popular iron ore hp flotation cell

investigation of the reverse flotation of iron ore in three different flotation cells: mechanical, oscillating grid and pneumatic - sciencedirect

investigation of the reverse flotation of iron ore in three different flotation cells: mechanical, oscillating grid and pneumatic - sciencedirect

Evaluation of the reverse flotation of hematite in a mechanical, oscillating grid and pneumatic flotation cell.Coarse quartz recovery increases with increasing impeller speed to an optimum.Coarse quartz recovery and fine hematite loss decrease with increasing froth height.Fine hematite loss decreases significantly with decreasing solids concentration.Theoverall flotation performance ofthepneumatic cell was better than the mechanical cell.

This paper investigates the reverse flotation of iron ore in a laboratory mechanical, oscillating grid (OGC) and pneumatic flotation cell. The main objectives are to investigate the recovery of coarse quartz (+150m) by flotation and fine hematite (25m) by entrainment. Agitation/energy input results show that coarse quartz recovery increases with increasing impeller speed to a maximum of 70%. The recovery of coarse quartz in the OGC is 10% higher than in the mechanical cell with an optimum at a low energy input of 0.1W/kg. Froth height results show that coarse quartz recovery and fine hematite loss decrease by over 50% with increasing froth height. Solids concentration results show that coarse quartz recovery remains relatively constant with decreasing solids concentration, but fine hematite loss decreases from 15 to 5% at the maximum froth height due to lower water recoveries. The OGC generally results in the best overall flotation performance at lower energy input. The pneumatic flotation cell achieves better flotation performance than the mechanical flotation cell for most operating conditions.

beneficiation of iron ore

beneficiation of iron ore

Beneficiation of Iron Ore and the treatment of magnetic iron taconites, stage grinding and wet magnetic separation is standard practice. This also applies to iron ores of the non-magnetic type which after a reducing roast are amenable to magnetic separation. All such plants are large tonnage operations treating up to 50,000 tons per day and ultimately requiring grinding as fine as minus 500-mesh for liberation of the iron minerals from the siliceous gangue.

Magnetic separation methods are very efficient in making high recovery of the iron minerals, but production of iron concentrates with less than 8 to 10% silica in the magnetic cleaning stages becomes inefficient. It is here that flotation has proven most efficient. Wet magnetic finishers producing 63 to 64% Fe concentrates at 50-55% solids can go directly to the flotation section for silica removal down to 4 to 6% or even less. Low water requirements and positive silica removal with low iron losses makes flotation particularly attractive. Multistage cleaning steps generally are not necessary. Often roughing off the silica froth without further cleaning is adequate.

The iron ore beneficiation flowsheet presented is typical of the large tonnage magnetic taconite operations. Multi-parallel circuits are necessary, but for purposes of illustration and description a single circuit is shown and described.

The primary rod mill discharge at about minus 10- mesh is treated over wet magnetic cobbers where, on average magnetic taconite ore, about 1/3of the total tonnage is rejected as a non-magnetic tailing requiring no further treatment. The magnetic product removed by the cobbers may go direct to the ball mill or alternately may be pumped through a cyclone classifier. Cyclone underflows usually all plus 100 or 150 mesh, goes to the ball mill for further grinding. The mill discharge passes through a wet magnetic separator for further upgrading and also rejection of additional non-magnetic tailing. The ball mill and magnetic cleaner and cyclone all in closed circuit produce an iron enriched magnetic product 85 to 90% minus 325 mesh which is usually the case on finely disseminated taconites.

The finely ground enriched product from the initial stages of grinding and magnetic separation passes to a hydroclassifier to eliminate the large volume of water in the overflow. Some finely divided silica slime is also eliminated in this circuit. The hydroclassifier underflow is generally subjected to at least 3 stages of magnetic separation for further upgrading and production of additional final non-magnetic tailing. Magnetic concentrate at this point will usually contain 63 to 64% iron with 8 to 10% silica. Further silica removal at this point by magnetic separation becomes rather inefficient due to low magnetic separator capacity and their inability to reject middling particles.

The iron concentrate as it comes off the magnetic finishers is well flocculated due to magnetic action and usually contains 50-55% solids. This is ideal dilution for conditioning ahead of flotation. For best results it is necessary to pass the pulp through a demagnetizing coil to disperse the magnetic floes and thus render the pulp more amenable to flotation.

Feed to flotation for silica removal is diluted with fresh clean water to 35 to 40% solids. Being able to effectively float the silica and iron silicates at this relatively high solid content makes flotation particularly attractive.

For this separation Sub-A Flotation Machines of the open or free-flow type for rougher flotation are particularly desirable. Intense aeration of the deflocculated and dispersed pulp is necessary for removal of the finely divided silica and iron silicates in the froth product. A 6-cell No. 24 Free-FlowFlotation Machine will effectively treat 35 to 40 LTPH of iron concentrates down to the desired limit, usually 4 to 6% SiO2. Loss of iron in the froth is low. The rough froth may be cleaned and reflotated or reground and reprocessed if necessary.

A cationic reagent is usually all that is necessary to effectively activate and float the silica from the iron. Since no prior reagents have come in contact with thethoroughly washed and relatively slime free magnetic iron concentrates, the cationic reagent is fast acting and in somecases no prior conditioning ahead of the flotation cells is necessary.

A frother such as Methyl Isobutyl Carbinol or Heptinol is usually necessary to give a good froth condition in the flotation circuit. In some cases a dispersant such as Corn Products gum (sometimes causticized) is also helpful in depressing the iron. Typical requirements may be as follows:

One operation is presently using Aerosurf MG-98 Amine at the rate of .06 lbs/ton and 0.05 lbs/ton of MIBC (methyl isobutyl carbinol). Total reagent cost in this case is approximately 5 cents per ton of flotation product.

The high grade iron product, low in silica, discharging from the flotation circuit is remagnetized, thickened and filtered in the conventional manner with a disc filter down to 8 to 10% moisture prior to treatment in the pelletizing plant. Both the thickener and filter must be heavy duty units. Generally, in the large tonnage concentrators the thickener underflow at 70 to 72% solids is stored in large Turbine Type Agitators. Tanks up to 50 ft. in diameter x 40 ft. deep with 12 ft. diameter propellers are used to keep the pulp uniform. Such large units require on the order of 100 to 125 HP for thorough mixing the high solids ahead of filtration.

In addition to effective removal of silica with low water requirements flotation is a low cost separation, power-wise and also reagent wise. Maintenance is low since the finely divided magnetic taconite concentrate has proven to be rather non-abrasive. Even after a years operation very little wear is noticed on propellers and impellers.

A further advantage offered by flotation is the possibility of initially grinding coarser and producing a middling in the flotation section for retreatment. In place of initially grinding 85 to 90% minus 325, the grind if coarsened to 80-85% minus 325-mesh will result in greater initial tonnage treated per mill section. Considerable advantage is to be gained by this approach.

Free-Flow Sub-A Flotation is a solution to the effective removal of silica from magnetic taconite concentrates. Present plants are using this method to advantage and future installations will resort more and more to production of low silica iron concentrate for conversion into pellets.

flotation cells in iron ore processing - froth flotation (sulphide & oxide) - metallurgist & mineral processing engineer

flotation cells in iron ore processing - froth flotation (sulphide & oxide) - metallurgist & mineral processing engineer

Does anybody have experience of working with WEMCO flotation cells to remove sulfur in iron ore reverse flotation circuits? Could it be a good choice for flotation of coarse and dense iron ore particles without any settlement?

I think by settlement you are referring to sanding of the flotation cell (where particles come out of suspension and settle in tank). To answer your question I think its best to consider the anatomy of forced air vs. induced air (e.g. WEMCO) flotation cells. The induced air flotation cell has the rotor position at the top of the cell as it needs to be close to the surface to pull in air; hence the majority of the mixing energy is dissipated in the top of the cell. True these cells are designed for pumping and circulating pulp throughout but as the high energy zone is generally adjacent to the rotor you would have to put in even more energy to ensure that particles entering the cell at the bottom remain suspended (especially when coarse). Conversely the forced air designs of cells have rotors at the bottom so the high energy zone of the mixing is where the particles are most likely to settle. If you think about this which arrangement is less likely to have coarse and high SG particles sanding?

In addition for a forced air cell if settling occurs you can stop the air, thus maximize the energy used for mixing/suspension, and get the material moving again (prior to turning the air back on). The mixing and air dispersion actions on an induced air cell cannot be decoupled so this is more difficult. Also it is quiet difficult for a rotor located at the top to get sanded material in the bottom of the cell moving.

There are also additional important considerations when dealing with coarse and heavy minerals; motor size and valve arrangement. Typical float cells are designed with a particle SG or around 2.8-3.0 SG if you have a majority magnetite or hematite feed then you are looking at particle SGs approaching 5.0 for the overall feed. This needs to be taken into account and an appropriate motor/mechanism selected. The valve arrangement is also important. For this type of application internal downflow dart valves are likely the best as this minimizes the chances of particles sanding within the ducting and transfer boxes. I suggest you find a manufacturer who has references in dealing with this type of material as you really cant afford to get this wrong and have the cells sanding up.

I mean sanding area. The problem during operation is that self aeration system could not suspend all particles in a cell, especially when particles are large (e.g. > 150 micron) with high specific gravity. So the materials choke in the cell and you have to stop the operation. What is the advantage of the rotor new position in WEMCO cells in comparison with others while we faced such problem in working with this cell?

In forced air cells we can control the turbulence zone by changing the air flow but in induced air cells we have to stable the froth zone manipulating the rotor speed or other mechanical parameters. Therefore, we reduce the required energy for particles suspension and sanding will emerge as a result.

May I ask what type of WEMCO cells you are referring to Tank Cells, or Trough Cells? From my experience with these cells the Tank Cells are more prone to sanding than the trough cells. As you say the high SG Iron minerals will tend to settle especially in a dilute pulp density, have you tried floating at 50-55wt% solids to see if the settling stops?

I propose to do some settling tests in laboratory with difference solid content, and then use lowest settling rate for flotation, but please note that in high concentrate pulps we will have some problems such as:

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treatment and recycling of the process water in iron ore flotation of yuanjiacun iron mine

treatment and recycling of the process water in iron ore flotation of yuanjiacun iron mine

Wen-li Jiang, Hai-feng Xu, "Treatment and Recycling of the Process Water in Iron Ore Flotation of Yuanjiacun Iron Mine", Journal of Chemistry, vol. 2017, Article ID 9187436, 8 pages, 2017. https://doi.org/10.1155/2017/9187436

Coagulating sedimentation and oxidation treatment of process water in iron ore flotation of Yuanjiacun iron mine had been studied. The process water of this mine carried residual polyacrylamide (PAM), poly(diallyldimethylammonium chloride) (PDADMAC), and Ca2+ from the flotation and caused decrease of the iron flotation recovery or grade of the concentrate. The studies on high-intensity magnetic separation (HIMS) tailings for coagulating sedimentation showed that the settling performance of coagulant (named CYH) was better than that of PDADMAC. The analyses of FTIR spectra and zeta potential demonstrated that CYH is adsorbed mainly through electrostatic attraction onto HIMS tailings. Sodium hypochlorite was adopted to oxidize the residual organics in tailings wastewater. When sodium hypochlorite is at the dosage of 1.0g/L, reaction temperature is of 20C, and reaction time is of 30 minutes, the removal rates of PAM, COD, and Ca2+ were 90.48%, 83.97%, and 85.00%, respectively. Bench-scale flotation studies on the treated tailings wastewater indicated that the iron recovery and grade of concentrate were close to those of freshwater.

Iron ore resources are extremely rich in China, but most of them belong to complex ultrafine iron ore with high content of impurities [1]. Reverse flotation has been proved to be an efficient process for economic reasons [26]. In order to ensure iron concentrate grade and iron recovery, a large number of processing reagents are selected and applied in the iron ore beneficiation. The process water carried plenty of residual processing reagents, and such wastewater with color depth and strong smell could seriously affect the environment and the local people. Prevailing campaign for a cleaner and safer environment with clean surface water and ground water has led to increased recycling of process water within the production cycle of mineral flotation [7]. Since the chemistry property of process water is entirely different from fresh water, there is a concern about the possible effects of the contained components on the efficiency of the flotation process [8]. In iron ore flotation process, a large amount of NaOH is taken to adjust the pH. The wastewater pH of iron ore is more than 9, so physicochemical treatment of iron wastewater from a certain degree is rather difficult [9]. At present, the common methods of treatment of wastewater from flotation are acid-alkali neutralization [10, 11], precipitation, coagulation, and sedimentation [1215], chemical oxidation degradation [16], constructed wetland [1719], ion exchange method [20], adsorption method [21, 22], and biological method [23, 24]. However, the single method above cannot completely clear wastewater pollution with harsh operating conditions. In addition, they may also produce secondary pollution.

Yuanjiacun iron mine of Shanxi province in China is the largest iron mine of micrograined hematite combined with magnetite in Asia. The annual processing capacity of iron ore reaches 22 million tons, and the wastewater from mineral processing is about 400 thousand m3 every day. If the dressing wastewater is directly discharged into the nature, it will not only pollute the surrounding environment but also has a great potential safety risk. Recycling of process water is a good way to solve the problem. In this study, the influence of tailings wastewater components were investigated on flotation of hematite in order to assess the practicability of recycling process water in flotation practice first. A novel coagulant CYH was introduced to coagulate HIMS tailings, and the coagulating sedimentation mechanism of CYH was investigated by FTIR spectra and zeta potential. Moreover, sodium hypochlorite was adopted to oxidize the organic pharmaceutical residues in wastewater. Besides, the effect of wastewater treatment was evaluated by recycling of tailings wastewater.

All test samples including tailings wastewater, high-intensity magnetic separation (HIMS) tailings, and flotation samples were procured from the Yuanjiacun iron mine concentrator of Shanxi province in China. The tailings wastewater was collected from flotation tailings water combined with magnetic separation tailings water, stirred evenly, and stored in plastic bottle. The wastewater quality was shown in Table 1. Test results showed that the tailings wastewater presented yellowish brown, suspended solids (SS) content and the concentration of Ca2+, Cl, and COD exceeded the standard.

The concentration of the HIMS tailings pulp was 11.93% by weight, and the main minerals were quartz (62.54%), amphibole (17.44%), chlorite (4.16%), hematite (4.75%), montmorillonite (3.82%), calcite (2.93%), and feldspar (4.36%). The XRD analysis of the sample was shown as Figure 1. The sample was classified into different size fractions as shown in Table 2. As shown in Table 2, most particle size of the sample was fine and more, even if the sample was on quiescent standing in a month, it also would not naturally subside.

The samples for flotation were taken from on-site samples of flotation, which were ground to 95% passing 0.045mm, and contained 34.90% specularite and hematite, 8.70% magnetite, 0.20% limonite, 39.40% quartz, 11.40% chlorite and hornblende, and 4.90% calcite and dolomite.

Coagulant (CYH) of the molecular weight of 80 thousands was synthesized in our lab and it was of technical grade. Amphoteric polyacrylamide (PAM) of the molecular weight of 12 million was of technical grade. Collector (named RA-715) and coagulant poly(diallyldimethylammonium chloride) (PDADMAC) were from the Yuanjiacun iron mine concentrator of Shanxi province in China and they were of all technical grade. CaCl2 and NaCl acted as sources of Ca2+ and Cl ions, respectively. Other chemical materials were bought from commercial companies and their purity was above chemical purity grade.

Use 300mL HIMS tailings pulp mentioned above at every turn to conduct coagulation contrast test. First, add the required amount of CYH into the testing pulp, and mix them up evenly; then add PAM into the testing pulp, and after a period of stirring, leave the samples standing and record the height of supernatant as a function of standing time.

Use 1.0L iron tailings wastewater mentioned above at every turn to conduct oxidation-sedimentation experiment. When the wastewater was heated to the desired temperature, sodium hypochlorite (10% of available chlorine) was added. After stirring the mixture for the desired time, FeCl2 were added to the mixture, and the KI-starch paper was used to detect the reaction progress until it did not change blue. Afterwards, the pH was adjusted to 9~10 with NaOH solution. After several hours of standing, the supernatant was separated, and then the PAM concentration, COD value, and Ca2+ content were measured.

The bench-scale flotation tests were conducted in a XFD-63 flotation cell (self-aeration) whose volume for rougher flotation and cleaning flotation was 0.5L, using 200g ore at every turn to obtain a Fe concentrate. Fatty acids (RA-715) were used as collector, NaOH was used as pH regulators, starch was used as depressant, and CaO was used as activator. The flotation flow sheet was illustrated in Figure 2.

The infrared spectra of samples were recorded by Nicolet AVATAR370 FTIR spectrometer (USA) using the KBr disk technique. The quartz samples used for this purpose were ground in an agate mortar and pestle to pass 5m. 50mg of samples was mixed with 30mL distilled water in the absence or presence of 100mg/L coagulant at pH 9 and 25C. After stirring for 3min, still standing for 4h, the solid product in the mixture was filtrated and rinsed three times and then dried in a vacuum oven and recorded infrared adsorption spectra from 400cm1 to 4000cm1.

Zeta potentials of HIMS tailings samples were measured by using a Brookhaven ZetaPlus zeta potential analyzer (USA). The samples used for this purpose were ground to less than 5m in an agate mortar and pestle. 50mg of the samples was added to 30mL aqueous solution with or without 100mg/L coagulant. After stirring for 10min, then the pH values were adjusted with HNO3 or NaOH solutions and measured. All measurements were conducted in a 0.1mol/L KNO3 background electrolyte solution. The agitated suspension was sampled to record the zeta potential. The results presented were the average of five independent measurements with a typical variation of 5mV.

Bench-scale flotation studies on the process water showed that tailings wastewater reduced the flotation iron concentrate grade and iron recovery [25]. Large doses of coagulants such as PAM and PDADMAC were used in wastewater treatment in Yuanjiacun concentrator previously. Only in the part of HIMS tailings concentration, doses of PAM and PDADMAC were several times of other similar mines [25]. In order to assess the practicability of recycling of process water in flotation practice, the influence of tailings wastewater components of PAM, PDADMAC, Ca2+, and Cl ions was investigated independently. The results were shown in Figure 3.

Figures 3(a) and 3(b) showed that an increasing PAM or PDADMAC concentration reduced the iron flotation recovery. However there was very little reduction in iron grade. When the concentration increased from 0mg/L to 3mg/L for PAM and 0mg/L to 30mg/L for PDADMAC, the recoveries of iron decreased from 74.66% to 66.74% and 74.66% to 64.63%, respectively. Figure 3(c) demonstrated that an increasing Ca2+ ions concentration reduced the iron grade and increased the iron flotation recovery obviously. When the concentration of Ca2+ ions increased from 0mg/L to 180mg/L, the iron grade of concentration decreased from 66.27% to 64.42%; the iron grade decreased sharply on addition of 360mg/L. However there was a slight increase in recovery in process water in presence of a number of Ca2+ ions. Figure 3(d) showed that, with increasing the dose of Cl, there was no change in iron grade and recovery decreased only slightly.

Single factor tests of components contained in tailings wastewater showed that PAM, PDADMAC, and Ca2+ ions reduced the flotation iron recovery or grade of the concentrate. The origins of PAM, PDADMAC, and other organic species in tailings wastewater were the coagulants, flocculants, and flotation reagents such as PAM and PDADMAC for coagulating sedimentation of concentration and wastewater treatment, starch for depressing hematite flotation, and RA-715 for flotation of activated silicate minerals. The origin of calcium species in tailings wastewater was the ore and flotation reagents such as lime for activating SiO2 and silicate minerals. The method of coagulating sedimentation was used in the process of concentration of HIMS tailings, flotation concentrate and flotation tailings, and treatment of wastewater of tailings pond in Yuanjiacun concentrator. In order to lower the content of suspended solids, PAM, and PDADMAC, coagulating sedimentation experiments were conducted with a novel coagulant CYH. Given the maximum amount of coagulants and flocculants used in HIMS tailings concentration in Yuanjiacun concentrator at present, we chose coagulating sedimentation testes of HIMS tailings concentration as a representative for detailed investigations to study the performance of CHY.

Figure 4 exhibited the effect of PDADMAC or CYH dosage on coagulation efficiency by using PAM as a flocculant at 26.88g/(t undressed ore, the same below) initial concentration. The results in Figure 4 showed that, at the coagulant dosage of 8.96g/t, the settle rate of CYH was faster than that of PDADMAC, even faster than that of PDADMAC at the dosage of 17.92g/t. The turbidity of liquid supernatant by using CYH as a coagulant at 8.96g/t initial concentration was lower than that of PDADMAC same as that of initial concentration and was rough equal to that of PDADMAC as a coagulant at 17.92g/t initial concentration. When the initial concentration of CYH increased from 8.96g/t to 17.92g/t, the settle rate and turbidity changed little. Compared with PDADMAC, CYH exhibited superior coagulating ability.

The flocculation response of PAM as a function of initial concentration by using CYH as a coagulant at 8.96g/t initial concentration was presented in Figure 5. As it could be observed from Figure 5, the settle rate rapidly increased with increasing flocculant concentration. However, increasing PAM concentration had minor influence on turbidity of liquid supernatant.

As shown in Figure 1, quartz was the highest content of mineral in HIMS tailings. So, we chose quartz as a representative for FTIR spectrum investigation to study the adsorption mechanism of quartz before and after interaction with CYH. The FTIR spectra were presented in Figure 6.

Figure 6 showed that, after interaction with CYH, the stretching and bending vibrations of saturated C-H bonds in CYH molecules appeared at around 2962.17, 2933.24, 2871.53, and 1432.15cm1 on quartz surfaces, respectively. The results of FTIR spectra exhibited that, after CYH treatment, new adsorption peaks on quartz surfaces did not appear except for CYHs adsorption bands, which inferred that CYH might adsorb onto quartz surface without the formation of new complexes.

Zeta potentials of HIMS tailings particles as a function of pH values in the absence and presence of CYH were shown in Figure 7. It indicated that the potential of HIMS tailings was high. So coagulating sedimentation treatment of HIMS tailings was rather difficult from a certain degree because of the electrostatic repulse force among particles. As it could be observed from Figure 7, CYH could lower -potential values within the scope of pH 5~12, inferring that cationic CYH might adsorb onto particles surfaces. The results of zeta potential indicated that CYH adsorbed onto HIMS tailings mainly through electrostatic attraction, which agreed with the FTIR spectra results.

CYH that is a good coagulant has strong binding force by using hydroxy. After the mixture of HIMS tailings and CYH, the stable silicate mineral groups in the wastewater were exposed; meanwhile, CYH entered into the wastewater and hydrolyzed strongly to be a polyhydroxy polymer compound. CYH adsorbed characteristically onto particles surfaces through electrostatic force, hydrogen bond, hydrophobic association, and van der Waals force, bridging the various silicate minerals in the long CYH chain, forming large flocs to reach rapid subsidence through trapping and rolling.

Table 3 showed that, by using CYH as a coagulant, the content of SS of tailings wastewater decreased obviously, and the wastewater became clear. However, the COD value and concentration of PAM in tailings water were still much higher than freshwater. The tailings water still could not meet the requirements of reuse for flotation. Thus, oxidation-sedimentation treatment was still needed in the process.

We chose removal rates of PAM and COD as representatives for detail investigations to study the effect of reaction parameters. Figure 8(a) showed the effect of dosage of sodium hypochlorite (NaClO) on the removal rates of PAM and COD. As shown in Figure 8(a), the removal rates of PAM and COD rapidly increased with increasing NaClO concentration when it was less than 1.0g/L and then slowly increased and reached 90.48% and 83.97% at 1.0g/L dosage, respectively. As it could be observed from Figure 8(b), the removal rates of PAM and COD increased with increasing reaction temperature. When the reaction temperature increased from 15C to 30C, the removal rates increased from 87.62% to 94.61% and 77.86% to 87.64% for PAM and COD, respectively. The reaction temperature is higher, the reaction rate is faster, but the decomposition of NaClO is faster. The choice of 20C as the reaction temperature can ensure NaClO has good oxidation ability, but also conform to the most of natural temperature of tailings wastewater in Yuanjiacun concentrator. Figure 8(c) demonstrated that the removal rates of PAM and COD rapidly increased with prolonging reaction time when it was less than 30min and then maintained roughly constant.

As shown in Table 4, after treatment by using oxidation-sedimentation method, pH of tailings wastewater increased from 9.12 to 9.35, suspended solids content decreased from 178mg/L to 48mg/L, and concentration of Ca2+ ions, TFe, PAM, and COD decreased from 240mg/L to 36mg/L, 4.97mg/L to 0.36mg/L, 3.15mg/L to 0.30mg/L, and 131mg/L to 21mg/L, respectively. And the removal rates of PAM, COD, and Ca2+ was 90.48%, 83.97%, and 85.00%, respectively. The water quality of treated tailings wastewater was close to the quality of freshwater.

Bench-scale flotation studies were conducted according to the procedure as shown in Figure 2. These studies would show whether oxidation-sedimentation treatment of the tailings wastewater occurring in the pilot plant had any effect on selectivity and/or recovery of minerals during flotation. Results were given in Table 5. The results showed that the concentrate yield, grade, and recovery increased by 0.95%, 1.25%, and 2.75%, respectively, by using treated tailings wastewater as flotation water compared to that of tailings wastewater without treatment. Compared to freshwater, in the case of the equivalent yield, treated tailings wastewater achieved an excellent concentration containing 65.45% Fe with 73.49% Fe recovery, and the Fe grade increased by 0.31%.

(1) Single factor tests of components contained in tailings wastewater in Yuanjiacun concentrator showed that PAM, PDADMAC, and Ca2+ ions reduced the flotation iron recovery or grade of the concentrate.

(2) When CYH was used to coagulate HIMS tailings, -potential decreased, and silicate minerals formed flocculent mass by bridging; thus suspended matters decreased effectively. This was subsequently confirmed by FTIR spectrum and zeta potential analysis. But the tailings wastewater could not reach recycling standards.

(3) Oxidation experiment showed that a 90.48% reduction in PAM, 83.97% reduction in COD, and 85.00% reduction in Ca2+ were achieved at the sodium hypochlorite dosage of 1.0g/L, reaction temperature of 20C, and reaction time of 30 minutes. Bench-scale flotation tests on the treated tailings wastewater indicated that the Fe recovery and grade of concentrate were close to those of freshwater.

The authors gratefully acknowledge the financial supports of the National Natural Science Foundation of China (no. 5160041305) and the China Postdoctoral Science Foundation (no. 2016M591382). This project is also supported by Lanxian County Mine Co., Ltd., TISCO, China.

Copyright 2017 Wen-li Jiang and Hai-feng Xu. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

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