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Article

Application of the Anammox Process for Treatment of Liquid Phase Digestate

by
Joanna Majtacz
,
Dominika Grubba
* and
Krzysztof Czerwionka
Faculty of Civil and Environmental Engineering, Gdansk University of Technology, Narutowicza Street 11/12, 80-233 Gdansk, Poland
*
Author to whom correspondence should be addressed.
Water 2020, 12(11), 2965; https://doi.org/10.3390/w12112965
Submission received: 11 September 2020 / Revised: 12 October 2020 / Accepted: 14 October 2020 / Published: 22 October 2020
(This article belongs to the Special Issue Sewage Sludge Treatment and Reuse)
Browse Figures
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Abstract

:
The liquid phase of the digestate (LPD) contains a relatively high concentration of nitrogen, with total ammonium nitrogen being the dominant form of nitrogen, as well as other essential nutrients such as phosphorus and potassium. Consequently, it must be treated before it is released into the environment. However, there are no reports of co-purification of LPD in the anammox process in sequencing batch reactor with granular sludge, which is a novelty for the presented research. The main objective of this paper is to assess the possibility of nitrogen removal in the anammox process with LPD from biogas plants conducting the co-fermentation process along with the participation of agricultural products (cattle slurry). This publication presents the research results of the efficiency of the anammox process, accounting for the effect of dissolved organic matter. The conducted experiments revealed the potential of LPD purification, which co-ferments waste activated sludge and bovine slurry for the anammox process. In the reactor ammonium utilization rate (AUR) process with LPD addition increased from 2.3 mg N/(g VSS∙h) with 0.5% LPD addition to 8.5 mg N/(g VSS∙h) with 7.5% LPD addition. SAA in the reactor with LPD addition increased from 5.3 mg N/(g VSS∙h) with 0.5% LPD addition to 18.5 mg N/(g VSS∙h) with 4 and 5% LPD addition. With the addition of 7.5% LPD, SAA dropped to a value of 18.1 mg N/(g VSS∙h) in the LPD reactor.

1. Introduction

The anammox process is the biological process of ammonium nitrogen (NH4-N) oxidation under anaerobic conditions to gaseous nitrogen (N2), where the electron acceptor is nitrite nitrogen (NO2-N), and the bacteria responsible for this process are anaerobic ammonia oxidizing bacteria (AAOB). Until now, the anammox process has been successfully used to treat wastewater with a high NH4-N content [1], such as leachate from landfills [2] or wastewater from pig farming [3].
The efficiency of the anammox process is influenced by many factors such as temperature, pH, the method of aeration, and the C/N ratio. Higher concentrations of chemical oxygen demand (COD) can lead to denitrification, in which the remaining nitrate nitrogen (NO3-N) can be converted to gaseous nitrogen (N2). However, excessive COD concentrations increase the proliferation of heterotrophic bacteria that compete for NO2-N with AAOB [4].
It has been shown that with a high enough concentration of sludge and increasing the rate of influent COD/N, anammox can coexist with some heterotrophic bacteria. Literature describes a mixed system based on anammox, in which denitrification consumes COD, anammox produces NO3-N, and in the meantime provides NO2-N for anammox [5,6]. However, the rapid growth of denitrifying bacteria and cell growth is the main threat [7]. It is necessary to ensure appropriate conditions for carrying out both processes simultaneously, which is a challenge.
The research of Pijuan et al. [8] indicated that the presence of a denitrifying community in the biocenosis carry out the anammox process. This community was able to absorb COD using NO3-N and NO2-N as electron acceptors. The activity of anammox was not suppressed by the addition of COD, as the presence of COD did not result in an increase in NH4-N concentration at the end of the tests. The long-term addition of COD resulted in a decrease in anammox activity and a shift in the microbial community, with a decrease in the anammox fraction. Despite this, the anammox process was never lost and was fully recovered after the COD addition was stopped.
Moreover, a study by Qin et al. [9] also showed that a higher concentration of organic compounds (glucose) in the reactor inhibits the sludge’s anammox activity and reduces the rate of NH4-N removal. However, when the NO2-N substrate was sufficient, and the glucose concentration was low, the inhibition of anammox activity was slowed. In the study by Chen et al. [10], when COD concentration in the feed was lower than 99.7 mg/dm3, nitrogen removal could be increased by the combination of denitrification and anammox. Increased COD negatively affects the activity of anammox with almost complete inhibition at COD concentration of 284.1 mg/dm3. However, the process was recovered by changing the COD/TN ratio from 2.33 to 1.25 after adding the NO2-N feed. Until now, research was based mainly on the C/N effect in the anammox process [11,12,13], not strictly the influence of COD concentration on NH4-N oxidation at constant C/N.
The digestate is a by-product of anaerobic digestion of biodegradable materials in biogas plants [14]. It is black in color due to the content of sulphides and humic substances. It can be divided into a solid and liquid phase [15]. The solid fraction can be incinerated, composted or used to fertilize agricultural crops. It is important to reduce hydration in the latter case, as it lowers the cost of transport thus enabling processing in greater distances from biogas plants and contributing to reduced negative effects of “over-fertilization”. The liquid phase of the digestate (LPD) contains a relatively high concentration of nitrogen, with total ammonium nitrogen being the dominant form, as well as other essential nutrients such as phosphorus and potassium [16,17,18]. Consequently, it must be treated before it is discharged into the environment.
The main method of managing LPD is the direct application to agricultural land as fertilizer, however in EU countries, the Nitrates Directive (91/676/EEC) protects land and surface waters from nitrate contamination by limiting the amount of LPD that can be applied to soil [19].
There are also solutions that reintroduce LPD into an anaerobic digestion chamber [20]. In some cases, LPD is treated as wastewater when its nutrients cannot be effectively used in the environment [15]. This increases the nitrogenous load in the wastewater treatment plant, which contributes to higher aeration costs. However, there are no reports of co-purification of LPD in the process of anaerobic oxidation of ammonium nitrogen (NH4-N)—anammox in sequencing batch reactor (SBR) with granular sludge, which is a novelty of this research. Due to the fact that LPDs are characterized by a relatively high COD content after the methane fermentation process, their co-purification in the anammox process seems to be a challenge.
Previous experiments have shown the potential of LPD in the deammonification process [21]. However, the proportion of LPD in the feed solution should be determined individually for each type of substrate after previous COD concentrations are analyzed. Stable deammonification efficiency was obtained for the C/N ratio of 1:1. It was decided to check the influence of LPD from the biogas plant on the anammox process itself, which is a component of the deammonification process.
The main objective of the presented research is to assess the possibility of nitrogen removal in the anammox process with LPD from biogas plants conducting the co-fermentation process with agricultural products (cattle slurry). The publication presents the the research results on the efficiency of the anammox process, taking into account the effect of the dissolved organic matter fraction. For this reason, tests with the addition of sodium acetate (i.e., a fully soluble and easily biodegradable organic compound) are the benchmark.

2. Materials and Methods

2.1. Laboratory Setup

The inoculated biomass originated from a full-scale side-stream deammonification system in Plettenberg, Germany.
The laboratory scale system used in this study consisted of one 10 dm3 SBR in the deammonification mode and three batch reactors in the anammox mode laid out according to the scheme in Figure 1. The SBR was equipped with a thermostatic jacket maintaining a constant temperature in the range of −35 to +200 °C with an accuracy of ±0.1 °C. The main reactor metered service probes were placed to measure pH (Endress + Hauser EH CPS 471D-7211, Switzerland) and measure dissolved oxygen (Endress + Hauser COS22D-10P3/O, Germany).
All measured data from the SBR was transmitted to the programmable logic controller (PLC), which were used for control and regulation. Measurement data was sent to an application called Intouch’a.

2.2. Operational Conditions

(a)  The Main Reactor SBR in the Deammonification Mode
The granular sludge was adapted to the deammonification process for 90 days in the SBR. During the entire test period, the SBR was operated at a constant temperature of 30 ± 1 °C. The pH was controlled in the range of 7.5–7.8 by the automatic addition of 4 M sodium hydroxide (NaOH). The concentration of dissolved oxygen (DO) in SBR was maintained at the level of 0.7 ± 1 mg/dm3. Synthetic wastewater was used to supply SBR prepared according to Dapena-Mora et al. [22], but with the addition of COD (in the form of sodium acetate-C2H3NaO2). After each batch reactor’s test, a 14-day adaptation to increase COD initial concentrations (in the form of C2H3NaO2) was performed in SBR according to Table 1.
(b)  The Batch Reactors in the Anammox Mode
Three batch reactors (R1, R2, R3) worked in anammox mode. Sludge was collected from the main SBR reactor for each test and divided into three batch reactors. Synthetic wastewater was used to supply each batch reactor prepared according to Dapena-Mora et al. [22], but with the addition of COD from LPD (R1) and C2H3NaO2 (R2). Temperature and pH were not controlled. An increasingly greater proportion of the LPD was added to R1 in 7 tests according to Table 1. COD in the form of C2H3NaO2 was added to R2 at the same concentration as in R1, to compare the different COD sources in the reactors and study the effect of the unknown compounds in the effluents in R1. Both R1 and R2 were maintained at a C/N ratio of 1 throughout the test period. NO2-N was added to each of the reactor batch in a precise amount so as to meet the optimal conditions for the anammox process (ratio 1:3 NO2-N/NH4-N). The same concentration of NH4-N and NO2-N was maintained in R3 as in R1 and R2, without the addition of COD, in order to check the effect of COD on the anammox process. The NH4-N, NO2-N and COD concentrations at the beginning of each test are shown in Table 1.

2.3. Characteristics of the Digestate

The digestate was obtained during the tests of the methane co-fermentation process carried out on a laboratory scale in reactors with a volume of 44 L. Reactors operated in batch mode. The initial feed was 20% inoculum, in the form of sludge, from the municipal sewage treatment plant fermentation chambers in Warsaw (Poland) and 80% substrate. In the analyzed studies, the substrate included waste activated sludge from the municipal sewage treatment plant in Warsaw and cattle slurry in the proportion of 1:3 (as wet mass of substrates). During the first two days, the feed hydrolysis was carried out at a temperature of approximately 30 °C. Then, for 28 days, the main fermentation process was carried out at a temperature of about 38 °C. The initial pH in the fermentor was adjusted to approximately pH 7. A more detailed description of the fermentation was presented in the previous publication [23].
After the fermentation process was completed, the digestate was separated into a solid and liquid fraction using a Jouan C3i laboratory centrifuge. A centrifugation speed of 4000 rpm, characteristic for the operation of industrial centrifuges, was adopted. The spin time was 30 min. The liquid fraction was then filtered through a 0.45 µm filter to separate the slurry fraction. Liquid fraction of digestates containing pollutants only, in the form of dissolved fractions, were used for the tests. The characteristics of the digestate and LPD are presented in Table 2. A detailed analysis of the nitrogen and phosphorus content in the liquid fraction of the digestate was presented in a previous publication [23].

2.4. Analytical Methods

The concentration of COD, NO3-N, NO2-N, NH4-N compounds were determined using a spectrophotometer, DR 3900 using cuvette tests from Hach Lange GmbH (Dusseldorf, Germany) for this type of analysis. High-temperature mineralizer was used for COD analysis. The device was equipped with twelve pockets for tested samples. It reached a maximum operating temperature of 170 °C and the complete cooling time of the test sample was about 40–45 min.
The biomass concentrations, were determined as a volatile suspended solids (VSS) fraction of the total suspended solids (TSS) in accordance to Standard Methods [24]. The biomass specific ammonium utilization rate (AUR), specific anammox activity (SAA), and nitrate production rate (NPR) were determined based on the maximum slope of NH4-N consumption, NH4-N together with NO2-N consumption, and NO3-N production in the reaction phase divided into MLVSS concentration, respectively.

3. Results and Discussion

During the tests, an increase in the speed of the AUR and SAA processes were observed in all batch reactors, as shown in Figure 2a,b. Miao et al. [25] also reported in their research that the activity of anammox increased with an increase in the C/N ratio. As the C/N ratio increased from 1.1 to 2, the improvement in nitrogen removal was attributed to increased AAOB counts.
The AUR value in the R1 increased from 2.3 mg N/(g VSS∙h) in the 1st test to 8.5 mg N/(g VSS∙h) in the 7th test. However, this ratio was the lowest when compared to R2 and R3. In R2, this rate increased from 3 mg N/(g VSS∙h) in the 1st test to 9 mg N/(g VSS∙h) in the 7th test. On the other hand, in R3, AUR increased from 3.3 mg N/(g VSS∙h) in the 2nd test to 14 mg N/(g VSS∙h) in the 7th test.
Figure 2b shows that in R3-SAA increased. This was due to the adaptation of AAOB and the fact that AAOB prefer high concentrations of NH4-N, and its concentration increased in subsequent tests (NH4-N was added in each reactor with the same concentration to keep C/N = 1 with increasing COD concentration, NH4-N concentration in the reactor increased). In R1 and R2 with COD in 5%, SAA was stabilized, which was probably due to the growing share of organic compounds in COD.
SAA in R1 increased from 5.3 mg N/(g VSS∙h) in the 1st test to 18.5 mg N/(g VSS∙h) in the 5th and 6th tests. In the 7th test, the SAA dropped to the value of 18.1 mg N/(g VSS∙h).
In the R2, SAA increased from 7.8 mg N/(g VSS∙h) in the 2nd test to 23.9 mg N/(g VSS∙h) in the 5th test. The SAA then decreased to 20.3 mg N/(g VSS∙h) in the 7th test.
The literature reports that high concentrations of COD suppresses anammox activity and that concentrations of COD up to 297 mg/dm3 can completely inhibit AAOB [26]. In our study, despite the addition of COD 329 mg/dm3 in the 7th test, there was no inhibition of AAOB due to the C/N ratio being equal to 1. On the other hand, the addition of acetate can be used by AAOB to remove NO3-N [27].
In R3, SAA increased from the value of 8.9 mg N/(g VSS∙h) in the 2nd test, while in the 7th test it was the highest and amounted to 26.3 mg N/(g VSS∙h).
In reactors with effluents containing organic compounds expressed in COD (both LPD and acetates), the SAA reached its maximum value in the 5th test. The higher the COD concentration, the more SAA decreased. On the other hand, in R3, SAA continued to grow.
Therefore, it can be seen that COD has a negative effect on the anammox process. Due to the similar trend in both R1 and R2, it can be concluded that the effect on SAA reduction is mainly due to the presence of COD.
This is also confirmed in the literature, which states that high concentrations of COD inhibit the activity of anammox, which could be caused by two potential pathways [12]. The first is “inhibition of competition” and the second is “inhibition of the conversion of the metabolic pathway” [28]. The first relates to competition of heterotrophic bacteria with AAOB for nutrients at high concentrations of COD, however heterotrophic bacteria grow faster than AAOB, as a result the proportion of AAOB is reduced or completely eliminated, which reduced their activity [29]. However, the anammox process restricted at high COD concentrations due to the growth of heterotrophic bacteria is reversible [30]. The second route focuses on dominant AAOBs that metabolize to organic carbon instead of NH4-N and NO2-N, leading to lower activity and reduced nitrogen removal efficiency [31].
Molinuevo et al. [26] report that AAOB compete with denitrifying bacteria when the C/N ratio > 1. AAOB can survive in laboratory reactors and wastewater treatment plants when the C/N ranges from 0.5–2.8 [32,33,34], with varying NH4-N removal efficiency (50–96%). Other sources say that at a C/N ratio of 0.5–0.8, the medium is dominated by autotrophic microorganisms [35,36], while at a C/N ratio in the range of 1–1.4 anammox and denitrification occur simultaneously, which is indicated for simultaneous anammox and denitrification (SAD) [37]. Based on the above reports, our C/N ratio of 1 seems to be appropriate for the anammox process.
NPR in all batch reactors were the highest on the first days of the research (see Figure 3a). This is due to the fact that such low concentrations of NH4-N and NO2-N meant that the majority of processes occurred with full nitrification. This situation is also confirmed by the fact that with the addition of 0.5 and 1% LPD, the highest ratio of NPR/AUR was achieved (see: Figure 3b).
In the 3rd test it can be seen that the NPR has dropped below 0. This may possibly be due to the use of COD compounds for denitritation. The concentration of COD compounds was so low that they did not interfere with nitrification or anammox, but also allowed the reduction of NO3-N. Compounds in synthetic effluents are the most bioavailable for denitrification and were the preferred carbon source because NPR was the lowest and the highest reduction in NO3-N concentration.
On the other hand, above 5% LPD in the reactor, it can also be seen that the NPR is higher (i.e., the greater part of the compounds are oxidized by the bacteria of the second nitrification phase—NOB)—the production of NO3-N confirms this. Moreover, above 5% LPD in R1 and R2, the NO2-N/NH4-N ratio increases during the test and it confirms the theory that part of NH4-N oxidation is caused by NOB bacteria (NO2-N does not decrease slower), in other words adding COD reduces the SAA.
Table S1 (Supplementary Data) summarizes the AUR, NPR, SAA rates and the NPR/AUR ratio achieved.
It is also worth paying attention to the time needed for the complete oxidation of NH4-N in R1. When the LPD addition was 1%, NH4-N was completely oxidized in 1.5 h. When the LPD addition was 3%, NH4-N was completely oxidized in 3 h, and when the LPD addition was 7.5%, NH4-N was completely oxidized in 6 h. Thus, it turns out that the reaction time increases with the increase in proportion of digestate added (see Figure 4a). This is also indicated by the decrease in NO2-N concentration in individual cases (see Figure 4b) and is due to the increased amount of NH4-N needed to be oxidized.

4. Conclusions

The conducted experiments revealed the potential of LPD purification, which co-ferments waste activated sludge and bovine slurry for the anammox process. AUR and SAA increase in subsequent tests for each of the three reactors, but the most favorable values were obtained for R3, which indicates that COD does not cause competition of heterotrophic bacteria for NO2-N, as is the case in R1 and R2. The AUR in R1 is lower than in R2 due to the possible presence of inhibitory substances contained in LPD, which are not well understood at the moment. Future research is planned to identify them. The addition of COD resulted in a negative NPR value with an initial COD concentration of 90 mg COD/dm3, which indicates heterotrophic denitrification in this period. The increase in NPR value in subsequent tests at higher substrate concentrations proves the advantage of AAOB over denitrifying bacteria. It was indicated in the study that the increased proportion of LPD in the anammox process also extended the time needed to oxidize NH4-N.

Supplementary Materials

The following are available online at https://www.mdpi.com/2073-4441/12/11/2965/s1, Table S1: AUR, NPR, SAA rates and the NPR/AUR ratio achieved.

Author Contributions

Conceptualization, D.G. and J.M.; methodology, J.M. and K.C.; software, J.M.; validation, K.C.; formal analysis, K.C.; investigation, D.G. and J.M.; resources, K.C.; data curation, J.M.; writing—original draft preparation, D.G. and J.M.; writing—review and editing, K.C.; visualization, D.G.; supervision, K.C.; project administration, D.G.; funding acquisition, K.C. All authors have read and agreed to the published version of the manuscript.

Funding

This research was funded by European Regional Development Fund within the framework of Smart Growth Operational Programme 2014-2020 grant number POIR.04.01.02-00-0022/17.

Conflicts of Interest

The authors declare no conflict of interest.

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Water 12 02965 g001 550
Figure 1. Scheme of the laboratory system.
Figure 1. Scheme of the laboratory system.
Water 12 02965 g001
Water 12 02965 g002 550
Figure 2. Values of (a) AUR (b) SAA for anammox process carried out with LPD addition, with synthetic effluents with COD and with synthetic effluents without COD.
Figure 2. Values of (a) AUR (b) SAA for anammox process carried out with LPD addition, with synthetic effluents with COD and with synthetic effluents without COD.
Water 12 02965 g002
Water 12 02965 g003 550
Figure 3. Values of (a) NPR (b) NPR/AUR for anammox process carried out with LPD addition, with synthetic effluents with COD and with synthetic effluents without COD.
Figure 3. Values of (a) NPR (b) NPR/AUR for anammox process carried out with LPD addition, with synthetic effluents with COD and with synthetic effluents without COD.
Water 12 02965 g003
Water 12 02965 g004 550
Figure 4. Concentration values of (a) NH4-N (b) NO2-N for the process carried out with 1%, 3% and 7.5% digestate leachate.
Figure 4. Concentration values of (a) NH4-N (b) NO2-N for the process carried out with 1%, 3% and 7.5% digestate leachate.
Water 12 02965 g004
Table
Table 1. Characteristics of tests.
Table 1. Characteristics of tests.
DaySBR in Deammonification ModeBatch Reactors
Description of Activities in Batch ReactorsR1 (with COD from LPD)R2 (with COD from C2H3NaO2)R3 (without COD)
Description of ActivitiesNH4-N Initial ConcentrationCOD Initial Concentration from C2H3NaO2Percentage of LPDin the ReactorVolume of LPDin the ReactorNH4-N Initial ConcentrationNO2-N Initial ConcentrationCOD Initial ConcentrationNH4-N Initial ConcentrationNO2-N Initial ConcentrationCOD Initial ConcentrationNH4-N Initial ConcentrationNO2-N Concentration
- m g   N   d m 3 m g   C O D   d m 3 -%dm3 m g   N   d m 3 m g   N   d m 3 m g   C O D   d m 3 m g   N   d m 3 m g   N   d m 3 m g   C O D   d m 3 m g   N   d m 3 m g   N   d m 3
0–90Adaptation for the deammonification process400No research
91No researchTest 10.50.151013221013221013
92–106Adaptation for the deammonification process3030No research
107No researchTest 210.032026452026452026
108–122Adaptation for the deammonification process4545No research
123No researchTest 320.064052904052904052
124–136Adaptation for the deammonification process9090No research
137No researchTest 430.09607813860781386078
138–152Adaptation for the deammonification process138138No research
153No researchTest 540.12801041808010418080104
154–168Adaptation for the deammonification process180180No research
169No researchTest 650.6100130225100130225100130
169–183Adaptation for the deammonification process225225No research
184No researchTest 77.50.225145190337.5150195337.5150195
Table
Table 2. Characteristics of the digestate and LPD.
Table 2. Characteristics of the digestate and LPD.
CompoundUnitConcentration in the DigestateConcentration in the LPD (SD)
TNmg N/dm331212627.7 (255.2)
TNfmg N/dm3n.a.1788.2 (113.8)
CODmg O2/dm3364007650 (739.9)
CODfmg O2/dm3n.a.2590 (197.5)
NH4-Nmg N/dm3n.a.1546.7 (36.9)
TPmg P/dm31075n.a.
Norgmg N/dm3n.a.1081 (223.3)
Norgfmg N/dm3n.a.241.5 (80.5)
TSS%4.13n.a.
VSS%53.27n.a.
TN-total nitrogen without filtration, TNf-total nitrogen after filtration, COD-chemical oxygen demand without filtration, CODf-chemical oxygen demand with filtration, TP-total phosphorus, Norg-organic nitrogen without filtration, Norgf-organic nitrogen with filtration, TSS-total suspended solids, VSS- volatile suspended solids, SD-standard deviation, n.a.-not applicable.
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Majtacz, J.; Grubba, D.; Czerwionka, K. Application of the Anammox Process for Treatment of Liquid Phase Digestate. Water 2020, 12, 2965. https://doi.org/10.3390/w12112965

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Majtacz J, Grubba D, Czerwionka K. Application of the Anammox Process for Treatment of Liquid Phase Digestate. Water. 2020; 12(11):2965. https://doi.org/10.3390/w12112965

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Majtacz, Joanna, Dominika Grubba, and Krzysztof Czerwionka. 2020. "Application of the Anammox Process for Treatment of Liquid Phase Digestate" Water 12, no. 11: 2965. https://doi.org/10.3390/w12112965

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