OA19764A - Concentration process of iron ore slimes. - Google Patents
Concentration process of iron ore slimes. Download PDFInfo
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- OA19764A OA19764A OA1202000131 OA19764A OA 19764 A OA19764 A OA 19764A OA 1202000131 OA1202000131 OA 1202000131 OA 19764 A OA19764 A OA 19764A
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Abstract
The present invention relates to a concentration process of iron minerals from ultrafine tailings (slimes) from iron ore processing through reverse flotation with pH between 8.5 and 10.5 with the addition of amide-amine type collector, or further a mixture thereof with traditional cationic collectors (amines), in the absence of any depressant, alternatively including a step of high field magnetic concentration, which allows to obtain a concentrate with iron content higher than 66% and contents of SIO2 + AI2O3 below 4%.
Description
CONCENTRATION PROCESS OF IRON ORE SUMES
FIELD OF INVENTION
[001] The présent invention is directed primarily to the mining industry and comprises a concentration process of iron minerais contained in iron ore ultrafine tailings (sûmes) through reverse cationic flotation with the addition of amide-amine type collectons or further, optionally, combinations thereof with conventional organic based branched chain cationic type collectors (amine), without depressant addition; said process including, alternatively, a step of high intensity magnetic concentration for the production of a product with high iron content, low contaminants content and high spécifie surface area.
BACKGROUND OFTHE INVENTION
[002] Flotation is the main concentration process of iron ore mining industry. Traditional processes require ultrafines removal before flotation, because of the impact on the efficiency of the concentration process. Currently, in most concentrators, ultrafines are removed by desliming, followed by thickening. The tailings (sûmes) from this process (thickener overflow) are directed to conventional tailings dams, which generates a sériés of impacts.
[003] Currently, the mining industry produces hundreds of millions of tons of waste and tailings per year. In the case of tailings, significant part of this material is disposed in dams, with high impact in the overall costs, due to construction, operation and management costs, as well facing serious environmental hazards, and danger of environmental disasters, such as disruptions. Such risks represent an important socioenvironmental concern, as they imply on difficulties to obtain environmental licensing. [004] Despite government's efforts, législation and available technologies, disruption of mining tailings dams still accounts for accidents, sometimes catastrophic, with serious économie, social and environmental conséquences. Dam failures can dump millions of cubic meters of tailings into the environment, displacing entire communities, contaminating drinking water supplies, such as rivers and lakes, and devastating local wildlife, human and animal livelihoods in the affected région.
[005] Considering this scénario, the mining sector has made great investments in order to develop processes that minimize the impacts produced by its activity in general and, in particular, by the mining tailings and waste. The development of processes able to mitigate the problems from iron ore Processing plays a major rôle in the mining industry.
[006] One of the alternatives that minimizes the impact of iron ore industry tailings génération is the development of a process able to reduce the amount of ultrafines 5 disposed in dams, through the exploitation of iron ore tailings.
[007] The sûmes from iron ore concentration operations in the Quadrilatère Ferrifero area (Minas Gérais State), has iron contents ranging from 40% to 50%. These sûmes are characterized by the high content of ultrafine particles, with approximately 30% solids by weight, being disposed in dams.
[008] Some processes hâve been used to recover iron minerais from the tailings, thus, reducing the amount of tailing sand their environmental impact. Reverse flotation at pH about 10.5, using depressant and cationic collecter can be mentioned as one option.
[009] In this traditionally known process, a cationic collecter is added to the pulp, which consists of a petroleum-derived organic branched-chain ether-amine class 15 reagent, having as purpose to change the surface of quartz particles from hydrophilic to hydrophobie so that they can be dragged to the surface by the bubbles introduced into the process. This type of cationic collecter normally requires a short conditioning time, approximately 1 minute, to act on the minerais to be floated.
[0010] Since this type of cationic collecter does not act selectively, it requires the use of a depressant, usually a polysaccharide, such as starch. In iron ore flotation, starch is employed to render the surface of iron bearing minerais hydrophilic to improve the flotation selectivity of other silicate minerais, inhibiting the action of the collecter on them and directing the iron minerais to the sunk.
[0011] The use of this conventional method to recover iron-bearing minerais from the tailings présents problems of low metallurgical recoveries and high contaminant content in the final product.
[0012] One of the major challenges for the recovery of iron minerais from tailings is an efficient séparation of quartz, kaolinite and other gangue minerais from iron ore minerais. Kaolinite, a gangue constituent in the finer fractions of the ore, is the main 30 inhibitor of the traditional reverse flotation process due to its morphological characteristics and surface load.
[0013] Iri the State of the art, there are séparation processes of gangue with kaolinite from minerais of interest, such as that described in Souza et al. (SOUZA, H. S.; TESTA, F. G.; BRAGA, A. S.; KWITKO-RIBEIRO, R.; OLIVEIRA, A. H.; LEAL FILHO, L. S. Desenvolvimento de uma rota de flotaçâo como alternativa para concentraçâo de minérios de manganês de baixo teor. In: ENCONTRO NACIONAL DE TRATAMENTO DE MINÉRIOS E METALURGIA EXTRATIVA, 26, 2015, Poços de Caldas). In this case, the process consists of concentrating manganèse from the fines produced in the beneficiation of this ore, where kaolinite is the main gangue minerai. The process perforais reverse cationic flotation using an amide-amine type collector sélective for kaolinite, and modified starch as a depressant for manganèse oxide dépréssion. Unlike the process used in the présent invention, the manganèse ore undergoes a desliming step prior to flotation, which means that the ultrafine fraction (< 10 pm) is removed from the process. The obtained results showed that the process did not hâve the desired efficiency, since manganèse content in the concentrate was only 34% by weight.
[0014] Rodrigues (RODRIGUES, O. M. S. Flotaçâo de caulinita em minérios de ferro e bauxiticos, 2012. 170. Thesis (Doctorate in Metallurgical Engineering - Escola de Engenharia, Universidade Fédéral de Minas Gérais, Belo Horizonte, 2012) describes a study about the efficiency of several cationic collectors and depressants used to separate kaolinite from bauxite ore, as well from iron ore by reverse flotation. The study analyzed the efficiency of eight distinct collectors such as amines, amine salts and DTAB (dodecyltrimethylammonium bromide). Some of the collectors studied, CTAB, Flotigam 2835® and DTAB, showed good selectivity in certain pH ranges and in the presence or absence of certain depressants. However, no satisfactory iron recovery was achieved in eithercase. ........ ' ------ ....
[0015] A similar situation is described in the technical paper by Rodrigues et al. (RODRIGUES, O. M. S., ROCHA, D. C., PERES, A. E. C., PEREIRA, C. A., CURI, A. Seletividade na separaçâo entre caulinita e hematita por flotaçâo. In: ENCONTRO NACIONAL DE TRATAMENTO DE MINÉRIOS DE METALURGIA EXTRATIVA. 24, 2011, Salvador, p. 360 to 366), where the successful use of a reverse cationic flotation process using an amine as a collector and starch as haematite depressant is reported.
[0016] The document of Bittencourt et al. (BITTENCOURT, L R. M., MILLER, J. D., LIN, C. L.) The flotation recovery of high-purity gibbsite concentrâtes from a Brazilian bauxite ore In: Adv Mater Appl Miner Metall Process Princi, 1990, Littleton, USA: Publ BySoc of Mining Engineering of AIME, 1990, p. 77 to 85) présents a study on the concentration of gibbsite for refractories production from bauxite ore containing 50% gibbsite, 35% quartz and 15% kaolinite. In the process described, gibbsite is concentrated in two steps: first, gibbsite and kaolinite are separated from quartz by direct flotation at pH 2; then, kaolinite is separated by reverse cationic flotation with a quaternary ammonium sait used as a collecter at pH 6.
[0017] Ail processes described above require, in addition to the cationic collecter, the use of a depressant to succeed in recovering the desired minerai. In addition, the achievement of efficient séparation of quartz and kaolinite in iron ore sûmes is still an obstacle to the use of tailings from its Processing. The présent invention aims to overcome the described problems.
[0018] The concentration of iron ore sûmes by column flotation using ether-amine and corn starch was studied by Rocha (ROCHA, L. Estudo de aproveitamento econômico das lamas de uma mineraçâo de ferro, através de concentraçâo catiônica reversa. Master Thesis, Escola de Engenharia, Universiade Fédéral de Minas Gérais, Belo Horizonte, 2008), where the achievement of a concentrate with 67% Fe and S1O2 of less than 1%, and an overall mass recovery near to 20%, with previous use of microdesliming to remove ultrafine particles smaller than 5 gm présent in the tailings was described.
[0019] The developed process, object of the présent patent application, is inserted in this context and provides a solution to reduce the volume of material discharged during the iron ore Processing by recovering the iron minerais contained in these residues.
OBJECTS OF THE INVENTION
[0020] It is an object of the présent invention to reduce the volume of tailings from iron ore Processing which is currently disposed of in dams.
[0021] Another object of the présent invention is to increase the use of ultrafines (sûmes) from iron ore Processing through a process of concentration of the iron minerais présent in the tailings.
[0022] It is a further object of the présent invention to provide a process which obtains efficient séparation of kaolinite and quartz from iron minerais in a simpler and economical way, with the obtainment of a product with high iron content, low contaminant content and high spécifie surface.
SUMMARY OF THE INVENTION
[0023] The présent invention discloses a concentration process of iron minerais from sûmes, without prior removal of ultrafine particles (< 5gm) from the iron ore Processing. While traditional processes are conducted after removal of ultrafine particles (< 5 pm), at high pH, of the order of 10.5, the présent process is characterized by containing a reverse flotation step with pH between 8.5 and 10.5 with addition of amide-amine collector, or a mixture thereof with traditional cationic collectors (amine). Unlike the traditional processes, the proposed process is carried out in the absence of any depressant and has the purpose of solving the problem of separating the iron ore from kaolinite and quartz, obtaining also a high recovery of iron and, consequently, a better use of the residues. Further, the flotation process of this invention may be associated with a wet high intensity magnetic concentration process with a field of 13,000 to 18,000 Gauss and a gap matrix of 1.1 to 1.5 mm.
BRIEF DESCRIPTION OFTHE DRAWINGS
[0024] The présent invention is described in detail based on the respective figures.
[0025] Figure 1 shows a flowsheet comparing the State of the art and the slimes concentration route of the présent invention.
[0026] Figure 2 shows the typical size distribution of iron ore slimes.
[0027] Figure 3 shows a flowsheet detailing the steps of the iron ore slimes concentration process of the présent invention.
[0028] Figure 4 illustrâtes the typical mineralogical composition of iron ore slimes.
[0029] Figure 5 shows the iron (Fe) content in the concentrâtes obtained in the continuous column flotation pilot tests + magnetic concentration.
[0030] Figure 6 shows the silica (S1O2) content in the concentrâtes obtained in the continuous column flotation pilot tests + magnetic concentration.
[0031] Figure 7 shows the alumina (AI2O3) content in the concentrâtes obtained in the continuous column flotation pilot tests + magnetic concentration.
DETAILED DESCRIPTION OF THE INVENTION
[0032] Although the présent invention may be susceptible to different embodiments, preferred embodiments are shown in the drawings and in the following detailed discussion with the understanding that the présent description should be considered an exemplification of the principles of the invention and is not intended to limit the présent invention to what has been illustrated and described herein.
[0033] Unless otherwise noted, ail parts and percentages are by weight.
[0034] The main approach of the présent invention relates to a process of concentration of iron ore from sûmes generated in the Processing of iron ore comprising the following steps:
a) adjusting sûmes pH to a value in the range of 8.5 to 10.5 by adding a base;
b) adding amide-amine cationic collector, or a mixture of said collecter with one or more other collectors, to the sûmes and performing the conditioning of said collecter;
c) adjusting the pulp percent solids by addition of water; and
d) performing reverse flotation, in the absence of depressant, to obtain an iron rich concentrate.
[0035] The most used iron ore beneficiation process in the mining industry consists of flotation. The use of this process requires previous steps of desliming, which is the removal of the ultra-fine particles, which impairs the efficiency of the concentration process.
[0036] The desliming of this ore is generally carried out by means of hydrocyclones. As shown in Figure 1, the overflow from desliming, composed of ultrafine particles, is led to a subséquent process known as thickening. In this operation of sûmes thickening, recovered process water and a thick product with 30% solids, the thickener underflow, are obtained. In the State of the art, the destination of these thickened sûmes, or thickened ultrafines, are the tailings dams, as represented by Figure IA.
[0037] The présent invention uses said sûmes as a starting material, carries out a concentration process as shown in Figure IB, and obtains a concentrate containing more than 60% of iron content.
[0038] The iron ore sûmes of the présent invention are preferably derived from iron ore concentration operations in the Quadrilatère Ferrifero Area, of Minas Gérais State, and are basically composed of gangue minerais, mainly quartz and kaolinite, and iron minerais. Slimes iron content ranges from 40% to 50%.
[0039] Preferably, the slimes used in the process of the invention are approximately 30% solids and are composed of ultrafine ore particles. The typical size distribution of iron ore slimes can be visualized by means of Figure 2. Typically, the slimes hâve about 50% particles below 10 pm and 20% below 3 pm, in addition to maximum particle size (topsize) nearto45 pm.
[0040] Asshown by the flowsheetof Figure 3, the fîrst step of the process of the présent invention consists of adjusting the pH of the slimes by adding a base, preferably sodium hydroxide (NaOH), until achieving a pH between 8.5 and 10.5, the preferred pH range of the présent invention.
[0041] The second step of the process consists of adding collectors and conditioning thereof. The collectors used in the présent invention are straight-chain amide-amine type formulated from vegetable fatty acids and are sélective for the extraction of quartz and kaolinite. Preferably, the présent invention uses a commercially available collector called Flotinor-5530®, produced by the company Clariant®. The collector can be used alone, or in combination with traditional cationic organic branched-chain collectors, in different ratios.
[0042] The collectors are preferably added in an amount ranging from 50 to lOOOg/t (grams of collector per ton of slimes). This value varies according to the surface area of the slimes and contaminants content (quartz and kaolinite).
[0043] Preferably, the conditioning of the collectors is carried out in stirred tank, with résidence time varying from 10 to 30 minutes, preferably 20 minutes, in order to promote and guarantee the adsorption of the collectors to the particles of quartz and kaolinite. The need for longer conditioning time compared to the conventional process, which takes about 1 minute, is explained by the high surface area of the iron ore slimes, which requires more time for the interaction between the minerai particles and the collecting reagents.
[0044] Preferably, the process of the présent invention occurs without the addition of any type of depressant. It is observed that the depressants act in the dépréssion of iron, as well kaolinite. Therefore, the addition of depressant would be detrimental to the process since it reduces the selectivity for the removal of this gangue minerai (kaolinite) présent in iron ore sûmes.
[0045] The third step of the process of the présent invention is adding water to the process at the stirred tank output to ensure that the pulp has approximately 20% solids, a condition suitable for the next step (reverse flotation).
[0046] The fourth step of the process of the présent invention is reverse column flotation, a method known in the State of the art. In this step, air, or any other suitable gas, is bubbled into the System, and the bubbles drags the particles of quartz and kaolinite to the surface.
[0047] The reverse flotation step preferably occurs in an open circuit, which can be carried out in one stage or in more than one stage, with a cleaner stage. The cleaner stage is a flotation step which uses a relatively poor concentrate, from a previous flotation step, and produces a concentrate and tailings with higher grade.
[0048] In the conventional column flotation process, the pulp résidence time is approximately 20 min. In the présent invention a longer time (20 to 60 min, preferably 40 min) is used because sûmes size characteristics: the thinner the particles, the longer the time required for sédimentation. In addition, the longer résidence time is necessary in order to reach the appropriate overflow speed, reducing the hydrodynamic drag of iron particles together with the gangue. The overflow rate comprises the ratio of the float material rate which exits the top of the column (ton/h), by the cross-sectional area of the column (m2). The overflow rate in the conventional flotation is about 5 ton/h/m2. In the présent invention, the overflow rate is not more than 2 ton/h/m2.
[0049] The use ofwashingwater, added atthe top ofthe column, promotes the washing of the foam and drives the iron minerais to the sunk, thereby increasing the séparation efficiency. Therefore, washing water is necessary to reduce the hydrodynamic drag of iron minerais and direct them to the sunk. '
[0050] Washing water also promotes pulp dilution. In the présent invention the pulp should contain about 15 to 20% solids, preferably 15%. In the conventional flotation process, solids percent is about 40 to 50%. The granulométrie characteristics of the slimes require a greater dilution in the flotation medium, for greater efficiency of contact of the gangue particles with the air bubbles, and less entrapment and dragging of iron particles by thefoam (hydrodynamic drag). Therefore, the amount of water used should be such as to promote the dilution of the pulp to the range of 15 to 20% solids.
[0051] Following the reverse flotation step, an iron concentrate is obtained. The présent invention allows the recovery of more than 90% of the iron présent in the slimes and to obtain concentrâtes with iron contents above 60% with low impurities content, enabling a possible commercialization of this new product that was previously discharged as tailings.
[0052] As described above, the process of invention takes place at a pH range different from that conventionally used. The process proposes the use of collectors other than those traditionally used hitherto, with conditioning time much longer than the time adopted in conventional reverse flotation technology and even longer flotation time, higher dilution of the pulp during flotation, in addition to the absence of any depressant. [0053] In an alternative embodiment of the présent invention, after the reverse column flotation step, the obtained concentrate is sent to a high intensity magnetic concentration step, aiming at the removal of contaminants, mainly quartz and kaolinite not been removed by flotation. In this step, a magnetic field of 13,000 to 18,000 Gauss is applied, gap matrix of 1.1 to 1.5 mm, solids percent in the feed can vary from 15% to 35%, and washing water from 3 to 5 times the feed rate. Magnetic concentration equipment can be used with matrices arranged horizontally orvertically, the latter being combined with pulsation of the pulp in the basin.
[0054] Optionally, Chemical reagents can be used in the magnetic concentration step, aiming at greater selectivity in the séparation between iron minerais and gangue minerais, mainly quartz and kaolinite. The Chemical reagents are dispersants, selected from the group consisting of sodium hexametaphosphate and sodium silicate, and also the reagent called colloïdal magnetite. Colloïdal magnetite increases the magnetic susceptibility of iron minerais, while the dispersants promote the greater dispersion between the iron minerais and the gangue minerais, promoting a greater séparation between them.
[0055] Said Chemical reagents are added to the process in a stirred conditioning tank, with résidence time varying from 2 to 5 minutes, following to the magnetic concentration step.
[0056] The dosages of the reagents applied duringthe magnetic concentration step are 200 to 400 g/t for the dispersants and 300 to 700 g/t for the colloïdal magnetite.
[0057] The combination of flotation steps and magnetic concentration promûtes the removal of quartz higher than 95% and kaolinite higher than 85%, allowing the final concentrate to be obtained with an iron content higher than 66% and SiOz + AI2O3 lower than 4, 0%, in addition to a global recovery of more than 45% and metallic recovery of more than 70%.
[0058] Thus, although only some embodiments of the invention hâve been shown, it will be understood that various omissions, substitutions and alterations may be made by a person skilled in the art without departing from the spirit and scope of the présent invention. The embodiments described should be considered in ail aspects only as illustrative and not restrictive.
[0059] It is expressly provided that ail combinations of the éléments performing the same function in substantially the same manner to achieve the same results are within the scope of the invention. Substitutions of éléments from one described embodiment to another are also fully intended and contemplated. It is also necessary to understand that the drawings are not necessarily in scale, but that they are only of a conceptual nature. The intention is, therefore, to be limited, as indicated by the scope of the appended daims.
[0060] The following examples are offered in the sense of aiding the understanding of the présent invention and should not be considered as limiting its scope.
Example 1
[0061] Iron minerais concentration tests were performed using slimes's samples from iron ore Processing. These sûmes samples were from iron ore operations located in the Quadrilatère Ferrifero Area (state of Minas Gérais, Brazil) and had Chemical, mineralogical and size distribution typical of this région.
[0062] Table 1 shows Chemical composition of the sample having the content of about 45% Fe, 28% SiOz and 3% AI2O3. It is important to remember that kaolinite is the main AI2O3 bearing minerai.
Table 1 - Chemical composition of iron ore sûmes
| Fe (%) | SiO2 (%) | P (%) | AI2O3 (%) | Mn (%) | TiO2 (%) | CaO (%) | MgO (%) | IL(%) Ignition Loss |
| 45.19 | 28.69 | 0.076 | 3.11 | 0.103 | 0.116 | 0.019 | 0.019 | 2.87 |
Ό063] Regarding the size distribution, the slimes sample had about 50% particles below 10 pm and a maximum particle size (top size) near to 45 pm, as shown in the graphie of Figure 2.
[0064] Regarding the mineralogical composition, the samples had about 63% of iron minerais (mainly haematite and goethite), 25% of quartz and 8% of kaolinite, as shown in the graphie of Figure 4.
[0065] The pH adjustment of the slimes, which had 30% solids, was performed in stirred tank with the addition of sodium hydroxide (NaOH) until pH 10.5 was reached.
[0066] 152 g/t of Flotinor-5530® collector, produced by the company Clariant®, was used and the conditioning time was 20 minutes. Water was added to the process in the stirred tank pipe output such that the slimes reached 20% solids.
[0067] Slimes samples were subjected to flotation tests on a single stage, 6-meter-high, 8-inch-diameter column with feed rate of 80 kg/h. The résidence time in the column was approximately 30 minutes and pulp solids percent remained in the range of 20 to 15%. No depressant was added.
[0068] The final concentrate successfully achieved high iron content and low quartz and kaolinite contents. The results presented in Table 2 show the results obtained, with a concentrate containing 62.81% Fe and only 3.21% SiO2 (quartz). A substantial portion of quartz was removed for the flotation tailings, and also a certain amount of kaolinite. In addition, the metallurgical recovery of iron was quite high: 93.83%.
Table 2 - Results from the iron ore slimes concentration route
| Flow | Mass (%) | Fe Rec. (%) | Fe (%) | SiO2 (%) | P (%) | AI2O3 (%) | Mn (%) | IL |
| Ignition Loss (%) | ||||||||
| Feed | 100.00 | 100.00 | 44.52 | 29.44 | 0.077 | 3.04 | 0.075 | 2.60 |
| Concentrate | 66.51 | 93.83 | 62.81 | 3.21 | 0.104 | 2.50 | 0.109 | 3.12 |
| Tailings | 33.49 | 6.17 | 8.20 | 81.54 | 0.024 | 4.12 | 0.007 | 1.57 |
Example 2
[0069] The same sûmes samples used in the previous example were tested with different process parameters, as reported in Table 3:
• Type of collector: traditional (ether-amine) or Flotinor-5530® (amide-amine) • Collector dosage: 50 to 500 g/t • Use of depressant: with or without starch • pH: 8.5 to 10.5
[0070] Slimes samples were subjected to flotation tests on a single stage, 6-meter-high, 8-inch-diameter column with a feed rate of 80 kg/h.
[0071] The results presented in Table 3 show that using traditional ether-amine collectors, the best metallurgical resuit of iron recovery is about 93%, however, a high impurity concentrate (S1O2 > 10%) is obtained. And, in order to obtain a low silica content in the concentrate (3.73%), a high amount of iron is drawn into the float (hydrodynamic drag), which can be proven with the low metallurgical recovery of iron (about 67%).
[0072] Tests using at least 100 g/t of Flotinor-5530®, an amide-amine type collector, at high pH, showed good results. The best resuit was the test using 152 g/t Flotinor-5530®, at pH 10.5, obtaining a concentrate with 63% iron, 3% silica and 94% of metallurgical recovery.
[0073] The use of depressant (starch) impaired results even using Flotinor-5530® as a collector. The results showed a réduction of the metallurgical recovery to about 64%, because it reduces the selectivity of the process.
Table 3 - Process parameters and results obtained in each test
| Collector | (g/t) | Starch (g/t) | pH | Metallic Rec. (%) | Concentrate %Fe | Concentrate %SiO2 |
| Traditional | 105 | 0 | 8.5 | 89.23 | 57.71 | 10.70 |
| Traditional | 113 | 0 | 9.5 | 67.59 | 64.01 | 3.73 |
| Traditional | 115 | 0 | 10.5 | 34.91 | 55.67 | 6.48 |
| Traditional | 112 | 552 | 8.5 | 92.58 | 57.66 | 10.31 |
| Traditional | 101 | 497 | 9.5 | 70.12 | 59.28 | 5.85 |
| Flotinor 5530® | 199 | 0 | 8.5 | 88.11 | 61.63 | 4.55 |
| Flotinor 5530® | 49 | 0 | 8.5 | 96.63 | 58.43 | 7.96 |
| Flotinor 5530® | 51 | 0 | 9.5 | 96.87 | 58.98 | 7.35 |
| Flotinor 5530® | 47 | 0 | 10.5 | 95.67 | 53.72 | 15.3 |
| Flotinor 5530® | 127 | 0 | 10.5 | 95.85 | 63.68 | 4.66 |
| Flotinor 5530® | 108 | 0 | 9.5 | 86.18 | 61.37 | 4.18 |
| Flotinor 5530® | 101 | 0 | 8.5 | 91.24 | 61.04 | 4.74 |
| Flotinor 5530® | 152 | 0 | 8.5 | 87.03 | 61.94 | 4.1 |
| Flotinor 5530® | 149 | 0 | 9.5 | 79.04 | 62.00 | 3.64 |
| Flotinor 5530® | 152 | 0 | 10.5 | 93.83 | 62.81 | 3.21 |
| Flotinor 5530® | 184 | 0 | 10.5 | 93.23 | 62.32 | 3.34 |
| Flotinor 5530® | 472 | 263 | 8.5 | 63.73 | 59.56 | 4.86 |
| Flotinor 5530® | 508 | 563 | 8.64 | 64.52 | 60.65 | 4.60 |
Example 3
[0074] Magnetic concentration tests were performed with the concentrate from the pilot scale flotation, with a feed rate ranging from 80 kg/h to 200 kg/h. Equipment with horizontally disposed matrix without pulsation of pulp and equipment with vertically 5 disposed matrix with pulsation of the pulp in the basin were tested, both with percent solids ranging from 15 to 35%, magnetic field of 13,000 to 18,000 Gauss and gap matrix, from 1.1 to 1.5 mm. The tests were performed with and without addition of Chemical reagents. The results obtained are shown in Table 4 below.
Table 4 - Process parameters and results obtained in magnetic concentration tests
| Matrix | Field (Gauss) | Gap (mm) | Dispersant (g/t) | Colloïdal Magnetite (g/t) | Met. Rec. (%) | Conc. %Fe | Conc. %SiO2 + %ai2o3 |
| Vertical | 13,000 | 1.5 | 0 | 0 | 74.86 | 67.33 | 3.08 |
| Vertical | 13,000 | 1.5 | 0 | 0 | 73.18 | 67.69 | 2.10 |
| Vertical | 13,000 | 1.5 | 0 | 0 | 73.10 | 66.35 | 3.46 |
| Vertical | 13,000 | 1.5 | 0 | 0 | 49.42 | 57.43 | 11.75 |
| Vertical | 13,000 | 1.5 | 300 | 0 | 69.34 | 63.63 | 4.17 |
| Vertical | 13,000 | 1.5 | 0 | 0 | 64.54 | 64.42 | 6.38 |
| Vertical | 13,000 | 1.5 | 0 | 500 | 69.84 | 64.71 | 5.32 |
| Horizontal | 13,000 | 1.1 | 0 | 0 | 70.50 | 65.23 | 5.83 |
| Horizontal | 18,000 | 1.1 | 0 | 0 | 66.30 | 66.40 | 4.09 |
0075] The results of Table 4 show that the application of the high field magnetic concentration, after the flotation step, allows the obtainment of concentrate with iron content above 67%. The addition of 300 g/t of sodium hexametaphosphate as a dispersant allows increasing the iron content in the concentrate from 57.43% to 63.63% and reduce SiO2 + AI2O3 contents from 11.75% to 4.17%. The addition of 500 g/t of colloïdal magnetite promoted an increase in metallic recovery from 64.54% to 69.84% and réduction in S1O2 + AI2O3 contents from 6.38% to 5.32%.
[0076] The tests presented in Table 4 also prove that the increase of the magnetic field from 13,000 Gauss to 18,000 Gauss promûtes an increase in the iron content from
65.23% to 66.40% and réduction in S1O2 + AI2O3 content from 5, 83% to 4.09%.
Example 4
[0077] In addition, continuous pilot scale tests were carried out using a flotation column of 508 mm diameter and 4 meters height in the rougher stage and a magnetic concentration with a field of 13,000 Gauss, gap of 1.5 mm and a pulsating bed in Longi
LGS-500EX 1.3 T equipment in cleaner step. The tests were carried out with a feed rate of 500 kg/h, 35% solids, 200 g/t Flotinor 5530 collector, pH 10.5, 7001iters/h wash water, magnetic field of 13,000 Gauss, gap of 1.5 mm and 300 rpm of basin pulsation. The results obtained are shown in Table 5 below and in Figures 5, 6 and 7.
Table 5 - Results on pilot scale in flotation column + magnetic concentration
| Circuit: Column (rougher) + magnetic concentration (cleaner) | ||||||
| Flow | Mass Rec. (%) | Metallic Rec. (%) | chemistry (%) | Blaine (cm2/g) | ||
| Fe | SiO2 | AI2O3 | ||||
| Feed | 100.00 | 100.00 | 44.79 | 30.87 | 2.70 | Xx |
| RG Concentrate | 78.15 | 92.69 | 53.13 | 17.40 | 2.98 | Xx |
| RG Tailings | 21.85 | 7.31 | 14.98 | 73.08 | 3.78 | Xx |
| CL Concentrate | 51.78 | 76.50 | 66.18 | 2 68 | 0.84 | 2,500 a 3,500 |
| CLTailings | 26.36 | 16.19 | 27.51 | 63.18 | 7.17 | xx |
[0078] The results show that column flotation followed by magnetic concentration allows obtaining concentrate with iron content higher than 66% and SiO2 + AI2O3 contents below 4%. In addition, this route allows obtaining iron concentrate with a spécifie surface (blaine) of more than 2,500 cm2/g, which allows the use of this concentrate as a feedstock (pellet feed) for the pelletizing process, and may also promote energy consumption réduction in the grinding step to obtain feed with a mean surface of 1,500 cm2/g.
Claims (23)
1. Concentration process of iron minerais from ultrafine tailings (slimes) from the Processing of iron ore characterized by comprising the following steps:
a) adjusting the pH of the slimes to a value in the range of 8.5 to 10.5 by adding a base;
b) adding amide-amine type cationic collector, or a mixture of said collector with one or more other collectors, to the sludge and performing the conditioning of said collector;
c) adjusting the pulp percent solids by addition of water; and
d) performing reverse flotation, in the absence of depressant, to obtain an iron rich concentrate.
2. Process, according to daim 1, characterized by further comprising a high field wet magnetic concentration step after step (d).
3. Process, according to claim 1, characterized in that the slimes comprises ultrafine particles containing iron minerais and gangue minerais (mainly quartz and kaolinite).
4. Process, according to claim 3, characterized in that the iron minerais consist mainly of haematite and goethite, and the iron content is 40 to 50%.
5. Process, according to claim 1, characterized in that the slimes hâve 20 to 40% solids.
6. Process, according to claim 1, characterized in that the base added in step (a) is sodium hydroxide (NaOH).
7. Process, according to claim 1, characterized in that the amide-amine type cationic collector is a straight-chain collector formulated from fatty acids of vegetable origin.
8. Process, according to claim 7, characterized in that the amide-amine type cationic collector used is commercially called Flotinor-5530®.
9. Process, according to claim 1, characterized in that the other collectors are selected from ether-amine class organic branched-chain cationic collectors.
10. Process, according to claim 1, characterized in that the collector is added in an amount in the range of 50 to 1000 g/t (grams of collector per ton of slimes).
11. Process, according to claim 1, characterized in that the conditioning time of the collector in step (b) ranges from 10 to 30 minutes, preferably 20 minutes.
12. Process, according to claim 1, characterized in that in step (c) the adjustment of the percent solids is carried out so that the pulp has a solid content in the 5 range of 15 to 25%, preferably 20% solids.
13. Process, according to claim 1, characterized in that, in step (d), reverse flotation occurs preferably in columns, with addition of water for washing the foam and directing the iron minerais to the sunk.
14. Process, according to claim 13, characterized in that the washing water 10 is added in an amount which promûtes the dilution of the pulp to the range of 15 to 20% solids.
15. Process, according to claim 1, characterized in that the résidence time of the pulp in the column flotation in step (d) is from 20 to 60 minutes, preferably 40 minutes.
15
16. Process, according to claim 1, characterized in that the float overflow rate in step (d) is not more than 2 ton/h/m2.
17. Process, according to claim 1, characterized in that the reverse flotation, in step (d), occurs in an open circuit and in one stage.
18. Process, according to claim 1, characterized in that the reverse flotation, 20 in step (d), occurs in open circuit in more than one stage with a cleaner stage.
19. Process, according to claim 2, characterized in that, in the high field wet magnetic concentration step, the field intensity is from 13,000 to 18,000 Gauss.
20. Process, according to claim 2, characterized in that magnetic concentration equipment with horizontally or vertically disposed dies, with or without
25 pulsing movement of the pulp in the basin, is employed.
21. Process, according to claim 2, characterized in that dispersing reagents selected from the group consisting of sodium hexametaphosphate and sodium silicate are employed.
22. Process, according to claim 2, characterized in that colloïdal magnetite is 30 employed as the reagent.
23. Process, according to claim 2, characterized in that the iron concentrate obtained has iron content above 66% by weight, SiOz + AI2O3 below 4.0%.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| BR102017021494-0 | 2017-10-06 | ||
| BR132018070227-0 | 2018-10-01 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| OA19764A true OA19764A (en) | 2021-04-08 |
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