WWTP E ﬄ uent Quality Improvement for Agricultural Reuse Using an Autonomous Prototype

: Wastewater reuse presents a promising way to mitigate the risk to global water resources and achieve sustainability in water, especially in agricultural areas in the southeast of Spain, such as the Murcia region. However, the risks related to the presence of contaminants of emerging concern (CECs) or pathogenic microorganisms in wastewater treatment plant (WWTP) e ﬄ uent suggest the need to implement e ﬀ ective and relatively low-cost tertiary treatments. With this aim, a self-sustainable pilot prototype based on three combined modules (disc-ﬁltration, granular activated carbon (GAC) bed adsorption and UV disinfection) assisted by solar panels was installed as an alternative tertiary treatment in a conventional WWTP in the Murcia region. The obtained results clearly conﬁrmed the e ﬃ ciency of the proposed prototype for CECs removal, and showed optimal results at a workﬂow of 500 L / h. In all cases, high removal e ﬃ ciency was obtained for the di ﬀ erent indicator microorganisms described in the recently published Regulation (EU) 2020 / 741 ( E. coli , F-speciﬁc coliphages, somatic coliphages, total coliphages, and Clostridium perfringens ). The protection of the activated carbon by disc-ﬁlters and the energy autonomy and self-operation of the prototype resulted in an e ﬃ cient and economically viable methodology for its implementation in both conventional WWTPs and in isolated areas attached to crops. TC-TOC-TN analyzer. Ions were measured by ion chromatography using a Metrohm chromatograph (Metrohm, Switzerland). Samples for DOC, TN, spectrometry and chromatography methods were previously ﬁltered using 45 µ m ﬁlters.


Introduction
Nowadays, the use of reclaimed water is seen as an excellent approach to deal with water scarcity. Indeed, water reuse is an important feature of water policies in most countries around the world, for example, it is included in WHO guidelines [1], and it is seen as a fundamental aspect of the concept of a circular economy [2]. In the European Union, one billion cubic meters of urban wastewater are reused annually (approximately 2.4% of treated effluents). However, this value is expected to increase by up to six times due to the development of numerous initiatives regarding water reuse for irrigation, industrial uses or aquifer recharge [3]. This practice not only promotes the efficient use of water, but also leads to prosperity from an environmental, human and economic point of view, and promotes management strategies for the safe discharge of wastewater into the environment and protection of surface and groundwater [4]. Possible reuse applications include agricultural or Recent studies have focused on several treatment processes applied for the removal of CECs such as advanced biological processes (membrane bioreactors and bio-electrochemical systems) [25,26], and advanced oxidation processes (AOPs) [27,28]. The main limitations of these types of technologies are their high operating costs, specific infrastructures and high energy consumption. Other alternatives such as activated carbon adsorption and ozonation are considered as economically feasible options that can be coupled to WWPTs [29], however, the use of ozone may be associated with the generation of by-products, which can be hazardous to health if the water is used for agricultural purposes.
In this context, the adsorption of CECs by granular activated carbon (GAC) is a promising technology due to its removal efficiency at relatively low cost [30]. In general, and due to its properties (such as its high porosity, high surface area and high degree of surface interactions), activated carbon has a high adsorption capacity for a wide spectrum of CECs [31,32]. In addition, this process has the advantage of not generating secondary by-products [32,33]. Although the effectiveness of adsorption processes in CECs removal is well-known, the introduction of tertiary treatments in conventional WWTPs for the purpose of safe water for agricultural reuse is poorly implemented. This is mainly due to a lack of knowledge about adsorption mechanisms, the great diversity of CECs present in wastewater, the large amount of wastewater interference, and lack of knowledge about the design of systems capable of removing CECs that guarantee the production of CEC-free effluent at relatively low costs.
The aim of this work was the integration of a self-sustainable pilot plant prototype in a conventional WWTP for the purpose of safe agricultural reuse. The design focused on the removal of CECs and microbiological risks by using a combined Filtration-GAC-UV system, in line with current and future legislation. The use of water from a real WWTP together with data on the efficiency and associated economic costs will give us a practical view of the implementation of such systems.

Wastewater Samples
The water source used in the experiments for this study was a WWTP located in the Murcia region (Spain), (latitude 37 • 47 48" N, longitude 0 • 57 36" W). This plant receives domestic and industrial effluent from three municipalities (Roldán, Lo Ferro and Balsicas) and has a maximum treatment capacity of 2,007,500 m 3 /year of wastewater.
This WWTP consists of a secondary treatment based on active sludge with extended aeration and secondary sedimentation. It also uses a tertiary treatment based on coagulation-flocculation, rapid sand filter and disinfection using ultraviolet (UV) radiation. Treated wastewater is commonly used for agricultural irrigation in the Campo de Cartagena area.

Compound Structure Mw (g/mol) Water Solubility (mg/L) Log Kow pKa
Acetaminophen (ACT) NSAIDs 1 Water 2020, 12, x 4 of 19 Table 1. Physico-chemical properties and chemical structure of selected contaminants of emerging concern (CECs). Water 2020, 12, x 4 of 19 Table 1. Physico-chemical properties and chemical structure of selected contaminants of emerging concern (CECs). Water 2020, 12, x Table 1. Physico-chemical properties and chemical structure of selected contaminants of emerging concern (CECs). A commercial coconut shell-based GAC with high density value (520 ± 30 kg/m 3 ) was used as adsorbent in accordance with Benstoem et al. [34]. In that paper, the authors described a high correlation between the high density of GAC sorbents and their capacity to adsorb CECs.

Compound
The selected GAC was activated thermally with steam and supplied by Chiemivall (Castellbisbal, Barcelona, Spain), . The main properties are described in Table S1, Supplementary Materials. A commercial coconut shell-based GAC with high density value (520 ± 30 kg/m 3 ) was used as adsorbent in accordance with Benstoem et al. [34]. In that paper, the authors described a high correlation between the high density of GAC sorbents and their capacity to adsorb CECs.

Analytical Determinations
The selected GAC was activated thermally with steam and supplied by Chiemivall (Castellbisbal, Barcelona, Spain). The main properties are described in Table S1, Supplementary Materials.

Analytical Determinations
Wastewater samples were characterized in terms of pH, turbidity, electrical conductivity (EC), dissolved organic carbon (DOC), total suspended solids (TSS), five-day biochemical oxygen demand (BOD5), and some ions (for conditions, see Appendix A).

Preliminary Lab-Scale Experiments
The adsorption capacity of the selected GAC was studied at lab scale using a methacrylate column of 550 mm length and 19 mm internal diameter containing 21.5 g of GAC. The experiments were carried out using secondary WWTP effluents fortified with 200 µg/L of each CEC. The mixture was added to a plastic tank and pumped into the column by a peristaltic pump (P-Selecta, Percom-I model, (J.P. Selecta, Abrera, Barcelona, Spain) Operational parameters ( Table 2) were selected according to previous results described in the literature [35], which were also compatible with the dimensions established for the design of the experimental prototype. Effluent was collected from the lab-system at different time intervals until the concentration remained constant over time. The amount of adsorbed CEC was calculated as follows [36,37]: where C 0 is the initial CEC concentration (µg/L), C i is the CEC concentration in treated wastewater (µg/L), V is the volume of treated wastewater (L) and m is the mass of GAC (g). All adsorption experiments were performed at least twice and the results are reported as an average.

Plant Prototype Design
The prototype ( Figure 1) was designed, manufactured and installed by AZUD in the CEBAS-CSIC's Research Platform inside the Roldán-Lo Ferro-Balsicas WWTP, and it was directly connected to effluent from the secondary treatment. The maximum workflow of the prototype is 1200 L/h although hydraulically it is capable of working with lower flows (minimum 500 L/h). The water treatment includes three steps: 1 The first step is based on disc filters AZUD HELIX AUTOMATIC ® .
The objective of the first step is to filter the water out of the secondary settling tanks in order to allow the next step of the treatment (GAC) to work specifically on the adsorption of the CECs without any interference due to suspended particles that might reduce the adsorption performance.
Disc filters were selected to achieve this because this allows for a deep filtration that eliminates all particles larger than the degree of filtration and a high percentage of smaller ones, regardless of the geometry or nature of the particles. This is also an effective way of protecting the rear media filter. The disc filter module has a specific design that combines three independent stages working in series with several selected particle retention capacities (50, 20 and 5 µm). This experimental module includes an automatic backwash system that combines water and compressed air, which allow for the disc recovery. The air-assisted backwash system (AA) works with low pressure (even during the backwash process), thus reducing the hydraulic interaction in the prototype during cleaning and optimizing the water and energy consumption as well as obtaining total recovery of the discs. The backwashing times was 30 s for each stage.

2
The second step is based on the adsorption process using a high-quality coconut shell-based GAC.
A total of 112 kg of CG900 (Chiemivall, Castellbisbal, Barcelona, Spain), (see Table S1, Supplementary Materials) was placed in a bed column made of polyester reinforced with fiberglass of 1945 mm high with an auto-control valve. Weekly cleaning of the module was scheduled to ensure maximum repetitiveness of the analytical results. 3 The third step is based on a system for disinfection with UV radiation. This step was designed for disinfection purposes and consists of a conventional λ = 245 nm UV lamp with 200-400 W that was self-assembled in the prototype.
The prototype is totally autonomous due to the automation of all processes. Five solar panels (270POL, Sunconnection WorldWide 2016®, Murcia, Spain) were installed outside to provide the The maximum workflow of the prototype is 1200 L/h although hydraulically it is capable of working with lower flows (minimum 500 L/h). The water treatment includes three steps: 1 The first step is based on disc filters AZUD HELIX AUTOMATIC ® .
The objective of the first step is to filter the water out of the secondary settling tanks in order to allow the next step of the treatment (GAC) to work specifically on the adsorption of the CECs without any interference due to suspended particles that might reduce the adsorption performance.
Disc filters were selected to achieve this because this allows for a deep filtration that eliminates all particles larger than the degree of filtration and a high percentage of smaller ones, regardless of the geometry or nature of the particles. This is also an effective way of protecting the rear media filter. The disc filter module has a specific design that combines three independent stages working in series with several selected particle retention capacities (50, 20 and 5 µm). This experimental module includes an automatic backwash system that combines water and compressed air, which allow for the disc recovery. The air-assisted backwash system (AA) works with low pressure (even during the backwash process), thus reducing the hydraulic interaction in the prototype during cleaning and optimizing the water and energy consumption as well as obtaining total recovery of the discs. The backwashing times was 30 s for each stage.
The prototype is totally autonomous due to the automation of all processes. Five solar panels (270POL, Sunconnection WorldWide 2016 ® , Murcia, Spain) were installed outside to provide the required electric energy (Figure 2a). The panels supply a total of 1650 W, while the prototype consumes energy in a range between 840 W and 1600 W depending on the selected configuration (For more details, see Table S2). Solar panels were connected to the electric feed of the system through a set of batteries ( Figure 2b) for the continuous operation of the system even when the solar radiation is low or during the hours without sun.
Water 2020, 12, x 8 of 19 required electric energy ( Figure 2a). The panels supply a total of 1650 W, while the prototype consumes energy in a range between 840 W and 1600 W depending on the selected configuration (For more details, see Table S2). Solar panels were connected to the electric feed of the system through a set of batteries ( Figure 2b) for the continuous operation of the system even when the solar radiation is low or during the hours without sun.

Characterization of WWTP Effluent
Samples from the secondary effluent from the WWTP were characterized between March and June 2019 in order to assess the variability in real effluents. Table 3 shows the average, minimum and maximum values of the different physico-chemical parameters analyzed. In general, low standard deviations were obtained for almost all parameters analyzed, indicating effluent stability. The greatest variations in standard deviation were found in the analysis of Cl − and SO4 2− , which coincided with samples taken from point of entry to the WWTP.

Adsorption Capacity of Selected GAC
Before the commissioning of the prototype, the GAC maximum adsorption capacity was determined at lab-scale. The results (reported as the average concentration of all selected CECs) showed that after 120 L of wastewater was treated, the concentration remains constant, so, with

Characterization of WWTP Effluent
Samples from the secondary effluent from the WWTP were characterized between March and June 2019 in order to assess the variability in real effluents. Table 3 shows the average, minimum and maximum values of the different physico-chemical parameters analyzed. In general, low standard deviations were obtained for almost all parameters analyzed, indicating effluent stability. The greatest variations in standard deviation were found in the analysis of Cl − and SO 4 2− , which coincided with samples taken from point of entry to the WWTP.

Adsorption Capacity of Selected GAC
Before the commissioning of the prototype, the GAC maximum adsorption capacity was determined at lab-scale. The results (reported as the average concentration of all selected CECs) showed that after 120 L of wastewater was treated, the concentration remains constant, so, with regard to Equation (1), the maximum adsorption capacity was determined as 0.8 mg CECs/g GAC. Therefore, a maximum adsorption of 89.6 g of CECs can be expected in the GAC bed column of the self-sustainable prototype.

Disc-Filter Module
To evaluate the operation and efficiency of the disc-filter module, the pressure differential was continuously monitored, since this parameter allows evaluation of the degree of filter fouling. A conservative maximum pressure value for each of the selected filters (50, 20 and 5 µm) was set at 0.6 bars. When this value was reached, the automatic backwashing process was activated. The results (Figure 3) showed that of the total volume of prototype influent, only 0.23% was used for cleaning the filters, while 8.9% was destined to a second module cleaning (GAC bed column), and the water obtained was 90.87% of the total volume.
Water 2020, 12, x 9 of 19 regard to Equation (1), the maximum adsorption capacity was determined as 0.8 mg CECs/g GAC. Therefore, a maximum adsorption of 89.6 g of CECs can be expected in the GAC bed column of the self-sustainable prototype.

Disc-Filter Module
To evaluate the operation and efficiency of the disc-filter module, the pressure differential was continuously monitored, since this parameter allows evaluation of the degree of filter fouling. A conservative maximum pressure value for each of the selected filters (50, 20 and 5 µm) was set at 0.6 bars. When this value was reached, the automatic backwashing process was activated. The results (Figure 3) showed that of the total volume of prototype influent, only 0.23% was used for cleaning the filters, while 8.9% was destined to a second module cleaning (GAC bed column), and the water obtained was 90.87% of the total volume.  Our results are in accord with Ravina et al. [38], who suggested that by using disc filters, the volume of the backwash water was generally less than 0.5% of the total volume passing though the filter. However, considering that this low percentage corresponds to the cleaning of the filter with the smallest particle size (5 µm), the number of backwashes with respect to the accumulated treated volume was studied in order to evaluate the long-term efficiencies of the module (Figure 4). A total volume of 1000 m 3 of real secondary WWTP effluents was passed through the filtering module. The variability in the frequency of cleaning is mainly due to the TSS that can enter the filters from secondary WWTP effluents according to Duran-Ros et al. [39], however, in almost all cases, values under 20 were obtained. The trend followed a virtually horizontal line, indicating that the incidence of cleaning remained constant over time, which suggests that the system is able to recover its initial state. In general, system fouling is related to the cleaning frequency, so that if the cleaning frequency increases, the filtering capacity decreases, until the filter clogs. For a detailed investigation of disc filter fouling, it would be necessary to do a study with much larger volumes or to work with effluents containing higher TSS values (as shown in Table 3, the selected effluents have low TSS values). Our results are in accord with Ravina et al. [38], who suggested that by using disc filters, the volume of the backwash water was generally less than 0.5% of the total volume passing though the filter. However, considering that this low percentage corresponds to the cleaning of the filter with the smallest particle size (5 µm), the number of backwashes with respect to the accumulated treated volume was studied in order to evaluate the long-term efficiencies of the module (Figure 4). A total volume of 1000 m 3 of real secondary WWTP effluents was passed through the filtering module. The variability in the frequency of cleaning is mainly due to the TSS that can enter the filters from secondary WWTP effluents according to Duran-Ros et al. [39], however, in almost all cases, values under 20 were obtained. The trend followed a virtually horizontal line, indicating that the incidence of cleaning remained constant over time, which suggests that the system is able to recover its initial state. In general, system fouling is related to the cleaning frequency, so that if the cleaning frequency increases, the filtering capacity decreases, until the filter clogs. For a detailed investigation of disc filter fouling, it would be necessary to do a study with much larger volumes or to work with effluents containing higher TSS values (as shown in Table 3, the selected effluents have low TSS values).

GAC Bed Column Module
• Flow rate effects on CECs removal efficiency In general, the retention time of CECs in the bed column is one of the most important factors affecting the efficiency of adsorption, due to its influence on both the adsorbate and adsorbent. The variation in empty bed contact time (EBCT) in the GAC bed column was studied through the variation in the workflow rate. The maximum and minimum prototype workflow (1200 and 500 L/h), and three intermediate points (1000, 800, and 600 L/h) were studied. The values of the EBCT that corresponded with these points are detailed in Table 4. All experiments were performed by introducing real secondary WWTP effluents into a 5000 L mixing tank where additional quantities of each CECs (200 µg/L) were added. In order to obtain representative results, experiments were performed during several months (September and November 2019 and February 2020) and all analytical samples were analyzed in duplicate. The overall results are shown in Table 4. In all experiments, pH values remained constant at neutral pH (7.1-7.9). The selected CECs were moderately to effectively removed over the entire course of the experiments, with mean (± standard deviation) removals ranging from 52.5% ± 2.2% to 74.6% ± 6.1%. Results showed that CECs removal increased with the EBCT values, indicating that lower flow rates are most effective for CECs adsorption compared with higher flow rates. The same tendency occurred with DOC and turbidity removals, while an increase of % transmittance was detected. According to Rahman et al., this is due to two phenomena: (i) lower workflow rates imply higher residence time in the bed column, and (ii) compounds or ions present in wastewaters have more time to diffuse into the pores of GAC through intra-particle diffusion [40]. Therefore, in order to obtain high-quality effluents for agricultural uses,

GAC Bed Column Module
• Flow rate effects on CECs removal efficiency In general, the retention time of CECs in the bed column is one of the most important factors affecting the efficiency of adsorption, due to its influence on both the adsorbate and adsorbent. The variation in empty bed contact time (EBCT) in the GAC bed column was studied through the variation in the workflow rate. The maximum and minimum prototype workflow (1200 and 500 L/h), and three intermediate points (1000, 800, and 600 L/h) were studied. The values of the EBCT that corresponded with these points are detailed in Table 4. All experiments were performed by introducing real secondary WWTP effluents into a 5000 L mixing tank where additional quantities of each CECs (200 µg/L) were added. In order to obtain representative results, experiments were performed during several months (September and November 2019 and February 2020) and all analytical samples were analyzed in duplicate. The overall results are shown in Table 4. Table 4. CECs, dissolved organic carbon (DOC), turbidity and transmittance values obtained at different workflows (n = 6). In all experiments, pH values remained constant at neutral pH (7.1-7.9). The selected CECs were moderately to effectively removed over the entire course of the experiments, with mean (±standard deviation) removals ranging from 52.5% ± 2.2% to 74.6% ± 6.1%. Results showed that CECs removal increased with the EBCT values, indicating that lower flow rates are most effective for CECs adsorption compared with higher flow rates. The same tendency occurred with DOC and turbidity removals, while an increase of % transmittance was detected. According to Rahman et al., this is due to two phenomena: (i) lower workflow rates imply higher residence time in the bed column, and (ii) compounds or ions present in wastewaters have more time to diffuse into the pores of GAC through intra-particle diffusion [40]. Therefore, in order to obtain high-quality effluents for agricultural uses, a workflow of 500 L/h (EBCT 27 min) showed the best adsorption efficiencies. Under these conditions, the ability to remove individual CECs was evaluated.

Workflow (L/h) EBCT (min) HLR * (m/h) Total CECs
The results ( Figure 5) showed that the adsorption capacity for individual CECs followed the following trend: ACT > CBZ > NPX > KTP > DCF > ERY > SMX. The best adsorption results (95.77 ± 4.3%) were obtained for ACT mainly due to its low molecular weight compared to the rest of the CECs and its aromatic structure (see Table 1). In general, adsorption capacity is strongly related to the physical-chemical properties of CECs. Those with smaller molecular weights and aromatic compounds are more susceptible to adsorption in GAC systems, while higher molecular weight or low aromatic compounds are poorly adsorbed by GAC [41,42].
Water 2020, 12, x 11 of 19 a workflow of 500 L/h (EBCT 27 min) showed the best adsorption efficiencies. Under these conditions, the ability to remove individual CECs was evaluated. The results ( Figure 5) showed that the adsorption capacity for individual CECs followed the following trend: ACT > CBZ > NPX > KTP > DCF > ERY > SMX. The best adsorption results (95.77 ± 4.3%) were obtained for ACT mainly due to its low molecular weight compared to the rest of the CECs and its aromatic structure (see Table 1). In general, adsorption capacity is strongly related to the physical-chemical properties of CECs. Those with smaller molecular weights and aromatic compounds are more susceptible to adsorption in GAC systems, while higher molecular weight or low aromatic compounds are poorly adsorbed by GAC [41,42]. Specifically, ERY has a significantly higher molecular weight than the rest (733.94 g/mol). Furthermore, it is not aromatic, which has proven to be a disadvantageous adsorption characteristic, and it showed lower adsorption values in comparison with the other compounds (61.81% ± 8.61%).
The behavior of SMX is unusual compared to the above-it showed the lowest adsorption capacity (52.24% ± 5.15%). This may be related to its reactivity in aqueous solution, which results in two dissociation constants [43]. Because of this, SMX may be present in solutions in anionic form. Anionic species have a low tendency to adsorption by GAC, and may also be displaced by other adsorbates according to Yang et al. [44]. The low adsorption efficiency of SMX in GAC systems has been reported by several authors. For example, Motwani et al. reported that only 27.27% of SMX was removed using GAC with a particle size of 2.0-5.0 mm, while none or little adsorption were described by Telgmann et al. using different GAC sorbents (8 × 30 mesh, 4 × 8 mesh and 8 × 14 mesh of particle size) [45,46].

Inlet CECs concentration effects
Similar to previous studies, the effects of inlet CECs concentration were studied using real secondary WWTP effluents. Additional quantities of each CEC (at two different concentrations that differ by almost an order of magnitude, 200 and 50 µg/L) were introduced in a 5000 L mixing tank, and spiked effluents were passed through the GAC bed column at a workflow of 500 L/h. All analytical samples were analyzed in triplicate and the results are reported in Figure 6. Specifically, ERY has a significantly higher molecular weight than the rest (733.94 g/mol). Furthermore, it is not aromatic, which has proven to be a disadvantageous adsorption characteristic, and it showed lower adsorption values in comparison with the other compounds (61.81% ± 8.61%).
The behavior of SMX is unusual compared to the above-it showed the lowest adsorption capacity (52.24% ± 5.15%). This may be related to its reactivity in aqueous solution, which results in two dissociation constants [43]. Because of this, SMX may be present in solutions in anionic form. Anionic species have a low tendency to adsorption by GAC, and may also be displaced by other adsorbates according to Yang et al. [44]. The low adsorption efficiency of SMX in GAC systems has been reported by several authors. For example, Motwani et al. reported that only 27.27% of SMX was removed using GAC with a particle size of 2.0-5.0 mm, while none or little adsorption were described by Telgmann et al. using different GAC sorbents (8 × 30 mesh, 4 × 8 mesh and 8 × 14 mesh of particle size) [45,46].

• Inlet CECs concentration effects
Similar to previous studies, the effects of inlet CECs concentration were studied using real secondary WWTP effluents. Additional quantities of each CEC (at two different concentrations that differ by almost an order of magnitude, 200 and 50 µg/L) were introduced in a 5000 L mixing tank, and spiked effluents were passed through the GAC bed column at a workflow of 500 L/h. All analytical samples were analyzed in triplicate and the results are reported in Figure 6. With regard to the high variability of real WWTP secondary effluents, no significant effects were found between two studied CECs concentrations, except for ERY, which increased from 37.29 ± 8.76% to 54.55 ± 12.86% with concentrations of 50 and 200 µg/L, respectively. This can be explained by considering that at high initial concentrations, the ratio of ERY molecules to adsorbent GAC active sites is high, therefore, the probability of the interaction of molecules increases. Similar effects of inlet concentration are common in GAC systems and these have been included in several studies. Sotelo et al. [47] reported an increase in the percentage of caffeine (from 77.71% to 91.74%) and diclofenac (from 58.75% to 71.54%) adsorption when the initial concentration of these compounds increased from 3 to 7 mg/L, while Ang et al. [48] reported an increase in sevoflurane (an anesthetic) adsorption (from 536 ± 5 mg/g to 604 ± 9 mg/g and from 329 ± 5 to 368 ± 5 mg/g) when two different GACs (E-GAC and H-GAC, respectively) were used at inlet concentrations from 55.9 and 527.9 mg/L.

UV-Module Efficiency
Removal of pathogenic microorganisms is essential to guarantee the high quality of prototype effluents. Therefore, the efficiency of the selected UV-lamp was evaluated by monitoring different indicator microorganisms as described in the recently published Regulation (EU) 2020/741 of the European Parliament and of the Council of 25 May 2020 on minimum requirements for water reuse (E. coli for pathogenic bacteria, F-specific coliphages, somatic coliphages and total coliphages for pathogenic viruses, and Clostridium perfringens spores for protozoa) [13]. The monitoring of these indicators in influent and effluent prototype samples was carried out for a period of one year (March 2019-March 2020) and the values are shown in Table 5. The maximum and minimum prototype workflow (1200 and 500 L/h) was also evaluated.  With regard to the high variability of real WWTP secondary effluents, no significant effects were found between two studied CECs concentrations, except for ERY, which increased from 37.29 ± 8.76% to 54.55 ± 12.86% with concentrations of 50 and 200 µg/L, respectively. This can be explained by considering that at high initial concentrations, the ratio of ERY molecules to adsorbent GAC active sites is high, therefore, the probability of the interaction of molecules increases. Similar effects of inlet concentration are common in GAC systems and these have been included in several studies. Sotelo et al. [47] reported an increase in the percentage of caffeine (from 77.71% to 91.74%) and diclofenac (from 58.75% to 71.54%) adsorption when the initial concentration of these compounds increased from 3 to 7 mg/L, while Ang et al. [48] reported an increase in sevoflurane (an anesthetic) adsorption (from 536 ± 5 mg/g to 604 ± 9 mg/g and from 329 ± 5 to 368 ± 5 mg/g) when two different GACs (E-GAC and H-GAC, respectively) were used at inlet concentrations from 55.9 and 527.9 mg/L.

UV-Module Efficiency
Removal of pathogenic microorganisms is essential to guarantee the high quality of prototype effluents. Therefore, the efficiency of the selected UV-lamp was evaluated by monitoring different indicator microorganisms as described in the recently published Regulation (EU) 2020/741 of the European Parliament and of the Council of 25 May 2020 on minimum requirements for water reuse (E. coli for pathogenic bacteria, F-specific coliphages, somatic coliphages and total coliphages for pathogenic viruses, and Clostridium perfringens spores for protozoa) [13]. The monitoring of these indicators in influent and effluent prototype samples was carried out for a period of one year (March 2019-March 2020) and the values are shown in Table 5. The maximum and minimum prototype workflow (1200 and 500 L/h) was also evaluated. Clostridium perfringens spores and Escherichia coli were detected in all prototype influent samples with average values of 3000 and 9484 CFU/100 mL, respectively, while lower values were detected for Coliphages (the average values for total, somatic and F-Specific were 47, 45 and 3 MPN/100 mL, respectively).
At a workflow of 500 L/h, all microbiological parameters were removed, while an average 0.1% decrease in Clostridium perfringens spores and Escherichia coli was detected for workflows of 1200 L/h. Despite this small loss of efficiency, high-quality effluents were obtained in all cases according to (EU) 2020/741 regulations [13], and they also complied with the most restrictive crop category values (Class A: All food crops consumed raw where the edible part is in direct contact with reclaimed water and root crops consumed raw).
Therefore, and independently of the workflow, high-quality effluents for reuse purposes were obtained, which minimized the microbiological risk of ingesting any type of crop irrigated with reclaimed waters.

Continuous Operation of the Prototype
Considering the previous results for CECs and microbiological indicators removal, the workflow was adjusted to 500 L/h and the continuous operational work mode was evaluated. The work time was set for 8 h of work per day and weekly samples were evaluated for several months (March 2019-2020). At each sampling, both the influents (samples from the secondary treatment of the WWTP) and the prototype effluents were analyzed.
Analysis of the CECs in the prototype influent showed low concentration values for the selected compounds, with a minimum and maximum of 0.4 µg/L (DCF) and 3.20 µg/L (KTP), while ACT and ERY were not found in any analyzed sample with values below the analytical limits (limit of quantitation (LOQ)) marked by the reference laboratory that analyzed the samples ( Table 6). The physico-chemical and microbiological analysis of prototype influents showed values within the ranges in all cases as previously described in Tables 1 and 5. Prototype effluent samples showed average values for turbidity removal (28.58% ± 5.15%) and transmittance increase (20.66% ± 2.30%) similar to those obtained in previously reported values for the GAC module (Table 4), so, the variation in these parameters is directly related to the GAC efficiency. On the other hand, an average removal of 43.36% ± 12.14% of DOC was found in the prototype effluent. This is partly due to the efficiency of organic matter disposal in the GAC step (approximately 27.2% ± 4.0%), and the rest is due to its retention in the first stage (disc filters).
In all cases, the values obtained in prototype effluents for turbidity, TSS and BOD 5 were lower than the most restrictive values reported in the recently published (EU) 2020/741 Regulation on minimum requirements for water reuse (turbidity ≤ 5 NTU, TS ≤ 10 mg/L and BOD 5 ≤ 5 mg/L), while EC and SAR were lower than 3 dS/m and 6, respectively, which is in accord with Spanish regulations (Royal Decree 1620/2007, https://www.boe.es/buscar/doc.php?id=BOE-A-2007-21092) [49]. In addition, microbiological indicators showed the total removal of selected parameters (according to Table 5), while values below the analytical limits set (Table 6) for the selected CECs were found in all cases, indicating high-quality agronomic effluents, suitable for safe, agricultural reuse purposes.
After the good results obtained, and taking into account the low concentrations of CECs found in the prototype influent and its stability, as shown in Table 1, an additional study using WWTP secondary effluents was carried out to evaluate the binomial high quality vs. volume of produced water, with a flow rate of 1200 L/h (maximum prototype workflow). The results were similar to those obtained for a 500 L/h workflow and showed high efficiency in terms of CECs removal with lower LOQ values in all cases, while the physico-chemical and microbiological indicators were below the standard limits indicated above. These results indicate that higher workflows could be used with medium-high quality water, while in water with a high concentration of CECs such as industrial wastewaters (which may also contain high values of turbidity or organic matter) it is necessary to work at low flows to ensure the high agronomic quality of the effluent. Thus, previous characterization of WWTP effluents is necessary.
Although high quality effluents were obtained in both minimum and maximum workflows (500 and 1200 L/h) in this particular case, after treatment of 715.33 m 3 of wastewater, traces of CECs were found in prototype effluents (1200 L/h workflow). In particular, between 0.5 µg/L to 1 µg/L of CBZ, DCF, KTP, and SMX were detected, suggesting the saturation of the GAC column.
For a more detailed study, the decrease in adsorption efficiency at different treated wastewater volumes was evaluated (Figure 7). In accord with the lower CECs concentration in real WWPT effluents, a few control experiments were programmed using real WWTP effluents containing selected CECs (200 µg/L of each). Different volumes of treated wastewater (330, 440 and 715 m 3 ) were evaluated until the detected CECs point described above. The 500 and 1200 L/h workflows were compared (Figure 7). Table 5), while values below the analytical limits set (Table 6) for the selected CECs were found in all cases, indicating high-quality agronomic effluents, suitable for safe, agricultural reuse purposes.
After the good results obtained, and taking into account the low concentrations of CECs found in the prototype influent and its stability, as shown in Table 1, an additional study using WWTP secondary effluents was carried out to evaluate the binomial high quality vs. volume of produced water, with a flow rate of 1200 L/h (maximum prototype workflow). The results were similar to those obtained for a 500 L/h workflow and showed high efficiency in terms of CECs removal with lower LOQ values in all cases, while the physico-chemical and microbiological indicators were below the standard limits indicated above. These results indicate that higher workflows could be used with medium-high quality water , while in water with a high concentration of CECs such as industrial wastewaters (which may also contain high values of turbidity or organic matter) it is necessary to work at low flows to ensure the high agronomic quality of the effluent. Thus, previous characterization of WWTP effluents is necessary.
Although high quality effluents were obtained in both minimum and maximum workflows (500 and 1200 L/h) in this particular case, after treatment of 715.33 m 3 of wastewater, traces of CECs were found in prototype effluents (1200 L/h workflow). In particular, between 0.5 µg/L to 1 µg/L of CBZ, DCF, KTP, and SMX were detected, suggesting the saturation of the GAC column.
For a more detailed study, the decrease in adsorption efficiency at different treated wastewater volumes was evaluated (Figure 7). In accord with the lower CECs concentration in real WWPT effluents, a few control experiments were programmed using real WWTP effluents containing selected CECs (200 µg/L of each). Different volumes of treated wastewater (330, 440 and 715 m 3 ) were evaluated until the detected CECs point described above. The 500 and 1200 L/h workflows were compared (Figure 7). In both cases, the adsorption capacity decreased when the treated volume increased, suggesting that adsorption capacity gradually deteriorates with use. Specifically, a 50.05% ± 4.48% and 34.58% ± 5.24% decrease in adsorption efficiency was obtained for 1200 and 500 L/h workflows at 715 m 3 , respectively. The results suggest that when the adsorption capacity percentage decreases to around 50%, the GAC should be replaced.
According to Chae et al. [50], the rate at which carbon is exhausted and the frequency at which carbon should be replaced/regenerated can be calculated by determining the carbon usage rate (CUR), which is the mass of activated carbon used per unit volume of wastewater treated (Equation (2)).

=
(2) In both cases, the adsorption capacity decreased when the treated volume increased, suggesting that adsorption capacity gradually deteriorates with use. Specifically, a 50.05% ± 4.48% and 34.58% ± 5.24% decrease in adsorption efficiency was obtained for 1200 and 500 L/h workflows at 715 m 3 , respectively. The results suggest that when the adsorption capacity percentage decreases to around 50%, the GAC should be replaced.
According to Chae et al. [50], the rate at which carbon is exhausted and the frequency at which carbon should be replaced/regenerated can be calculated by determining the carbon usage rate (CUR), which is the mass of activated carbon used per unit volume of wastewater treated (Equation (2)).
Therefore, according to this equation, and selecting 715.33 m 3 as the maximum safety volume (conservative value for all possible prototype workflows), the CUR value obtained would be 0.15 kg of GAC per m 3 of treated volume (112 kg/715.33 m 3 ), which can be used as a predictive value for scaled-up GAC systems.

Applicability and Cost Assessment
Although several technical or environmental factors have to be taken into account in the selection or feasibility of implementing an effective tertiary system, cost is often the determining factor. Taking into account the advantages of the selected GAC in the adsorption of CECs, we considered two possible scenarios.
The first scenario involves the implementation of the prototype in isolated areas, where an improvement in water quality is necessary prior to irrigating crops, in a conventional WWTP that does not have an installed tertiary treatment. An estimation of the operation and maintenance costs of the prototype (excluding installation) are shown in Table 7. Considering 8 h of work per day and 365 days/year (2920 h/year), the theoretical cost is 1300 €/year. On the other hand, if we consider the possibility of working at the maximum flow rate of the prototype (1200 L/h), the expected treated volume of water is 3504 m 3 /year. However, since the treated volume is approximately 90% of the total entry to the prototype (see Figure 3), the treated volume of water would be 3154 m 3 /year. This means a maintenance cost of 0.37 €/m 3 treated or 0.41 €/m 3 produced, which is a relatively acceptable value given that the average cost of reused water treatment in Spain is about 0.46 €/m 3 for a system that includes a physico-chemical operation, membrane filtration, reverse osmosis and chlorination [51]. The second scenario is the inclusion of GAC modules in a conventional WWTP that already contain filtration steps and disinfection tertiary treatments. Thus, the long-term operational data from a WWTP with a conventional design was compared with the same design including a GAC step.
In the particular case of the Murcia region, the largest urban waste water regeneration system for the production of quality regenerated water 2.1 (according to the criteria of the Royal Decree 1620/2007 (2007), and MAPAMA recommendations (2010)) includes several stages: (1) coagulation-flocculation suspended matter reduction, using polyaluminium chloride (PAC) and anionic polyelectrolyte (PA); (2) filtration by sand filters, micro-sieves or textile filters; and (3) disinfection with UV lamps, and a final dose of NaClO.
Assuming a duration of 20 years, and that inversion costs are evenly distributed over that time, the implementation of a GAC system in a conventional WWTP would increase costs from approximately 0.117 €/m 3 to 0.142 €/m 3 , that is, an increase of 21%. This increase is mainly due to the costs of replacing the GAC and the increased energy consumption of installations (around 25%), while the remaining increase in costs is due to the initial investment (12%) and 5% is due to equipment and facilities maintenance.
In both scenarios, the higher costs are related to the current limited capacity to regenerate GAC (replacement costs). However, regeneration studies, together with the development of new adsorbents capable not only of purifying water but also recovering valuable substances, provide useful perspectives on the implementation of these processes.

Conclusions
This work clearly demonstrates the feasibility of implementing a self-sufficient prototype in conventional WWTP as a tertiary treatment of effluent for agricultural reuse purposes. Regardless of the workflow, the use of GAC provides a promising way to reduce CECs concentration, while the UV lamp was able to remove all microbiological parameters analyzed (E. coli, total coliphages (F-specific and somatic) and Clostridium perfringens spores).
Lower workflows (high EBCT) increased the CECs removal efficiency, particularly for low molecular weight and aromatic compounds. However, to select the workflow, it is necessary to know the initial quality of the water to be treated (concentration and nature of CECs, presence of interferences, etc.), as well as the required quality of the produced water.
The use of the previous filtration stage (disc filters) obtained a good proportion of filtered water versus water consumption, while the energy autonomy and self-operation of the prototype resulted in an economically viable methodology for its implementation in conventional WWTPs, and in isolated areas linked to crops.
In view of the limited information available on the large-scale use of efficient tertiary treatments for reuse purposes, the information obtained in this study will help to provide a reference for efficient industrial designs.