Stripping Of Cobalt Research Articles

Recovery of Samarium and Cobalt from Sm–Co Magnet Waste Using a Phosphonium Ionic Liquid Cyphos IL 104

Due to outstanding thermal stability and corrosion resistance, samarium–cobalt alloy is being used in rare earth magnet. So, this permanent magnet waste can be a potential source for rare earth metal samarium and critical metal cobalt. Recovery and reuse of Sm, Co from Sm–Co magnet waste can reduce the burden on primary resources and environmental issues related to primary resources. In this work, a hydrometallurgical method for recovery of samarium and cobalt from Sm–Co magnet waste has been developed using an ionic liquid Cyphos IL 104. The optimum separation condition for cobalt and samarium has been determined by varying the concentration of HCl, NaCl, and mixture of HCl and NaCl in the leach liquor. The McCabe–Thiele plot is constructed using 0.075 mol/L Cyphos IL 104. Three counter-current stages at A:O ratio of 1:1.5 are needed for complete extraction of cobalt into the ionic liquid phase leaving samarium in the raffinate. Precipitation stripping of cobalt from the loaded organic is carried out using oxalic acid and the cobalt oxalate, thus formed, is calcined at 450 °C to form Co3O4. The raffinate obtained from the counter-current extraction contains 2.02 g/L Sm and 0.02 mg/L Co. Sm2O3 from raffinate is produced by precipitation of samarium with oxalic acid followed by calcination of samarium oxalate at 800 °C. Both the oxide products are confirmed by XRD.

Cobalt Extraction from Sulfate/Chloride Media with Trioctyl(alkyl)phosphonium Chloride Ionic Liquids.

The application of phosphonium-based ionic liquids (ILs) on the selective extraction of cobalt is presented. The extraction mechanism is established, and different parameters of the process are evaluated. It has been found that it is possible to extract cobalt from aqueous solutions in sulfate media, with the addition of sodium chloride, using phosphonium ILs. The cobalt extraction was selective with respect to nickel and strongly dependent on the chloride concentration in the aqueous solution. The cobalt extraction is given by an anion exchange mechanism through an endothermic process. Cobalt extractions greater than 98% were obtained using the proposed methods. Cobalt stripping from the loaded IL phase using water was proved. Therefore, an alternative extraction process to traditional organic solvents is proposed. This alternative has additional advantages such as easy handling, lower costs in reagents and equipment, and risk reduction.

A Comparative Study of Experimental Optimization and Taguchi Design of Co(II) Recovery by Aliquat 336 as Ionic Liquid Carrier

Experiments of extraction and stripping of cobalt(II) were carried out. The liquid–liquid extraction process was considered, in which the organic phase was constituted of Aliquat 336 extractant that is the quaternary ammonium salt, and oleyl alcohol modifier dissolved in dodecane where the aqueous phase contained the metal ion in a concentrated hydrochloric acid solution. The optimization of Co(II) recovery was determined by optimizing one parameter at the time. Therefore, several experimental parameters such as Aliquat 336 concentration, extraction time, hydrochloric acid concentration, and the initial concentration of metal ion were studied. The cobalt(II) ions were extracted at 62.5% and stripped from the metal-loaded organic phase at 41.0% by distilled water as stripping agent. The mass balances were checked for all the studied parameters with an average deviation percentage of 2%. In fact, the McCabe–Thiele showed six theoretical stages for total recovery of cobalt. The separation tests of Co(II) and Ni(II) were carried out on the basis of the optimal conditions of Co(II) recovery. It showed that the nickel ions were slightly extracted (< 10%) whatever the composition of mixture. A Taguchi design with a L4 orthogonal array was used for the statistical study to determine the influence and the contribution percentage of certain experimental parameters on the Co(II) extraction. Analysis of variance and analysis of means showed a total absence of the uncontrollable factors (noise), in which the chosen model has described our extraction process with accuracy. In fact, only the main effects without interaction of controllable factors (A, B, and C) contribute to the optimal extraction of cobalt as follows: A (50.10%), B (28.33%), and C (21.47%) at levels: 2/2/1 with high signals as 32.07, 28.38 and 25.13, respectively.

Solvent extraction process for the selective recovery of copper and cobalt from carrollite leach solution

A solvent extraction application consisting of three-sequential solvent extraction steps to selectively recover the copper and cobalt from carrollite leach solution was conceived and experimentally explored. The first step allowed the simultaneous extraction of 95.5% copper, 0.87% cobalt and 4.79% iron using 20% Lix984 in sulfonated kerosene and O/A ratio of 1 at initial pH of 2. Two-stage scrubbing at pH = 4 using diluted sulphuric acid solution allowed the removal of most of the cobalt (98.56%), iron (97.25%) and small amount of copper (0.36%). Complete stripping of copper was achieved at H2SO4 concentration of 1.5 mol/L and an O:A ratio of 1. This raffinate was the feed for the second step. The use 30% P204 in sulfonated kerosene, sodium-saponification rate of 30% and initial pH of 2.5 allowed the removal of 100% iron, 98.45% zinc, 93.64% calcium and 22.77% magnesium under the O:A ratio of 1 but with substantial co-removal of cobalt (8.23%). Two-stage scrubbing of this loaded organic phase at pH = 2.5 using diluted sulphuric acid solution allowed the extraction of most of the cobalt (92.75%). This raffinate was the feed for the third step. The simultaneous extraction of 99.08% cobalt, 5.12% magnesium and 2.87% nickel was found using 35% P507 in sulfonated kerosene, sodium-saponification rate of 65% and initial pH of 4 at an O:A ratio of 1:2. Two-stage scrubbing at pH = 3.5 using diluted sulphuric acid solution allowed the removal of most of the magnesium (96.82%), nickel (93.49%) and small amount of cobalt (2.87%). Complete stripping of cobalt was achieved at H2SO4 concentration of 1.0 mol/L at an O:A ratio of 3:1. Meanwhile, as long as the phase ratio (O/A) of extraction and stripping were properly controlled, this diluted cobalt solution can be concentrated before being sent to a subsequent step such as recovery of the metal by electrowinning. Based on the experimental results, a flowsheet for the extraction process is presented.

Simultaneous extraction and separation of cobalt and nickel from chloride solution through emulsion liquid membrane using Cyanex 301 as extractant

In the present work, emulsion liquid membrane (ELM) is investigated to select the suitable conditions for extraction of Co (II) ions from acidic chloride solutions using Cyanex 301 as extractant. The effects of extractant and surfactant concentrations, mixing speed, concentration and type of stripping solution, phase ratio, treatment ratio, and nature of diluent on the extraction rate were studies. Under the optimum conditions, extraction of cobalt in competition with nickel has been also studied for different feed mixture solution. Solvent extraction and stripping of cobalt and nickel in mixture was first carried out in order to have an idea about this extractant. Solvent extraction results show that almost 99% of cobalt and nickel are extracted with 0.1M Cyanex 301 at pH above 2 within 2min. However, Based on the stripping process, it was possible to separate cobalt and nickel at low acid concentration (0.5M) with separation factor of 502. ELM results show that under the optimum conditions, the system is selective for cobalt than nickel, especially within the first minutes of all experiments.

Solvent extraction process for the recovery of nickel and cobalt from Caldag laterite leach solution: The first bench scale study

A solvent extraction application consisting of two-sequential solvent extraction circuits to separate the nickel and cobalt from a synthetic sulphate leach solution which simulates a typical Caldag lateritic leach solution was conceived and experimentally explored. The first circuit allowed the simultaneous extraction of most of the nickel (98%), cobalt (98%) and manganese (94%) with 20% neodecanoic acid (Versatic 10) and 5% tri-n-butyl phosphate (TBP) in ShellSol 2046 at pH7.2 together with substantial amounts of calcium (65%) and magnesium (12%). Three stages of scrubbing at pH5.6 using diluted sulphuric acid solution allowed the removal of most of the magnesium (90%) and substantial amount of calcium (16%). Complete stripping of nickel, cobalt, manganese, magnesium and calcium was achieved at pH0.75. This loaded strip solution was the feed for the second circuit. The use 15% bis(2,4,4-trimethylpentyl) phosphinic acid (Cyanex 272) and 5% TBP in ShellSol 2046 allowed the extraction of most of the cobalt (94%) and manganese (98%) at pH5.0 but with substantial co-extraction of magnesium (41%) and calcium (40%) and a minor amount of nickel (3%). A two-stage scrubbing of this loaded organic with cobalt (20g L−1) solution was performed. Magnesium, calcium and nickel were completely displaced with cobalt. Most of the manganese (93%) was removed from the organic. Complete stripping of the cobalt and manganese in the scrubbed organic phase was achieved at pH1.0. Therefore, nickel (94%) and cobalt (91%) were totally separated from the feed solution. In addition, slope analyses were carried out to determine the nature of the extracted complexes of the nickel and cobalt with each extractant. Based on the experimental results, a flowsheet for the separation process is presented.

Selective recovery of cobalt, nickel and lithium from sulfate leachate of cathode scrap of Li-ion batteries using liquid-liquid extraction

This paper focuses on the extractive separation and selective recovery of cobalt, nickel and lithium from the sulfate leachate of cathode scrap generated during manufacture of lithium ion batteries (LIBs). The conditions for extraction, scrubbing and stripping of cobalt from nickel and lithium are optimized with an aqueous feed containing 25.1 g·dm−3 cobalt, 2.54 g·dm−3 nickel and 6.2 g·dm−3 lithium using Na-PC-88A. 99.8% Co is extracted with 60% Na-0.56 mol·dm−3 PC-88A in two counter-current stages at an O/A phase ratio of 3/1 and an equilibrium pH of 4.5. The “crowding effect” shown for the first time provides effective scrubbing of impurities (Ni and Li) with 2.0 g·dm−3 CoSO4 solution. The McCabe-Thiele diagram predicts the scrubbing of 99.9% Ni and 99.9% Li at an equilibrium pH of 4.75 and O/A of 2/1 in two stages. High purity (99.9%) cobalt sulfate along with Ni and Li from the leach liquor of cathode scrap is recovered by solvent extraction. The proposed process ensures complete recycling of the waste of the manufacturing process of LIBs.

Evaluating a solvent extraction process route incorporating nickel preloading of Cyanex 272 for the removal of cobalt and iron from nickel sulphate solutions

Crude nickel sulphate solutions are produced during the first stage leach of Platinum Group Metal (PGM) containing converter matte in a Sherrit® atmospheric matte leach process. Iron and cobalt sulphates contaminate the nickel sulphate stream due to dissolution during the matte leach process. While iron is an unwanted contaminant, cobalt sulphate production presents a potentially valuable by-product, as long as removal of these metal ions does not introduce other forms of contamination into the solution.Experimental work was performed to evaluate the removal of 1g/l cobalt and 3g/l iron from a sulphuric acid leach solution containing 80g/l nickel using solvent extraction with Ni-Cyanex 272. The effects of various process parameters on preloading, extraction, and stripping were investigated. Based on full factorial experimental designs, the parameters with the largest effects on the process performance were determined to be pH and organic/aqueous (O/A) ratio for preloading, nickel loading and O/A ratio for extraction, and H2SO4 concentration and O/A ratio for stripping. These variables were evaluated in further batch experiments to determine conditions that would allow the production of a high purity nickel sulphate solution and selective stripping of cobalt and iron from the organic phase, and the batch tests results were validated by performing continuous tests on a laboratory scale mixer-settler setup. A flow sheet that allows the production of refined nickel sulphate and cobalt sulphate solutions by extraction with nickel preloaded Cyanex 272 and selective stripping has been proposed. Regeneration of the organic phase is achieved by stripping with 1M sulphuric acid, which yields an iron containing aqueous stream as effluent.

Separation of Co (II) and Ni (II) from the mixed sulphate/chloride solution using NaPC-88A

The mixed sulphate/chloride leach liquor of manganese nodules bearing 11.8 iron, 24.8 copper, 0.23 zinc, 3.8 cobalt, 35.2 nickel, 176.3 chloride and 48.9 sulphate in g/L was processed for separation of Fe, Cu and Zn and the leach liquor free from Fe, Cu and Zn was used for separation of cobalt and nickel with 75% saponified 0.09 M and 0.7 M PC-88A, respectively in which the effect of pH, extractant concentration and organic to aqueous phase ratio was studied. For extraction of a mole of cobalt and a mole of nickel separately, two moles of the extractants were used to release a mole of H + ion into the aqueous phase in each case. The extraction of cobalt was carried out in 2 stages at a 1:1 phase ratio, and extraction of nickel was carried out in 2 stages at an organic to aqueous phase ratio of 4:5. The extracted species were CoA 2.3HA and NiA 2.3HA. The stripping of cobalt loaded organic was carried out with 5 g/L H 2SO 4 in 2 stages at an organic to aqueous phase ratio of 2:1, and stripping of the nickel loaded organic was carried out with 144 g/L H 2SO 4 in 2 stages at an organic to aqueous phase ratio of 1:4.

Process for the Recovery of Cobalt and Nickel from Sulphate Leach Liquors with Saponified Cyanex 272 and D2EHPA

In this paper, a process is reported for the recovery of cobalt and nickel from copper raffinate solutions using partially saponified Cyanex 272 and D2EHPA as the extractants. The aqueous feed contains 1.65 g/L cobalt and 16.42 g/L nickel. More than 99.9% cobalt separation was achieved with 0.13 M Cyanex 272 (60% neutralized with alkali) in two counter‐current stages at an aqueous to organic phase ratio of 1.1:1. Co‐extraction of nickel was 0.18% only. Stripping of cobalt from a loaded organic phase was carried out with synthetic spent electrolyte solution at an organic to aqueous phase ratio of 2.5 in two counter‐current stages to generate a pregnant electrolyte solution to produce cobalt metal by electrowinning. Similarly, optimum conditions for nickel extraction with 60% neutralized 1 M D2EHPA at O/A ratio of 1.4 in 2 two stages and stripping of metal with synthetic spent electrolyte at O/A ratio of 1.6 in two stages were standardized. Extraction and stripping efficiencies were >99% and the flowsheet of the process is demonstrated.

Process for cobalt separation and recovery in the presence of nickel from sulphate solutions by Cyanex 272

The present paper deals with the extraction of cobalt from a solution containing cobalt and nickel in a sulphate medium similar to the leach liquor obtained by the dilute sulphuric acid pressure leaching of the Pacific Ocean nodules matte followed by copper extraction. The commercial extractant Cyanex 272 (bis (2, 4, 4-trimethylpentyl) phosphinic acid) is used for this purpose. The leach liquor used for the present study contains Co =1.78 g/L and Ni=16.78 g/L. Before cobalt extraction, impurities, such as copper and iron, are removed from the leach liquor by the precipitation method. Increasing the concentration of Cyanex 272 increased the extraction percentage of cobalt due to the increase of equilibrium pH. Cobalt extraction efficiency of >99.9 % is achieved with 0.20 M Cyanex 272 in two counter-current stages at an aqueous: organic (A:O) phase ratio of 1.5∶1. Complete stripping of cobalt from the loaded organic containing 2.73 g/L Co was carried out at pH 1.4 by a synthetic cobalt spent electrolyte in two stages at an A:O ratio of 1∶2. The enrichment of cobalt during extraction and stripping operations was about 3.5 times. A complete process flowsheet for the separation and recovery of cobalt is presented.

Separation of cobalt and lithium from mixed sulphate solution using Na-Cyanex 272

The paper embodies the solvent extraction behavior of cobalt and lithium from mixed sulphate solution using Na-Cyanex 272 as an extractant. The effect of different parameters such as pH of feed solution, extractant concentration, cobalt and lithium ion concentrations in the feed solution and stripping behavior using different mineral acids such as H 2SO 4, HCl, HNO 3 have been studied. The highest separation factor of 62 was obtained with 0.03 M Na-Cyanex 272 at an equilibrium pH of 6.90 from mixed solution of 0.01 M cobalt and lithium sulphate. About 84% of cobalt was extracted with a minimum of 8% lithium co-extraction at this condition. Cobalt was extracted as [CoA 2·3HA] org with 65% Na-Cyanex 272. 2 mol of Na-Cyanex 272 are required for the extraction of 1 mol of cobalt. A complete stripping of cobalt can be achieved from the loaded organic with 0.01 M sulfuric acid solution. Cobalt sulphate solution with > 99% purity can be obtained.

The recovery of nickel from high-pressure acid leach solutions using mixed hydroxide product – LIX ®84-INS technology

This route for the recovery of nickel from HPAL laterite solutions was successfully demonstrated by the Centaur Mining Cawse Nickel Operation and has been selected by BHPBilliton for their Ravensthorpe Nickel–Yabulu Refinery circuit. The mixed hydroxide route is also well suited to treatment of solutions by other leach processes such as Activox ®. The technology can use an acid strip coupled to nickel electrowinning or an ammonia strip and basic nickel carbonate production. The solvent extraction technology involved in these two circuits is reviewed and compared. The ancillary operations of pregnant leach solution clarification, reagent remediation, reductive stripping of cobalt, zinc and copper transfers are discussed. The treatment of ammoniacal leach solutions containing higher copper concentrations than those normally seen in laterite processing is also addressed. Possible routes for recovery of cobalt and nickel from the solvent extraction circuit are also discussed.

CYANEX® 301 binary extractant systems in cobalt/nickel recovery from acidic sulphate solutions

The extraction and stripping characteristics of CYANEX 301® binary extractant systems were investigated for the recovery of cobalt and nickel from sulphate solutions. The selectivity properties of these systems against calcium, manganese and magnesium were also studied. These binary extractant systems consisted of mixtures of CYANEX 301 with basic extractants (Primene® JMT, Amberlite® LA-2, Alamine® 336 and Aliquat® 336). Based on criteria such as extraction and stripping characteristics (efficiency and rates) and selectivity against calcium, manganese and magnesium, screening experiments were performed to select the most appropriate binary extractant systems. From this screening work, the CYANEX 301/amine systems all demonstrated that cobalt and nickel could be selectively extracted from calcium, manganese and magnesium. A large synergistic effect on the stripping kinetics and efficiencies of cobalt and nickel was also observed when any amine extractant was added to CYANEX 301. Among the amine extractant systems, CYANEX 301/Aliquat 336 was shown to be the most promising binary extractant system. McCabe–Thiele extraction and stripping isotherms with this system were then constructed to determine the number of stages required. Complete extraction of cobalt and nickel could be achieved in 2–3 stages while still maintaining a high selectivity against calcium, manganese and magnesium. Complete stripping of cobalt could also be achieved in 2–3 stages while complete nickel stripping was shown to still be difficult. The loading capacity of the binary system for cobalt and nickel was determined and found to be lower than the loading capacity of CYANEX 301.

CYANEX® 301 binary extractant systems in cobalt/nickel recovery from acidic chloride solutions

The extraction and stripping characteristics of CYANEX 301 binary extractant systems were investigated for the recovery of cobalt and nickel from chloride solutions. The selectivity of these systems against calcium, manganese and magnesium was also studied. These binary extractant systems consisted of mixtures of CYANEX 301 with basic extractants (Primene® JMT, Amberlite® LA-2, Alamine® 336 and Aliquat® 336). Based on criteria such as extraction and stripping characteristics (efficiency and rates) and selectivity against calcium, manganese and magnesium, screening experiments were performed to select the most appropriate binary extractant systems. From this screening work, the CYANEX 301–amine systems all demonstrated that cobalt and nickel could be selectively extracted from calcium, manganese and magnesium. A large synergistic effect on the stripping kinetics and efficiencies of cobalt and nickel was also observed when either amine was added to CYANEX 301. Depending on the amine concentration, near complete stripping of cobalt could be achieved with all systems, while the stripping of nickel still remained very low with the amines Primene JMT, Amberlite LA-2 and Alamine 336. Among the amine extractant systems, CYANEX 301–Aliquat 336 was shown to be the most promising binary extractant system. McCabe–Thiele extraction and stripping isotherms with this system were then constructed to determine the number of stages required. Complete extraction of cobalt and nickel could be achieved in 2–3 stages while still maintaining a high selectivity against calcium, manganese and magnesium. A decrease in cobalt stripping was observed when the hydrochloric acid concentration was increased from 2 to 4 M. The hydrochloric acid concentration had a reverse effect on nickel where nickel stripping was shown to increase with increase in acid concentration from 2 to 4 M.

Separation of cobalt and nickel from acidic sulfate solutions using mixtures of di(2‐ethylhexyl)phosphoric acid (DP‐8R) and hydroxyoxime (ACORGA M5640)

AbstractDP‐8R and ACORGA M5640 extractants diluted in Exxsol D100 were used to co‐extract cobalt and nickel from aqueous acidic sulfate media. The influences of equilibration time, temperature, equilibrium pH and reagent concentrations on the extraction of both metals have been studied. It was observed that both cobalt and nickel extraction are slightly sensitive to temperature but are pH dependent. Metal extraction equilibria are reached within about 5 min contact time. In addition, cobalt extraction depends on the extractant concentration in the organic phase. For a solution containing 0.5 g dm−3 each of cobalt and nickel and an initial pH of 4.1, conditions were established for the co‐extraction of both metals and selective stripping (with H2SO4) of cobalt and nickel. Using the appropriate reagent concentrations the yield (extraction stage) for both metals exceeded 90%, and stripping of cobalt and nickel was almost quantitative. Copyright © 2004 Society of Chemical Industry

Separation and recovery of cobalt and nickel from sulfate solutions of Indian Ocean nodules using Cyanex 272

A process for the separation and recovery of cobalt and nickel was optimized for a sulfate leach solution of Indian Ocean sea nodules containing 80 g/m3 cobalt and 730 g/m3 nickel using the sodium salt of Cyanex 272 as the extractant. Extraction of both cobalt and nickel increased with an increase in equilibrium pH and extractant concentration. The extracted species with respect to cobalt appears to be CoA2·3HA. More than 99.6% extraction of cobalt was achieved using 0.04M solvent in a three-stage counter current simulation at the A:O phase ratio of 3:2. The co-extraction of nickel was about 0.6% only. Two-stage countercurrent stripping of cobalt from the loaded organic at an A: O ratio of 1:7 resulted in a pregnant electrolyte enriched by 0.8 kg/m3, thus enabling a ten times overall enrichment of cobalt. From the cobalt-free raffinate, nickel extraction was carried out using 0.25M solvent in two countercurrent stages, and the extraction showed a 99.8% recovery. Stripping of nickel from the loaded solvent was carried out at an equal phase ratio with the advance electrolyte of pH 1.75 in two countercurrent stages. The nickel stripping efficiency was found to be 98.8%. The present studies indicated that complete recovery of cobalt and nickel was possible using nine counter-current stages.

Photoreductive Stripping of Cobalt Loaded on Hydroxyoxime Extractant in a Liquid−Liquid Extraction System

The photoreductive stripping of cobalt from hydroxyoxime extractants was investigated, employing 2-hydroxy-5-nonylacetophenone oxime (LIX-84I) and 2-hydroxy-5-nonylbenzophenone oxime (LIX-65N) as extractants, n-dodecane as the diluent, and a halogen lamp as the light source. The stripping of cobalt is barely achieved by conventional stripping, in this extraction system, because of the oxidation of the cobalt−hydroxyoxime complex by electron attraction with the O2 molecule. The stripping of cobalt is, however, substantially improved by photoirradiation using light of visible radiation wavelength. The organic solution obtained following photoirradiation can be reused for repeated extraction and photoreductive stripping processing.

Cobalt-manganese separation: the extraction of cobalt(II) from manganese sulphate solutions by cyanex 301

The extraction and stripping reactions of cobalt(II) by Cyanex 301 in Iberfluid diluent from aqueous manganese sulphate solutions has been investigated. The effect of different variables which should influence the extraction-stripping of cobalt was evaluated, including equilibration time, temperature, organic diluent, extractant concentration, aqueous pH, cobalt loading, strip solution concentration, etc. The number of stages required for the extraction and stripping of cobalt was also evaluated. The results were used to define the conditions for the purification of manganese sulphate solutions. © 1998 Society of Chemical Industry

ＬＩＸ８４‐Ｉを吸着させた溶媒浸漬樹脂によるニッケル，コバルト，銅の抽出

Amberlite XAD-4 is used for catching a very small amount of organic substances in the water. LIX84-I is indicated a good ability on the extraction of various metal elements, as known in the field of solvent extraction. In the present study, solvent impregnated resin (SIR) was devised by adsorbing LIX84-I to XAD-4, as a result, it would be having the metal extraction ability. The extraction properties of nickel, cobalt and copper were investigated by using the SIR. In the case of metal extraction by batch method, the extraction behavior of each metals using the SIR was similar to the solvent extraction using LIX84-I. Copper was selectively extracted at the pH of 3.0, nickel and cobalt were almost extracted at the pH of 9.0. As a result of using fine particle size of XAD-4 and high concentration of LIX84-I when the SIR was made, the nickel, cobalt and copper could be extracted at a more short time. In the case of column method, the SIR was enclosed in the column, metal solution was flowed from top of the column. The extraction curve of each metals were similar to the case of solvent extraction using LIX84-I and SIR batch method. As flow rate was rapid, the amount of saturated adsorption was increased. For giving back extracted metals to the water phase, stripping was carried out. In the solvent extraction using chemical reagents of LIX system, the stripping of cobalt was difficult, but in the solid-liquid extraction using the SIR, cobalt was stripped easier. It is considered that the cobalts in organic phase of SIR could not form stable Co-LIX complexes.