Introduction

One of the important challenges for water treatment technologies is effective elimination of organic contaminants present in water in colloidal or diffuse form. Particular attention is paid to the removal of the fraction of biodegradable organic matter that is ubiquitous in aquatic ecosystems. This fraction includes a heterogeneous mixture of organic compounds with different physical and chemical properties, including humic and fulvic substances, proteins, amino acids, lipids, polysaccharides and biopolymers (Huber et al. 2011; Gilbert et al. 2013; Pruss 2015; Pruss and Pruss 2016a,b). The presence of the biodegradable fraction of organic matter in water may cause secondary development of microorganisms in the water supply network and thus deterioration of organoleptic properties of water directed to the consumer (Szuster-Janiaczyk 2016; Szuster-Janiaczyk and Bylka 2019). Biodegradable organic carbon is also a precursor of harmful by-products of the disinfection process (Włodyka-Bergier and Bergier 2011; Rosińska and Rakocz 2013; Wolska 2014; Hrudeys and Fawell 2015; Włodyka-Bergier et al. 2016; Liu et al. 2017; Domoń et al. 2018; Zimoch and Bartkiewicz 2018, 2019; Wolska et al. 2019).

Frequently, low pH value and high content of organic compounds contribute to high concentrations of iron in groundwater (Maziarka and Krogulska 2018). Organic substances present in water are classified into those of natural and anthropogenic origin. Natural organic substances include humic acids, fulvic acids, humines, products of microbial metabolism and compounds from the decomposition of dead animals and plants (Krupińska 2016a,b). Substances of anthropogenic origin include phenols, PAHs, surfactants, chlorinated organic compounds, oil derivatives and pesticides which are found in the leachate from landfills, fertilizers, sewage and plant protection products (Visco et al. 2005).

In groundwater treatment plants which rely on a typical, non-reagent technology, iron removal consists in oxidising dissolved iron (II) to a water-insoluble iron (III) by aeration. Iron (III) hydroxide is finally removed by sedimentation and filtration. That was the case in the treatment of water from well no. 2 (Fig. 6) during pilot studies described in this publication. Many WTPs are supplied with groundwater whose impurities prevent oxidation of iron with oxygen. Iron removal from groundwater is limited by organic substances as they form stable complexes with this element, both in bivalent and trivalent form (Krupińska 2017a,b). In this case, the use of aeration to oxidise iron (II) will not bring the expected results, because of the formation of colloidal and coloured ferro-organic compounds dissolved in water, which will increase the colour and turbidity of the treated water, and the stability of such compounds will increase with the rising concentration of organic ligands (Krupińska 2017a,b). Groundwater may be contaminated with humic compounds, which occur in dissolved, insoluble or colloidal form. In combination with iron, these substances form permanent complexes of different solubility and colloids. The stability of humic substances increases with the growing pH value. This causes an increase in the degree of dissociation of functional groups. A reverse situation occurs when the water reaction decreases. Lower pH contributes to decreasing the degree of dissociation of humic compounds and causes particle aggregation. The resulting colour of humic substances results from changes in the concentration of H+ ions, which are the cause of changes in the structure of chromophore groups. According to many studies, it is probable that with the decrease in hydrogen ion concentration and an increase in the colour of groundwater, the content of humic acids is observed. Such a situation most likely occurred during the studies described in this article in the case of water taken from well no. 1 (Fig. 7). The consumption of water with basic humic compounds is not harmful to human health. However, it should be noted that these substances have the ability to adsorb other contaminants, often toxic, which are dangerous and unacceptable in water intended for human consumption and should therefore be removed. Treatment of water containing humic compounds requires the use of advanced technological systems. Organic substances should be removed before the disinfection process, as they are believed to contribute to the formation of by-products of this process (Kłosok-Bazan 2013; Szuster-Janiaczyk 2016; Szuster-Janiaczyk and Bylka 2019; Nhamo et al. 2020). The water quality parameters which indicate the presence of humic compounds in groundwater are colour, total organic carbon, oxidation and UV absorbance at 254 nm wavelength (Kaleta and Elektorowicz 2009).

In many studies described in the literature, methods of iron removal in combination with organic compounds are presented. These compounds cause extension of the oxidation time of Fe (II) to Fe (III), decrease its effectiveness and the products formed in this process are colloidal (Albrektiene et al. 2011). The recommended method of removal is to use strong oxidants such as chlorine, potassium manganate (VII), ozone and hydrogen peroxide. The safety of the process should be taken into account so that no inorganic and organic by-products, which are harmful to human health, are produced during oxidation (Krupińska 2017a,b). Other processes that are used for the removal of humic compounds are: coagulation, filtration, sorption on active carbon together with biodegradation on biological active carbon filters, ion exchange and membrane processes. It has been proved that the most effective method of removing humic compounds is the coagulation process combined with filtration on active carbon.

According to Knocke et al. (1991), free chlorine, ozone and hydrogen peroxide are not completely effective in iron (II) oxidation when this element is combined with certain humic and fulvic acids. The author has proved that organic compounds with a higher molecular weight are more effective in protecting iron against oxidants. Moreover, the use of chlorine may lead to the formation of iron compounds in a colloidal form, which is not retained on filters. The use of chlorine compounds is also not recommended due to the danger of formation of chlorine organic compounds, including trihalomethanes. However, chemical oxidation with ozone or hydrogen peroxide may cause the fractionation of large organic particles into smaller ones (Krupińska 2017a,b). Indirect organic oxidation products of organic compounds that remain in water can stabilise iron. Sedimentation and filtration processes will not be sufficient to remove the created ferro-organic bonds (Krupińska et al. 2013).

Chemical oxidation of iron with potassium manganese (VII) is recommended when there are also manganese (II) compounds in groundwater. This process improves the adsorption and catalytic properties of precipitated manganese (IV) oxide. The oxidation reaction produces iron (III) hydroxide and manganese (IV) oxide, which acts as a catalyst for the oxidation of iron (II) and manganese (II). Catalytic oxidation of these ions allows for the use of smaller doses of potassium manganate (VII) (Krupińska 2017a,b).

The coagulation process is considered necessary to remove colloidal connections between iron and organic compounds. The efficiency of the process depends on the type and dose of coagulant and the co-occurrence factor of organic substances to total iron in untreated water (Krupińska 2017a,b). In the case of treatment of groundwater containing iron in combination with organic compounds, the oxidation of iron (II) ions is often required before the coagulation process. Using potassium (VII) manganese as an oxidant will most effectively reduce the colour, turbidity, concentration of manganese and organic compounds (Krupińska 2016a,b). Commonly used coagulants are iron and aluminium salts. In a study by Krupińska (2017a,b), popular coagulants were compared. The best results were obtained with polyglycol chloride, which removed iron compounds together with organic impurities causing too high colour and turbidity values of the tested water. The study was carried out on groundwater with high concentration of total iron and high content of organic substances. The analysed water was subjected to the coagulation process together with aeration. Thanks to such technological processes, the colour, turbidity and concentration of iron compounds were reduced. According to many researchers, iron coagulants are more effective in removing manganese and aluminium reagents in reducing the content of organic iron complexes. This is due to the fact that iron (III) ions or their hydrolysis products interact more strongly with organic compounds and form colourful complexes with them. According to Krupińska (2015), aluminium coagulants increase their effectiveness in removing organic and inorganic substances from water with an increase in the dose of reagents and temperature and a concurrent decrease in the value of organic substances and total iron. The coagulation process removes colloidal organo-iron compounds but does not affect the concentration of dissolved organo-iron compounds (Krupińska 2017a,b).

The effectiveness of coagulation combined with filtration was confirmed in the study carried out by Kłosok-Bazan (2013). Aeration, coagulation in the clarifier and filtration were applied. Hydrolysed aluminium polychlorosulphate was used as a coagulant. The water was characterized by high concentration of iron and the presence of organic compounds. In the experiment, a high effect of iron removal (75–90%) and organic compounds (42–60%) was obtained. Krupińska (2016a,b) also concluded in her paper that the most effective method of removing humic substances from water was the coagulation process combined with filtration on active carbon which allows to remove up to 80% of humic substances.

The sorption process used to remove humic substances from water is not perfect. When adsorbing large particles, there is a risk of blocking the adsorbent micropores. In order to increase the efficiency of the process, a chemical oxidation process should first be used to fractionate large organic compounds. The resulting compounds take the form of adsorption and biodegradation-prone compounds. The efficiency of the adsorption process depends on the type of adsorbent and pH. Adsorption of humic compounds on active carbon is most effective at pH 5–7. An increase in pH above 8 resulted in deterioration of the process efficiency (Kaleta et al. 2017). The study carried out by a research team from Poznań (Holc et al. 2019) showed that the use of biologically active filters in which sorption occurred was a very effective method of removing organic compounds from water. Tap water and water modified with humic compounds were tested. Filters with active carbon deposit allowed to achieve over 91% efficiency of organic compounds concentration reduction. On the other hand, the research conducted by Krupińska (2015) showed that microbiological transformations played an important role in the treatment of groundwater containing iron with humic compounds. The transformations take place in filtration sludge, in which microorganisms are present. The activated granular carbon used as a filter material acts as an adsorbent of organic substances and a growth medium for organisms which participate in the oxidation of iron, manganese and organic substances. As a result of iron (II) oxidation, insoluble oxides and hydroxides are formed, which are retained on cellular organelles of microorganisms and activated carbon (Krupinska 2015).

The study conducted by Pietrzyk and Papciak (2018) assessed the effectiveness of organic compounds removal in the technological system consisting of aeration, coagulation, filtration on anthracite-sand deposits and biofiltration on activated granular carbon. Groundwater rich in organic compounds was purified in the range of 49–100% depending on the parameter. The following parameters were determined: dissolved organic carbon, particulate organic carbon and total organic carbon content. The process of coagulation resulted in a decrease in the content of organic compounds, which are responsible for the colour of water and the content of organic carbon in the form of particles. Elimination of organic substances which determine the UV absorbance value was guaranteed by filtration on sand and anthracite deposits. The process of biofiltration resulted in a reduction of all parameters indicating the presence of organic matter, i.e. colour, UV absorbance, total organic carbon content and water COD KMnO4.

A pilot water treatment plant was installed in the city of Nida, Lithuania and used for tests which lasted 8 months. The groundwater was characterized by a high content of organic matter, iron, manganese and ammonium ions. The authors (Albrektiene et al. 2017) applied the following processes: open aeration, coagulation, a first stage filtration, closed aeration, second stage filtration and third stage filtration. The water flowed through the weirs in order to saturate it with oxygen and remove hydrogen sulphide. Then, polyglycol chloride was dosed into the water that was pumped to the first filtration stage. The reagent, together with the water, flowed through the reaction chamber where sludge was formed. The treatment water flowed to a pressure filter filled with quartz sand which was to reduce the concentration of iron and organic compounds. Then, the water flowed to a closed aerator, which enriched it with oxygen necessary for oxidation of manganese compounds and ammonium ions. The subsequent filters were filled with natural zeolite and quartz sand containing ammonium nitrogen oxidizing bacteria, respectively. The applied technology allowed for minimum coagulant consumption with high water treatment efficiency. The concentration of iron decreased by 98%, of manganese by 87% and of ammonium nitrogen by 99%. An 80% reduction in the concentration of organic compounds and water colour was achieved.

To sum up, in order to remove from groundwater iron which occurs in combination with organic compounds, it is necessary to apply preliminary oxidation and a coagulation process. Unfortunately, in many small water treatment plants, such processes are not viable; therefore, when there are several water intakes providing water of good quality, the aim is to eliminate the intakes with heavily polluted water or to determine the possible rate of mixing such water safely for a typical non-reagent technology. Such a solution is presented in this publication.

In the face of changing legal regulations, growing consumer demands and high costs of water production, water supply companies intending to build or modernize water treatment plants need effective support to safely determine the directions of project and investment activities. The overriding goal is to achieve the most advantageous water treatment technology in technological and economic terms. In the case of existing plants, pilot technology tests offer an economical method of testing alternative and often innovative technologies without affecting the existing water treatment process. They are useful in developing changes in the existing water treatment process in order to improve water quality and/or reduce water production costs. The possibility to test alternative processes independently of those implemented on a technical scale is particularly valuable. The right approach to the topic is to perform pre-design technological research to determine the water treatment technology, parameters of individual processes and the necessary scope of investment. The result of technological research is the knowledge of the proper technological system, approximate investment and operating costs of the investment. Designers are provided with guidelines which enable the proper execution of technical documentation. A well-thought-out construction and execution project allows for proper implementation of the investment, which will be completed by launching and receiving the investment and achieving the intended technological effect (Pruss and Pruss 2010, 2016a,b; Pruss 2015).

Existing plant works with processes and equipment as follows: groundwater from wells is pumped to buffer tank with chemical oxidation by potassium permanganate before. Next step is filtration in 6 continuous sand filters. After filtration, water is disinfected by UV ray and sodium hypochlorite. In this plant, removal of manganese is insufficient and unstable. Other problem are organic compounds, not removed in process, which causes high disinfectant demand and impossibility to use one of existing well. Water from this protective well has to be wasted because of high concentration of organic compounds.

The aim of the research presented in this article was to select an economic and environmentally friendly non-reagent technology of groundwater treatment other than the one used so far on WTP with particular emphasis on the effectiveness of organic matter removal. An attempt was also made to treat water from a protective well which had not previously been used for water production. In addition, safe mixing ratios of water from the protection well with water from other wells were established for the proposed non-reagent groundwater treatment technology. The results were used to prepare the concept of a new groundwater treatment plant.

Methods and materials

Pilot water treatment plant (WTP)

The pilot WTP was operated at the capacity of 2800—3000 L/h. The test stand consisted of an aerator for water aeration, two contact tanks, a multi-stream settling tank and three filter columns working in parallel. The flow rate of water flowing to the aerator, the settling tank and filtration columns, depending on the needs, was regulated by using rotameters installed before each of the abovementioned devices (Fig. 1).

Fig. 1
figure 1

The diagram of the pilot station technology

Full size image

The water taken directly from the well was fed to the research installation and directed to the first device of the process line which was the aerator. Due to the characteristics of raw water, in particular the occurrence of the alkaline aspiration compounds in the intake water, the use of open aeration was proposed (water pumped into air) with a contact chamber. The aerator was a high-socket column of about 2.5 m made of acid-resistant steel consisting of five segments in which the water grids were placed. Raw water flowed from the top into the inlet chamber of the aerator and then flowed successively through five segments of the device (Fig. 2). In the lowest segment, through openings placed in the wall of the aerator segment, the water flowed out to a tray where it was aerated and degassed and then flowed down by gravity into the reaction chambers (Fig. 3). Due to quite high concentrations of iron in the groundwater, the use of a contact chamber past the water aeration process was proposed, optionally with a multi-stream settling tank (Fig. 4). In order to ensure effective de-ironing across the whole thickness of the bed, the time of water contact between the water and the air was experimentally determined so that at the moment of reaching the filtration bed, the Fe(III) content in water was 30—50% of the total Fe content. The optimal contact time between aerated water and dissolved oxygen was determined at the beginning of the pilot studies using aerated water sampled directly after aeration.

Fig. 2
figure 2

Aerator for water aeration

Full size image
Fig. 3
figure 3

Last segment of the aerator with aerated water outflow

Full size image
Fig. 4
figure 4

Pilot station—two reaction chambers (chamber no. 1 filled with water) and a multi-stream settling tank

Full size image

Typical 1000 L and 600 L tanks were used as reaction chambers. The testing installation allowed to operate both tanks simultaneously or each of them separately. Such a configuration of the reaction chambers enabled the entire station to operate at different contact times. In the installation, it was also possible to omit the reaction chambers and pump the aerated water directly to the settling tank or to the filters. The results of the tests presented in this article concern the operation of the pilot WTP with the use of the reaction chambers and the multi-stream settling tank. The water retention time in the reaction chambers was 10 min for water from well no. 1 and about 18 min for water from well no. 2 and the mixtures of the two waters.

Past the reaction chambers water flowed into the settling tank. A multi-stream settling tank was used in the research. During the tests, the flow rate of water directed to the settling tank was 150 L/h. The water from the outlet chamber of the settling tank was directed to rapid filters, while the sludge was directed to a sludge hopper.

The pilot station had three filter columns. The filtration rate was 5 m/h. At the beginning, two filtration columns made of polymethyl methacrylate pipes with a diameter of 0.094 m and a height of 3.0 m were operated. In both filtration columns, the bed height was 1.5 m. In the first filtration column, a 120 cm filter bed of quartz sand (0.71—1.25 mm; WR < 1.5) and 30 cm filter bed of anthracite (1.4—2.5 mm; WR < 1.5) were used. The second column was filled with 30 cm of G-1 catalytic mass layer (1.0–3.0 mm) and 120 cm of quartz sand filter bed (0.71—1.25 mm; WR < 1.5). The third filtration column was 0.2 m in diameter and 4.0 m high. It was filled with a 1.55 m high filter bed consisting of the following layers 15 cm gravel support layer, 30 cm G-1 catalytic mass layer (1.0–3.0 mm), 60 cm filter bed of quartz sand (0.71—1.25 mm; WR < 1.5), 20 cm of quartz sand filtration bed (0.1—1.25 mm; WR < 1.5) and 30 cm of anthracite filter bed (1.4—2.5 mm; WR < 1.5).

The signal to backwash the filters was a pressure loss of 200 cm or a bed breakage (presence of Fe in the outlet). The filter bed was backwashed with air and water at an intensity ensuring 30% expansion.

Water samples analysis

Water for analyses was taken past each device installed in the pilot WTP. The sampling points are marked on Fig. 1. The studies were carried out for four types of groundwater: water from well no. 1, water from well no. 2 and a mixture of the two waters containing 27% and 18% of water from well no. 1. The average quality of water entering the pilot WTP is shown in Table 1. Well no. 1 is a protective well and its water is not currently treated, but due to hydrogeological recommendations in order to properly operate the remaining wells, water must be taken from it.

Table 1 The average groundwater quality
Full size table

The regular analytical tests (every 24 h) included: temperature, pH, alkalinity, turbidity, colour, smell, dissolved oxygen, redox potential, total and bivalent iron, manganese, COD KMnO4 and periodically TOC. All analyses were performed in accordance with the Standard Methods. Detailed information on the steps to be taken to select the appropriate configuration of the pilot groundwater treatment plant and the benefits of carrying out the pilot studies are described in the publication (Pruss et al. 2018).

Results and discussion

Figures 5, 6, 7 and 8 show changes in COD KMnO4, total iron, iron II and pH of water from well no. 1, no. 2 and the mixtures of the two waters in different proportions during treatment in the technological system of the pilot WTP.

Fig. 5
figure 5

Changes in the COD KMnO4, TOC, iron and pH of water from well no. 1 during its treatment in technological processes of the pilot WTP

Full size image
Fig. 6
figure 6

Changes in the COD KMnO4, TOC, iron and pH of water from well no. 2 during its treatment in technological processes of the pilot WTP

Full size image
Fig. 7
figure 7

Changes in the COD KMnO4, TOC, iron and pH of mixed water from both wells with 27% of water from well no. 1 during its treatment in technological processes of the pilot WTP

Full size image
Fig. 8
figure 8

Changes in the COD KMnO4, TOC, iron and pH of mixed water from both wells with a 27% share of water from well no. 1 during its treatment in technological processes of the pilot WTP

Full size image

The water taken from well no. 1 was characterized by a high organic matter content, i.e. COD KMnO4 of 14.77 mg O2/L on average and TOC at 6.9 mg C/L. The pH of raw water was at the level of 7.1. In the treatment process based on classical non-reagent technology of groundwater treatment, the aim was to reduce the concentration of organic substances present in the water as a result of co-precipitation with Fe III. However, observing the results of the studies (Fig. 5), it can be seen that lowering the concentration of organic matter was very difficult. This was probably due to the co-occurrence of humic compounds and iron in water. The water from well no. 1 was characterized by an intensive brown colour, which would confirm the assumptions. The water past filter no. 1 had an average COD KMnO4 of about 10.53 mg O2/L, while the water past filter no. 2 had an average COD KMnO4 of 9.82 mg O2/L with the simultaneous substitution of iron II. The results of the analysis of total iron and iron II confirm that about 30% of iron II present in the raw water was not oxidized. Therefore, the proposed treatment technology can certainly be considered to have failed for the water from well no. 1 which is difficult to treat. Humic substances include humic acids, hymatomelanic acids and fulvic acids. They cause strong colouring of water. The colour ranges from brown to black. Their presence does not directly affect human health, however, as they are precursors of disinfection by-products and thanks to complexing of heavy metals and adsorption of toxic organic substances, their removal is necessary during the production of water intended for human consumption. The presence of organic compounds in connection with iron in groundwater can make its treatment much more difficult. This is due to the fact that iron in humic compounds is more difficult to oxidise than Fe(OH)2 because the organic substance has to be melted first and only then can Fe(II) be oxidised to Fe(III) (Kłosok-Bazan 2013; Krupinska 2015, 2016a,2017a; b, b).

Raw water from well no. 2 compared to well no. 1 had a much lower organic content, i.e. COD KMnO4 was 3.9 mg O2/L on average, while the TOC was 4.2 mg C/L and the content of iron was similar. The pH of raw water was at the level of 7.1. Based on the test results (Fig. 6), a decrease in organic matter concentration can be observed. The water past filter no. 2 had a COD KMnO4 of 3.3 mg O2/L on average, while the water past filter no. 3 had a COD KMnO4 of 2.88 mg O2/L. The TOC on the outlet of filter 2 was 3.6 mg C/L and on the outlet of filter 3 approximately 3.3 mg C/L. It should be noted that the concentration of total iron on the outlet of filter no. 2 was 0.09 mg Fe/L and of filter no. 3 was 0.08 mg Fe/L, which confirmed that the iron present in water from well no. 2 was not combined with organic compounds.

The analysis of changes in COD KMnO4, TOC and iron in the mixed water from both wells with a 27% share of water from well no. 1 shows a significant decrease in the achieved results of water treatment in the proposed process line (Fig. 7). Only in the last stage of the water treatment process, i.e. filtration through filter bed 3, the observed concentrations of organic substances were in accordance with the guidelines specified in the Regulation of the Polish Minister of Health of 2017, i.e. the average COD KMnO4 value of the treated water was 4.52 mg O2/L and TOC was 3.95 mg C/L. The average concentration of total iron in the water past filter no. 3 was 0.97 mg Fe/L, of which the concentration of Fe(II) was 0.23 mg Fe/L.

The increase in COD KMnO4 of the water in the process line past the reaction chambers, as shown in Fig. 8, was most probably related to the leaching of sludge from the reaction chambers. The average COD KMnO4 of the water mixture flowing into the pilot station was 5.2 mg O2/L with an average reaction rate of 7.14. The efficiency of organic matter concentration reduction during the whole process was only 7% for TOC and 12% for COD KMnO4. Iron was reduced on average by 72%. In the treated water, the average TOC value was 4.0 mg C/L, COD KMnO4 was 4.6 mg O2/L, the concentration of total iron was 0.7 mg Fe/L and the concentration of Fe(II) was 0.3 mg Fe/L. The results indicated the possibility of achieving iron concentration values consistent with the Regulation of the Polish Minister of Health by increasing the filtration efficiency. The desired iron removal efficiency was obtained by adding a 20 cm layer of quartz sand with less granulation than previously applied (0.63 to 1.0 mm granulation) to filter 3. In the last filtration cycle carried out after sealing the bed of filter 3, iron concentrations below 0.2 mg Fe/L were obtained in the filter.

In the analyzed technological line of the pilot water treatment plant, the manganese content was lowered in the filtration process. It should be emphasized that on the rapid filters, satisfactory manganese removal effects were obtained for each of the tested water. The tests showed that in filters with a catalytic layer (filter no. 2 and 3), manganese was removed to values close to 0.0 mgMn/L.

In the case of both analysed water mixtures, the effect of lowering the concentration of organic compounds present in water to values consistent with the guidelines given in the Regulation of the Polish Minister of Health of 2017 was achieved. Iron concentration in mixed waters from both wells was significantly reduced as a result of the applied technological processes and it was only by sealing the filter no. 3 that the iron concentration compliant with the requirements for water for human consumption could be obtained. It should be emphasized that in order to achieve the targeted effect, water from well no. 2 should be treated with a small addition of water from well no. 1, not exceeding 20%.

Conclusions

Technological research carried out on a pilot scale is the best way to select appropriate water treatment technology. The testing installation met all the necessary criteria of hydraulic and technological similarity to the installation on the technical scale which is the subject of the future project. This guarantees identical quality of treated water both on a pilot and technical scale.

The research has shown that water from well no. 2 and a mixture of waters from well no. 2 and well no. containing maximum 20% of water from well no. 1 can be effectively treated with the use of the technology based on natural aeration and rapid filtration processes. Such a technology will ensure the achievement of drinking water quality parameters consistent with the guidelines specified in the Regulation of the Polish Minister of Health.

Pilot studies have shown that more advanced technological systems are needed to treat water from well no. 1, which is characterized by high content of organic substances (most probably humic compounds).