland Gmbh | Chelatharze |
WO2009013142A2 (de) * | 2007-07-23 | 2009-01-29 | Lanxess Deutschland Gmbh | Chelatharze |
US20130245140A1 (en) * | 2007-07-23 | 2013-09-19 | Lanxess Deutschland Gmbh | Chelate resins |
US20100252506A1 (en) * | 2007-07-23 | 2010-10-07 | Lanxess Deutschland Gmbh | Method for producing chelate resins |
US20100307979A1 (en) * | 2007-07-23 | 2010-12-09 | Lanxess Deutschland Gmbh | Chelate resin |
US8506818B2 (en) * | 2007-07-23 | 2013-08-13 | Lanxess Deutschland Gmbh | Method for producing chelate resins |
US8563622B2 (en) * | 2008-03-03 | 2013-10-22 | Lanxess Deutschland Gmbh | Picolylamine resins |
US20110091365A1 (en) * | 2008-03-03 | 2011-04-21 | Lanxess Deutschland Gmbh | Picolylamine resins |
US20110086935A1 (en) * | 2008-03-03 | 2011-04-14 | Lanxess Deutschland Gmbh | Picolylamine resins |
WO2009109522A1 (de) * | 2008-03-03 | 2009-09-11 | Lanxess Deutschland Gmbh | Picolylaminharze |
US8562922B2 (en) * | 2008-03-03 | 2013-10-22 | Lanxess Deutschland Gmbh | Picolylamine resins |
WO2009109520A1 (de) | 2008-03-03 | 2009-09-11 | Lanxess Deutschland Gmbh | Picolylaminharze |
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WO2011067340A1 (de) * | 2009-12-04 | 2011-06-09 | Lanxess Deutschland Gmbh | Methylenaminoethylsulfonsäure-chelatharze |
WO2017013110A1 (de) * | 2015-07-20 | 2017-01-26 | Lanxess Deutschland Gmbh | Aluminiumdotierte, iminoessigsäuregruppe enthaltende chelatharze |
CN107849179A (zh) * | 2015-07-20 | 2018-03-27 | 朗盛德国有限责任公司 | 新颖的铝掺杂的、含亚氨基乙酸基团的螯合树脂 |
CN107849179B (zh) * | 2015-07-20 | 2019-12-13 | 朗盛德国有限责任公司 | 新颖的铝掺杂的、含亚氨基乙酸基团的螯合树脂 |
CN109112316A (zh) * | 2018-10-15 | 2019-01-01 | 郴州市金贵银业股份有限公司 | 一种高效选择性分离铋渣中铜的方法 |
Also Published As
Publication number | Publication date |
---|---|
ZA200806595B (en) | 2009-10-28 |
BRPI0707473A2 (pt) | 2011-05-03 |
AU2007211680A1 (en) | 2007-08-09 |
DE102006004953A1 (de) | 2007-08-02 |
CA2640479A1 (en) | 2007-08-09 |
RU2008134862A (ru) | 2010-03-10 |
US20090158896A1 (en) | 2009-06-25 |
RU2434062C2 (ru) | 2011-11-20 |
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