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UDC 669.054.8
RECOVERY OF PRECIOUS METALS FROM DASHKESAN MINERAL TAILINGS
BY COMBINED METHODS
A.A.Haydarov, Ch.M.Kashkay*, A.A.Guliyeva, A.B.Huseynova,
**
A.N.Aghayev*, Z.R.Jafarov*
M.Nagiyev Institute of Catalysis and Inorganic Chemistry, NAS of Azerbaijan Institute of Geology and Geophysics, NAS of Azerbaijan
Received 26.05.2016
In the article information is given on recovery of some valuable metals from tailings of obtained iron ore, their enrichment by using diaphragmatic electrolysis and sorption methods. There were investigated recovery conditions, determined regymes and evaluated efficiency at all stages. As a result of conducted studies the methods able to provide protection of enviroment and technological scheme which allows complex processing of tailings are offered.
Keywords: tailings, percolation column, irrigation, alunite, diaphragmatic electrolysis, sorption.
Introduction
More than 90 million tons of iron ore have been processed from Dashkesan Ore Purification Company's mines since 1954 ("Azerbaijan Mountain-Mine Ore Purification" till 2001). During this period as a result of iron ore processing 46.5 million tons of tailings have been collected. While producing concentrates of purification by wet and dry methods obtained tailings have been collected to 42 hectares of planned area. By natural irrigation with rain and snow water metals of this tailings migrates to environment damaging ecological norms. Exploitation of Dashkesan iron ore deposits for the years gathered mineral tailings around the mines which can be used as a source for producing precious metals.
The calculations based on approximate amount, weight and other parameters of tailings in sand showed that it was around 20 million tons.
There should be favorable factors for the extraction of metals from tailing materials. The most important among them is that these rocks should be crushed while recovering out earth's surface. There is no need to perform these stages while processing sand size tailings. On the other hand, in spite of lack concentration of metals in tailings, complex production process enables efficient implementation. At the same time this allows using modern extractive and selective sorbents.
One of the methods considered economically advantageous is underground irrigation process of tailings based on selective solving or non-ferrous, rare and noble metals with chemical reagents [1-3]. Underground irrigation and crushing technology of metals in the world mining industry increases day by day. The reason for this is exhaustion of large and close to earth surface ore deposits, on the other hand, tightening economic and ecological requirements. It is known that, currently, all uranium mining in Kazakhstan and Uzbekistan more than 27% of world copper production, also rare and noble metals are produced by this method. Not surprisingly, the US National Academy of Sciences, referring to the technology of in-situ leaching (ISL) mining technologies created The Committee on Evolutionary and Revolutionary for the mining of the National Academy of Sciences, 2002. It shows that the ISL technology is considered the latest technology and in many cases irreplaceable one. Underground producing technology can be used in all kinds of ore deposits and their tailings processing. Not only in all fields, even in different parts of the field it can be applied separately. Scientists of Institute of Geology and Geophysics and Institute of Catalysis and Inorganic Chemistry have considerable experience in the field of complex or selective irrigating metals from raw materials, extract them from each other or make them pure.
Table 1. Physical and mechanical properties of enriched wet tailing materials
Samples taken from fields Moisture of samples, % Weight of moist samples, g/sm3 Dry weight of samples Avera ge granulometric composition of waste, %
+ 0.63 mm - 0.63 + 0.4 mm - 0.4+0.315 mm - 0.315+0.1 mm - 0.16 + 0.1 mm - 0.1+ 0.063 mm 0.063+0.005 mm - 0.005 mm
I field 112.5 1.89 11.83 1.3 1.9 6.9 42.5 22.3 11.4 7.7 6.0
II field 00.74 1.85 11.89 6.5 6.1 6.1 44.8 14.2 5.9 2.3 3.0
III field 44.6 1.66 22.0 3.2 3.3 3.3 31.5 20.7 14.7 4.5 13.3
Table 2. The average chemical composition of the tailing samples taken from different areas
Samples taken from the field Average quality content of mixed composition, %
SiO2 Fe magnetic Fe3O4 Al2Os CaO MgO S Total
I field 49.7 5.0 8 11.0 24.8 0.9 0.4 99.8
II field 44.1 8.1 13.3 7.0 24.3 2.0 0.4 99.2
III field 36.5 19.1 26.1 5.5 11.2 0.7 0.2 99.3
Taking into account research part of this study and existence of required equipment for half-industrial testing makes the project commercially profitable and possible.
The purpose of presented study is to determine and organize production process of economically feasible metals in Dashkesan iron ore mineral tailings.
Chemical analysis of initial samples taken from different places and deposits of beach tailing field was carried out with Thermo Scientific x-ray fluorescence (XRF) spectrometer. Analysis showed that Co, Cu, Mn, Al have a high concentration and Zn, Pb, It, Sr and As have low concentration in tailings. Investigated physical and mechanical properties of tailings which was enriched by wet method and the results were given in Table 1.
Granulometric composition of 70-90% of tailings insist of particles smaller than 0.3 mm.
In the Table 2 the chemical composition of the samples is given according to macroelements which were taken from different areas of landfill. The main components of tailings as follows: Fe, Al, Ca, Mg, Si. There were few valuable components in tailings such as, g/t: Co - 27-60, Cu - 432-517, MnO - 0.24-0.71, Zn - 155, Pb - 82, Y - 27, Zr - 28, Ar - 121. These elements located in tailings as an isometric mixture. Min-eralogical analysis of tailings showed contained,
%: hematite - 5.6, quartz - 13.3, pyrite - 1.5, calsite - 14.8, dolomite - 3.0, kaolinite - 12.2, clinochlor - 9.3, androdite - 40.3.
Research methods
For testing the heap and underground irrigation process iron ore tailings in laboratory by the simple and cheap methods percolation columns of 25 cm of height and a diameter 45 cm were used. Tailings in 0.3-0.5 kg weight was filled to columns and irrigated with different concentration of sulfuric acid by drop method. Factors affected to the quality of solution (concentration of leaching solution, time, pH, and eH) and concentration of valuable components which was extracted to solution were followed during the process. In efficient solutions pH, eH, acidity, Co, Mn, Cu, Zn, Fe and other metals were analyzed. Determination of metals in tailings products was carried out with "Bruker S2 Picofox" x-ray fluorescence spectrometer. Irrigation of tailings in columns was done in two modes: a) solutions received from irrigation, bringing to initial acidity again were sent to re-irrigation process; b) in order to study comparative dynamics yield of metals with acid of known concentration deliver to complete irrigation of valuable components from tailings with new portions. Sulfuric acid for irrigating tailings conduced in handmade diaphragmatic
electrolysis device. In device as cathode was used a stainless steel plate and as anode used lead board was. The space between electrodes was bordered with asbestos board. When K2SO4 solution flowed with 0.25 litre in minute and 6 V tension and 3 A currency shifted from solution at pH=12-13 in cathode zone and at pH=2-2.5 in anode zone.
Experimental part
We have defined the concentration of acid used in complete irrigation of tailings in work [4]. Provided numerous experiments showed that when the concentration of used acid was pH=1, yield percent of metals which replaced from tailings to solution increased.
Changes of pH and oxidation-reduction potential (eH) during six irrigation process (every time added new acid) were given in Figures 1 and 2. As it can be seen from Figure 1 at pH=0.95, when the solution undergone to irrigation this number increased to 7.44, at next irrigation stages decreased to 0.95 again, oxidation-reduction potential of process increased from 170 to 435 mV (Figure 2). This is explained by the fact that calcium-containing minerals (calcite and dolomite) in waste neutralized the sulfuric acid solution in first minutes (pH rises). It can be seen in further irrigation of sulfate contained compounds decrease of acidity, increase in concentration of metals. Changes in eH in 5th irrigation associated with changing concentration of metals and sulfuric
0 -I-,-,-,-,-,-,-,
0 1 2 3 4 5 6 7 Irrigation (times)
Fig. 1. Changing of pH of solution depending on irrigation (weight of tailing is 500 g, concentration of used acid in irrigation is 1N, S:L=5:1, temperature -200C, irrigation duration by drop method - 4 h).
acid in solution.
Concentrations of metals in received solutions were as follows, mq/l: Al - 3228, Co -58.9, Mn -1899.6, Cu - 635, Zn - 81.16, Fe -13628.7. The extraction of metals to solution from tailings were as follows, %: Al-1.82; Co-65.9, Mn-17.5, Cu-30.5, Zn-25.1, Fe-4.1. The next series of experiments was not provided with solution, but by circulation of received solution after irrigation to percolation columns. The results were given in Figure 4.
The results of irrigated tailings 6 times in 6 days were given in Figure 3. Irrigated 1N solution of H2SO4 was kept in percolator within 24 hours. As it can be seen that when irrigation stages increases also increases concentration of metals in solution, but decreases pH. Concentrations of metals in received solutions were as follows: Al-3228; Co-58.9; Mn-1899,6; Cu-635, Zn-81.16; Fe-13628.7. The extraction of metals to solution from waste were as following: Al-1.82; Co-65.9%, Mn-17.5%, Cu-30.5%, Zn-25.1%, Fe-4.1%. The next series of experiments was not provided with solution, but by circulation of received solution after irrigation to percolation colons. The results were given in figure 4.
The first three irrigation period gradually increased extraction of metals to solution and pH degree of solution increased from 3 to 6.5. The amount of manganese and copper in solution were 65.85 and 52.99 mg/l respectively.
Irrigation (times)
Fig. 2. Changing of oxidation-reduction potential of solution depending on irrigation stage (weight of tailings is 500 g, concentration of used acid in irrigation is 1N, S:L=5:1, temperature - 200C, irrigation duration by drop method - 4 h).
2000 1800 1600 -
г- 1400 ^ ы>
ä 1200 ^
0
1 юоо ^ £
9 on
600 400 200 0
pH 1 pH 7 pH 5
pH 4 pH 3.5 pH 2 pH 1.5 acidity
0
1
5
6
2 3 4
Irrigation, times
Fig. 3. The results of irrigation of iron-ore waste with 1N sulfuric acid (weight of waste is 500 g, concentration of used acid in irrigation is 1N S:L=5:1, temperature - 200C, irrigation duration by drop method - 4 h): 1 - Mn, 2 - Cu, 3 - Co.
pH
Fig. 4. Dependence of concentration of metals by re-adding solutions received after irrigation to circulation from pH of solution (pH of solution received from the first circulation is 3, in the second circulation pH=4.4, in the trird circulation pH=6, in the fourth circulation pH=6.5); 1 - Mn, 2 - Cu, 3 - Fe, 4 - Zn, 5 - Co.
1
The reason of small amount of metals in solutions was lack of acidity in circulated solutions. As it can be seen from Figure 4 after 4th irrigation pH degree of solution reached 6.5. In this pH Fe, Cu, Zn gets to sediment not ionic. Received sediments catched by iron-hydroxides in the down part in percolator.
Irrigation, times
Fig. 5. The dependence of concentration of metals from pH degree of solutions after return to circulation of solutions received from irrigation. Initial pH=2 (pH after first circulation is 2, in the second circulation pH=2.3, in the trird circulation pH=2.5, in the fourth circulation pH=2.6, in the fifth pH=2.7, in the sixth pH=2.8), S:L=1:1; 1 - Mn, 2 - Cu, 3 -Fe, 4 - Zn, 5 -Co.
It can be explained by gradually increasing equilibrium pH of solution from 3 to 6.5. In pH>6.5 leads to decreasing of concentration some metals such as Co, Cu, Zn, Fe. At the lower part of percolator observed brown colored iron hydroxide sediment (pH range is 5.2-6.5). All iron in the solution accumulated as 100% sediment of Fe(OH)3 (at 6.5 pH). Cu+2, Zn+2, Co+2, Al ions sediments and sorbes on Fe(OH)3.
The experiments showed that one of the main factors for irrigation of metals was selecting S:L phases ratio. When S:L ratio is 1:1 pH of the solution which enter and drop out from percolator does not change. In six irrigation period pH of solution changes in 2-2.1-2.8 ratio. In this case there was a significant changes in concentration of Mn, Cu, Fe but small changes in concentration of Co and Zn (Figure 5).
The results got substantiate how to keep a value of initial pH of solution for un-precipitation of the valuable components in efficient solution. If irrigate heap waste with sul-fated solution then metals replaced to solution will be in sulphate form. Sulfate salts in solution dissosiate like below:
Mn„(SO4)m ~ mMn"+ + nSOmA- .
The cations hydrolyzes in solution by stage and appears hydroxso compounds:
Mn"+ + H2O^Me(OH)
+(«-1)
+ H+
2+
Me(OH)+(" ^i^O Me(OH) Me(OH)0 + OH- = Me(OH)
When pH increases Zn2+, Cu2+, Fe Fe3+, Co2+, Mn2+ ions may be also in a different molecular or ion forms depending on concentration of metal. In a neutral solutions (pH=7) irrigated cations again absorb on waste particles and precipitated iron hydroxides [Fe(OH)2, Fe(OH)3].
Numerous experiments show that to raise irrigation of non-ferrous metal-containing solution with solutions over 3.5-4 pH is not appropriate.
Obtaining sulfuric acid from irrigation products of alunite. As a result of our experiments it was defined that the use of sulfuric acid for extracting metals were 18 l, 1 N per 1 ton tailings. The necessary sulfuric acid can be produced from tailings deposite which is close to Dashkesan-Zaylik alunite deposite by obtaining heap solving of alunite from K2SO4 with dia-phragmic electrolysis method. There are 4 stages of technological process:
1) heap solving of alunite ore :
KA13(S04)2(0H)6+6K0H^3KA102+2K2SC>4+6H2C>;
2) neutralizing aluminate solution:
2KA102+H2S04+2H20 -> K2S04+2A1(0H)3;
3) electrolysis of sulfuric salts in dia-phragmic electrolysis device:
2K2SO4+6H2O electrolys2H2 (K)+4KOH+O2 (A)+ +H2SO4;
4) thermal decomposition of aluminium:
1300C
Al(OH)3
AlOOH + H2O.
The essence of electrolysis process can be explained so: K+ + e =K0 Standard electrode potential of this system is negative with respect to potential of water electrode in water environment (-0.41 V). That's why electrochemical reduction happens on cathode by emissing H2; K+ by closing to cathode collects to cathode zone. In anode emisses O2 by electrochemical oxidation of water, accompained by O2 emission, takes place:
2H2O - 4 e = O2 + 4H+.
Because of the standard electrod potential of this system eH=1.23 V considerably lower than 2SO2~ +2 e = S2O82~ system (2.01 V)
during electrolysis ( SO^ ) ions take direction to anode and collects on anode. Finally, in cathode emisses H2, around cathod zone KOH, in anode O2 and around anode observes H2SO4. pH of solution flowed from anode zone is approximately 11-13, from cathode zone pH=1-2. Acid received from the process sent to irrigation of tailing ores, alkaline solution is sent to irrigation of alunite ore.
Sorption of metal ions from irrigative solution of tailings
Extract Mn, Al, Cu, Zn and Co elements from the solutions received after irrigation of tailings with weak sulfuric acid is an important point. Analysis of the samples which were taken from various areas showed that as the compound and amount of elements in tailings are different, concentration of elements in irrigated solutions were different too.
The analysis of modern references showed that to extract and enrich metals from the solutions and to make them harmless against high dosage of irrigative solutions the most relevant method was ion exchange [1]. It is possible to extract and enrich non-ferrous, noble and rare metals from complex technological solutions with high yields by using ion exchange sorbents. Sorption of metal ions from sulfate solutions were carried out in static and dynamic conditions [2]. For sorption of ions from sulfate solutions they used high acidic cationite KY-2-8 (Na- and H-form).
Firstly there has been studied sorption of Zn2+, Cu2+, Co2+ and Fe3+ ions in 0.02 M sulfuric model solution in the static condition. In the Table 3 were given dependence of static volume from duration of phases and pH.
As it can be seen in the Table equilibrium system restored as soon as possible. Compare to other ions selectivity for Fe3+ is 25-30%. Arresting two-valent metal ions with sorbent occurs in the same acidity and in similar amount. At pH=1 compared to other concentrations sorption of metals reduced around 10-15%.
The most important affect to sorption of metals is acidity of solution and concentration of metals (Table 4). In the this Table the results of sorption of metals depending on initial pH of solution from irrigative solutions of tailings in static condition are given. The results show that at high concentration of acid (1 M) sorption of metals does not occur. When pH increases from 1 to 6 sorption of metal ions increases to. As it can be seen from the table when pH is higher than 3.5 arrest degree of metal ions is 97-100%, but selectivity depending on yield of metals does not occur. All ions arrested as cati-onite by KY-2-8.
Control of static ion exchange volume by using different concentration of elements in tailing solutions showed that the numbers for Cu, Zn and Co are lower, 0.065, 0.490 and 0.52 mmol-ekv/q ionite respectively. Because concentration of alkaline-earth metals in initial solutions were higher and KY-2-8 showed high selectivity for this elements (2.04 - Ca2+, 1.46 mmol-ekv/q ionite).
Sorption of metals in tailings solution controlled also at dynamic conditions. Concentration of copper, zinc, cobalt, manganese, iron and aluminium in filtrate changed from 0.012 to 1.21 mg/l. Compare to initial concentration observed whole practic arrest of this metals. Dinamic ion exchange for copper - 1.75, zinc -22.1, iron - 1.6, calcium - 36.19, magnesium -
22.0, cobalt - 21 mq/q.
Desorption of metals from KY-2-8 gum controlled by using different concentration of H2SO4, HCl and NaCl. Using H2SO4 for desorption showed that irrigate saturated ionite with 10% solution as a result of formation less soluble K2SO4 precipitation in ionite phase observed slag formation. It leads to become worsening diffusion conditions of reagents, reduce yield percentage of metals which will desorb.
Because of the high price and volatility using HCl as the desorbent is not economically profitable. But using salt solution for desorption allows regeneration ionite as cationite form. Compare to mineral acids desorption rate of Cu, Co, Mn with NaCl solution from ionite in static conditions were lower. Despite this desorption with NaCl solution have some advantages. During irrigation with sulfuric solution cationite changes to H+ form, but if we do againiest sorption it is necessary being in Na form of sorbent. In this case using KY-2-8 cationite for desorb-ing metals by using NaCl solution have some advantages (Table 5).
Special volume of solution which flows from columns was 2.5 times more than volume of ionite. So if we use NaCl solution as a de-sorbent special volume of irrigative solution will reduce, desorption degree of metals will increase. At the same time occurs regeneration of ionite to natrium form.
Table 3. The dependence of static volume of sorption exchange of metal ions with KY-2-8 cationite on touch duration of phases and ^ pH____
Touch duration, min Co2+ Cu2+ Zn2+ Fe3+
pH
1 2 5.6 1 2 5.6 1 2 5.5 1 2
30 1.90 2.1 2.2 1.82 2.2 2.25 2.2 2.23 2.25 2.5 3.1
60 1.95 2.2 2.3 1.84 2.3 2.38 2.22 2.30 2.34 2.60 3.15
90 1.98 2.3 2.4 1.86 2.35 2.42 2.24 2.40 2.42 2.65 3.2
120 2.0 2.4 2.6 1.88 2.40 2.45 2.26 2.42 2.5 2.7 3.0
180 2.20 2.42 2.7 1.92 2.46 2.6 2.28 2.46 2.6 2.80 3.25
240 2.25 2.45 2.75 1.94 2.5 2.7 2.29 2.48 2.7 2.85 3.3
Equilibrium pH Concentration of metals before sorption, g/l Sorption degree, %
Ca Zn Fe Cu Mn Co Ca Zn Fe Cu Mn Co
Cationite КУ-2-8
1.0 721 1.71 3.18 17.21 16.48 0.23 97 93.5 92 93 94 95
3.5 3115.7 35.53 220 94.26 293.69 23.3 98 95 93.4 94.2 95 97
4.2 4046.7 76.0 2344 227.0 567.9 48.16 100 100 100 100 100 100
6.0 4046.7 43.39 220 160.0 567.99 48.16 100 100 100 100 100 100
Table 4. Effect of pH to processing solution of tailings arresting metals by sorption method (Cmitial= 1M)
Table 5. Eluation of metals from ionite with NaCl solution (speed - 5 cm3/hour)
№ Volume of irrigative solution, ml Concentration of metals in irrigative solution, mq/l Desorbtion degree of metals, %
Cu Zn Fe Co Mn Cu Zn Fe Co Mn
1 50 463 23.98 60.72 26.19 269.7 52.0 38.0 27.6 53.5 47.5
2 50 258.4 18.99 51.7 14.30 153.9 29.0 30.1 23.5 29.2 26.4
3 100 174.6 11.358 20.24 4.5 88.6 19.6 18 9.2 13.2 15.6
4 100 11.14 1.0 2.2 0.5 68.73 1.25 1.58 1.0 2.0 12.1
Total desorption degree, % 102 87.7 61.3 97.9 101
According to obtained results prepared technological scheme of extracting Co, Cu, Mn,
Al metals from tailings of Dashkesan Ore Purification combinate (Figure 6):
Fig. 6. Extract of the valuable metals from Dashkesan ore deposite.
The approximate reserve and price of metals in tailings. It Table 6 were given price and reserve of notable metals in beach tailings, price and approximate reserve of microelements were given in table 7.
As a result of experiments which conducted in the Institutes of NAS of Azerbaijan identified irrigation modes of these metals with weak sulfuric acid. As tailings contains less amount of metals the main problem was to create cheaper technological scheme. Taking into account this terms, considered the engineering
schemes of production process in beach waste zone and tested with small models in laboratory. As a result two alternatives were offered: 1) irrigation of beach tailings in location (Figure 7), 2) partly irrigation with conveyer system (Figure 8).
For extracting precious metals from tailings and enriching their solutions there has been offered to irrigate the surface of beach tailings mass with weak sulfuric acid (pH=0.5-1) and to create natural or manmade drainage system in lower horizonts of area.
Table 6. The price and reserve of notable metals in beach waste (total weight of tailings was accepted 20 000 000 tons)
Metals Average amount (range g/t) Total weight of metal/ the lowest extracted amount (50%) ton S ale pric e * (Till 2015 october ) USA $ Total pric e of metal in tai l -ings/price of extracted metal, mln USA $
Co 27-60 540-1200/270-600 29 000 15.66-34.8/7.83-17.4
Cu 432-517 8640-10340/4320-5170 5 200 45.0-53.77/22.5-28.88
Mg 2411-2800 48220-56000/24110-28000 880 42.43-49.28/21.22-24.64
Total: The price of reserve: 103.09-137.85 The price of the lowest extracted amount: 51.55-70.0
* Sale price of metals were taken from MetalPrice.com
Table 7. The price and reserve of notable metals in beach waste (total weight of tailings was accepted 20 000 000 tons)
Metals Average amount, g/t Total weight of metal/ at least extracted amount (50%) ton S ale price (Till 2015 october ) USA $ Total pric e of metal in tai lings/price of extracted metal mln USA $
Zinc 155 3100/1550 1600 5.0/2.5
Lead 82 1640/820 1700 2.8/1.4
Ittrium(oxide) 27 540/270 6400 3.5/1.75
Zirconium 28 560/280 1280 0.717/0.36
Arsen 121 2420/1210 1800 4.36/2.178
Total : The price of reserve: 16.36 mln The price of the lowest extracted portion: 8.18 mln
Fig. 7. Irrigation of beach tailings in location.
Mobile analyti cal laboratory
Fig. 8. Partly irrigation with conveyer system.
If rains fill beach area with water by reaching required level of pH of water with sulfuric acid it will be possible to carry out and evaporate metals with complex and selective ways by irrigating and using sorption and extraction methods.
In this way beach sand continuously poured on conveyer and washing solution splashed on it. As conveyer is slope productive solution collected in one side and irrigated sand in another side.
Anticipated economic benefits. Because of the high precious metal potential of Dashkesan mineral tailings as a result of organizing production it will give benefits economical activity of "Dashkesan Purification" company and will compensate metal need of country's industry and lead to use and recultivation of environmentally harmful tailings free heavy metals in different areas.
Results
By using other useful fields of Dashkesan ore deposite these were defined efficient parameters and regime of extracting valuable components from tailings of Ore Purification combinate (Zaylik alynite deposite, cobalt deposite in north Dashkesan, processing tailings of limestone).
This project was supported by the Science Development Foundation under the President of the Republic of Azerbaijan. Grant № SDF/MQM/ Industry-2014-4(19)-06/06/2.
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KOMBÍNO OLUNMUS ÜSULLARLA DA§KOSONÍN MÍNERAL TULLANTILARINDAN QÍYMOTLÍ
METALLARIN ÇIXARILMASI
A.0.Heydarov, Ç.M.Kaçkay, A.A.Quliyeva, A.B.Hüseynova, Э-N.Agayev, Z.R.Caf3rov
Maqalada damir filizinin zanginlaçmasindan alinan tullantilardan bir sira qiymatli metallann topa hallolma, diafraqmali elektroliz va sorbsiya üsullarindan istifada etmakla çixarilmasi haqqinda malumat verilir. Bütün marhalalar üzra metallarin çixarilma çaraiti araçdrnlmiç, rejmlari mûayyanlaçdirilmiç va samaraliliyi qiymatlandirilmiçdir. Aparilan tadqiqatlar naticasinda müasir dovrün an qlobal problerindan biri olan atraf mühitin mühafizasini tamin edan, tullantilarin kompleks emalina imkan veran texnoloji sxem taklif olunmuçdur.
Açar sozlar: tullanti, perkolyasyon kolonka, sulanma, alunit, diafraqmali elektroliz, sorbsiya.
ИЗВЛЕЧЕНИЕ ЦЕННЫХ МЕТАЛЛОВ ИЗ МИНЕРАЛЬНЫХ ОБОГАЩЕННЫХ ХВОСТОВ ДАШКЕСАНА КОМБИНИРОВАННЫМИ СПОСОБАМИ
ААХейдаров, ЧЖ.Кашкай, АА.Кулиева, А.Б.Гусейнова, А.Н.Агаев, З.Р.Джафаров
Сообщается об извлечении некоторых ценных металлов из обогащенных хвостов железных руд с использованием способов: кучное выщелачивание, диафрагменный электролиз и сорбции. Установлены параметры и режимы процесса извлечения ценных металлов по всем этапам переработки и оценена рациональность исследуемого процесса. На основе проведенных исследований предложена технологическая схема комплексной переработки отвалов, отвечающей современным экологическим требованиям по охране окружающей среды.
Ключевые слова: обогащенные хвосты, перколяционная колонка, орошение, алунит, диафрагменный электролиз, сорбция.
