Sorption by active filter media can be a convenient option for phosphorus (P) removal and recovery from wastewater for on-site treatment systems. There is a need for a robust laboratory method for the investigation of filter materials to enable a reliable estimation of their longevity. The objectives of this study were to (1) investigate and (2) quantify the effect of hydraulic loading rate and influent source (secondary wastewater and synthetic phosphate solution) on P binding capacity determined in laboratory column tests and (3) to study how much time is needed for the P to react with the filter material (reaction time). To study the effects of these factors, a 22 factorial experiment with 11 filter columns was performed. The reaction time was studied in a batch experiment. Both factors significantly (α = 0.05) affected the P binding capacity negatively, but the interaction of the two factors was not significant. Increasing the loading rate from 100 to 1200 L m−2 d−1 decreased P binding capacity from 1.152 to 0.070 g kg−1 for wastewater filters and from 1.382 to 0.300 g kg−1 for phosphate solution filters. At a loading rate of 100 L m−2 d−1, the average P binding capacity of wastewater filters was 1.152 g kg−1 as opposed to 1.382 g kg−1 for phosphate solution filters. Therefore, influent source or hydraulic loading rate should be carefully controlled in the laboratory. When phosphate solution and wastewater were used, the reaction times for the filters to remove P were determined to be 5 and 15 minutes, respectively, suggesting that a short residence time is required. However, breakthrough in this study occurred unexpectedly quickly, implying that more time is needed for the P that has reacted to be physically retained in the filter.
Citation: Herrmann I, Jourak A, Hedström A, Lundström TS, Viklander M (2013) The Effect of Hydraulic Loading Rate and Influent Source on the Binding Capacity of Phosphorus Filters. PLoS ONE 8(8): e69017. https://doi.org/10.1371/journal.pone.0069017
Editor: Vishal Shah, Dowling College, United States of America
Received: March 26, 2013; Accepted: June 3, 2013; Published: August 2, 2013
Copyright: © 2013 Herrmann et al. This is an open-access article distributed under the terms of the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original author and source are credited.
Funding: This study was financed by the Swedish Research Council Formas and J. Gust Richert Foundation. The funders had no role in study design, data collection and analysis, decision to publish, or preparation of the manuscript.
Competing interests: The authors have declared that no competing interests exist.
It has been suggested that filters for the removal and recovery of phosphorus (P) from wastewater would be beneficial for on-site wastewater treatment e.g. in constructed wetlands. Many filter materials have been investigated ,  but it is still uncertain how well they would work in full-scale installations. Long-term field studies are not widely available . Usually, P binding capacity is determined from laboratory batch or fixed-bed column experiments and used to calculate the filter’s lifetime. To speed up the laboratory testing, parameters such as influent source (real wastewater or synthetic P solution), hydraulic loading rate, residence time, P loading and temperature do not match field conditions. These parameters vary substantially between different studies although it has been shown that the method used to test the materials influences the measured P binding capacity and thus the predicted performance of the filters as well as their predicted lifetime . There is a need for a robust test method that can be used to investigate filter materials and that gives reliable estimates of how well and how long they will function under given conditions. Therefore, it needs to be investigated as to which parameters can be altered in the laboratory to determine P binding capacity in a reasonable amount of time whilst assuring that the binding capacity determined in the laboratory resembles the one expected under field conditions.
Hydraulic loading rate and hydraulic residence time are closely connected and it has been shown that there is a relationship between these parameters and P binding capacity . The effect of varying residence time has been discussed by Brooks, Rozenwald et al. (2000) who stated that residence times from 15 to 143 hours (corresponding to loading rates of 905 and 114 L m−2d−1) positively affect the percentage of P removed from wastewater by wollastonite. Ádám et al.  suggested that the hydraulic loading rate does not affect the P binding capacity in Filtralite P, however, increased loading rate led to a faster breakthrough of P in their study. Also, the hydraulic loading rate was found to increase P binding capacity in Filtra P (unpublished data). The results of these studies show that the effect of hydraulic loading rate has not been comprehensively investigated. In particular, it is still unclear if loading rate or residence time is responsible for variations in binding capacity.
The measured P binding capacity can also vary depending on whether wastewater or synthetic P solution is used in the test: using wastewater decreases P binding. This effect has been shown in batch experiments with blast furnace slag  and a column experiment with Filtralite P . However, the conditions in which the batch experiments performed by Hedström and Rastas  were carried out did not resemble field conditions at all and the experiment by Ádám et al.  was performed with only two filter columns that were fed with different influent P concentrations which could have confounded the effect of the influent source. Therefore, the effect of influent source on P binding capacity still needs to be evidenced. Additionally, the effect has not yet been quantified.
The present study contributes to developing a sound testing method by investigating the effect of influent source and hydraulic loading rate on the determined P binding capacity. The objectives of this study are to investigate and quantify the effects of hydraulic loading rate and influent source (wastewater and phosphate solution) on P binding capacity and to study how much time is needed for the P to react with the filter material.
Materials and Methods
Two laboratory experiments were performed: a batch experiment to determine the time needed for the P to react within the filter material and a factorial column experiment to investigate the effect of different influent sources and hydraulic loading rates on the P binding capacity of the material.
1. Ethics statement
Oral permission for sampling wastewater at Sundom’s wastewater treatment plant was issued by Luleå municipality, Technical Department.
2. Filter material
The filter material used for the experiments was Filtralite P®. Its elemental composition was determined using inductively coupled plasma (ICP) analysis (Table 1). According to the product data sheet, Filtralite P® has a porosity of ca. 0.6 and a bulk density of 370 kg m−3.
3. Experiment to determine the time needed for the P to react
The time needed for the P to react with the filter material was determined with two series of batch experiments performed in dublicate (n = 2): one was conducted using phosphate solution and the other one using wastewater. The concentration of dissolved P was 12 mg L−1 in the phosphate solution and 11 mg L−1 in the wastewater (the wastewater used is further described in 2.4.3). The conditions in this experiment should resemble those in full-scale filters in terms of the liquid to solid ratio. This was 1.77±0.05 L kg−1 and was made by weighing 201.9 g of material (corresponding to ca. 200 g of dry material) into 1L-glass beakers. Then, 353.5±9.0 g of phosphate solution was added to one set of beakers and 356.7±7.9 g of wastewater was added to the other set of beakers until the material was almost covered but did not start floating up. Beakers were covered with plastic sheets and left standing at room temperature for 5 min, 15 min, 30 min, 1 h, 2 h, 4 h, 8 h and 16 h. The liquid phase was then poured through a 0.5 mm sieve, analyzed with respect to pH and redox potential, further filtered through a 0.45 μm filter and analyzed with respect to dissolved P.
4. Factorial column experiment
4.1. Factorial design.
The effect of influent source and hydraulic loading rate on the P binding capacity of the filter material was investigated in a laboratory experiment with a 22 full factorial design  with replicates (n = 2) and 3 centre points (one with wastewater and two with phosphate solution, Table 2). In total, 11 filters were tested (Table 2). The influents used were urine-spiked wastewater and synthetic phosphate solution. The low, medium and high levels of hydraulic loading rates and the corresponding flows, residence times and filter velocities are shown in Table 2.
4.2. Experimental set-up.
11 acrylic glass columns with a diameter of 7.4 cm were used in the experiments and run in up-flow mode using peristaltic pumps. For even flow distribution, a ca. 3 cm thick layer of glass beads (diameter 4 mm) was placed at the bottom of the columns. 100 g of oven-dried (105°C) and desiccator-cooled filter material were placed on top of these. A funnel filled with glass beads was put on top of the columns to ensure a smooth outflow. The effluent was collected in plastic containers.
4.3. Influent solution.
The ideal P concentration of the phosphate solution and secondary wastewater used in the experiments was 12 mg L−1; this resembles the P concentrations of secondary effluent to be treated by on-site P filters that can be between ca. 5 and 14 mg L−1 . The phosphate solution was prepared by dissolving KH2PO4 in distilled water.
Secondary wastewater was sampled twice weekly from a nearby wastewater treatment plant serving 300 pe. At the plant, the wastewater had been subjected to screening, primary sedimentation and biological treatment in a tower trickling filter. As the P concentration in the wastewater was below the target concentration, it was increased by adding human urine. The total and dissolved P concentrations in the urine-spiked wastewater were 13±3.6 and 11±1.7 mg P L−1, respectively. The pH was 7.1±0.2, the redox potential 127±31 mV, the TSS content 87±104 mg L−1 and the turbidity 56±66 NTU. The contents of total organic carbon (TOC) and dissolved organic carbon (DOC) were 126±34 mg L−1 and 108±8 mg L−1, respectively. The high deviations in TSS and turbidity in the wastewater were due to a temporarily non-functioning sludge pump in the pre-sedimentation at the treatment plant. The phosphate solution had an average concentration of 13±0.6 mg phosphate-P L−1, a pH of 5±0.4 and a redox potential of 304±48 mV. The above stated means and standard deviations were calculated over the entire experimental run-time although some filters were saturated earlier.
4.4. Effluent sampling.
Effluent samples were taken at least twice weekly from the plastic containers for each column. High and medium flow columns were sampled more frequently at the beginning. Samples were analyzed with respect to total and dissolved (filtered through a 0.45 μm filter) P, turbidity and TSS. Total and dissolved (filtered through a 0.45 μm filter) organic carbon (TOC and DOC) were only analyzed in samples from the wastewater-fed filters. pH and redox potential were measured from grab samples of the outflow taken at the same time as the effluent samples.
A P filter can generally be described as well-functioning as long as the outflow P concentrations are below 1 mg L−1, which is the normal limit used for small systems in Norway . Therefore, breakthrough of P through the filters was defined as to have happened when the concentration of dissolved outflow P divided by the concentration of dissolved inflow P was ≥0.08. The filters were assumed to be saturated when the dissolved P concentration in the outflow divided by the dissolved P concentration of the influent was ≥0.92. Moving averages were used to determine the point of saturation. The Ptot binding capacity was calculated using the total P concentrations of the influent and effluent:
Ptot binding capacity (1)
Ptot = binding capacity in g kg−1
n = number of samples taken
cin, out = total P concentration of the influent and effluent [mg L−1]
Vi = volume of wastewater or P solution that has passed through the filter between sample i-1 and i [L]
m = mass of the filter material [g].
Data were evaluated using analysis of variance and multiple linear regression with the MODDE software package . The significance level was set to α = 0.05.
The pH was measured using a WTW pH330 pH meter with a WTW SenTix41 pH electrode. The redox potential was measured using a pHM95 pH/ion meter (Radiometer, Copenhagen). TSS was determined following the European standard EN 872: 2005 . Turbidity was measured using an HACH 2100N turbidimeter (nephelometric method). All P analyses were performed using a Quattro spectrometer and the device-specific method no. A-031-04, following the European standards (ascorbic acid method) with modified digestion (persulfate oxidation) . Organic carbon was analysed using a Hach Lange photometric TOC analyzer.
Time needed for P to react
Using phosphate solution, the concentration of dissolved P could be decreased to below detection limit in the solution in less than 5 minutes (Fig. 1). The P detection limit was 0.05 mg L−1. When wastewater was used, it took longer to remove the phosphate from solution and the concentration could not be decreased that much: after 5 min, 10±2% of the P remained in solution and it took 15 minutes to remove about 99% of it (Fig. 1). The pH was generally lower when wastewater was used with the difference in pH being greater for shorter contact times (Fig. 1). The redox potential decreased logarithmically with contact time, from 11±11 mV (after 5 min) to −84±6 mV (after 16 h) in the wastewater and from 29±6 mV (after 5 min) to −74±11 mV (after 16 h) in the phosphate solution.
Factorial column experiment
Dissolved P effluent concentrations and pH for the three loading rates are shown in Fig. 2. Dissolved P concentrations in the effluent from the wastewater filters were generally higher when compared to the phosphate solution filters. Already at the first sampling occasion, these concentrations were, for wastewater (P solution) filters, 2.3 (0.06), 8.5 (1.8) and 6.1 (0.5) mg L−1 for low, medium and high loading rates, respectively (Fig. 2). Breakthrough was only observed for filters D1, 2 and F1, 2 (Fig. 2). In the other filters, breakthrough occurred before the first sample was taken. The pH at breakthrough for D1 and D2 was 10.8 and 10.7; for F1, 2 it was 10.2 (Fig. 2).
Ratios between effluent and influent dissolved P concentration (unfilled markers) and pH (filled markers) over bed volumes for low loading rate filters (A), medium loading rate filters (B) and high loading rate filters (C). The horizontal dashed lines show the criteria for breakthrough and saturation.
The P binding capacities determined for the filters are shown in Fig. 3. A small part of the P binding capacity in wastewater filters was due to the retention of particle-bound P. Both hydraulic loading rate and influent source had a significant negative effect on the Ptot binding capacity whilst the interaction effect of these two factors was not significant (Fig. 4). The effect of loading rate was stronger than the effect of influent source.
The P binding capacity of the wastewater filters is made up of two parts: one part is due to the uptake of dissolved P (gray bars) and the other part is due to the uptake of particle-bound P (cross-hatched bars).
The error bars show the 95% confidence interval on the effect value. The scaling of the data makes the coefficients comparable.
A linear model based on the factor main effects was fitted to the Ptot binding capacity data (Eq. 2). The fit was good (R2adjusted = 0.96) which means there is a strong linear relationship between the two factors and Ptot binding capacity. In Eq. 2, influent source must be set to −1 for wastewater filters and to +1 for P solution filters; the unit of loading rate is L m−2 d−1. The equation can only be used within the levels of loading rate (and the corresponding residence times) investigated in this study.(2)
Eq. 2 can be used to demonstrate the effects of influent source and loading rate by quantification: when increasing the loading rate from 100 to 1200 L m−2 d−1, Ptot binding capacity decreased from 1.152 to 0.070 g kg−1 for wastewater filters and from 1.382 to 0.300 g kg−1 for phosphate solution filters (Eq. 2). Holding the loading rate at the low level, the average Ptot binding capacity of wastewater-fed filters was 1.152 g kg−1 as opposed to 1.382 g kg−1 for phosphate solution filters. As the model fits the data well, these calculated values are very close to the Ptot binding capacities shown in Fig. 3.
pH generally decreased over time in all filters (Fig. 2, Table 3). Wastewater filters had a significantly lower start pH and mean pH compared to phosphate solution filters. When the filters were saturated, the pH was equally low for all filters (on average 8.7±0.3, Table 3). The redox potential was positive for all filters throughout the experiment; the average redox potential was significantly lower in the wastewater filters compared to phosphate solution filters. For phosphate solution filters, increasing the loading rate led to an increase in mean redox potential which was not observed for the wastewater filters (Table 3).
Particle-bound P escaped from the filters, which is shown by the concentration measurements of particle-bound P as well as TSS and turbidity measurements in the effluent (Table 3). For all but the low loaded phosphate solution filters, turbidity and TSS were significantly positively correlated. The turbidity and the total mass of TSS in the effluent were significantly higher in wastewater filters, and turbidity significantly increased with increasing loading rate. Both TSS and the average concentration of particle-bound P in the effluent showed an increasing trend over loading rate (Table 3).
The reduction of TOC and DOC in the wastewater filters was 71% and 75%, respectively. One-way analyses of variance showed no significant effect of loading rate on the effluent TOC, DOC and particulate OC nor on the reduction of TOC and DOC (in %) in the filters.
Reliability of produced data
In this study, a replicated factorial design was used producing a solid and valid evaluation. The effect of influent source and loading rate could be quantified using a regression model (Eq. 2) and also tested for statistical significance. The regression was significant (p = 0.000) and the high value of R2adjusted = 0.96 indicates a good fit to the data. The model is valid (showed no lack of fit). The replicated filters generally showed very similar responses (Fig. 2, Fig. 3, Table 3). The pure error was therefore very small indicating a high reproducibility of the experiment. For the aforementioned reasons, the estimations of the factor effects made in this study can be considered reliable.
When the effect of different factors is to be investigated, a solid design is necessary to enable a comparison between the levels of those factors. The factors studied here, influent source and loading rate, have been previously studied, although their effects were not the main focus of those studies. Therefore, the comparison between their levels has been difficult either because of the lack of replicates and too few observations at each level , , or because standard deviations were not presented , or because the effects were influenced by nuisance factors such as different influent P concentrations .
Effect of loading rate
The loading rate affected the determined Ptot binding capacity in this study negatively (Fig. 4). To understand the negative effect of loading rate in this study, it is important to look at the processes in the filter. When the filter material makes contact with water, calcium (Ca) ions probably hydrolyze through the weathering of Ca-containing compounds in the material, reacting with phosphate and precipitate. The precipitates are then physically/mechanically retained in the filter. The negative effect of loading rate could be explained by an increased wash-out of P precipitates. In this study, the concentration of particle-bound P in the effluent showed an increasing trend with loading rate (Table 3) which means that more particle-bound P was washed out at higher loading rates. This effect was observed for both influent sources, however it was less pronounced for the wastewater filters because of the retention of particles contained in the influent wastewater. Influent particles in the wastewater that accumulated in the filter might also have enhanced the filters’ ability to filtrate (small) particles. Another explanation for the lower Ptot binding capacity at high loading rates could be the washout of reactive Ca ions which has been observed in a study by Ádám et al. . The negative effect of loading rate could also be explained by a poor contact between influent and filter particles: Suliman et al.  showed with tracer tests that increasing the loading rate can lead to a higher preferential flow and less porosity used for active flow.
Increasing the loading rate also implies a shorter residence time of the solution in the filters. Filtralite P®-filters are usually constructed as subsurface horizontal flow filter beds implying that the area used for the calculation of the hydraulic loading rate would be the cross-sectional area. It can be debated as to whether residence time or loading rate is the relevant design parameter for filters. Most probably, both parameters are of importance: loading rate is the factor governing the pore velocity in the filter and can thus influence surface reactions on the material as well as the fixation of Ca-P precipitates on the surfaces of the filter particles and between particles. Residence time, on the other hand, determines the time available for Ca-P precipitates to form and to form bigger particles e.g. hydroxyapatite (Hap) crystals. This study shows that the time needed for the formation of Ca-P compounds is short (Fig. 1). Also, Hap has been shown to form within minutes at pH 9 in the presence of boehmite . This indicates that a short residence would be sufficient and the hydraulic loading rate would be the more relevant parameter. However, P breakthrough in the filters occurred quickly: before the first samples were taken for all wastewater filters and for filters E1, 2 (Fig. 2) although the first samples were taken after 5 days for the low loading rate filters, after 2 days for the medium loading rate filters and after 1 day for the high loading rate filters. This rapid breakthrough was unexpected because the levels of loading rate chosen (96, 638 and 1122 L m−2 d−1) were well in line with the hydraulic loading rates used in full-scale Filtralite P®-facilities that used loading rates of 90 to 160 L m−2 d−1 , 222 L m−2 d−1 , 250 L m−2 d−1  and 444 L m−2 d−1 . Very high loading rates of several thousands of L m−2 d−1 have been applied in some facilities that have removed 99% P in the first three years . Therefore, the loading rates used in this study seem justified. However, the size of the filter bed we used was small (100 g of material per filter column) and therefore, the residence times of the filters were short (49 min, 85 min and 9.5 h). The previously mentioned full-scale facilities use residence times of about 1.7 days , 2.9 to 5.6 days  and about 18 days . Therefore, despite the short reaction time (Fig. 1), the residence time seems to play a major role in P retention and might, for the material investigated, be the more relevant parameter. Possibly, the residence times connected to the chosen loading rates in this study were too short for the precipitates to agglomerate or crystallize to particles that were big enough to be physically retained in the filter matrix. Also, mechanisms other than Ca-phosphate precipitation might contribute to the retention of P in the material. In used Filtralite® P, Ádám et al.  found P bound to surfaces of aluminium-containing particles. These surface processes might take more time and therefore require a longer residence time.
Effect of influent source
Although the effect of the different influent sources was less pronounced than the effect of loading rate, the Ptot binding capacity in the wastewater filters was significantly lower compared to phosphate solution filters (Fig. 4). This agrees with the findings of Ádám et al.  whose P solution-fed column treated a higher cumulative amount of P before breakthrough compared to their wastewater-fed column. Three possible explanations for this will now be discussed: a different pH regime, inhibition of Ca-phosphate formation by humic substances and clogging of the filter by accumulation of particles with the formation of a biofilm.
Both the start pH and average pH (over the experimental runtime) were significantly lower in the wastewater filters (Fig. 2, Table 3) which could explain the higher outflow P concentrations in the wastewater filters right from the beginning and thus the early breakthrough and the lower Ptot binding capacity. A great part of the soluble organics in wastewater are volatile acids, most of them being acetic acids . The wastewater is a buffer solution in itself, thus decreasing the buffer effect of the material resulting in a lower outflow pH compared to the phosphate solution filters. Ca-phosphate precipitation, however, is favoured at high pH . Song et al.  found that the saturation index of Hap is a polynominal function of the solution pH and increases when pH increases from 7 to 11. Hap is a stable Ca-phosphate phase that is likely to be formed in P filters and has been found in filter materials after use , .
The average pH in the wastewater filters was 8.7 and 9.0 (Table 3), which is the pH range within which humic substances can inhibit the precipitation of Ca-phosphates. The inhibitory effect is pronounced at pH 8, small at pH 9 and non-existent at pH 10 . This effect has been attributed to the combination of humic substances with Ca, but also to the blocking of active growth sites on newly nucleated Ca-phosphate precipitates by organic matter .
The reduction of DOC in the wastewater filters was as high as 75% (see chapter 3.2) indicating a sorption of DOC in the filters. It has previously been suggested that the formation of Ca-phosphate precipitates is responsible for the removal of dissolved organic matter: newly formed Ca-phosphate precipitates have a large surface area and adsorb the organic matter . Particulate organic matter was removed by filtration, indicated by an average TOC reduction of 71%. The retained organic matter in the filters may have clogged the filter and contributed to the formation of a biofilm layer on the filter particles which possibly hampered the dissolution of Ca from the material. If less Ca is dissolved, the Ca/P ratio is lower. Song et al.  found the Ca/P ratio to increase the saturation index for Hap. As Hap is an important reaction product, the Ca/P ratio may be a relevant parameter governing P removal. Song et al.  further suggested that organic matter (other than humic substances) consumes Ca but is not precipitated, which would mean in this case that Ca may have been washed out by organic matter, thus decreasing the Ca/P ratio further. Biofilm formation and decreased Ca dissolution could therefore explain the lower P binding capacity (Fig. 3) and lower numbers of bed volumes that could be treated with the wastewater filters (Table 3).
Factor settings in laboratory filter tests
In one way or another, laboratory tests need to be accelerated in comparison to full-scale filters to obtain results in a reasonable amount of time. Therefore, at least one filter parameter must change. Hydraulic loading rate seems to be an unsuitable parameter to adjust in order to decrease the time needed for testing, as it had a significant negative effect on the Ptot binding capacity in this study (Fig. 4) and previous studies , . Increasing the influent P concentration can affect P binding capacity both negatively (unpublished data) and positively , although in the former study data were evaluated until breakthrough whilst in the latter, data until saturation were used. Using a synthetic P solution, instead of wastewater, would overestimate the determined P binding capacity because of the negative effect of wastewater (Fig. 4). A way of compensating for this effect would be to adjust the achieved P binding capacity with a correction factor. Based on the results of this study, the correction factor would be 0.8 if the experiment is carried out at the low loading rate.
When down-sizing a full-scale filter to laboratory scale, all parameters (such as hydraulic loading rate and influent properties) could be held at the same level while only the residence time would decrease. This approach seems reasonable as the time needed for the reaction of P in the filter material was very short (Fig. 1). However, the reaction time was determined using fresh material only and probably changes over the operational lifetime. Furthermore, the time needed for the reaction does not equal the residence time that is necessary for P retention: the growing of Ca-P crystals that can be retained in the filter might take more time than the actual reaction of dissolved P with Ca. As breakthrough in our experiment occurred earlier than would have been expected from full-scale filter usage, residence time seems to be an important design parameter for both laboratory and full-scale filters, at least for the material investigated in this study. To increase residence time in laboratory filters, however, would considerably prolong the duration of the testing.
The effects of hydraulic loading rate and influent source on the P binding capacity of Filtralite®P was investigated in a replicated 22 factorial laboratory experiment. Ptot binding capacity was significantly affected by both hydraulic loading rate and influent source. Hydraulic loading rate affected Ptot binding capacity more strongly than influent source. An interaction effect of the two factors was not present. Increasing loading rate from 100 to 1200 L m−2 d−1 caused the Ptot binding capacity to decrease from 1.15 to 0.07 g kg−1 for wastewater filters and from 1.38 to 0.30 for phosphate solution filters. At a loading rate of 100 L m−2 d−1, the average Ptot binding capacity of wastewater filters was 1.15 g kg−1 as opposed to 1.38 g kg−1 for phosphate solution filters. Hence, altering these two factors in the laboratory can lead to misleading results that do not reflect a material’s expected performance in field.
The time needed for the reaction of P in fresh filter material was determined to be 5 minutes when phosphate solution was used. Using wastewater, the reaction took longer: after 15 min, the remaining dissolved P in the solution was about 1%. This suggests that a rather short residence time in the filter would be sufficient. However, the reaction times were determined using fresh material and might change with time. Furthermore, as breakthrough in the experiment was reached unexpectedly quickly compared to full-scale filters, there is evidence that it is important to consider not only hydraulic loading rate but also residence time.
The authors thank Lea Rastas Amofah and Jiri Marsalek for valuable discussions, Kerstin Nordqvist and Oleksandr Panasiuk for help with the experimental work and Jan-Erik Ylinenpää for kind support at the wastewater treatment plant.
Conceived and designed the experiments: IH AH TSL. Performed the experiments: IH. Analyzed the data: IH AH. Wrote the paper: IH AH MV TSL AJ. Valuable discussions with the first author: AH MV TSL AJ.
- 1. Vohla C, Kõiv M, Bavor HJ, Chazarenc F, Mander Ü (2011) Filter materials for phosphorus removal from wastewater in treatment wetlands–A review. Ecol Eng 37: 70–89.
- 2. Johansson Westholm L (2006) Substrates for phosphorus removal–Potential benefits for on-site wastewater treatment? Water Res 40: 23–36.
- 3. Drizo A, Comeau Y, Forget C, Chapuis RP (2002) Phosphorus saturation potential: A parameter for estimating the longevity of constructed wetlands. Environ Sci Technol 36: 4642–4648.
- 4. Ádám K, Krogstad T, Suliman FRD, Jenssen PD (2005) Phosphorus sorption by Filtralite P–Small scale box experiment. J Environ Sci Health 40: 1239–1250.
- 5. Hedström A, Rastas L (2006) Methodological aspects of using blast furnace slag for wastewater phosphorus removal. J Environ Eng 132: 1431–1438.
- 6. Ádám K, Krogstad T, Vråle L, Søvik AK, Jenssen PD (2007) Phosphorus retention in the filter materials shellsand and Filtralite P®–Batch and column experiment with synthetic P solution and secondary wastewater. Ecol Eng 29: 200–208.
- 7. Montgomery DC (2001) Design and analysis of experiments. New York: John Wiley & Sons. 684p.
- 8. Arias CA, Brix H, Johansen NH (2003) Phosphorus removal from municipal wastewater in an experimental two-stage vertical flow constructed wetland system equipped with a calcite filter. Water Sci Technol 48: 51–58.
- 9. Heistad A, Paruch AM, Vråle L, Ádám K, Jenssen PD (2006) A high-performance compact filter system treating domestic wastewater. Ecol Eng 28: 374–379.
- 10. Umetrics AB (2006) MODDE. 8. 0. 0. 0, May 31 2006.
- 11. Swedish Standards Institute (2005) Water quality–Determination of suspended solids–Method by filtration through glass fibre filters. EN 872: 2005.
- 12. Swedish Standards Institute (2005) Water quality – Determination of phosphorus – Ammonium molybdate spectrometric method. SS-EN 6878: 2005.
- 13. Brooks AS, Rozenwald MN, Geohring LD, Lion LW, Steenhuis TS (2000) Phosphorus removal by wollastonite: A constructed wetland substrate. Ecol Eng 15: 121–132.
- 14. Suliman F, Haugen L, Jenssen PD (2005) Salinity effect on the characteristics of saturated horizontal flow in small boxes containing Filtralite-P. J Environ Sci Health 40: 1403–1413.
- 15. Li W, Xu W, Parise JB, Phillips BL (2012) Formation of hydroxylapatite from co-sorption of phosphate and calcium by boehmite. Geochim Cosmochim Acta 85: 289–301.
- 16. Ádám K, Søvik AK, Krogstad T (2006) Sorption of phosphorus to Filtralite-PTM–The effect of different scales. Water Res 40: 1143–1154.
- 17. Vråle L, Heistad A, Jenssen P (2005) Results and experiences from the two pilot plants at Norderås in Norway. Report Norwegian University of Life Sciences, Ås, Norway: 54p.
- 18. Vilpas R, Valve M, Räty S (2005) Report from the pilot plants in Finland.
- 19. Weber (2008) Upper Uvdal wastewater treatment plant–Filter bed. Available: http://filtralite.maxit-cms.com/media/92/References/Uvdal_EN_Print.pdf. Accessed 2012 May 21.
- 20. Narkis N, Henefeld-Fourrier S, Rebhun M (1980) Volatile organic acids in raw wastewater and in physico-chemical treatment. Water Res 14: 1215–1223.
- 21. Feenstra TP, De Bruyn PL (1979) Formation of calcium phosphates in moderately supersaturated solutions. J Phys Chem 83: 475–479.
- 22. Song Y, Hahn HH, Hoffmann E (2002) Effects of solution conditions on the precipitation of phosphate for recovery: A thermodynamic evaluation. Chemosphere 48: 1029–1034.
- 23. Song YH, Hahn HH, Hoffmann E, Weidler PG (2006) Effect of humic substances on the precipitation of calcium phosphate. J Environ Sci (China) 18: 852–857.
- 24. Eveborn D, Gustafsson JP, Hesterberg D, Hillier S (2009) XANES speciation of P in environmental samples: An assessment of filter media for on-site wastewater treatment. Environ Sci Technol 43: 6515–6521.