# Improving Anaerobic Digestion of Wheat Straw by Plasma-Assisted Pretreatment

Authors: Stefan Heiske; Nadja Schultz-Jensen; Frank Leipold; Jens Ejbye Schmidt
Journal: Journal of Atomic and Molecular Physics
 (2013)

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## Abstract

Plasma-assisted pretreatment (PAP) of lignocellulosic biomass has been shown to be an efficient method to decompose lignin and consequently facilitate microbial access to cellulose and hemicellulose. In the present study, PAP was tested for its suitability to enhance bioconversion of wheat straw to methane. In thermophilic batch experiments, methane yields of up to 366 mL/g volatile solids (VSs) were achieved, accounting for a yield increase of 45%. Common lignin-derived inhibitors like 5-hydroxymethylfurfural (5-HMF) and furfural were not detected after PAP, but toxicity test resulted in lower methane yields at higher substrate concentrations, indicating the presence of other unidentified inhibitors. However, in a continuous lab-scale biogas reactor experiment, stable codigestion of cattle manure with 20% PAP wheat straw was demonstrated, while no signs of adverse effects on the anaerobic digestion process were observed. After the introduction of the pretreated wheat straw to the reactor, volatile fatty acid concentrations remained low and stable, while gas production increased. In co-digestion, the PAP wheat straw was converted at an average yield of 343 mL CH4/gVS.


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## Body

## 1. Introduction

Anaerobic digestion (AD) is a widely applied method of managing agricultural byproducts such as animal manure and crop residues with multiple benefits. Treating organic material in biogas plants can produce renewable energy in the form of biogas, reduce land-use related environmental impacts, and improve the fertilizer quality of manure. These benefits have increased the interest in biogas technology worldwide. At present, the economic benefits of AD of agricultural residues are, however, limited because manure has a low energy density and many fibrous residues are only poorly degraded. This results in a low biogas yield which is a barrier to the expansion of biogas technology for energy production purposes. However, manure and crop residues hold the potential for a more efficient conversion to biogas as a considerable fraction of the organic material remains undigested in currently applied biogas processes.The main reason for the low yields lies in the structure of the biomass. Crop residues and fibers contained in manure mainly consist of lignocellulose, which is poorly degraded in biogas reactors as lignin is not degradable under anaerobic conditions and prevents microbial access to cellulose and hemicelluloses [1, 2]. Hence, removing lignin can facilitate anaerobic degradation of the fibers and thereby increase the biogas yield of manure and crop residues significantly.Various pretreatment methods aiming at the destruction of the fiber structures or the removal of lignin have been investigated. The majority of these studies are related to the improvement of sugar release, for example, ethanol production [3, 4]. However, a number of studies have investigated pretreatment methods that specifically aim to increase the methane yield of recalcitrant biomass. Size reduction (maceration) of manure fibers led to an increase of 25% [5]. Also, 23% and 30% improvement was achieved with chemical and biological treatment of manure, respectively [6]. Thermal pretreatment of the solid fraction of manure was reported to improve the yield by 9%–24% [7]. Extrusion applied on straw and the solid fraction of manure resulted in 70% and 27% increases, respectively [8]. Up to 40% more methane was exploited from biowaste by applying thermal wet oxidation [9]. However, many pretreatment methods have disadvantages such as low efficiency, the addition of chemicals, or the formation of compounds that inhibit subsequent digestion. Moreover, the energy consumption is often too high when compared to the energy gained by the pretreatment.Few studies have tested plasma to assist the pretreatment of biomass. The potential of using cold plasma at atmospheric pressure and ambient temperature for the pretreatment of wheat straw has been described by Vidal [10]. The reagent in such a process is ozone which is produced from air or pure oxygen in the plasma. Ozone is predicted to degrade unsaturated organic compounds in lignin, whereas saturated compounds such as carbohydrates are degraded only to a minor extent [11]. Experiments with PAP of wheat straw carried out by Schultz-Jensen et al. [12, 13] indicated an efficient and selective degradation of lignin, confirming Vidal’s findings. These studies suggest PAP to be a potentially suitable and promising method for the treatment of crop residues and manure fibers prior to AD. However, the effect of PAP on the biogas process and the methane yield of wheat straw has not been investigated yet and is the focus of this study.The PAP method applied in this study follows the method established by Schultz-Jensen et al. [13], using the same custom-made lab-scale reactor employed in Schultz-Jensen’s previous works. In addition, a modified reactor was used for PAP, which featured three separate layers of wheat straw with different treatment intensities. The treated biomass was analyzed for lignin concentration and available sugars. The effect of the PAP on the methane potential of wheat straw was investigated in batch trials. Furthermore, we tested long-term performance of an AD process fed with a substrate mixture of manure and PAP wheat straw in a continuous biogas reactor experiment.


## 2. Materials and Methods

### 2.1. Substrate

The wheat straw (Triticum aestivum L.) was grown and harvested after a drying period in Denmark during summer 2008. The straw was baled into 500 kg bales and stored at ambient temperature.


### 2.2. Ozone Generation by means of Plasma

The O3 was generated by means of a dielectric barrier discharge (DBD) operating at atmospheric pressure and ambient temperature. The electrodes were coaxially arranged and separated by an Al2O3 cylinder serving as a dielectric barrier (Figure 1). The design is based on the DBD used in [14]. Typical waveforms for voltage, current, and spectra from optical emission for pulsed DBDs can be found in [15]. The discharge was powered by AC voltage pulses. One pulse consisted of three full sinusoidal periods. The period time was set to 54 μs. The average power delivered to the DBD could be varied by varying the time between two pulses and was indicated by the power supply. The operation gas of the DBD was oxygen enriched air (40% O2, 60% N2) at a flow of 12 standard liters per minute (SLM). The power was adjusted to 230 W.Figure 1
Schematic drawing of the dielectric barrier charge (front view). Electrodes (dark gray), dielectric barrier (gray), and plasma volume (white).The relevant reactions for generating ozone in a DBD are given in reactions (1)–(4) (later). The oxygen molecule is dissociated by electron impact (reactions (1) and (2)). The output products are O(1D) and O(3P) [16]. As described by Penetrante [17], reaction (1) is dominant in this type of discharge. The oxygen atom reacts with an oxygen molecule to ozone (reactions (3) and (4)). Reactions (3) and (4) are three body reactions where M is O2 or N2. Consider
(1)e+O2⟶e+O(1D)+O(3P)(2)e+O2⟶e+O(3P)+O(3P)(3)O2+O(1D)+M⟶O3+M(4)O2+O(3P)+M⟶O3+M


### 2.3. The Pretreatment Reactor

The core of the reactor was a stainless steel sieve (Retsch test sieves, Retsch GmbH, Germany) with a mesh size of 0.2 mm carrying the wheat straw (single layer reactor). The sieve has a diameter of 30 cm corresponding to an area of 706 cm2. O3 containing gas was forced through the sieve from the bottom. The exhaust gas was collected from the top for analysis.The O3 concentration in the intake and exhaust was detected by means of ultraviolet absorption spectroscopy. A mercury lamp served as light source and a UV-photo diode in combination with an interference filter served as detector. The transmission maximum of the filter is at 254 nm where O3 has an absorption maximum. The ozone measurement technique is detailed in [18]. Depending on the pretreatment progress, the O3 concentration in the exhaust gas varied. The difference between the supplied O3 and the O3 in the exhaust was a measure of the O3 consumption of the straw. A more detailed description of the pretreatment process can be found in [12].Additionally, a modified version of the described pretreatment reactor was used in this study, which contained a core of three vertically cascaded stainless steel sieves in exchange to just one stainless steel sieve. This setup allowed accounting for different treatment intensities, as O3 penetrated through the biomass via bottom, mid, and top layer successively while gradually being consumed. In the following, this modified version is referred to as multiple-layer reactor and its layers are labeled as BOT, MID, and TOP (bottom, middle and top layer, resp.). The original setup without separate layers is referred to as single-layer reactor (SIN). Apart from the layers, both reactor types had identical technical features which have previously been described [13].


### 2.4. Pretreatment

The wheat straw was milled to a final particle size of 1 mm using a technical mill (MF 10 basic, IKA-Werke GmbH & Co. KG, Germany). After milling, water was added to the wheat straw to obtain a dry matter content of 45%. Particle size and dry matter content were chosen according to the method established by Schultz-Jensen et al. [12, 13]. The PAP was applied at atmospheric pressure for 1 h. The concentration of O3 was 0.6%–1% at a gas flow rate of 12 SLM into the reactor. Mass loss by pretreatment was neglected as it was found to be below 1% after 1 h of treatment [12].


### 2.5. Determination of Methane Potentials

Methane potentials were determined for raw and pretreated samples in batch trials. Pretreated wheat straw was tested separately for material from the top, mid, and bottom layers (multiple-layer reactor) as well as from the treatment in the single layer reactor. Triplicates of each sample were distributed in 116 mL serum bottles in amounts of 0.4 g substrate (except for bottom layer where 0.2, 0.4, and 0.8 g substrates were used, corresponding to substrate concentrations of 5, 10, and 20 gVS/L, resp.). The bottles were inoculated with 20 g of digestate (inoculum), taken from a lab-scale reactor treating cattle manure (4% VS) at a temperature of 53°C. Water was added to each bottle to reach a total volume of 40 mL. For subtraction of methane produced by the inoculum, vials only containing 20 g of inoculum were also made. All bottles were flushed with a gas mixture of N2/CO2 (80%/20%), to obtain anaerobic conditions, closed with butyl rubber stoppers and aluminium crimps and incubated at 53°C for a period of 63 days. Methane production in the bottle headspace was measured by gas chromatography at increasing intervals, starting with 2 measurements a week during the first 15 days of incubation.


### 2.6. Codigestion of Pretreated Wheat Straw and Cattle Manure in a Lab-Scale Reactor

A 4.5-liter continuously stirred tank reactor (CSTR) with a working volume of 3.0 liter was run for a period of 167 days. The reactor was inoculated with effluent from a thermophilic (55°C) full scale biogas plant (Snertinge, Denmark) which treats cattle/pig manure (80%) and industrial waste (20%). The reactor was operated at 53°C with a hydraulic retention time (HRT) of approximately 15 days. Stirring was done by a top-mounted propeller at intervals of 5 minutes for 45 seconds at 100 rpm. Substrate was automatically supplied by a peristaltic pump three times a day in loads of app. 66 mL. The substrate initially consisted of cattle manure (ca. 4% VS) and accounted for an average organic loading rate (OLR) of 2.5 gVS L−1d−1. After a startup phase, the reactor was run for 40 days to establish a stable digestion process and to ensure steady state conditions. In the following period (referred to days 0–59), the reactor was run under unchanged conditions. Data obtained during this period served as a reference for comparison with the following feed change. On day 60, the OLR was increased to 3.0 gVS L−1d−1 by feeding a mixture of ozone-pretreated wheat straw from the single layer treatment and cattle manure. In this period, the fraction of added straw accounted for 20% of the OLR. The process was run for further 67 days, with otherwise unchanged process parameters. The performance of the digestion process in the reactor was monitored by total gas production, methane concentration and yield, pH, and the concentration of volatile fatty acids (VFAs). The methane yield of the pretreated wheat straw was estimated as the average of the entire codigestion period by relating the sum of additionally produced methane (compared to the average methane production from the digestion of manure alone) to the total amount of added straw.


### 2.7. Analysis

#### 2.7.1. Monitoring of Anaerobic Digestion Trials

Total solids (TSs) and VS were determined using standard methods [19]. The accumulating CH4 production in the batch flasks was measured by gas chromatography using flame ionization detection (Hewlett and Packard 6890 GC system). The total gas production of the reactor was measured by an automated metering system based on the principle of liquid displacement [20]. CH4 and CO2 concentrations in the produced biogas were determined by gas chromatography using a Mikrolab ML GC 82 with thermal conductivity detection (Mikrolab, Århus, Denmark). Biogas and methane production is given in norm liters (at 273 K and 1013 mbar). For VFA determination, 1 mL samples were acidified with 3 M sulphuric acid, centrifuged at 4000 rpm for 20 min, and analyzed on HP 6890 GC system equipped with flame ionization detector.


#### 2.7.2. Strong Acid Hydrolysis

The composition of the raw and pretreated wheat straw was measured by strong acid hydrolysis of the carbohydrates. Dried and milled samples (160 mg) were treated with 72% (w/w) H2SO4 (1.5 mL) at 30°C for 1 h. The solutions were diluted with 42 mL water and autoclaved at 121°C for 1 h. The hydrolysates were filtered, and the Klason lignin content was determined as the weight of the insoluble residue minus the ash content. The recovery of D-glucose, D-xylose, and L-arabinose was determined by standard addition of sugars to the samples before autoclaving. The sugars were determined after separation on an high-performance liquid chromatography (HPLC) system (Shimadzu) with an Aminex HPX-87H column (BioRAD) at 63°C using 4 mM H2SO4 as eluent and a flow rate of 0.6 mL/min; detection was done by a refractive index detector [21]. The samples were centrifuged with approximately 4,000 rpm for 10 min. The supernatant was analyzed for glucose, xylose, arabinose, and acetic acid by HPLC as described earlier.


#### 2.7.3. Inhibitor Analysis

The pretreated wheat straw was washed in order to extract lignin degradation products. The obtained washing water was analyzed for phenols by gas chromatography (GC). The concentrations of furans were measured using high-performance liquid chromatography (HPLC). Washing procedure, GC, and HPLC analysis are described in detail in [12].


## 2.1. Substrate

The wheat straw (Triticum aestivum L.) was grown and harvested after a drying period in Denmark during summer 2008. The straw was baled into 500 kg bales and stored at ambient temperature.


## 2.2. Ozone Generation by means of Plasma

The O3 was generated by means of a dielectric barrier discharge (DBD) operating at atmospheric pressure and ambient temperature. The electrodes were coaxially arranged and separated by an Al2O3 cylinder serving as a dielectric barrier (Figure 1). The design is based on the DBD used in [14]. Typical waveforms for voltage, current, and spectra from optical emission for pulsed DBDs can be found in [15]. The discharge was powered by AC voltage pulses. One pulse consisted of three full sinusoidal periods. The period time was set to 54 μs. The average power delivered to the DBD could be varied by varying the time between two pulses and was indicated by the power supply. The operation gas of the DBD was oxygen enriched air (40% O2, 60% N2) at a flow of 12 standard liters per minute (SLM). The power was adjusted to 230 W.Figure 1
Schematic drawing of the dielectric barrier charge (front view). Electrodes (dark gray), dielectric barrier (gray), and plasma volume (white).The relevant reactions for generating ozone in a DBD are given in reactions (1)–(4) (later). The oxygen molecule is dissociated by electron impact (reactions (1) and (2)). The output products are O(1D) and O(3P) [16]. As described by Penetrante [17], reaction (1) is dominant in this type of discharge. The oxygen atom reacts with an oxygen molecule to ozone (reactions (3) and (4)). Reactions (3) and (4) are three body reactions where M is O2 or N2. Consider
(1)e+O2⟶e+O(1D)+O(3P)(2)e+O2⟶e+O(3P)+O(3P)(3)O2+O(1D)+M⟶O3+M(4)O2+O(3P)+M⟶O3+M


## 2.3. The Pretreatment Reactor

The core of the reactor was a stainless steel sieve (Retsch test sieves, Retsch GmbH, Germany) with a mesh size of 0.2 mm carrying the wheat straw (single layer reactor). The sieve has a diameter of 30 cm corresponding to an area of 706 cm2. O3 containing gas was forced through the sieve from the bottom. The exhaust gas was collected from the top for analysis.The O3 concentration in the intake and exhaust was detected by means of ultraviolet absorption spectroscopy. A mercury lamp served as light source and a UV-photo diode in combination with an interference filter served as detector. The transmission maximum of the filter is at 254 nm where O3 has an absorption maximum. The ozone measurement technique is detailed in [18]. Depending on the pretreatment progress, the O3 concentration in the exhaust gas varied. The difference between the supplied O3 and the O3 in the exhaust was a measure of the O3 consumption of the straw. A more detailed description of the pretreatment process can be found in [12].Additionally, a modified version of the described pretreatment reactor was used in this study, which contained a core of three vertically cascaded stainless steel sieves in exchange to just one stainless steel sieve. This setup allowed accounting for different treatment intensities, as O3 penetrated through the biomass via bottom, mid, and top layer successively while gradually being consumed. In the following, this modified version is referred to as multiple-layer reactor and its layers are labeled as BOT, MID, and TOP (bottom, middle and top layer, resp.). The original setup without separate layers is referred to as single-layer reactor (SIN). Apart from the layers, both reactor types had identical technical features which have previously been described [13].


## 2.4. Pretreatment

The wheat straw was milled to a final particle size of 1 mm using a technical mill (MF 10 basic, IKA-Werke GmbH & Co. KG, Germany). After milling, water was added to the wheat straw to obtain a dry matter content of 45%. Particle size and dry matter content were chosen according to the method established by Schultz-Jensen et al. [12, 13]. The PAP was applied at atmospheric pressure for 1 h. The concentration of O3 was 0.6%–1% at a gas flow rate of 12 SLM into the reactor. Mass loss by pretreatment was neglected as it was found to be below 1% after 1 h of treatment [12].


## 2.5. Determination of Methane Potentials

Methane potentials were determined for raw and pretreated samples in batch trials. Pretreated wheat straw was tested separately for material from the top, mid, and bottom layers (multiple-layer reactor) as well as from the treatment in the single layer reactor. Triplicates of each sample were distributed in 116 mL serum bottles in amounts of 0.4 g substrate (except for bottom layer where 0.2, 0.4, and 0.8 g substrates were used, corresponding to substrate concentrations of 5, 10, and 20 gVS/L, resp.). The bottles were inoculated with 20 g of digestate (inoculum), taken from a lab-scale reactor treating cattle manure (4% VS) at a temperature of 53°C. Water was added to each bottle to reach a total volume of 40 mL. For subtraction of methane produced by the inoculum, vials only containing 20 g of inoculum were also made. All bottles were flushed with a gas mixture of N2/CO2 (80%/20%), to obtain anaerobic conditions, closed with butyl rubber stoppers and aluminium crimps and incubated at 53°C for a period of 63 days. Methane production in the bottle headspace was measured by gas chromatography at increasing intervals, starting with 2 measurements a week during the first 15 days of incubation.


## 2.6. Codigestion of Pretreated Wheat Straw and Cattle Manure in a Lab-Scale Reactor

A 4.5-liter continuously stirred tank reactor (CSTR) with a working volume of 3.0 liter was run for a period of 167 days. The reactor was inoculated with effluent from a thermophilic (55°C) full scale biogas plant (Snertinge, Denmark) which treats cattle/pig manure (80%) and industrial waste (20%). The reactor was operated at 53°C with a hydraulic retention time (HRT) of approximately 15 days. Stirring was done by a top-mounted propeller at intervals of 5 minutes for 45 seconds at 100 rpm. Substrate was automatically supplied by a peristaltic pump three times a day in loads of app. 66 mL. The substrate initially consisted of cattle manure (ca. 4% VS) and accounted for an average organic loading rate (OLR) of 2.5 gVS L−1d−1. After a startup phase, the reactor was run for 40 days to establish a stable digestion process and to ensure steady state conditions. In the following period (referred to days 0–59), the reactor was run under unchanged conditions. Data obtained during this period served as a reference for comparison with the following feed change. On day 60, the OLR was increased to 3.0 gVS L−1d−1 by feeding a mixture of ozone-pretreated wheat straw from the single layer treatment and cattle manure. In this period, the fraction of added straw accounted for 20% of the OLR. The process was run for further 67 days, with otherwise unchanged process parameters. The performance of the digestion process in the reactor was monitored by total gas production, methane concentration and yield, pH, and the concentration of volatile fatty acids (VFAs). The methane yield of the pretreated wheat straw was estimated as the average of the entire codigestion period by relating the sum of additionally produced methane (compared to the average methane production from the digestion of manure alone) to the total amount of added straw.


## 2.7. Analysis

### 2.7.1. Monitoring of Anaerobic Digestion Trials

Total solids (TSs) and VS were determined using standard methods [19]. The accumulating CH4 production in the batch flasks was measured by gas chromatography using flame ionization detection (Hewlett and Packard 6890 GC system). The total gas production of the reactor was measured by an automated metering system based on the principle of liquid displacement [20]. CH4 and CO2 concentrations in the produced biogas were determined by gas chromatography using a Mikrolab ML GC 82 with thermal conductivity detection (Mikrolab, Århus, Denmark). Biogas and methane production is given in norm liters (at 273 K and 1013 mbar). For VFA determination, 1 mL samples were acidified with 3 M sulphuric acid, centrifuged at 4000 rpm for 20 min, and analyzed on HP 6890 GC system equipped with flame ionization detector.


### 2.7.2. Strong Acid Hydrolysis

The composition of the raw and pretreated wheat straw was measured by strong acid hydrolysis of the carbohydrates. Dried and milled samples (160 mg) were treated with 72% (w/w) H2SO4 (1.5 mL) at 30°C for 1 h. The solutions were diluted with 42 mL water and autoclaved at 121°C for 1 h. The hydrolysates were filtered, and the Klason lignin content was determined as the weight of the insoluble residue minus the ash content. The recovery of D-glucose, D-xylose, and L-arabinose was determined by standard addition of sugars to the samples before autoclaving. The sugars were determined after separation on an high-performance liquid chromatography (HPLC) system (Shimadzu) with an Aminex HPX-87H column (BioRAD) at 63°C using 4 mM H2SO4 as eluent and a flow rate of 0.6 mL/min; detection was done by a refractive index detector [21]. The samples were centrifuged with approximately 4,000 rpm for 10 min. The supernatant was analyzed for glucose, xylose, arabinose, and acetic acid by HPLC as described earlier.


### 2.7.3. Inhibitor Analysis

The pretreated wheat straw was washed in order to extract lignin degradation products. The obtained washing water was analyzed for phenols by gas chromatography (GC). The concentrations of furans were measured using high-performance liquid chromatography (HPLC). Washing procedure, GC, and HPLC analysis are described in detail in [12].


## 2.7.1. Monitoring of Anaerobic Digestion Trials

Total solids (TSs) and VS were determined using standard methods [19]. The accumulating CH4 production in the batch flasks was measured by gas chromatography using flame ionization detection (Hewlett and Packard 6890 GC system). The total gas production of the reactor was measured by an automated metering system based on the principle of liquid displacement [20]. CH4 and CO2 concentrations in the produced biogas were determined by gas chromatography using a Mikrolab ML GC 82 with thermal conductivity detection (Mikrolab, Århus, Denmark). Biogas and methane production is given in norm liters (at 273 K and 1013 mbar). For VFA determination, 1 mL samples were acidified with 3 M sulphuric acid, centrifuged at 4000 rpm for 20 min, and analyzed on HP 6890 GC system equipped with flame ionization detector.


## 2.7.2. Strong Acid Hydrolysis

The composition of the raw and pretreated wheat straw was measured by strong acid hydrolysis of the carbohydrates. Dried and milled samples (160 mg) were treated with 72% (w/w) H2SO4 (1.5 mL) at 30°C for 1 h. The solutions were diluted with 42 mL water and autoclaved at 121°C for 1 h. The hydrolysates were filtered, and the Klason lignin content was determined as the weight of the insoluble residue minus the ash content. The recovery of D-glucose, D-xylose, and L-arabinose was determined by standard addition of sugars to the samples before autoclaving. The sugars were determined after separation on an high-performance liquid chromatography (HPLC) system (Shimadzu) with an Aminex HPX-87H column (BioRAD) at 63°C using 4 mM H2SO4 as eluent and a flow rate of 0.6 mL/min; detection was done by a refractive index detector [21]. The samples were centrifuged with approximately 4,000 rpm for 10 min. The supernatant was analyzed for glucose, xylose, arabinose, and acetic acid by HPLC as described earlier.


## 2.7.3. Inhibitor Analysis

The pretreated wheat straw was washed in order to extract lignin degradation products. The obtained washing water was analyzed for phenols by gas chromatography (GC). The concentrations of furans were measured using high-performance liquid chromatography (HPLC). Washing procedure, GC, and HPLC analysis are described in detail in [12].


## 3. Results and Discussion

### 3.1. Lignin Removal and Sugar Availability

Untreated wheat straw (RAW) contained 20.0% lignin and 7.0% of total sugars (Table1). The straw treated in the single layer reactor had reduced lignin concentration (16.2%) and more sugars (14.56%) were available. The analysis of straw treated in the different layers of the multiple-layer reactor indicated a decrease of the lignin content, when comparing the layers from top (17.5%) over mid (13.0%) to bottom (7.2%). Correspondingly, the amount of available sugars increased from top to bottom (top 8.8%, mid 16.9%, and bottom 28.4%). This suggests that the highest treatment efficiency is to be found in the bottom layer, where most ozone was available for lignin degradation.Table 1
Methane yields, lignin content, and concentration of available sugars of raw and PAP wheat straw.
Treatment (layer)
Series name
VS load (gVS/L)
Yield (mL CH4/gVS)
Lignin (% of TS)1
Total sugars (% of TS)2
Raw material
RAW
10
254.04 ± 19.49
20.0
7.0
Single layer
SIN
10
317.04 ±  19.49
16.2
14.56
Top layer
TOP
10
286.05 ± 7.35
17.5
8.78
Mid layer
MID
10
300.97 ± 0.09
13
16.93
Bottom layer (low load)
BOT5
5
366.46 ± 9.36
7.2
28.43
Bottom layer (medium load)
BOT10
10
311.58 ± 10.45
7.2
28.43
Bottom layer (high load)
BOT20
20
277.96 ± 8.59
7.2
28.43
1Strong acid hydrolysis; 2enzymatic hydrolysis.


### 3.2. Effect of the PAP Treatment on the Methane Yield

In the batch digestion trials, the effect of the PAP treatment on the anaerobic digestibility of wheat straw was tested. The digestion of raw wheat straw resulted in a specific methane yield of 254 ± 19 mL/gVS, while all batches with pretreated wheat straw had higher specific methane yields (Table1). Wheat straw treated in the single layer reactor (SIN) resulted in a yield of 317 ± 5 mL/gVS. After treatment in the multiple layer reactor, wheat straw was converted to methane with yields of 311 ± 10 mL/gVS (BOT (10)), 301 ± 0.1 mL/gVS (MID), and 286 ± 7 mL/gVS (TOP). These yields indicate little but no substantial difference between the layers with respect to their effect on anaerobic digestibility. This was otherwise suggested by the differences in lignin content and available sugars. Presumably, inhibitory effects of lignin degradation products have balanced out the beneficiary effects of a stronger treatment. However, SIN achieved the highest yield among the tested treatments, while only having a comparatively moderate lignin removal and sugar availability.


### 3.3. Effect of Substrate Concentration

The highest lignin removal was achieved in the bottom layer. Accordingly, a higher concentration of potentially inhibiting lignin degradation products is expected in BOT, which therefore was tested for inhibition by using different substrate amounts in the batch trial. The previous assumption of adverse effects by lignin derivatives is supported by the methane yields achieved when digesting different substrate concentrations of BOT, indicating inhibition at higher concentrations (Figure2). BOT20 showed a 7-day lag-phase as well as a lower final methane yield (278 ± 9 mL/gVS) when compared to BOT10 (312 ± 10 mL/gVS). BOT10 did not show a distinct lag-phase but resulted in a lower final methane yield than BOT5 (366 ± 9 mL/gVS). The analysis of washing water from plasma pretreated wheat straw [12] revealed the presence of various phenolic compounds, which are known to have a negative effect on methane production [22, 23]. Phenolic compounds can inhibit enzymatic hydrolysis of cellulose [24] and thereby lower the methane yield from lignocellulosic substrate as straw. As phenols can be degraded anaerobically [25, 26], the lag-phase for BOT20 could have been caused by the initial phenol concentration, which was subsequently lowered due to degradation. However, the differences in the final methane yield indicated the presence of other, nondegradable inhibitors. Furfural and 5-HMF, known inhibitors typically found after, for example, thermal pretreatment of lignocellulosic material [27], were under detection limit after PAP (data not shown). Thus, the inhibiting effect of PAP wheat straw at high substrate concentrations is presumably related to other nonidentified compounds.Figure 2
Accumulated methane production of bottom layer-treated wheat straw digested at different substrate concentrations.Despite potential inhibition, the beneficial effect of the pretreatment on the methane potential of the straw is significant at low substrate concentrations. When compared to raw wheat straw (for which no substrate inhibition was assumed in the present concentration range of from 5 to 20 gVS/L [28]), the increase in methane potential amounts to 45% for BOT5.


### 3.4. Continuous Trials

Adding PAP wheat straw to the manure-feed of the CSTR increased the methane production rate (daily methane production per liter reactor volume) from 593 ± 79 mL L−1d−1 (days 0–59) to 761 ± 94 mL L−1d−1 (days 60–127) (Figure 3(a)). Data from day 100 to day 115 has been excluded due to a technical failure on day 100, followed by a two-week period for rebalancing the process. The average volumetric methane yield increased from 9.34 ± 1.24 mL/g feedstock (manure) to 11.86 ± 1.35 mL/g feedstock (manure and straw) (Figure 3(b)). The yields obtained in the continuous process confirmed the results of the batch trials; the straw was digested with an average yield of 343 ± 17 mL CH4/gVS, corresponding to an increase of 35% when compared to untreated wheat straw in batch digestion. Adverse effects on the digestions process by the addition of straw have not been observed. The pH in the reactor remained stable at 7.77 ± 0.06 during the entire experiment. The concentrations of acetate (13 ± 1.4 mMol) and propionate (1.8 ± 0.31 mMol) were low and stable, which indicates that the process adapted well to the introduction of the pretreated straw as cosubstrate since propionate fluctuation is a widely used indicator of process stress in anaerobic reactors [29, 30]. The methane concentration showed minor fluctuations during the reference period (64.1 ± 1.8%) and stabilized during codigestion (63.8 ± 0.9%) indicating no effect of the addition of pretreated wheat straw on the biogas composition (Figure 3(a)).Methane production rate and CH4 concentration in the course of the continuous trial (a). Volumetric methane yield in the course of the continuous trial (b).
(a)
(b)


### 3.5. Energy Considerations

The PAP setup used in this study consumed 160 g Ozone per hour treatment time and kg biomass (dry weight), requiring 3.8 MJ for ozone production [13]. The additional methane gained from the pretreatment accounts for of 112 L/kg straw, corresponding to an energy gain of 3.8 MJ/kg. Hence, the energy demand for PAP cancels out the energy benefits of the treatment. Considering the early stage of development of PAP and the simple, not optimized ozone feed of the lab-scale setup, we assume that the method has potential for significant improvements which could result in a positive energy budget. Ozone could be fed more efficiently and recycled from the outgas. Further, treatment times could be optimized with respect to lignin degradation and ozone consumption.


### 3.6. Utilization of Lignin Products

PAP is potentially a particularly suitable technology for the recovery of high value compounds from lignocellulosic biomass; Schultz-Jensen et al. [12] noted that the temporal release pattern of various degradation products (e.g., phenols, benzene, fatty acids, etc.) during the treatment suggests further investigation on more targeted recovery of lignin derived products by PAP. As lignin is the only renewable source of aromatic compounds [31], the utilization of lignin degradation products adds an important aspect to the objective of PAP. Besides facilitating microbial access to cellulose and hemicellulose, the recovery of lignin derivatives could contribute to a more complete utilization of biomass which combines biogas production with the extraction of value added chemical products.


### 3.7. Future Perspective

Technical improvements towards a minimal use of ozone are crucial to make PAP a feasible method for large scale applications. Tests with modified reactor design need to be carried out to evaluate the margins for increasing process efficiency. Broader screening for inhibitory compounds and detailed monitoring of lignin derivate formation patterns would provide the knowledge necessary to specifically adjust PAP parameters for applications like biogas production and/or selective recovery of derivatives.  Investigations on the long-term performance of AD with high concentrations of PAP substrate could give valuable information about adverse effects and microbial adaptation.


## 3.1. Lignin Removal and Sugar Availability

Untreated wheat straw (RAW) contained 20.0% lignin and 7.0% of total sugars (Table1). The straw treated in the single layer reactor had reduced lignin concentration (16.2%) and more sugars (14.56%) were available. The analysis of straw treated in the different layers of the multiple-layer reactor indicated a decrease of the lignin content, when comparing the layers from top (17.5%) over mid (13.0%) to bottom (7.2%). Correspondingly, the amount of available sugars increased from top to bottom (top 8.8%, mid 16.9%, and bottom 28.4%). This suggests that the highest treatment efficiency is to be found in the bottom layer, where most ozone was available for lignin degradation.Table 1
Methane yields, lignin content, and concentration of available sugars of raw and PAP wheat straw.
Treatment (layer)
Series name
VS load (gVS/L)
Yield (mL CH4/gVS)
Lignin (% of TS)1
Total sugars (% of TS)2
Raw material
RAW
10
254.04 ± 19.49
20.0
7.0
Single layer
SIN
10
317.04 ±  19.49
16.2
14.56
Top layer
TOP
10
286.05 ± 7.35
17.5
8.78
Mid layer
MID
10
300.97 ± 0.09
13
16.93
Bottom layer (low load)
BOT5
5
366.46 ± 9.36
7.2
28.43
Bottom layer (medium load)
BOT10
10
311.58 ± 10.45
7.2
28.43
Bottom layer (high load)
BOT20
20
277.96 ± 8.59
7.2
28.43
1Strong acid hydrolysis; 2enzymatic hydrolysis.


## 3.2. Effect of the PAP Treatment on the Methane Yield

In the batch digestion trials, the effect of the PAP treatment on the anaerobic digestibility of wheat straw was tested. The digestion of raw wheat straw resulted in a specific methane yield of 254 ± 19 mL/gVS, while all batches with pretreated wheat straw had higher specific methane yields (Table1). Wheat straw treated in the single layer reactor (SIN) resulted in a yield of 317 ± 5 mL/gVS. After treatment in the multiple layer reactor, wheat straw was converted to methane with yields of 311 ± 10 mL/gVS (BOT (10)), 301 ± 0.1 mL/gVS (MID), and 286 ± 7 mL/gVS (TOP). These yields indicate little but no substantial difference between the layers with respect to their effect on anaerobic digestibility. This was otherwise suggested by the differences in lignin content and available sugars. Presumably, inhibitory effects of lignin degradation products have balanced out the beneficiary effects of a stronger treatment. However, SIN achieved the highest yield among the tested treatments, while only having a comparatively moderate lignin removal and sugar availability.


## 3.3. Effect of Substrate Concentration

The highest lignin removal was achieved in the bottom layer. Accordingly, a higher concentration of potentially inhibiting lignin degradation products is expected in BOT, which therefore was tested for inhibition by using different substrate amounts in the batch trial. The previous assumption of adverse effects by lignin derivatives is supported by the methane yields achieved when digesting different substrate concentrations of BOT, indicating inhibition at higher concentrations (Figure2). BOT20 showed a 7-day lag-phase as well as a lower final methane yield (278 ± 9 mL/gVS) when compared to BOT10 (312 ± 10 mL/gVS). BOT10 did not show a distinct lag-phase but resulted in a lower final methane yield than BOT5 (366 ± 9 mL/gVS). The analysis of washing water from plasma pretreated wheat straw [12] revealed the presence of various phenolic compounds, which are known to have a negative effect on methane production [22, 23]. Phenolic compounds can inhibit enzymatic hydrolysis of cellulose [24] and thereby lower the methane yield from lignocellulosic substrate as straw. As phenols can be degraded anaerobically [25, 26], the lag-phase for BOT20 could have been caused by the initial phenol concentration, which was subsequently lowered due to degradation. However, the differences in the final methane yield indicated the presence of other, nondegradable inhibitors. Furfural and 5-HMF, known inhibitors typically found after, for example, thermal pretreatment of lignocellulosic material [27], were under detection limit after PAP (data not shown). Thus, the inhibiting effect of PAP wheat straw at high substrate concentrations is presumably related to other nonidentified compounds.Figure 2
Accumulated methane production of bottom layer-treated wheat straw digested at different substrate concentrations.Despite potential inhibition, the beneficial effect of the pretreatment on the methane potential of the straw is significant at low substrate concentrations. When compared to raw wheat straw (for which no substrate inhibition was assumed in the present concentration range of from 5 to 20 gVS/L [28]), the increase in methane potential amounts to 45% for BOT5.


## 3.4. Continuous Trials

Adding PAP wheat straw to the manure-feed of the CSTR increased the methane production rate (daily methane production per liter reactor volume) from 593 ± 79 mL L−1d−1 (days 0–59) to 761 ± 94 mL L−1d−1 (days 60–127) (Figure 3(a)). Data from day 100 to day 115 has been excluded due to a technical failure on day 100, followed by a two-week period for rebalancing the process. The average volumetric methane yield increased from 9.34 ± 1.24 mL/g feedstock (manure) to 11.86 ± 1.35 mL/g feedstock (manure and straw) (Figure 3(b)). The yields obtained in the continuous process confirmed the results of the batch trials; the straw was digested with an average yield of 343 ± 17 mL CH4/gVS, corresponding to an increase of 35% when compared to untreated wheat straw in batch digestion. Adverse effects on the digestions process by the addition of straw have not been observed. The pH in the reactor remained stable at 7.77 ± 0.06 during the entire experiment. The concentrations of acetate (13 ± 1.4 mMol) and propionate (1.8 ± 0.31 mMol) were low and stable, which indicates that the process adapted well to the introduction of the pretreated straw as cosubstrate since propionate fluctuation is a widely used indicator of process stress in anaerobic reactors [29, 30]. The methane concentration showed minor fluctuations during the reference period (64.1 ± 1.8%) and stabilized during codigestion (63.8 ± 0.9%) indicating no effect of the addition of pretreated wheat straw on the biogas composition (Figure 3(a)).Methane production rate and CH4 concentration in the course of the continuous trial (a). Volumetric methane yield in the course of the continuous trial (b).
(a)
(b)


## 3.5. Energy Considerations

The PAP setup used in this study consumed 160 g Ozone per hour treatment time and kg biomass (dry weight), requiring 3.8 MJ for ozone production [13]. The additional methane gained from the pretreatment accounts for of 112 L/kg straw, corresponding to an energy gain of 3.8 MJ/kg. Hence, the energy demand for PAP cancels out the energy benefits of the treatment. Considering the early stage of development of PAP and the simple, not optimized ozone feed of the lab-scale setup, we assume that the method has potential for significant improvements which could result in a positive energy budget. Ozone could be fed more efficiently and recycled from the outgas. Further, treatment times could be optimized with respect to lignin degradation and ozone consumption.


## 3.6. Utilization of Lignin Products

PAP is potentially a particularly suitable technology for the recovery of high value compounds from lignocellulosic biomass; Schultz-Jensen et al. [12] noted that the temporal release pattern of various degradation products (e.g., phenols, benzene, fatty acids, etc.) during the treatment suggests further investigation on more targeted recovery of lignin derived products by PAP. As lignin is the only renewable source of aromatic compounds [31], the utilization of lignin degradation products adds an important aspect to the objective of PAP. Besides facilitating microbial access to cellulose and hemicellulose, the recovery of lignin derivatives could contribute to a more complete utilization of biomass which combines biogas production with the extraction of value added chemical products.


## 3.7. Future Perspective

Technical improvements towards a minimal use of ozone are crucial to make PAP a feasible method for large scale applications. Tests with modified reactor design need to be carried out to evaluate the margins for increasing process efficiency. Broader screening for inhibitory compounds and detailed monitoring of lignin derivate formation patterns would provide the knowledge necessary to specifically adjust PAP parameters for applications like biogas production and/or selective recovery of derivatives.  Investigations on the long-term performance of AD with high concentrations of PAP substrate could give valuable information about adverse effects and microbial adaptation.


## 4. Conclusions

Plasma-assisted pretreatment significantly reduced the lignin content of wheat straw and increased the sugar availability substantially. The methane yield of wheat straw was increased up to 45% by PAP, suggesting the method to be efficient in facilitating the conversion of lignocellulosic biomass to biogas. PAP of wheat straw in a multiple-layer reactor indicated a better lignin removal and higher methane yields at a higher ozone exposure. Presumably, a higher ozone exposure also leads to an increased formation of inhibitory compounds which counteract the benefits of the lignin removal; batch digestion trials indicated moderate inhibition at high substrate concentrations. However, continuous trials demonstrated that codigestion with 20% PAP wheat straw and 80% cattle manure was possible. The pretreated straw was codigested with a specific methane yield of 343 mL CH4/gVS. The anaerobic process was stable and no adverse effects were observed during the continuous experiment.In this lab-scale study, the energy benefit from a higher methane yield was cancelled out by the energy demand for ozone production. Further development and research is necessary to evaluate the applicability of plasma-assisted pretreatment of crop residues prior to anaerobic digestion.



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*Source: 791353-2013-06-05.xml*