Introduction

In quarries, tailings are extracted along with valuable minerals in ores, which are separated during the crushing and purification steps. Tailings are usually piled up more or less near a mine or processing plant. One of the long-term effects of this operation in mining areas is the increase of some elements concentration in the tailings accumulation areas (Ghose and Sen 2001; Badeenezhad and Azhdarpoor 2019; Jalili 2020). Due to the leakage of produced mineral drains throughout the leaching of mineral deposits by precipitation to the surface and groundwater, they caused many destructive environmental effects. These pollutants' environmental impacts can lead to public health deficiencies in human societies (Xu et al. 2009; Badeenezhad et al. 2019). The iron ore content must also be decomposed and purified after extraction. If impurities such as silica and alumina are above the acceptable range and the iron content is less than 60%, the need for mine effluent treatment will be more necessary than ever (Ding et al. 2017). Most effluents in ore mines are concentrated in the crushing, grinding, sieving, washing, using magnetic separators, or flotation stages (Ghose 2003). Iron ore waste after the preparation process may contain coarse and fine particles in the wash water, which forms tailings.

Due to the climatic conditions of Yazd province and water shortage in this area, the water reuse in the iron ore mining process can be a cost-effective option. In central iron ore, refined tailings contain amounts of water that must be dehydrated and dried have the save mien, and their moisture content should be reached 9–10%. For this purpose, filters are used to separate the resulting concentrated water. Then the dewatered concentrate transferred to the dumpsite and stored there. The tailings are also diverted to thickener for dewatering. There, the solids settle, and water overflows from the top of the thickener. The deposited solid particles are directed to the center by the thickener floor collector arm and pumped to the tailings dam.

On the other hand, due to the mineral nature of the produced effluent in this type of mine, it is not possible to completely dehydrate by filter press. Maximum water reduction of such tailings prevent contaminants infiltration into groundwater and other related environmental problems. For this purpose, the combined processes of sludge dehydration, the reduction of annual polymer consumption, and the reduction of the produced sludge by these mines are an option. On the other hand, particle settling rate and water supply with less turbidity can be achieved for water reuse in this process (Nasrollahi et al. 2014; Jalili et al. 2019).

Due to the limited efficiency of organic matter removal in the conventional coagulation process (Hou et al. 2017), Hybrid Ozone-Coagulation (HOC) process for effluent treatment used in this study. This could be effective according to the pre-tests. Based on the pre-test results, the ozonation coagulation- flocculation was effective, due to the nature of the produced sludge by coagulation with alum and its tendency to absorb water, dewatering is expected to be more difficult. Therefore, reducing polymer consumption can be effective in improving dehydration. Finally, the use of ozone to elements removal has been associated with less sludge production compared to polymerization. The innovation of this study was the conversion investigation of Fe2+ to Fe3+ and Al2+ to Al3+ during the ozonation process. This process significantly can lead to Al3+ and Fe3+ coagulants production and ultimately, it exceedingly reduces the need for coagulant consumption.

Organic matter is one of the most troublesome constituents of water and wastewater that interferes with coagulation and flocculation processes. Coagulation and flocculation are complex treatment technologies that aim to maximize the removal of suspended solids, maximize the removal of natural organic matter (NOM), and minimize the coagulant residual in treated water. Coagulant selection, dosing rates and performance are heavily influenced by the nature and concentrations of NOM, which is a mixture of organic compounds that vary greatly in terms of their physical and chemical characteristics (Leopold and Freese 2009). If the coagulant dose is insufficient to overcome this demand, aluminum-NOM complexes will form and remain in dissolved or colloidal form. The coagulant dose must be increased to allow the dissolved/colloidal aluminum-NOM complexes to form particles that are heavy enough to settle. Alternatively, a coagulant aid such as activated silica, bentonite or lime can be added. It is important to note that some NOM fractions cannot be removed by coagulation at any pH or dose (Canada 2019). Finally, this study aimed to evaluate and compare the efficiency of the coagulation and flocculation process with the hybrid process, coagulation and flocculation with ozonation/lime in crushing lines effluent treatment of Iran's Iron Ore Company.

Materials and methods

The current study was done to determine the efficiency of the combined process of coagulation and flocculation-ozonation/lime in the effluent treatment of Iran's Central Iron Ore crushing line. The laboratory analyzes were performed by using the jar test method. The experimental parameters in this study included the contact time of ozonation, the polymer concentration, settling time, and coagulation and flocculation time.

Sampling

In this study, Iran's Central Iron Ore Refinery crushing line's raw effluent was investigated. For sampling, the specimen was collected manually through the effluent passage and before polymerization (Alum-based Cationic polymers).

Experimental analysis

All experiments were performed at pH = 7–8 (because the pH of the effluent leaving the crusher line and before adding the polymer in the effluent transfer line to the treatment unit was 7–8 on average) and it was at an average ambient temperature of 22–27 °C. The independent parameters were determined step by step, and the range of anyone is expressed in Table 1.

Table 1 Evaluated independent parameters in this study
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To determine the efficiency of the investigated method in this subject, the chemical oxygen demand (COD), total suspended solids (TSS), sludge volume index (SVI), suspended solids (SS), and turbidity and finally were measured as a response and compared to the initial effluent.

In the first step, the optimal contact time with ozone was investigated. First, after 5 min of effluent contact with ozone (gO3/hr.5 = nominal capacity of the ozonation device), the jar test (Jar test technical specifications: with timer, distance meter and color touch screen microprocessor speed control, adjustable in 3 different steps, adjustable speed from 10 to 250 rpm and unlimited time adjustment, propeller and rod made of 316 steel, direct current motor without round swing with dimensions 230 × 450 × 1000 (mm)) was run by keeping the polymer/lime concentration and settling time constant, COD, turbidity, and SVI removal percentage was determined. These steps were done for a contact time of 5 min (0.42 gr.O3), 10 min (0.83 gr.O3), and 15 min (1.25 gr.O3) to determine the optimal contact time with O3.

The jar test included ozonation contact time (5, 10, and 15 min) and polymer concentration (three concentrations of 10, 20, and 30 g per ton of dry sludge). Also, three settling times (5, 10, and 20 min), coagulation times (30, 60, and 90 s), and flocculation times (10, 15, and 20 min) were examined. In each step, the optimal value for each parameter was checked. In total, polymer/lime concentration and ozonation time were investigated. So, nine enforcements were performed. In each step, a control sample was considered. After determining the optimal conditions for both processes (coagulation and flocculation process and coagulation and flocculation process with ozonation/lime), two samples were considered for scanning electron microscope (SEM) analysis. Three samples were taken after three ozonation times (5, 10, and 15 min) to determine the conversion of Fe2+ and Al2+ to Fe3+ and Al3+, respectively, by Inductively coupled plasma-optical emission spectrometry (ICP-OES) analysis. Two samples were taken from the iron ore refinery crushing line for ICP-OES analysis to determine some elements concentration in the effluent. The total number of required samples was equal to 63 (56 + 7 = 63).

Instrumental analysis

Due to the oxidation of Fe2+ to Fe3+ and Al2+ to Al3+ during the ozonation, the oxidized particles were deposited into the sludge. In the case of aluminum-based coagulants, the form of aluminum (e.g., particulate or dissolved) that will be present depends on a wide variety of environmental parameters, including pH, temperature, NOM and the presence of inorganic ligands such as fluoride, sulfate, silicate and phosphorus (Canada 2021). When aluminum-based coagulants are added to water, chemical reactions occur with the organic and inorganic particles in that water. NOM acts as a ligand that complexes the positively-charged aluminum ions, exerting a coagulant demand that must be overcome before flocculation can occur (Haarhoff and Edzwald 2013) but NOM amount in iron ore effluent is low. Thus, the amount of dissolved Fe and Al in the supernatant and sedimentation was measured separately by ICP-OES (Élan 6100 DRC-e). Then it was compared with the initial concentration of iron in the effluent. In addition, the other elements concentrations were determined using ICP-OES. The SEM image (SEM FEI Quanta 200) was used to study the three-dimensional image of the formed sludge. Turbidity was measured by the HACH portable turbidity meter. COD was measured by the COD vial according to the Standard Methods for the Examination of Water and Waste Water 2005-B5220 (Palácio et al. 2016). After each experiment, the COD amount relative to the raw sample was evaluated, and its removal percentage was determined. The amount of SVI was also assessed at each stage of the experiments. SEM and ICP-OES analyses were performed by sending samples to the laboratory.

Methods of data analysis

Statistical analysis

In this study, descriptive statistical indicators such as mean, standard deviation, and percentage were used to express the parameters concentrations and process efficiency. The difference between the parameters was determined by T-test. The significance level was considered 0.05. The correlation of the removal efficiency to each variable was determined using Pearson correlation. All statistical analyzes were performed in SPSS 2018. The figures were also drawn using the Origin-pro software 2020.

Cost–benefit analysis

Since this method was used on an industrial scale, the cost–benefit estimation of the process is very valuable. Therefore, in the present study, the cost–benefit analysis of each procedure was determined using EQ. (1) (Gaziano et al. 2006):

$$\mathrm{ICER}=\frac{\left({C}_{0}-{C}_{1}\right)}{\left({E}_{0}-{E}_{1}\right)}$$
(1)

Which:

C0: the initial COD concentration, C1: the final COD concentration, E0: process cost, and E1: the coagulation-flocculation cost.

Results

At first, the characteristics of the studied raw effluent and the environmental discharge standard are presented in Table 2.

Table 2 Specifications of the studied raw effluent and environmental discharge standard of Iran
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According to Table 2, the achieved results for all parameters significantly were higher than Iran's standard, as COD = 305 ± 21.06 mg/L (> 60 mg/L), turbidity = 312 ± 12.71 NTU (> 50NTU), and SS = 161 ± 51.34 ml/l (> 0 ml/l). So, the evaluation of advanced oxidation processes such as ozonation is essential. To reach this goal, ozonation process's effect on coagulation and flocculation of effluent from Iran's iron ore was investigated. Finally, the effect of the operative parameters on process efficiency was evaluated. The effluent quality in each of the processes was assessed and measured.

Figure 1 shows the ozonation effect on the amount of COD, turbidity, SVI, and SS remaining in the effluent at different polymer concentrations use.

Fig. 1
figure 1

The effect of polymer concentration on COD, turbidity, SVI, and SS (b non-ozonation a ozonation (15 min)) (coagulation = 30 s, flocculation = 10 min and precipitation = 30 min)

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As shown in Fig. 1, with increasing the polymer dose COD, the turbidity, SVI, and SS removal efficiency increased. But this removal rate was not cost-effective (see Fig. 8: Cost-effectiveness of each process). Thus, without ozonation, parameters including turbidity, the concentrations of COD, and SS at 30 mg/L were lower than other concentrations. SVI is the only indicator that has reached its minimum at a concentration of 30 mg/L (73.68 ml/g). In the presence of 15 min of ozonation, with increasing polymer concentration, the turbidity (59%), COD (37%), and SS (22.22%) decreased. Only the SVI index did not change much (7.38%) with increasing polymer concentration in the presence of ozonation.

In addition, the amount of these indicators in the treated effluent in the presence of the ozonation process was much less than the process without ozonation (p < 0.05). In other words, the elimination rate of the studied parameters in the ozonation process was higher than in the free of ozonation process. According to the results, the COD removal (p = 0.011), turbidity (p = 0.023), SVI (p = 0.028), and SS (p = 0.031) in ozonation process was higher than that in process without ozonation. The effect of ozonation at different coagulation times on COD, turbidity, SVI, and the remaining amount of SS in the effluent is shown in Fig. 2.

Fig. 2
figure 2

Effect of coagulation time on COD, turbidity, SVI, and SS. b non-ozonation a ozonation = 15 min. (polymer concentration = 30 gr/dry SL, flocculation time = 10 min and settling time = 30 min)

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When the coagulation time increased, SVI and SS decreased, and turbidity and COD increased significantly (p < 0.05) (Fig. 2a). Moreover, with increasing the coagulation time in the absence of ozonation, COD, turbidity, and SVI increased (Fig. 2b), but in the presence of the ozonation process, COD, SVI, and SS were less compared to the process without ozonation in the effluent (p < 0.023). However, the maximum effect of ozonation during coagulation time variation was related to the turbidity in the effluent, and it decreased from 374 to 350 NTU in the process without ozonation to 160–110 NTU (59%). Thus, ozonation was a significant factor in reducing the turbidity of iron ore effluent. Figure 3 shows the effect of ozonation on COD, turbidity, SVI, and SS indices during flocculation time alterations.

Fig. 3
figure 3

Effect of Flocculation time on COD, turbidity, SVI, and SS a ozonation = 15 min and b non-ozonation. (Polymer concentration = 30 gr/dry SL, coagulation time = 30 s, and settling time = (30) min)

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According to Fig. 3, with increasing flocculation time, COD, turbidity, SVI, and SS decreased in the ozonation and in the process without ozonation (p > 0.05). Thus, increasing the flocculation time can be suitable for effluent treatment, and the optimal amount of which was obtained in 20 min. However, cost estimation studies resulting from this increase in flocculation time are essential for real use.

However, the use of ozonation with the coagulation and flocculation process has been an effective factor in reducing all the studied indicators, which has a very significant reduction in turbidity. The ozonation effect on COD, turbidity, SVI, and SS removal in different settling times is shown in Fig. 4.

Fig. 4
figure 4

Effect of settling time on COD, turbidity, SVI, and SS. a ozonation = 15 min and b non-ozonztion. (Polymer concentration = 30 gr/dry SL, coagulation time = 30 s, flocculation time = 20 min)

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As shown in Fig. 4, with increasing sedimentation time, the studied indices decreased. The optimal sedimentation time was 30 min. It should be noted that the cost-effective of the process is an influential factor in reducing the COD and SS indices which should be considered. However, these differences were more significant at different sedimentation times in the ozonation process, especially turbidity (p < 0.05). Finally, according to the optimal conditions obtained from the above experiments, the effect of ozonation time on COD, turbidity, SVI, and SS is shown in Fig. 5.

Fig. 5
figure 5

COD, turbidity, SVI, and SS at different ozonation times (5, 10 and, 15 min) and comparison with raw wastewater (0 min or non-ozonation)

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In Fig. 5, each studied parameter, including SVI, COD, SS, SVI, and turbidity, was measured ten minutes after each ozonation step. The results showed that with increasing ozonation time, a significant decrease was observed in COD, turbidity, and SVI (p < 0.05), which was COD (5 min: 12%, 10 min: 24%, and 15 min: 34.42%), turbidity (5 min: 22.43%, 10 min: 32.69%, and 15 min: 37.5%), SVI (5 min: 24.96%, 10 min: 27.64%, and 15 min: 44.7%), and SS (5 min: 13.04%, 10 min: 16.14%, and 15 min: 19.25%).

The SS variations were not significant with changes in ozonation time (p < 0.02). So, SS decreased from 160 mg/L in process without ozonation to 140 mg/L (ozonation time = 15 min). Besides, the lime adding effect in the polymerization and ozonation process on the COD, turbidity, SVI, and SS in the effluent is shown in Fig. 6.

Fig. 6
figure 6

COD, turbidity, SVI, and SS in the combined process of ozonation-coagulation and flocculation and coagulation and flocculation in combination with lime

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According to Fig. 6, the amount of COD after lime addition in the coagulation and flocculation process and the combined coagulation and flocculation-ozonation process were 145 mg/L and 105 mg/l, respectively. The addition of lime in the combined coagulation and flocculation-ozonation process at 40 mg/l has been more effective in removing COD in the coagulation and flocculation process. Also, the turbidity after lime addition in the coagulation and flocculation process and the combined process were 230 and 28 NTU, respectively. The lime addition in the combined coagulation and flocculation-ozonation process were more effective than the coagulation and flocculation-ozonation process at 81.82 ml/g. In the case of SS, it was more effective in removing turbidity than the coagulation and flocculation process. The reduction reached 150 ml/l in the coagulation and flocculation process, and it reached 120 ml/l in the hybrid process.

Despite the effects and proper efficiency of ozonation in iron ore effluent treatment and reducing the produced sludge volume, it is necessary to study the characteristics, elemental analysis, and microscopic changes of sludge. The sludge flocs from both coagulation and flocculation and the combined process with ozonation were examined by SEM. Figure 7 shows the SEM of iron ore effluent sludge under optimal conditions of two coagulation and flocculation processes and coagulation and flocculation-ozonation.

Fig. 7
figure 7

Sludge SEM image of both processes in optimal condition, A Coagulation and flocculation process, B Hybrid process

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The sludge structure from the combined process had a smooth and dense surface (Fig. 7B). Besides, Fe2O3 particles with white rod-shaped and cylindrical clusters were observed on the sludge surface (Fig. 7 B-2). According to Fig. 7 (B-1), the deposited particles size on the sludge was less than 1 μm, while the sludge particle size in 7A was less. Table 3 shows the elements and metals concentration in the raw effluent in comparison to obtained effluent from ozonation, polymerization, and simultaneous ozonation and polymerization processes.

Table 3 Concentration of elements and metals in raw effluent in comparison with ozonation, polymerization and simultaneous ozonation and polymerization processes
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The simultaneous use of ozonation and polymerization process was an effective factor in removing elements from the effluent (> 90%). Hence hazardous elements' concentration such as arsenic, silver, cadmium, cobalt, chromium, mercury, manganese, molybdenum, nickel, and lead are below the Iran's standard level. In addition, the concentration of manganese decreased by about 75% during the study process (Table 3) and reached a concentration lower than the standard. In addition, the ozonation process combined with coagulation was able to remove 99.9% of the iron from the iron ore effluent.

Cost-effectiveness

According to the importance of investigating the economic aspects in choosing the application of a method in the industry, estimating the effluent treatment cost from the crusher line by using the current method in Iran's central iron ore (using 30 g polymer/ton of dry SL, an expression of 1.15 g/m3 effluent) was investigated. The results obtained from EQ. 3 for estimating the cost-effectiveness are given in Fig. 8.

Fig. 8
figure 8

Cost-effectiveness of each process

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According to Fig. 8, the highest cost-effectiveness is related to the process P (30gr/dry SL) + O3 (5 min) (83.49) and then the highest cost-effectiveness is related to P (30gr/dry SL) + O3 (10 min) (63.23, (10 min) (23.63), P (30gr/dry SL) + O3 (15 min) (55.4), P (30gr/dry SL) (16.42), and P (10gr/dry SL) (14.99), respectively. The lowest cost-effectiveness rate was related to P (20gr/dry SL) + O3 (15 min), with a cost-effectiveness rate of -65.23. The cost and efficiency of each process are shown in Fig. 9.

Fig. 9
figure 9

Cost and effectiveness of each process

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The highest and lowest cost was related to P (30gr/dry SL) + O3 (15 min) and P (10gr/dry SL) + O3 (5 min) with the cost of 38 × 10–4 and 12 × 10–4 Dollar/m3 effluent, respectively. In contrast, the highest and lowest efficiencies were related to P (30gr/dry SL) + O3 (15 min) and P (10gr/dry SL) + O3 (5 min) with 63.8% and 30.5% efficiency, respectively.

Discussion

In this study, the effectiveness of the ozonation process on the current treatment of iron ore mine effluent (coagulation and flocculation by polymerization) in Iran central iron ore with a focus on SVI, COD, SS, and turbidity indices was investigated. To determine the optimal conditions, the effect of changes in design and operation variables including coagulation, flocculation, sedimentation time, polymer concentration, and ozonation time, at a constant speed on the process performance was determined. At first, the treated effluent with the current used process in the mine was examined. It was found that all parameters except SVI in the prototype were higher than the standards, while it has not had a significant effect on other indicators elimination. Thus, the ozonation process efficiency in comparison with the current polymerization was evaluated during the change of effective parameters. In general, all indicators during the combined process with ozonation were less than the polymerization process (p < 0.05). Further, during the ozonation process (Fig. 5), with increasing ozonation time, the number of studied indicators significantly decreased (p < 0.05).

In the study of (Jin et al. 2019), the ozonation-coagulation hybrid process has been effective in improving the purification process. Because with increasing ozonation time, the concentration of available ozone to produce hydroxyl and superoxide radicals and oxidation processes increase. Hence, ozonation changes particle charge, improves hydration, and increases the surface activity of coagulants and coagulants aid. In addition, metal coagulants such as aluminum and iron in the presence of ozone act as a catalyst that produces higher levels of hydroxyl radicals compared to the absence of coagulants (Fe-HOC) and modified precipitation process (Jin et al. 2019; López-Vinent et al. 2021). Although less attention has been paid to ozone use in improving the iron ore effluent treatment, but similar studies have shown a significant reduction in the sludge volume of other industrial wastewaters using combined ozonation processes (Solís et al. 2021; Hashimoto et al. 2021; Yang et al. 2021; Wu et al. 2020).

According to the results, with increasing the polymer concentration and settling time and coagulation time decreasing, the level of all four indicators decreased (Fig. 1). While such a trend is not observed for the current non-integration process. As the polymer concentration increases, the turbidity and COD increase, which in addition to the inorganic nature of the carbon content, it can be due to the re-suspension of flocs at high polymer concentrations. In contrast, in the hybrid process, the additional flocs become unstable by ozonation, and the settling capacity was increased.

In the study by (Setareh et al. 2020), the hybrid ozonation-ultrasonic process removed 33—50% of the turbidity. In other study, in 60 min, the COD and turbidity removal rate was 59% and 76%, respectively (Ashraf et al. 2016). Although no results have been reported on the effect of ozonation on mineral effluents, but with increasing flocculation time, the studied indices have decreased. However, the variation trend in the hybrid process has been proportional to the increase in time (R = 0.63). The SVI index did not change much. However, it was within the recommended standard range.

In a study by (Zhang et al. 2018), the ozonation with the micro coagulation and precipitation process was an effective factor in improving the treatment process due to organic pollutants removal. In the study of (Kato et al. 2018), the virus removal efficiency increase in the combined process of ozonation and coagulation-settling. Because during the increase of flocculation time, sufficient time was provided for large and sedimentable flocs formation, which increased the sedimentation time in the hybrid process, its effects were intensified (Fig. 4).

Additionally, the radicals from the ozonation process can neutralize the stable particles that precipitate the colloids (Canada 2019, 2021). However, with the increasing coagulation time, the indicators amount has increased (Fig. 2), which creates unfavorable conditions for the instability of colloids. Thus, reducing the coagulation time in this process is recommended.

In the study of (Forsido et al. 2020), the use of lime increases the removal rates of Al (98%), Ba (95.8%), and Mg (99.7%). Moreover, elements and metals concentration, turbidity, and SS decreases significantly (Sun et al. 2020; Salmani et al. 2021; Salehi et al. 2020). Because in the coagulation-flocculation process, the amount of acidity increased, so lime can provide alkalinity as a simple, cheap, available, and effective method (pH > 9.5) and is effective in removing metal oxides. For example, the study by (Zheng et al. 2020) showed that the addition of lime increases the turbidity removal rate by 99.99% and SS by 99.84%.

Based on ICP-OES analysis results in raw effluent, the combined ozonation-polymerization process was an important factor in removing elements from the effluent. The concentration of hazardous elements such as arsenic, silver, cadmium, cobalt, chromium, mercury, manganese, molybdenum, nickel, and lead was less than the standard (p < 0.001). The results of other study in 2020 also showed that the combination of ozonation and coagulation process results in Cu removal (99.7%) (Salmani et al. 2021; Nguyen et al. 2021; Abbasia et al. 2020).

Manganese is an insoluble compound of Mn2O3 in the face of ozone-producing radicals (Ryu et al. 2019). The combined ozonation process with coagulation can remove 99.9% of iron from iron ore effluent, which is less efficient for the polymer at a concentration of 30 mg/L.

In the SEM image of the sludge under optimal conditions, spherical particles due to the presence of aluminum compounds and nanometer particles of iron oxide on the surface of the it were observed. The structure of the sludge layers from the coagulation and flocculation-ozonation process is discernible. The presence of white clusters of rods and cylinders cavities with micro and nano-size in the precipitated sludge has also been confirmed, which may be due to the presence of calcium oxide or other precipitated compounds (Seifan et al. 2020; Sibiya 2020; Smoczynski et al. 2019; Smoczyński et al. 2014; Lange 1994). However, the cavities dimensions in the coagulation and flocculation process were bigger than in hybrid process. In the study of iron oxide compounds produced during the oxidation process, their size was less than 100 μm (Mari et al. 2020). Thus, in the current process, only iron particles with larger sizes have been removed. While in the hybrid process, fine iron particles, which are usually in the form of colloids, were also removed.

Based on previous studies, the use of ozonation in combination with other processes, including Fenton, accounts for about 85% of the total operating cost (Wu et al. 2020), and the costs of sludge management were reduced (Fig. 9). It requires further studies in the target industries. Besides, the modification of the ozonation process, such as micro-sized bubbles for volume reduction or photocatalytic effect on sludge volume reduction, is recommended.

Conclusion

The combined ozonation-coagulation and flocculation process was effective in improving the quality of central iron ore crusher line effluent. Adding lime reduces SS, SVI, and turbidity. By using the ozonation process, the elements in the effluent, such as iron, aluminum, and others, were decreased more than the use of coagulant alone, which was statistically significant (p < 0.005). Also, the lime by increasing the effluent alkalinity reduced toxic elements and elements in the effluent. Other parameters such as final sludge volume and turbidity have also improved after the lime addition. However, lime is a cheaper and more accessible material than polymers used in the Bafgh iron ore refinery. Finally, the simultaneous use of the ozonation/calcination process with coagulation and flocculation was effective than coagulation and flocculation alone for effluent treatment.