Ex-situ biogas upgrading to methane and removal of VOCs in a system of zero valent iron and anaerobic granular sludge

doi:10.21203/rs.3.rs-546207/v1

Download PDF

Research Article

Ex-situ biogas upgrading to methane and removal of VOCs in a system of zero valent iron and anaerobic granular sludge

https://doi.org/10.21203/rs.3.rs-546207/v1

This work is licensed under a CC BY 4.0 License

Version 1

posted

You are reading this latest preprint version

In the current study, a novel process of ex-situ biogas upgrading to biomethane is presented which is based on a system consisted of anaerobic sludge and zero valent iron (ZVI). The ZVI when is added in an aquatic system with anaerobic granular sludge generates H₂ under anaerobic abiotic conditions. Then, the H₂ and CO₂ are converted by the hydrogenotrophic methanogens to CH₄. Biogas upgrading to biomethane was achieved in 4 days in a system of anaerobic granular sludge, 50 g L¹ ZVI initial pH 5 and 20 g L¹ NaHCO₃. In this system when zero valent scrap iron (ZVSI) was added instead of ZVI required longer period (21 days) to achieve biogas upgrading. Volatile organic compounds (VOCs) analysis in raw biogas (in system of anaerobic sludge and ZVI) showed mainly the reduction of low mass straight- and branched-chain alkanes (C₆-C₁₀); however, no other particular trend regarding the removal of other VOCs was observed. H₂S and NH₃ were found to be substantially reduced, when the anaerobic sludge was exposed to ZVI compared to no decrease in serum bottles free of ZVI.

Environmental Engineering

Environmental Policy

anaerobic granular sludge

biogas upgrading

hydrogenotrophic methanogens

zero valent iron

volatile organic compounds (VOCs)

H2S removal

Biogas upgrading to biomethane not only significantly increases its calorific value, but also enables biomethane to be transported and utilized far from the anaerobic digester (Muñoz et al. 2015). Therefore, there is growing interest for biogas upgrading technologies as they can be applied closed to an anaerobic digester. Up to date, most commercial technologies used for biogas upgrading are mainly based on physicochemical processes; however, these technologies are energy intensive and present a high operational cost (Sun et al. 2015). Recently, several studies (Sun et al. 2015; Angelidaki et al. 2018) proposed an alternative option for biogas upgrading based on the injection of H₂ and the utilization of CO₂ and H₂ by hydrogenotrophic methanogens according to Eq. (1).

At this process, H₂ needs to be produced by an external source using water electrolysis that can be generated from renewable energies (solar or wind energy) (Muñoz et al. 2015; Angelidaki et al. 2018). The addition of H₂ can take place in-situ, in which H₂ is delivered inside the liquid phase of a biogas reactor or ex-situ in which CO₂ from external sources and H₂ are injected inside the liquid phase of a reactor containing hydrogenotrophic methanogens (Angelidaki et al. 2018; Angenent et al. 2018). Towards this, several challenges of this system exist; the low gas-liquid mass transfer rate of H₂, which limits its availability for methanogens and therefore the gas recirculation flow rate and reactor design are considered key factors for the successful biogas upgrading process (Bassani et al. 2016), as well as the relatively high cost of electrolysis (Schiebahn et al. 2015; Angenent et al. 2018).

In recent studies (Vyrides et al. 2018; Menikea et al. 2020), it was showed that CO₂ as a sole carbon source can be converted to CH₄ in a system consisted of anaerobic granular sludge (AnGrSl), zero valent iron (ZVI) and zero valent scrap iron (ZVSI), respectively. Under anaerobic aquatic condition, ZVI released H₂ and oxidized according to Eq. (2) (Menikea et al. 2020)

The Gibbs free energy changes ΔG⁰ of Equation 1 in standard conditions (pH 0, all concentrations 1 M and all partial pressures 1 atm) to -79.9 kJ mol^-1, whereas at pH 7 ΔG⁰ is −39.9 kJ mol^-1.

Then, the H₂ from abiotic oxidation of ZVI and the CO₂ is utilized by hydrogenotrophic methanogens according to Eq. 1 for the generation of CH₄.

Until today, this system (mix anaerobic sludge and ZVI) was tested for CO₂ conversion to CH₄ and (Vyrides et al. 2018; Menikea et al. 2020) it was not examined for ex-situ biogas upgrading under a semi-batch system. Apart from this, the use of ZVI can potentially contribute to the potential removal of volatile organic compounds (VOCs); a parameter that was also examined in the current study.

Some VOCs present low odor thresholds and even at trace levels can contribute to unpleasant smells for workers and for people who live nearby wastewater treatment plants (WWTPs). Many types of VOCs are toxic or even hazardous to humans and can be detrimental to the environment. In addition, low concentrations (ppb_vlevels) of volatile sulfur compounds (VSCs) can also impact to human health causing headaches and nausea, as well as eye, respiratory, and neuropsychological symptoms (Andersson et al. 2004). They can also cause operational problems by corroding the respective equipment (e.g., compressors and pipes) used for certain tasks, such as for upgrading and cleaning the gas (Andersson et al. 2004).

Apart from VOCs, biogas often contains hydrogen sulfide (H₂S), which can severely limit its application as it is related with harmful environmental emissions and corrodes the engines of biogas purification machinery (Farghali et al. 2020). As was stated in recent studies (Ruan et al. 2017; Andriamanohiarisoamanana et al. 2018; Wei et al. 2018; Farghali et al. 2020), ZVSI could also help to prevent the emissions of H₂S via iron-sulfide (FeS) precipitation. Based on these findings, this study will examine the ex-situ biogas upgrading and H₂S removal in the same system.

The scope of this study is to examine a new proof of concept for the simultaneous ex-situ biogas upgrading to biomethane and also to examine the potential removal of VOCs, as well as NH₃ and H₂S, using an aquatic system of ZVI and anaerobic granular sludge (AnGrSl).

2.1. Biogas sources

The following sources of biogas were used:

a) A Synthetic biogas (Linde - Hadjikyriakos Gas Ltd; Cyprus) 60% CH₄ and 40% CO₂ was used at serum bottle experiments and on feeding laboratory bioreactor on day 17.

b) Raw biogas produced from a pilot anaerobic digester that was treating with food waste and operated at Moni municipal WWTP (Limassol, Cyprus) was employed. The biogas was collected using Tedlar® gas inspecting bags with Thermogreen® LB-2 septa (1L, Supelco) sampled from Moni, Limassol. The raw biogas fed laboratory batch reactor on days 1, 8 and 28. Raw biogas composition was 59 +1.5 CH₄ % and 41 + 1.5 CO₂ %, respectively

2.2 Serum bottle experiments

Serum bottle anaerobic experiments were conducted in 125 mL serum bottles with a working volume of 80 mL. The anaerobic granular sludge (withdrawn from a full scale upflow anaerobic sludge blanket (UASB) reactor) was daily treated with wastewater at pH 6.8–7.3, sieved (1 mm) and washed with distilled water and used as inoculum (2 g of wet weight was added in 80 mL)). The total solids (TS) and volatile solids (VS) of granular sludge were 9.5% (wet basis) and 85.5% (of TS), respectively. ZVI (Iron ≥ 99%, reduced, powder (fine), Sigma Aldrich code 12310) was added in various concentrations of 25 g L¹, 50 g L¹, 75 g L¹, 100 g L¹. ZVSI was obtained from university machinery (lathe machines) and was approximately 2–4.0 mm in width and 0.2–0.5 mm in thickness as described in (Menikea et al. 2020). The ZVSI was added in concentrations of 100 g L¹ and 200 g L¹.

The remaining volume (up to 80 mL) was filled with media (Owen et al., 1979); however, the concentration of NaHCO₃ was increased to 20 g L¹ in order to prevent back pressure in the serum bottle due to the consumption of CO₂ by methanogens and due to absorption of CO₂ from the liquid phase and pH increase.

The pH was monitored (pH meter, Mettler Toledo) by withdrawing around 1 mL from each serum bottle. The pH was also daily adjusted by using 2M HCl or 2M NaOH. In case where no pH adjustment was needed, the equal volume of medium was added in order to maintain the working volume.

For creating anaerobic conditions, synthetic biogas (60% CH₄ and 40% CO₂) was introduced to each serum bottle for 5 min to remove oxygen, and then, the bottles were capped, sealed with butyl septa and aluminium crimps and stirred in a shaking incubator (100 rpm) at 30 ^oC during the experiment. The headspace pressure was initially regulated at 1.5–1.6 atm (the absolute pressure was measured by manometer) in order to avoid back pressure, due to CO₂ consumption and due to 1 mL sampling from the headspace for gas analysis.

The anaerobic batch experiments at various ZVI concentrations were carried out in duplicates (Fig. 1a), whereas the experiments regarding ZVI and ZVSI over time were repeated twice (in duplicates each time) and the standard deviation was calculated. Gaseous samples of various inorganic gases (CH_4, CO₂, H₂, N₂, and O₂) were analysed over time. In every experiment, controls were prepared without addition of ZVI (consisted of granular sludge only) and without addition of AnGrSl consisted only of ZVI.

2.3 Operation of laboratory bioreactor and batch biogas feeding

Semi-batch laboratory experiment took place in a bottle of 500 mL with a working volume of 350 mL and a final concentration of NaHCO₃ (20 g L¹) for 31 days. The bottle was inoculated with 10 g of AnGrSl (wet weight sludge); the ZVI (Iron ≥ 99%, reduced, powder (fine)-Sigma Aldrich CAS Number 7439-89-6 and code 12310) concentration at the bioreactor was 50 g L¹. ZVI was added only once (in the start-up phase) of bioreactor which was operated at 37 ^oC. 200 mL of raw biogas (59% CH₄ and 41% CO₂) was added on days 1, 8 and 28 and 200 mL of synthetic biogas was added on day 17.

2.4. VOCs sampling and analysis

The liquid samples were also analysed for their VOCs evolution using the headspace Solid Phase Microextraction-Gas Chromatography/Mass Spectrometry (HS-SPME-GC-MS) approach. In particular, the SPME 75-µm CAR/PDMS fiber (Supelco, 57344-U) was thermally desorbed in a combined GC/MS (Agilent 7890B/5977B) system. The respective fiber was exposed for 30 min at room temperature over the samples liquid phase and then exposed at the GC inlet (280 ºC) and remained for 1 min to implement the VOCs desorption. The SPB-624 capillary column (60 m × 0.25 mm × 1.4 µm, Supelco) with the help of He (1.7 mL min^− 1) enabled the VOCs separation. The following thermal cycle was set at the chromatographic furnace: 35 °C for 5 min, increasing at a rate of 4 °C min^− 1 up to 180 °C, constant for 20 min. The MS system worked at full scan, in split mode 1:10 and from 35–350 amu. Ion source, quadrupole and transfer line temperatures were stable at 230, 150 and 250 °C, respectively. NIST17 mass spectral library contributed to chromatographic peaks identification, next to a standard solution mixture consisting of 60 VOCs (EPA 524 VOC Mix A, Supelco).

The Area Under Curve (AUC) of dimethyl sulfide (DMS) was used as a reference compound and all detected VOCs were divided by that of DMS, as follows AUC = A_i/A_DMS. If the measured AUC was from 0.1-2 is presented as + in Table 1, from 2.1–10 as + + and higher than 10 as +++. When the respective compound was not detected, then n.d. was placed in the Table 1.

Table 1

VOCs that were detected with HS-SPME-GC-MS in time and the concentrations of H₂S and NH₃ analysed by the respective sensors on day 7.
VOCs	Anaerobic granular (day 2)	Anaerobic granular ZVI (day 2)	Anaerobic granular (day 7)	Anaerobic granular ZVI (day 7)
Alkanes
Pentane	++	++	+	+
2-methyl-Pentane	n.d.	+	++	+++
3-methyl-Pentane	++	++	+++	+++
2,3-dimethyl Pentane	n.d.	n.d.	++	++
n-Hexane	+++	+++	+++	+++
2-methyl-Hexane	+++	+++	++	+++
3-methyl-Hexane	+++	+++	++	+++
2,2,5-trimethyl-Hexane	n.d.	n.d.	+	++
Heptane	+++	+++	++	++
2,5-dimethyl-Heptane	++	++	+	n.d.
3-ethyl-2-methyl-Heptane	++	++	+	n.d.
2,6-dimethyl-Octane	+++	+++	+	n.d.
4-methyl-Octane	++	++	+	n.d.
Octane	+++	+++	++	++
Nonane	+++	+++	+	n.d.
4-methyl-Nonane	++	++	+	n.d.
2-methyl-Nonane	++	++	n.d.	n.d.
4-methyl-Decane	+++	+++	+	n.d.
2,3,8-trimethyl-Decane	n.d.	n.d.	++	++
Undecane	++	++	+	n.d.
3-methyl-Dodecane	+++	+++	n.d.	n.d.
2,6-dimethyl-Undecane	n.d.	n.d.	++	n.d.
methyl-Cyclopentane	++	++	+++	+++
1,1-dimethyl-Cyclopropane	n.d.	+	+	++
Alkenes
2-methyl-1-Propene	++	++	+	++
2,4,4-trimethyl-1-Pentene	+	+	+	++
3,7-dimethyl-2-Octene	+++	+++	++	n.d.
2,6-dimethyl − 4-Octene	+++	+++	+	n.d.
Aromatic hydrocarbons
Benzene	++	++	+	++
1,2,4-trimethyl-Benzene	++	+++	++	++
Toluene	+++	+++	+++	+++
Terpenes
D-Limonene	+++	+++	++	++
.alpha.-Pinene	+++	+++	++	++
beta.-Pinene	+++	+++	++	++
o-Cymene	+++	+++	+++	++
Sulfur compounds
Methanethiol	n.d.	n.d.	+	+
Dimethyl sulfide	n.d.	n.d.	+	+
Carbon disulfide	++	n.d.	+	n.d.
Sensors (ppm_v)
H₂S			82	1
NH₃			266	48
* Values from 0.1-2 are presented as +, 2.1–10 as + + and higher than 10 as +++, whereas n.d. stands for not detected. The respective values of AUC are derived from A_i/A_DMS.

Immediately after the HS-SPME-GC-MS analysis, Dräger X-am 8000 photo ionisation detector (PID) equipped with 4 sensors (H₂S, NH₃, CO₂, O₂), was used for measuring the respective H₂S and NH₃ gaseous emissions.

2.5. Analysis of gas composition

Gas composition of H₂, O₂, N₂, CH₄ and CO₂ from the batch experiments was measured via gas chromatography (Agilent technologies 7820A GC system, Wilmington, DE) coupled to a thermal conductivity detector (GC-TCD), with argon as a carrier gas (as described by Vyrides et al. 2018). The coefficient of variation for 10 identical samples was ± 2%.

3.1. Ex-situ biogas upgrading by anaerobic granular sludge and ZVI

Anaerobic granular sludge (AnGrSl) was independently inoculated with 25, 50, 75 and 100 g L¹ ZVI and fed with synthetic biogas (60% CH₄ and 40% CO₂) at initial pH 6 and 20 g L¹ NaHCO₃ in the media. The headspace after 6 days showed that the exposure to 50 and 75 g L¹ ZVI resulted in 97% CH₄ in the headspace whereas, the exposure to 25 g L¹ and 100 g L¹ ZVI resulted in 85% and 81% CH_4, respectively (Fig. 1a). The CH₄ (%) in the control remained stable after 6 days.

Figure 1b shows the gas composition over time for AnGrSl exposed to 50 and 75 g L¹ ZVI at initial pH 6 and 20 g L¹ NaHCO₃ in the media. For both ZVI concentrations, from the beginning of the experiment until day 2, CO₂ gradually minimized whereas H₂ gradually increased. Then, from day 2 to 7, the H₂ is progressively decreased and the CH₄ steadily increased to 97% for both ZVI concentrations. The initial increase of H₂ is due to abiotic anaerobic oxidation of ZVI whereas, the reduction of H₂ and CO₂ is mainly attributed to hydrogenotrophic methanogens (Eq. 1). Part of the CO₂ was absorbed, solubilized in the media and formed siderite according to Eq. 2. That explains its absence from the headspace after day 2 and the simultaneous generation of CH₄ from the days 2 to 7.

At the next experiment, the initial pH was set to 5 since the lower initial pH can increase the H₂ production rate from ZVI (Menikea et al. 2020). In addition due to ZVI anaerobic oxidation (Eq. 2), the pH rapidly increases up to 8.3 (Vyrides et al. 2018) and therefore the methanogens can function well in the range 6.8–7.8 during the anaerobic ZVI oxidation. At initial pH 5, the following initial concentrations of NaHCO₃ was varied in the media 2.3 g L¹, 20 g L¹, 35 g L¹, and 50 g L¹. As can be seen form Fig. 2a, at serum bottle with 20 g L¹ NaHCO₃ resulted in 95% CH₄ composition after 4 days. At concentrations 35 g L¹, and 50 g L¹ the biogas upgrading took place at a slower rate. This could be due the inhibition of hydrogenotrophic methanogens by sodium (at 35 and 50 g L¹) (Vyrides and Stuckey 2009), as results of H₂ (%) in the headspace at these concentrations are in higher level compared to the serum bottles that the NaHCO₃ concentrations was lower (Fig. 2b). At concentration of 2.3 g L¹, NaHCO₃ a back pressure is created due to simultaneous consumption of CO₂ by methanogens and due to absorption of CO₂ to liquid, when pH increases (Eq. 2); therefore, the optimum concentration for this system was 20 g L¹ NaHCO₃ since no back pressure was formed and the higher production of CH₄ was detected.

Anaerobic bioreactor inoculated with AnGrSl and 50 g L¹ ZVI received real biogas (200 mL each time) at days 1, 8 and 28, as well as synthetic biogas at day 17. As shown in Fig. 3, the bioreactor inoculated with 50 g L¹ ZVI during the first biogas fed-batch increased the CH₄ composition from 63% (day 1) to 75.5% (day 8), whereas the H₂ detected on day 8 was 21%. At the 2nd biogas fed-batch (day 8–17), the CH₄ reached 80.7% (day 15) and then due to increase of N₂ the CH₄ decreased to 75.3%. The increase of N₂ was likely due to the creation of under pressure, because of pH increase to 8.9 and the subsequent CO₂ absorption. On day 17, synthetic biogas was injected and the CH₄ increased from 60% to 92.7% in one day (day 18) and then increased to 95.1% on day 19. On day 28, a raw biogas was injected to bioreactor and the CH₄ composition in the headspace of the bioreactor increased from 67.8% to 90.5% after a day and then reached 94.7% on day 31. Noteworthy, during this period (17–31) the pH raised around 8.5 and then was daily regulated to pH 7.5. Therefore, part of the CO₂ reduction was due to CO₂ adsorption in the media and not due to the consumption by hydrogenotrophic methanogens. In addition, part of the soluble CO₂ formed siderite according to Eq. 2 and previous findings (Menikea et al. 2020).

3.2 Ex-situ biogas upgrading by anaerobic granular at 100 g L¹ and 200 g L¹ zero valent scrap iron

The use of zero valent scrap iron (ZVSI) was also tested in current system as a strategy for synthetic biogas upgrading to biomethane. Figure 4 shows that at inoculation of 100 g L¹ and 200 g L¹ of ZVSI in AnGrSl resulted in CH₄ composition of 90.7% and 95.5%, respectively after 21 days. Interestingly, very little H₂ was detected in the headspace and this could be explained due to the slow release of H₂ by ZVSI followed by immediate consumption of hydrogenotrophic methanogens (Menikea et al. 2020). The longer period for biogas upgrading by ZVSI compared to ZVI (in the presence of AnGrSl) is counterbalance by the lower price of ZVI, which is estimated 5 times lower (Cheng et al. 2020). In a recent study, Charalambous and Vyrides (2020) independently added ZVI and ZVSI in anaerobic sludge for the treatment of cheese whey; they found substantial increase in CH₄ production, biogas upgrading and that ZVI and ZVSI can provide alkalinity in the system. Under these conditions, in a desktop scale study it was found that only ZVSI was economically feasible process for the anaerobic treatment of cheese whey (Charalambous and Vyrides 2020).

3.3. VOCs removal by anaerobic granular and ZVI

Serum bottles inoculated with AnGrSl, 50 g L¹ ZVI and AnGrSl (without ZVI) were fed with raw biogas that was generated from a pilot anaerobic digester treated with food waste and VOCs were analysed on days 2 and 7. The serum bottle in which ZVI was added in AnGrSl upgraded the biogas to approximately 95% CH₄ after 7 days. The inorganic gas composition (CH₄, H₂, CO₂) followed the same trend, as was previously shown at Fig. 1a (using synthetic biogas).

The VOCs analysis over time for samples exposed to ZVI plus anaerobic sludge and anaerobic sludge only are shown at Table 1. These samples were fed with raw biogas from a pilot anaerobic digester fed with food waste. The main VOCs detected can be separated in five main groups: (a) alkanes, (b) alkenes, (c) aromatic hydrocarbons, (d) terpenes and (e) organic sulfur compounds (Table 1). Similar compounds were also detected by other studies (Salazar Gómez et al., 2016; Paolini et al., 2018). The main linear and branched alkanes that were detected were pentane, 3-methyl-pentane, hexane, heptane, methyl-cyclopentane and 3-methyl-dodecane. The main aromatic hydrocarbons that were identified was benzene, tolouene, and 1,2,4-trimethyl-benzene. The key terpene was D-limonene and the main sulfur compounds were DMS and carbon disulfide. The addition of ZVI in AnGrSl reduced mainly the low mass straight-chain and branched alkanes such as heptane, branched heptanes, octane and branched octanes, nonane, branched nonane as well as 3-methyl-dodecane. However, the removal of other VOCs and VSCs has not revealed any particular pattern by this system (AnGrSland ZVI).

Noteworthy, in the first days several compounds were not present in the headspace gas, but as the experiments were in progress more VOCs were released (e.g. 2,2,5-trimethyl-hexane, methanethiol, DMS, see Table 1); this could be attributed to the auto-biodegradation of the anaerobic sludge and the release of these compounds. In addition, these compounds could be initially absorbed from raw biogas in the liquid phase and then were gradually released in the gas phase.

Interestingly, the H₂S and NH₃ were significantly reduced in the serum bottle that anaerobic granular sludge was inoculated with ZVI. This process highlights a great potential for simultaneous biogas upgrading and H₂S removal, however as the analysis of H₂S was performed with an electrochemical sensor, further experiments need to be contacted to verify this. The chromatographs on day 7 for the both conditions can be seen at Figs. 5a and 5b, respectively.

Similar experiment was contacted using ZVSI (200 g L¹) and AnGrSl and the serum bottles were fed with raw biogas. In this experiment, not a particular trend was detected as several of these compounds were decreased, whereas other were increased over time. However, as in the previous experiment with ZVI, using the respective electrochemical sensors, the H₂S and NH₃ were significantly lower for the AnGrSl that ZVSI was added compared to AnGrSl without ZVSI.

The main technologies for biogas upgrading are based on several physicochemical processes such as cryogenic separation, membrane separation, pressure swing adsorption, high-pressure water scrubbing and amine scrubbing. These physicochemical processes are considered very efficient but expensive technologies requiring complex technical equipment and enabled methane losses (Muñoz et al. 2015; Zabranska and Pokorna 2018). In the last decade, it was pointed out that biogas upgrading can also be implemented by power to gas technology using hydrogenotrophic methanogens that convert the CO₂ and externally provided H₂ to CH₄. However, the water electrolysis can increase the operational and capital cost (Schiebahn et al. 2015; Angenent et al. 2018). As a strategy to reduce the operational cost and to increase the efficiency, many studies directly submerged the cathode into the biomethanation system; this system is called microbial electrosynthesis. However, as reported in recent studies (Jiang et al. 2019; Bajracharya 2020; Prévoteau et al. 2020) high capital and operating/maintenance costs and particularly the cost of the proton exchange membrane are the key limitations in the industrialization of microbial electrosynthesis. According to recent review (Fu et al. 2020) biological biogas upgrading by CO₂-to-CH₄ bioconversion depends on an accessible, available, and cost-effective H₂. Despite the environmental benefits currently in situ biological biogas upgrading by bioconversion of CO₂ into4 seems to be more expensive than physicochemical biogas upgrading and more research need to take place for optimization of this process (Fu et al. 2020).

On the other hand, as was shown in this study, using ZVI and anaerobic granular sludge, the biogas can be upgraded to CH₄ without the complicate configuration of electrolysis (electrodes, connection with power supply and proton exchange membrane in case of microbial electrosynthesis). The present proof of concept study, indicates that the addition of ZVI to anaerobic granular sludge, apart from biogas upgrading to biomethane, can substantially decrease H₂S and NH₃, as well. Regarding H₂S removal, this is in line with the findings of other studies (Liu et al. 2015; Ruan et al. 2017; Andriamanohiarisoamanana et al. 2018; Wei et al. 2018; Farghali et al. 2020), whereas the current study also found that the presence of ZVI reduced mainly the low mass straight-chain and branched alkanes.

This is the first laboratory study experimentally demonstrated the ex-situ biogas upgrading under these conditions. Briefly, H₂ generated by the abiotic anaerobic oxidation of ZVI (Eq. 2) and then is consumed along with soluble CO₂ by hydrogenotrophic methanogens for CH₄ production (Eq. 1). However, part of the CO₂ is precipitated as siderite as shown in Eq. 2) (Menikea et al. 2020, Samanides et al. 2020). In addition, homoacetogens can also utilized H₂ and CO₂ however they are supressed by hydrogenotrophic methanogens as was found by Vyrides et al. (2018) in a similar system. Based on the aforementioned reactions, the overall equation of this system shown at Eq. 3 :

4Fe⁽⁰⁾ + CO₂ + 4HCO₃⁻ + 4H⁺ ◊ 4 FeCO₃ + CH₄ + 2H₂O (Eq. 3)

Clearly, further research will be needed regarding the biogas upgrading in this system under operation at continuous mode, demonstration at a larger scale for longer period, as well as performance and economic comparison with power-to-gas technology. Recent studies (Menikea et al., 2020; Samanides et al., 2020), found that under these conditions the main oxidized product in the outer surface from ZVI is siderite. Siderite can decrease the H₂ released from ZVI (Menikea et al., 2020) and this can hinder the sustainability of this process. Based on this, several approaches can be examined to increase the competitiveness of this process such as: (a) the conversion of siderite to ZVI; however, this is not an easy process and considerable amount of energy need to be consumed, (b) the selective removal of the oxidized layer after ZVI and anaerobic sludge separation can be another process for the sustainability of this process, (c) the formation of nano ZVI from plant extract, however, can be used for reducing the capital cost of the process; although this process can be limited due to the formation of mixture of other iron such as iron oxides of iron hydroxides (Mystrioti et al., 2015). The results of this study pointed out that ZVSI can also be used for biogas upgrading; however, this process is approximately 3 times slower compare with the same process using ZVI. Nevertheless, ZVSI is cheaper than ZVI and both factors need to be considered for larger scale studies.

The ex-situ biogas upgrading to biomethane in a system of anaerobic granular sludge and ZVI is exhibited for the first time. The ZVI when is added in an aquatic system with anaerobic granular sludge produces H₂ under anaerobic conditions. Then, the H₂ and CO₂ are utilized by the hydrogenotrophic methanogens to CH₄. The biogas upgrading to biomethane can be achieved in 4 days at a batch system of anaerobic granular sludge, 50 g L¹ ZVI, initial pH 5 and 20 g L¹ NaHCO₃. The presence of ZVSI instead of ZVI resulted in slower rate of biogas, upgrading probably due to slower release of H₂ by ZVSI compared to ZVI. Raw biogas (from a pilot anaerobic digester treated with food waste) was fed in a system of anaerobic sludge and ZVI and VOCs composition was analyzed by HS-SPME-GC-MS over time. The presence of ZVI in anaerobic sludge mainly decreased the low molecular weight straight-chain and branched alkanes, but other chemical categories such as alkenes, aromatic hydrocarbons, terpenes and organic sulfur compounds did not exhibited any particular trend regarding their reduction. In addition, gaseous H₂S and NH₃ measurements were found to be substantially decreased when the anaerobic sludge was exposed to ZVI compared to no decrease in serum bottle free of ZVI.

Ethics approval and consent to participate

Not applicable.

Consent for publication

Not applicable.

Availability of data and materials

The datasets used and/or analysed during the current study are available from the corresponding author on reasonable request.

Competing interests

The authors declare that they have no competing interests.

Funding

This work was funded by the Cyprus University of Technology

Authors Contribution

Nikolaos Lytras: Writing- Original draft preparation, data curation, validation, Maria Andronikou: Writing- Original draft preparation, data curation, Validation, Georgia Chrysanthou: Data curation, Marinos Stylianou: Data curation Writing - Review & Editing, Methodology, Agapios Agapiou: Supervision, Writing - Review & Editing, Methodology, Ioannis Vyrides: Conceptualization, Methodology, Supervision, Writing - Review & Editing

Acknowledgments

I.V. would like to thank Cyprus University of Technology for the internal financial support.

Andersson, F.A.T., Karlsson, A., Svensson, B.H., Ejlertsson, J., 2004. Occurrence and abatement of volatile sulfur compounds during biogas production. J. Air Waste Manag. Assoc. 54, 855–861. https://doi.org/10.1080/10473289.2004.10470953

Andriamanohiarisoamanana, F.J., Shirai, T., Yamashiro, T., Yasui, S., Iwasaki, M., Ihara, I., Nishida, T., Tangtaweewipat, S., Umetsu, K., 2018. Valorizing waste iron powder in biogas production: Hydrogen sulfide control and process performances. J. Environ. Manage. 208, 134–141. https://doi.org/10.1016/j.jenvman.2017.12.012

Angelidaki, I., Treu, L., Tsapekos, P., Luo, G., Campanaro, S., Wenzel, H., Kougias, P.G., 2018. Biogas upgrading and utilization: Current status and perspectives. Biotechnol. Adv. 36, 452–466. https://doi.org/10.1016/j.biotechadv.2018.01.011

Angenent, L.T., Usack, J.G., Xu, J., Hafenbradl, D., Posmanik, R., Tester, J.W., 2018. Integrating electrochemical, biological, physical, and thermochemical process units to expand the applicability of anaerobic digestion. Bioresour. Technol. 247, 1085–1094. https://doi.org/10.1016/j.biortech.2017.09.104

Bajracharya, S., 2020. Microbial fuel cell coupled with anaerobic treatment processes for wastewater treatment, in:, Integrated Microbial Fuel Cells for Wastewater Treatment. Butterworth-Heinemann, pp. 295–311. https://doi.org/https://doi.org/10.1016/B978-0-12-817493-7.00014-X

Bassani, I., Kougias, P.G., Angelidaki, I., 2016. In-situ biogas upgrading in thermophilic granular UASB reactor: key factors affecting the hydrogen mass transfer rate. Bioresour. Technol. 221, 485–491. https://doi.org/10.1016/j.biortech.2016.09.083

Charalambous, P. and Vyrides, I., 2020. In situ biogas upgrading and enhancement of anaerobic digestion of cheese whey by addition of scrap or powder zero-valent iron (ZVI). J. Environ. Manage, p.111651. https://doi.org/10.1016/j.jenvman.2020.111651

Cheng, J., Zhu, C., Zhu, J., Jing, X., Kong, F., Zhang, C., 2020. Effects of waste rusted iron shavings on enhancing anaerobic digestion of food wastes and municipal sludge. J. Clean. Prod. 242, 118195. https://doi.org/10.1016/j.jclepro.2019.118195

Farghali, M., Andriamanohiarisoamanana, F.J., Ahmed, M.M., Kotb, S., Yamamoto, Y., Iwasaki, M., Yamashiro, T., Umetsu, K., 2020. Prospects for biogas production and H2S control from the anaerobic digestion of cattle manure: The influence of microscale waste iron powder and iron oxide nanoparticles. Waste Manag. 101, 141–149. https://doi.org/10.1016/j.wasman.2019.10.003

Fu, S., Angelidaki, I. and Zhang, Y., 2020. In situ Biogas Upgrading by CO2-to-CH4 Bioconversion. Trends in Biotechnol. https://doi.org/10.1016/j.tibtech.2020.08.006

Jiang, Y., May, H.D., Lu, L., Liang, P., Huang, X., Ren, Z.J., 2019. Carbon dioxide and organic waste valorization by microbial electrosynthesis and electro-fermentation. Water Res. 149, 42–55. https://doi.org/10.1016/j.watres.2018.10.092

Liu, Y., Zhang, Y., Ni, B.J., 2015. Zero valent iron simultaneously enhances methane production and sulfate reduction in anaerobic granular sludge reactors. Water Res. 75, 292–300. https://doi.org/10.1016/j.watres.2015.02.056

Menikea, K.K., Kyprianou, A., Samanides, C.G., Georgiou, S.G., Koutsokeras, L., Constantinides, G., Vyrides, I., 2020. Anaerobic granular sludge and zero valent scrap iron (ZVSI) pre-treated with green tea as a sustainable system for conversion of CO2 to CH4. J. Clean. Prod. 268. https://doi.org/10.1016/j.jclepro.2020.121860

Muñoz, R., Meier, L., Diaz, I., Jeison, D., 2015. A review on the state-of-the-art of physical/chemical and biological technologies for biogas upgrading. Rev. Environ. Sci. Biotechnol. 14, 727–759. https://doi.org/10.1007/s11157-015-9379-1

Mystrioti, C., Sparis, D., Papasiopi, N., Xenidis, A., Dermatas, D., Chrysochoou, M., 2015. Assessment of polyphenol coated Nano zero Valent iron for hexavalent chromium removal from contaminated waters. Bull. Environ. Contam. Toxicol. 94, 302–307. https://doi.org/10.1007/s00128-014-1442-z

Owen, W.F., Stuckey, D.C., Healy, J.B., Young, L.Y., McCarty, P.L., 1979. Bioassay for monitoring biochemical methane potential and anaerobic toxicity. Water Res. 13, 485–492. https://doi.org/10.1016/0043-1354(79)90043-5

Paolini, V., Petracchini, F., Carnevale, M., Gallucci, F., Perilli, M., Esposito, G., Segreto, M., Occulti, L.G., Scaglione, D., Ianniello, A., Frattoni, M., 2018. Characterisation and cleaning of biogas from sewage sludge for biomethane production. J. Environ. Manage. 217, 288–296. https://doi.org/10.1016/j.jenvman.2018.03.113

Prévoteau, A., Carvajal-Arroyo, J.M., Ganigué, R., Rabaey, K., 2020. Microbial electrosynthesis from CO2: forever a promise? Curr. Opin. Biotechnol. 62, 48–57. https://doi.org/10.1016/j.copbio.2019.08.014

Ruan, R., Cao, J., Li, C., Zheng, D., Luo, J., 2017. The influence of micro-oxygen addition on desulfurization performance and microbial communities during waste-activated sludge digestion in a rusty scrap iron-loaded anaerobic digester. Energies 10. https://doi.org/10.3390/en10020258

Salazar Gómez, J.I., Lohmann, H., Krassowski, J., 2016. Determination of volatile organic compounds from biowaste and co-fermentation biogas plants by single-sorbent adsorption. Chemosphere 153, 48–57. https://doi.org/10.1016/j.chemosphere.2016.02.128

Samanides, C.G., Koutsokeras, L., Constantinides, G., Vyrides, I., 2020. Methanogenesis Inhibition in Anaerobic Granular Sludge for the Generation of Volatile Fatty Acids from CO2 and Zero Valent Iron. Front. Energy Res. 8, 1–16. https://doi.org/10.3389/fenrg.2020.00037

Schiebahn, S., Grube, T., Robinius, M., Tietze, V., Kumar, B., Stolten, D., 2015. Power to gas: Technological overview, systems analysis and economic assessment for a case study in Germany. Int. J. Hydrogen Energy 40, 4285–4294. https://doi.org/10.1016/j.ijhydene.2015.01.123

Sun, Q., Li, H., Yan, J., Liu, L., Yu, Z., Yu, X., 2015. Selection of appropriate biogas upgrading technology-a review of biogas cleaning, upgrading and utilisation. Renew. Sustain. Energy Rev. 51, 521–532. https://doi.org/10.1016/j.rser.2015.06.029

Vyrides, I., Andronikou, M., Kyprianou, A., Modic, A., Filippeti, A., Yiakoumis, C., Samanides, C.G., 2018. CO2 conversion to CH4 using Zero Valent Iron (ZVI) and anaerobic granular sludge: Optimum batch conditions and microbial pathways. J. CO2 Util. 27, 415–422. https://doi.org/10.1016/j.jcou.2018.08.023

Vyrides, I., Stuckey, D.C., 2009. Effect of fluctuations in salinity on anaerobic biomass and production of soluble microbial products (SMPs). Biodegradation 20, 165–175. https://doi.org/10.1007/s10532-008-9210-6

Wei, J., Hao, X., van Loosdrecht, M.C.M., Li, J., 2018. Feasibility analysis of anaerobic digestion of excess sludge enhanced by iron: A review. Renew. Sustain. Energy Rev. 89, 16–26. https://doi.org/10.1016/j.rser.2018.02.042

Zabranska, J., Pokorna, D., 2018. Bioconversion of carbon dioxide to methane using hydrogen and hydrogenotrophic methanogens. Biotechnol. Adv. 1–14. https://doi.org/10.1016/j.biotechadv.2017.12.003

Download PDF

Version 1

posted

You are reading this latest preprint version

Ex-situ biogas upgrading to methane and removal of VOCs in a system of zero valent iron and anaerobic granular sludge

Status:

Version 1

Abstract

Figures

1. Introduction

2. Material And Methods

3. Results

4. Discussion

5. Conclusion

Declarations

References

Status:

Version 1