Bowei Zhao,
Fei Xie,
Xiao Zhang and
Xiuping Yue*
College of Environmental Science and Engineering, Taiyuan University of Technology, 79 Yingzexi Road, Taiyuan 030000, P. R. China. E-mail: yuexiuping@tyut.edu.cn; Tel: +86 0351-3176586
First published on 23rd June 2020
Trickling biofilters (TFs) allow for a simultaneous nitrification and denitrification (SND) process, and offer a favorable solution for the treatment of swine-wastewater digested liquid due to their simple operation and low cost. In this study, a soil trickling biofilter (STF) was developed to enhance nitrogen removal. A gravel trickling filter (GTF) and a woodchip trickling filter (WTF) were also constructed and operated synchronously to demonstrate the advantage of micron-sized media. The results showed that the STF had a higher ammonium nitrogen (NH4+-N) removal capacity of 21.4%, 24.9%, and 18.3% in comparison to the GTF when the influent NH4+-N was 192.9 mg L−1, 500.2 mg L−1 and 802.1 mg L−1, respectively. The total nitrogen (TN) removal capacity of the STF was 104.6%, 89.4%, and 37.5% higher than that of the WTF. Thus, the addition of micron-sized soil to TF could increase the systemic nitrogen removal capacity.
The key point of swine wastewater treatment is the removal of nitrogen from the digested liquid with a low carbon/nitrogen ratio (C/N).7 Most technologies for nitrogen removal are based on the conventional nitrification and denitrification processes. Generally, the traditional biological nitrogen removal process includes plug flow reactors [e.g., anoxic oxic (A/O)]8 and continuous stirred tank reactors [e.g., sequencing batch reactor (SBR)].9,10 Although these techniques have a favorable effect on nitrogen removal during swine-wastewater digested liquid treatment, they are disadvantageous in terms of their running costs.
The modern nitrogen removal processes include single high ammonia removal over nitrite (SHARON), anaerobic ammonium oxidation (ANAMMOX), complete autotrophic nitrogen removal over nitrite (CANON), and oxygen-limited autotrophic nitrification–denitrification (OLAND). These methods have several advantages in terms of their low running costs due to the money saved for aeration, the organic carbon source for denitrification, and the reactor volume.11–13 Unfortunately, these technologies require strict operational conditions to maintain the stability of the system, which increases the operation difficulties and restrict their widespread application.
Trickling biofilter (TF) is a biofilm wastewater treatment process that has been generally recognized as providing an effective simultaneous nitrification and denitrification (SND) process with a low-cost and convenient management. TF has been widely used to treat domestic wastewater, piggery wastewater, textile wastewater, and leachate.14 The biochemical process is the main pollutant removal pathway, whereby the microbes growing on the surface of the filter material play the major role.15 Hence, the characteristics of the filter material are key factors affecting the efficiency of TF.
An excellent filter material should have a large specific surface area and a good biofilm adhesion. Various materials have been investigated as filter material for use in TF systems, for example, zeolite, sand, plastic, woodchip and complex material.16 This study focused on the surface characteristics of the filter media to obtain favorable treatment efficiency. With the exception of the surface characteristics, the size of the filter material is the most direct factor affecting the specific surface area of the material. In principle, the smaller the size of a filter material, the larger specific surface area is for the enrichment of microbes. Soil, as the natively weathered gravel, generally has a small size between millimeters and microns. Hence, soil infiltration technology has long since been used for water treatment.17,18 However, the clogging and blocking of the soil layer limit the treatment capacity of soil infiltration, and also prevent the utilization of soil in TF systems.1
In this study, a novel soil TF (STF) is proposed to solve the clogging problem of a micron-sized soil filter material under a high hydraulic and organic load. This novel technique involves the micron-sized soil adhering to a woodchip framework. Thus, the soil layer that becomes fixed to the framework can resist a certain hydraulic load and has a large specific surface area to adhere to the biofilm. In order to compare the advantages of this STF process, a gravel TF (GTF) and a woodchip TF (WTF) were also constructed and synchronously operated. The aim of using GTF is to demonstrate the size advantage of the micron-size soil for the enrichment of microbes, whereas the aim of using the WTF is to show the effect of the woodchip framework in the STF.
Period | Day | COD (mg L−1) | NH4+-N (mg L−1) | TKN (mg L−1) | TN (mg L−1) | TP (mg L−1) | pH |
---|---|---|---|---|---|---|---|
Startup | 1–55 | 295.1 | 489.7 | 492.8 | 496.6 | 18.7 | 8.3 |
I | 56–155 | 180.9 | 192.9 | 194.5 | 198.1 | 8.7 | 8.0 |
II | 156–255 | 293.1 | 500.2 | 502.2 | 503.8 | 19.3 | 8.3 |
III | 256–346 | 508.9 | 802.1 | 804.5 | 807.3 | 29.2 | 8.5 |
To create a soil layer within the framework of the STF, the woodchips were soaked in fresh water and then rolled over the prepared dry soil powder. As the woodchips were damp, the soil adhered onto the surface of the woodchips. The bulk volume ratio of the woodchips to the soil in the STF was approximately 2:1. To compare the efficiency of the three TFs, the void volume ratio for each of the three TFs was about 50%.
Fig. 2 SEM images of the filter media before operation: (A) wood chips; (B) gravel; (C) soil; (D) wood chips adhered by soil; (E) wood chips 3000×; (F) gravel 3000×; (G) soil 3000×. |
The influent COD during period I, II, and III was 180.9 mg L−1, 293.1 mg L−1, and 508.9 mg L−1 with an organic load of 30.8 g m−3 d−1, 49.8 g m−3 d−1, and 86.5 g m−3 d−1, respectively (Fig. 3A). The COD removal efficiencies of all three TFs recovered and were stable again within 5 days once the influent changed. This indicates that the TF process in all of the reactors had a good capacity to resist the organic load impact, which agrees with previous studies.19,20 The average COD removal rate of the WTF during the stable stages of periods I, II, and III (i.e., day 56 to day 155, day 156 to day 255, and day 256 to day 346, respectively) was 11.0%, 44.2%, and 60.6%, respectively. Meanwhile, the COD removal rate of the GTF during the stable stages of periods I, II, and III was 35.1%, 41.7%, and 60.1%, and that of the STF was 3.9%, 21.7%, and 49.6%, respectively (Fig. 3B).
The NO2−-N and NO3−-N concentrations in the effluents of the three TFs are shown in Fig. 3E and F. All three TFs had a similar variation in the NO2−-N concentration, which first increased and then decreased. When the effluent NO2-N concentration reduced, the effluent NO3−-N concentration increased, which agrees with the general rule of bio-nitrification. The highest effluent NO2-N concentration in the WTF, GTF, and STF occurred on day 21 (282.8 mg L−1), day 31 (268.6 mg L−1), and day 31 (222.4 mg L−1), respectively. Towards the end of the start-up period, the effluent NO3−-N concentration of the WTF, GTF, and STF was 52.6 mg L−1, 45.6 mg L−1, and 70.5 mg L−1, whereas the effluent NO2−-N decreased to 200.9 mg L−1, 200.5 mg L−1, and 155.6 mg L−1.
There were two main processes involved in the removal of NH4+-N: physiochemical and microbe catalysis. During the start-up period, the abundance of microbes was lower with a relatively low activity; thus, absorption to the filter media was the main process of NH4+-N removal. Although Buelna21 considered that NH4+-N stripping was a main removal process at high pH, absorption may have been more important in the start-up period of TFs in this study. Different trends were evident when comparing the NH4+-N removal in the WTF, GTF, and STF, which could have been caused by adsorption to the filter material. Due to the high adsorption to soil, the STF had a relatively high NH4+-N removal during the first 10 days.
During period I, the average influent NH4+-N concentration was 192.9 mg L−1 with an average nitrogen loading ratio (NLR) of 32.79 g m−3 d−1. The NH4+-N removal rate of the three TFs increased gradually (Fig. 3C) and the effluent NO2−-N concentration reduced sharply as the NO3−-N concentration increased (Fig. 3E and F). All three reactors subsequently entered a stable stage from day 81 to day 151, during which, the NH4+-N removal rate of the WTF, GTF, and STF was 84.50%, 69.80%, and 84.86%, respectively. The average NO2-N concentration in the effluents of the WTF, GTF, and STF during this period was 2.1 mg L−1, 11.7 mg L−1, and 2.5 mg L−1, respectively, whereas the NO3−-N concentration was 90.6 mg L−1, 90.0 mg L−1, and 88.4 mg L−1, respectively. The average NH4+-N concentration in the influent increased to 500.2 mg L−1 during period II, while the NLR was 85.03 g m−3 d−1. The NH4+-N removal rates of the three TFs reduced sharply during period II before recovering in following 45 days. From day 206 to day 251, the amount of NH4+-N removed by the WTF, GTF, and STF was maintained at approximately 186.2 mg L−1, 295.6 mg L−1, and 195.7 mg L−1, respectively. The NO2−-N concentration in the effluents of the three TFs increased in early stage and then reduced. During the stable stage of period II, the average NO2-N concentration in the effluents of the WTF, GTF, and STF was 14.1 mg L−1, 21.1 mg L−1, and 31.0 mg L−1, respectively. The NO3−-N concentration in the effluents of the WTF, GTF, and STF all increased gradually before stabilizing after day 206 at approximately 241.4 mg L−1, 207.3 mg L−1, and 181.0 mg L−1.
When the influent NH4+-N concentration was further increased during period III, the average NLR was 136.35 g m−3 d−1, and the NH4+-N removal rate of the three TFs was further lowered. When stabilized, the average NH4+-N removal rate of the WTF, GTF, and STF was 50.13%, 48.44%, and 57.32%, respectively. After day 291, the NO2−-N concentrations in the effluents of the WTF, GTF, and STF were stable at approximately 32.5 mg L−1, 58.8 mg L−1, and 116.1 mg L−1. The NO3−-N concentration in the effluents of the GTF, STF, and WTF fluctuated slightly around the average values of 169.3 mg L−1, 116.8 mg L−1, and 182.2 mg L−1, respectively.
As shown in Fig. 4, simultaneous nitrification and denitrification occurred in the three reactors, accounting for the nitrogen removal. The Ca2+ and Na+ adsorbed to the surface of the soil was replaced by NH4+, and the Ca2+ and Na+ precipitated after combining with OH−. The cations associated with OH−, HCO−, and CO32− anions form a dynamic balance of alternating ion changes. In the AOB process, oxygen is consumed for the oxidization of ammonia to nitrite. In addition, H+ ions are generated from this reaction (eqn (1)). The nitrite and nitrate that are produced are reduced to N2 during the denitrification process while H+ ions are consumed (eqn (2)):22
NH4+ + 1.24O2 + 0.16CO2 + 0.04HCO3− → 0.04C5H7O2N + 0.96NO2− + 0.94H2O + 1.9H+ | (1) |
0.1561NO3− + 0.1167CH3OH + 0.1561H+ → 0.0095C5H7O2N + 0.119CO2 + 0.3781H2O | (2) |
The identified species belonged to Nitrosomonas (bands A1, A2, A4, A8, and A11), Nitrosospira (A9 and A10), Rhodanobacter (A6 and A12), Streptococcus australis (A13), Clostridiales (A3), Actinomycete (A7), and an unidentified bacteria (A5). The AOB were divided into the β-subclass and γ-subclass.23 There were two genera in the β-subclass: Nitrosomonas and Nitrosospira. The later included two subgenera: Nitrosolobus and Nitrosovibrio.24 In this study, all identified AOB species belong to the β-subclass, although some identified species were not AOBs, which was due to the specificity of the primers. The specificity of PCR is usually limited by only one AOB specific primer. The CTO189f/CTO654r primers held a higher specificity within the AOB specific primer.25 Bacterium for bands A1, A2, A4, and A8 were identified (98%) as Nitrosomonas sp. Band A11 was identified (99%) as Nitrosomonas eutropha, which has been reported to be a special AOB in aerobic environments and has a capacity for autotrophic denitrification.26 Band A9 was 99% similar to an uncultured Nitrosospira sp. Band A10 was identified (100%) as Nitrosospira multiformis. Nitrosospira is a common AOB genus that can compose nitrite reductase and NO oxidoreductase. These enzymes can both catalyze nitrite to N2O.27–29
Period I | Period II | Period III | ||||||||
---|---|---|---|---|---|---|---|---|---|---|
WTF | GTF | STF | WTF | GTF | STF | WTF | GTF | STF | ||
NH4+-N | Volume loading (g m−3 d−1) | 32.79 | 85.03 | 136.35 | ||||||
Influent (mg L−1) | 192.86 | 550.17 | 802.08 | |||||||
Effluent (mg L−1) | 29.90 | 58.24 | 29.21 | 83.84 | 164.14 | 80.94 | 400.00 | 413.58 | 342.33 | |
Removal (%) | 84.50 | 69.80 | 84.86 | 83.24 | 67.18 | 83.82 | 50.13 | 48.44 | 57.32 | |
Load removal (g m−3 d−1) | 27.71 | 22.89 | 27.83 | 70.78 | 57.12 | 71.27 | 68.35 | 66.05 | 78.16 | |
TN | Volume loading (g m−3 d−1) | 33.67 | 85.64 | 137.25 | ||||||
Influent (mg L−1) | 198.05 | 503.76 | 807.33 | |||||||
Effluent (mg L−1) | 122.63 | 159.97 | 120.09 | 339.33 | 392.62 | 292.93 | 597.02 | 615.14 | 517.88 | |
Removal (%) | 38.08 | 19.23 | 39.36 | 32.64 | 22.06 | 41.85 | 26.05 | 23.81 | 35.85 | |
Load removal (g m−3 d−1) | 12.82 | 6.47 | 13.25 | 27.95 | 18.89 | 35.84 | 35.75 | 32.68 | 49.20 | |
COD | Volume loading (g m−3 d−1) | 30.76 | 49.83 | 86.51 | ||||||
Influent (mg L−1) | 180.92 | 293.13 | 508.89 | |||||||
Effluent (mg L−1) | 160.97 | 117.43 | 173.86 | 163.46 | 170.87 | 229.53 | 200.67 | 202.82 | 256.68 | |
Removal (%) | 11.03 | 35.09 | 3.90 | 44.24 | 41.71 | 21.70 | 60.57 | 60.14 | 49.56 | |
Load removal (g m−3 d−1) | 3.39 | 10.79 | 1.20 | 22.04 | 20.78 | 10.81 | 52.40 | 52.03 | 42.87 | |
Influent COD/TN | 0.94 | 0.59 | 0.63 | |||||||
Average effluent NO2−-N | 2.10 | 11.70 | 2.50 | 14.10 | 21.10 | 31.00 | 13.00 | 32.30 | 58.60 | |
Average effluent NO3−-N | 90.60 | 90.00 | 88.40 | 241.40 | 207.30 | 181.00 | 169.30 | 182.20 | 116.80 | |
Removal COD/TN | 0.26 | 1.67 | 0.09 | 0.79 | 1.10 | 0.31 | 1.46 | 1.59 | 0.87 |
In a biochemical system, nitrification is carried out by AOBs, whereby their abundance has a primary impact on the NH4+-N removal capacity. The abundance of the AOBs was indicated by the brightness of bands A1, A2, and A4 in the lanes of the three TFs, which showed that the abundance of Nitrosomonas was similar in the three reactors. However, bands A8, A9, A10, and A11 in the STF somewhat brighter than those of the WTF and much brighter than those of the GTF. The abundance of Nitrosospira in the WTF and STF was greater than that in the GTF. This demonstrates that the soil layer in the STF was a more suitable micro-environment for the growth of AOBs, and thus more suitable for increasing their abundance and activity. There were two reasons for the higher NH4+-N removal and greater abundance of AOBs. The mixed microbes and cellulose formed a biofilm as woodchips were decomposed in the WTF, and the soil layer further extended the appositional growth of the AOBs in the STF. Moreover, the soil layer could impede the transfer of oxygen in the STF, although this increased the ammonia concentration gradient to protect the AOBs in the soil layer against free-ammonia inhabitation, which may have led the better performance of the STF for NH4+-N removal.
The accumulation of nitrite in the effluents (Table 2) of the STF and WTF was similar in period I (2.5 mg L−1 and 2.1 mg L−1), whereas this was 31.0 mg L−1 and 58.6 mg L−1 in the STF during in period II and III, respectively, which were much higher in comparison to the WTF. This demonstrates that there was a much stronger “short-cut” nitrification in the STF. This may have been due to the DO gradient in the soil layer of the STF, which strengthened the anaerobic micro-environment on the surface of the filter material. Band A3 of anaerobic bacteria (Clostridiales) in the lane of the STF was brighter than that of the other two TFs, which suggests that the anaerobic micro-environment was relatively higher in the STF. It is known that NOB are more sensitive than AOB to low DO environments,30,31 and such a lack of DO could decrease the activity of NOB.
Overall, the STF had a slightly higher ammonia oxidizing capacity in comparison to the WTF; however, the STF also had a much higher nitrite accumulation. This demonstrates that wrapping the soil on to the woodchips did not impact the ammonia oxidization, and “short-cut” nitrification was easily realized.
In terms of heterotrophic denitrification, the STF had better anaerobic conditions because the woodchips were wrapped by the soil layer. This could have advanced the decomposition of the woodchips, thus increasing the carbon resources for heterotrophic denitrification, which is supported by the high COD in the effluent of the STF. Moreover, the high accumulation of nitrite in the STF indicates that there should have been a strong “short-cut” nitrification, in which nitrite could directly converted to N2 and the carbon resources used for nitrate denitrification could be decreased. This was, therefore, very beneficial for the swine-wastewater digested liquid with a low COD/TN ratio.
Some autotrophic nitrogen removal processes have been observed in wastewater treatment, for example, ANAMMOX. This requires the coexistence of nitrite accumulation and an anaerobic environment in a nitrification reactor.6,34–36 The STF in this study satisfied this requirement; hence, ANAMMOX may have occurred to a certain extent. Besides, some autotrophic nitrogen removal has been ascertained, for example, earlier research found that some AOBs could oxidize NH4+-N to N2O in a low DO environment.26
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