This research was supported by the German Federal Ministry of Research and Education to Project Management Julich (PtJ). The authors thank Mr. Ulf L&#252;der, for technical support in the biochar laboratory. The authors are also thankful to Ms. Maria Sanchez, and Mr. Jonas Nekat for their volunteer activities in the biogas, and analytical laboratory, respectively. Marcel Schmidt and Antje Schmidt are also acknowledged for their valuable efforts on videography and editing.

1. Anaerobic Digestion of Wheat Straw
Note: For anaerobic digestion in 39&#160;L UASS reactors, use 5-65 mm long raw wheat straw chops as feed. The organic dry matter content of the feedstock in this particular experiment was 85.9% and crude fiber fraction was 46.3%. The UASS reactors are made of stainless steel with an inspection window made of acrylic glass. Two 30 L anaerobic filter (AF) are combined with each 39 L UASS reactor. The AFs are built of transparent acrylic glass. The schematic of the reactor systems are shown in Figure 2 and architectural design described elsewhere4. Details on inoculating and starting up the reactors are given elsewhere5.
<ol>
	<li>Fill each AF with 325 barrel-shaped polyethylene biofilm carriers. 
	Note: The biofilm carriers used have a surface area of 305 m2/m3.</li>
	<li>Set the water pumps for process liquid circulation in both mesophilic and thermophilic reactors for a flow rate of 1.15 L/hr.</li>
	<li>Set heating baths to the desired reactor&#180;s temperature level, 37 &#176;C for the mesophilic and 55 &#176;C for the thermophilic reactor.</li>
	<li>For daily feeding of the UASS reactors, weigh 120 gFM of wheat straw (= 99.5 gVS) for each reactor to achieve an organic loading rate of 2.5 gVS/L&#183;day.</li>
	<li>Open UASS&#180; feeding tube and remove the stamp.</li>
	<li>Pour wheat straw into the diagonal feeding tube and push it into the reactor&#180;s bottom with the help of the feeding stamp. From there on, the straw will float up against a sieve and form the solid-state bed.</li>
	<li>Clean the sealing surface to make sure, it is gastight and then close the feeding tube.</li>
	<li>The pumps will run continuously, conveying 1.2 L/hr&#160;process liquor through the reactor system (UASS and AF).</li>
	<li>Measure biogas flow continuously using drum-type gas meters and store in a 20 L gas bag. 
	Note: Make an exit from the gas bag to the biogas analyzer. In the biogas analyzer, CH4, H2S, O2, CO2, and H2 are measured. First the biogas has to pass 3&#160;different filters to remove the moisture, and other toxic compounds that are harmful for the detector. The analyzer needs to be calibrated once in a week for accurate biogas composition.</li>
	<li>Measure biogas composition regularly using an industrial biogas analyzer. Note: The biogas analyzer can only measure the biogas when the biogas bag is at least half full. For measuring the biogas composition, the valve at the gas bag needs to be opened and wait for the steady biogas composition (it takes about 20-30 sec).</li>
	<li>For process control, measure pH and temperature online using installed pH meter and thermometer.</li>
	<li>Remove approximately 3 kg of digestate (80-90% wet) once a week, which gives a solids retention time (SRT) of 2-3 weeks. Use this digestate as the feed for HTC process. The biogas produced afterwards is sufficient to extrude any air and establish anaerobic conditions within few hours.</li>
	<li>Analyze process liquor and digestate on a weekly basis for their chemical properties (pH, EC, TS, VS, fatty acids, CHNS, ammonia, trace elements, and crude fiber).</li>
</ol>
2. Hydrothermal Carbonization of Wheat Straw Digestate
Note: For hydrothermal carbonization of digestate from step 1, an 18&#160;L batch stirred reactor is used. The controlling and timing of process is effected via reactor controller 4848 and the software SpecView 32 849, running on a computer. In the program, the reactor temperature, heating jacket temperature, pressure, and stirring rate can be shown. Moreover, the program for the process parameters (start temperature, set temperature, heating rate, stirring rate) can be set for each HTC experiments.
<ol>
	<li>Weigh 2.5 kg of straw digestate using a balance with the accuracy of 0.1 g and transfer to the reactor vessel.</li>
	<li>Use the same balance to measure 10 kg makeup water, and pour it into the reactor vessel as well. This will maintain digestate, water ratio 1:4.</li>
	<li>Before pneumatically closing, stir manually the reactor content to prevent blockage of propeller stirrer. Close the reactor and secure it by crosswise tightening the bolts with a force of 50 Nm.</li>
	<li>Set the reaction by the following ramp soak:</li>
	<li>Reach the start temperature of 30 &#176;C in 15 min&#160;from room temperature.
	<ol>
		<li>Set the heating time for reaction temperature of 230 &#176;C is 100 min.</li>
		<li>Hold the final reaction temperature for 6 hr.</li>
		<li>After 6 hr&#160;of holding time, cool the reactor 15 hr&#160;from 230 &#176;C to room temperature.</li>
		<li>Stir the reactor content at 30 rpm throughout the complete HTC process.</li>
		<li>Switch off the stirrer after the cooling phase and purge the gas in a 20 L gas bag.</li>
		<li>Make sure the gas passes through a condensate trap as well as an activated carbon filter.</li>
		<li>Store the gas for further analysis.</li>
	</ol>
	</li>
	<li>After gas sampling, drain the slurry from the vessel to a container through a high temperature, high pressure ball valve and then filter it through a mesh with a pore size of around 0.5 mm.</li>
	<li>Collect the fluid and tare the produced HTC biochar to determine the amount of HTC-produced char compared to feedstock.</li>
</ol>
3. Elemental Analysis of Raw, Digestate, and HTC Biochar of Wheat Straw
Note: For any solid fuel analysis, an elemental analyzer or CHONS analyzer is often used. The elemental composition of atomic carbon, hydrogen, oxygen, nitrogen, and sulfur can be obtained from this analysis. From CHONS, one can estimate the higher heating value or energy value of the fuel. Moreover, the atomic sulfur content will also indicate the quality of the fuel. In this study, an elemental analyzer will be used to determine the fuel value of HTC biochar, raw wheat straw and digestate. As the analyzer only allows a very small sample size, analyze each sample at least three times for better reproducibility.
<ol>
	<li>In a sample pan (tin, 6 x 6 x 12 mm), weigh 30 mg of tungsten(VI) oxide using the specific balance in the elemental package. Note: The precision of such a balance is usually 1 &#181;g. Tungsten(VI) oxide works as a catalyst in the elemental analyzer.</li>
	<li>Weigh 5-10 mg of dry sample and put into the same sample pan, mix it, and wrap it. The wrapped sample pan size should be around 2 x 2 x 5 mm3.</li>
	<li>Place the samples in the autosampler. Note the position of each sample and use sulfonic acid in this elemental analysis as a reference</li>
	<li>Start the Vario software in the computer connected to the Elemental analyzer, define the conditions, samples gas flow, temperatures of the 2&#160;ovens (the 2&#160;ovens are at 1,150&#160;and 850 &#176;C, respectively). Then, define the sample names according to autosampling positions. Start the program. The machine works automatically, performs the analysis, and stores the results in the computer. 
	Note: Elemental CHNS are the output of the elemental analyzer and usually are reported directly on the computer screen.</li>
</ol>

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<li>Reza, M. T., et al. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/pubmed?term=((Hydrothermal+carbonization+for+energy+and+crop+production%5BTitle%5D)+AND+%22Applied+Bioenergy%22%5BJournal%5D)">Hydrothermal carbonization for energy and crop production.</a> Applied Bioenergy. 1, 11-28 (2014).</li>
<li>Reza, M. T., Becker, W., Sachsenheimer, K., Mumme, J. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/pubmed?term=((Hydrothermal+Carbonization+%28HTC%29%3A+Near+Infrared+spectroscopy+and+Partial+Least-Squares+Regression+for+determination+of+Selective+Components+in+HTC+Solid+and+Liquid+Products+Derived+from+Maize+Silage%5BTitle%5D)+AND+%22Bioresource+Technology%22%5BJournal%5D)">Hydrothermal Carbonization (HTC): Near Infrared spectroscopy and Partial Least-Squares Regression for determination of Selective Components in HTC Solid and Liquid Products Derived from Maize Silage.</a> Bioresource Technology. 161, 91-101 (2014).</li>
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The authors have nothing to disclose.

UASS reactors are capable to mitigate the shortcomings discussed in introduction. However, there is much room for improvement. Feeding system and digestate withdrawing are still manual. The UASS system faces problems handling feedstocks larger than 60 mm. The system works better with fibrous feedstocks as they float across the liquid, but other feedstocks like animal manure and sludge might not favor the UASS system. The UASS system is designed in such a way that the process liquor circulates from reactor to AF to the reactor again. However, even 2-5% solid in the circulating liquid was proven to be problematic, as they deposit in the AF or block the pipe entrance and hinder liquid circulation. Chemical analysis of the process liquid is important, as the production of free fatty acid and nitrogen can change the microbial system resulting in uncharacteristic biogas production. The UASS system is robust, and can run more than 200 days without showing any significant problems. The tubes connecting from pumps to reactors to AFs need to be replaced every alternative month. The water level in the waterbath needs to be checked on a weekly basis and refilled if necessary.
HTC of wet digestate is very effective for waste treatment as well as producing solid biofuel. The dewateribility of the solid product will also be facilitated by the HTC process as shown in the Figure 7. However, HTC of digestate needs to be performed as soon as possible, preferably the same day that the digestate is removed. Otherwise, the digestate starts degrading biologically, which is not favorable for HTC. As HTC is a high temperature (200-260 &#176;C) and high pressure (20-50 bar) process, taking necessary precautions throughout the HTC procedure is very important. All the connections are checked at least once a month to make sure they are gas-tight. HTC process liquid has a higher concentration of furfural, 5-HMF, and phenolic compounds, which are rated as toxicants. So, it is recommended to use a face mask and gloves while handling HTC process liquid, especially when HTC process liquor is drained from reactor vessel to another container. Although HTC has many advantages for handling wet feedstock like digestate, it is still a batch process. In an economic evaluation, HTC batch process will be hard to justify. More research is thus required to facilitate continuous operation of HTC.
Elemental analysis is an effective method for homogeneous solid substrates, but not for heterogeneous substrates. As solid biofuel is usually heterogeneous and elemental analyzer only allows 5-10 mg of sample size, it is recommended to perform at least three replicates and use average. Another limitation of elemental analysis is measuring solid substrates with high ash content. Elemental analyzers only measure CHONS, and no other inorganics. So, elemental analysis of high ash solid substrates might not reveal the actual CHONS concentrations. Sample preparation in elemental analysis is vital, as sample needs to be wrapped precisely, otherwise, there will be an inconsistency in analyses. Fuel value of the solid fuel can be estimated from CHONS, but it is recommended to use a bomb calorimeter for precise fuel value determination.
About 92-161 L of methane was produced per kilogram of volatile solid in the feed. The volatile solid or organic total solid of the dry wheat straw was 86.9%. Dry digestate has lower atomic oxygen and hydrogen concentration, which is another indication of degradation of polysaccharides and simple sugar degradation during anaerobic digestion22,23. Moreover, lower H, and O concentrations increase the HHV of the digestate24. HHV of dry digestate is 22% higher than dry raw feedstock. The similar results are obtained with a detailed statistical analysis by Pohl et al23.
Digestates from anaerobic digestion contains 80-90% water6. These are hydrophilic and water is partially bound in microbial or plant cells. As a result dewatering or drying of digestates is cumbersome and very energy intensive. For example, 2 kg of dry digestate binds 8 kg of water (80% wet), which requires 20.7 MJ of heat to dry digestate. Moreover, it tends to bio-degrade relatively quickly in ambient conditions, loses plant nutrients, and releases GHG (greenhouse gas) emissions such as N2O and CH4. So, despite higher energy potential, fresh digestate cannot be used directly as a solid fuel. It would need to be dried right after the digestion20.
From Table 1, it can be shown that the dry digestate has a similar atomic carbon content as raw straw, and they are visually similar before and after anaerobic digestion (Figure 6). This suggests that lignin and lignin-encrusted cellulose are mostly unreacted. However, a mass yield of 63% observed, meaning processed straw is 37% lighter than dry raw straw. Similar elemental carbon concentration means no carbonization occurred during anaerobic digestion22. As shown in Figure 7, HTC biochar from digestate (thermophilic) is very stable and soft. Because of the significant increase in hydrophobicity, it can literally submerge into water for months without its physical and chemical structure being affected12,25. The hydrophobicity also enhances dewatering of HTC biochar14. Structure of the straw is not discernable in the HTC biochar anymore, which means that cellulose might have been reacted. A significant carbonization is observed in HTC biochar along with the reduction of atomic oxygen. This is another indication of cellulose being reacted rather than lignin. Atomic carbon concentration in lignin is much higher than that of cellulose24-29. As a result, HTC biochar has an HHV of 29.6 MJ/kg, which are 61% higher than raw straw and 32% higher than dry digestate, respectively.
HHV of HTC processed straw is 28.8 MJ/kg, which is also similar to that of HTC processed straw digestate (29.6 MJ/kg). However, mass yield is 40.7% higher in HTC straw than that of HTC digestate with comparing to raw feedstock. As a result, if 1 kg of raw straw (18.4 MJ) is hydrothermally carbonized, HTC straw biochar will have the potential of 11.0 MJ. Otherwise, if same amount is applied to AD and HTC, a total 13.2 MJ bioenergy, in forms of biomethane (5.2 MJ) and HTC biochar from digestate (8.0 MJ), can be produced (Figure 8). Also, liquid phase of the UASS process is a potential liquid fertilizer. Moreover, HTC biochar might have higher potential on high value material use or use as soil amendment. For the carbon sequestration or carbon cycle point of view, material use of HTC biochar is more feasible that energy production.
Anaerobic digestion combined with hydrothermal carbonization can yield more bioenergy than the individual processes. However, a cascaded design is needed for better efficiency. The overall energy balance, followed by an economic evaluation, is required to validate this process. Future research should include use of HTC liquor and post-treatment (chemical or biological) of HTC biochar. Also, automation of both UASS and HTC systems will be needed. This study was carried on using a lab-scale UASS and HTC reactor, but scale-up of the process would be necessary if the process is to be commercialized.

Finding renewable and sustainable energy sources are major concerns in the world&#8217;s energy sector. Recently, the United Nations reported that up to 77% of the world&#8217;s energy in 2050 will be expected from renewable sources1. Lignocellulosic biomass such as straw, grasses, rice hulls, corn cobs have no conflicts with the food versus fuel issue. Moreover, biomass is probably the only renewable energy source with structural carbon, compared to other renewable energy sources such as wind, solar, and water2. However, handling characteristics, lower bulk density, high ash content, and lower energy content hinder the use of lignocellulosic biomass for energy production2.
Anaerobic digestion (AD) is one of the prime examples of producing bioenergy from waste biomass.3 In general, there are four degradation steps involve in anaerobic digestion as shown in Figure 14. In first three consecutive steps, the polysaccharides of the biomass are converted into organic acids. In the final step, methanogenic organisms produce biomethane. Traditional AD is a time and energy consuming process. The continuous stirring reduces overall economics of AD, especially for AD of lignocellulosic biomass. A novel upflow anaerobic solid-state (UASS) reactor has the potential to overcome the stated shortcomings (Figure 2)4. Spontaneous solid-liquid separations is one of the significant advantages of UASS, since the designed facilitates biogas bubbles to lift unreacted solid residues upwards5. This eliminate the use of stirrer and therefore reduces the consumption of on-site power. Moreover, liquid circulation ensures distribution of microorganisms and metabolites throughout the reactor as well5. Compared to solid biofuels, biogas is easier to handle, and leaves little or no residue. In fact, the specific energy density of biogas is several times higher raw biomass4. However, AD favors simple polysaccharides like starch, fatty acids, and hemicellulose1. As a result, cellulose, and lignin, major portion of fibrous lignocellulosic biomass like wheat straw, remains as a solid digestate after AD5. Although, biogas production varies from the feedstock, type of microorganisms, reaction temperature, and reaction time, a huge amount of digestate is usually produced.
While biogas is used for energy, digestates (up to 90% water) are usually stored in a fermentation residue-depot to collect remaining methane emissions. Afterwards these are dried and spread on the cropland to improve soil fertility and water retention capacity. High inorganic content often hinder digestate directly for fuel, as high amounts of slag might corrode the equipment6. Hydrothermal carbonization (HTC) is a thermochemical treatment process especially designed for wet feedstock, where biomass (with 80-90% water) is heated up to 200-260 &#176;C at water saturation pressure and hold for 0.5-6 h (Figure 3)7,8.Subcritical water has the maximum ionic product at 200-260 &#176;C, which means water under these conditions is reactive and behaves as a mild acid and a mild base simultaneously9. Hemicellulose, along with other extractives, degrade around 180-200 &#176;C, while cellulose reacts around 220-230 &#176;C, and lignin reacts at relatively higher temperature (&#62;250 oC), but much slower than cellulose and hemicellulose10. Due to significant dehydration and decarboxylation, HTC results solid product named HTC biochar, with mass yield (dry HTC biochar/dry feed) of 40-80%, liquor containing carboxylic acids, furan derivatives, phenolic substances, and sugar monomers, and 5-10% CO2 rich gaseous product11. During HTC, oxygen containing volatile substances are significantly reduced and thus leave a carbon-rich solid. HTC biochar is also stable, hydrophobic, and friable compare to raw moist feedstock12,13. Due to its hydrophobic characteristics, dewateribility of HTC biochar increases several times compared to raw digestate or even raw biomass.14-18 Moreover, HTC biochar has fuel values similar to lignite coal16,17. However, cellulose and lignin partially degrade in the HTC environment18.
Now hemicellulose and cellulose in the biomass contribute to biogas during AD, while cellulose and lignin mostly contribute to solid HTC biochar4,5. Thus, the combination of AD-HTC can potentially increase overall bioenergy yield. Hoffmann et al. simulated a similar combination but using AD and HTL (hydrothermal liquefaction) rather than AD-HTC19. HTL is a common method of liquefying biomass fraction and liquid product has high fuel value [43.1 MJ/kg]. However, HTL requires very high pressure (250 bar) compare to HTC (10-50 bar), which implies a high installation and operation costs than HTC. Again, the combination sequence of AD and HTC can be questioned as Wirth et al. recently reported AD of HTC process liquid20. However, an effective AD depends on the sugar concentration in the feedstocks. Sugars in HTC process liquid, produced during hydrolysis, often degrade rapidly under subcritical water. That&#8217;s why AD before HTC is more favorable in terms of bioenergy. However, AD of HTC process liquid can produce additional bioenergy, in which case, the combination sequence would be AD-HTC-AD.
The aim of the work was to evaluate the integration of AD and HTC processes for bioenergy production (Figure 3). The biogas production potential for thermophilic and mesophilic AD from UASS reactor was evaluated at a continuous operation of more than 200 days. Subsequently, HTC biochar production from digestate was also studied. The mass and energy balance of the cascaded AD-HTC was carried out and compared with the individual processes.

<table><tbody><tr><td>UASS reactor</td><td></td><td></td><td>Patented design</td></tr><tr><td>Balance</td><td>KERN</td><td>440-55N</td><td>0.2 g precision</td></tr><tr><td>Biofilm carrier</td><td>RVT Process Equipment GmbH, Germany</td><td>Bioflow 40</td><td>Establish 305 m&lt;sup&gt;2&lt;/sup&gt;/m&lt;sup&gt;3&lt;/sup&gt;</td></tr><tr><td>Heating bath</td><td>Lauda-Konigshofen, Germany</td><td>Lauda Ecoline 011</td><td>Ensure mesophilic and thermophilic temperature</td></tr><tr><td>Recirculation pump</td><td>Heidolph pumpdrive</td><td>5201</td><td></td></tr><tr><td>Wheat straw</td><td>Dittmannsdorfer Milch GmbH, Germany</td><td></td><td>5-65 mm length</td></tr><tr><td>Biogas analyzer</td><td>Pronova, Germany</td><td>SSM 6000</td><td></td></tr><tr><td>Gas meter</td><td>Ritter, Germany</td><td></td><td>Drum type</td></tr><tr><td>HTC reactor</td><td>Parr instrument, Moline, IL USA</td><td>Parr 4555</td><td>5 gallon volume</td></tr><tr><td>HTC Temperature controller</td><td>Parr instrument, Moline, IL USA</td><td>4848</td><td>K type thermocouple</td></tr><tr><td>Balance</td><td></td><td>KERN FKB</td><td>0.1 g precision</td></tr><tr><td>Heating system</td><td>Parr</td><td>A1600EEE</td><td>Band heater, 2 &amp;deg;C/min</td></tr><tr><td>Software</td><td>SpecView</td><td>32849</td><td>Digital monitoring and programming interface</td></tr><tr><td>Catalyst</td><td></td><td>Tungsten(VI) oxide</td><td>Elemental analyzer</td></tr><tr><td>Balance</td><td>Mettler Toledo</td><td>SN-1128123281</td><td>1 &amp;micro;g precision</td></tr><tr><td>Sample pan</td><td>Elemental Analyssystem GmbH</td><td>Tin 6 x 6 x 12 mm pan</td><td>Elemental analysis</td></tr><tr><td>Drying oven</td><td>Binder GmbH, Germany</td><td>FP 115</td><td>105 &amp;deg;C oven</td></tr><tr><td>Elemental analyzer</td><td>Vario</td><td>EL III</td><td>CHNS analyzer</td></tr></tbody></table>

evaluation of integrated anaerobic digestion and hydrothermal carbonization for bioenergy production

Lignocellulosic biomass is one of the most abundant yet underutilized renewable energy resources. Both anaerobic digestion (AD) and hydrothermal carbonization (HTC) are promising technologies for bioenergy production from biomass in terms of biogas and HTC biochar, respectively. In this study, the combination of AD and HTC is proposed to increase overall bioenergy production. Wheat straw was anaerobically digested in a novel upflow anaerobic solid state reactor (UASS) in both mesophilic (37 &#176;C) and thermophilic (55 &#176;C) conditions. Wet digested from thermophilic AD was hydrothermally carbonized at 230 &#176;C for 6 hr for HTC biochar production. At thermophilic temperature, the UASS system yields an average of 165 LCH4/kgVS&#160;(VS: volatile solids) and 121 L CH4/kgVS&#160;at mesophilic AD over the continuous operation of 200 days. Meanwhile, 43.4 g of HTC biochar with 29.6 MJ/kgdry_biochar was obtained from HTC of 1 kg digestate (dry basis) from mesophilic AD. The combination of AD and HTC, in this particular set of experiment yield 13.2 MJ of energy per 1 kg of dry wheat straw, which is at least 20% higher than HTC alone and 60.2% higher than AD only.

Anaerobic digestion
The biogas experiments revealed that the UASS system is capable of utilizing 38% and 50% of the methane forming potential at mesophilic (37 &#176;C) and thermophilic (55 &#176;C) operation, respectively. At thermophilic AD, the UASS system yields an average of 165 LCH4/kgVS&#160;(VS: volatile solids) and 121 LCH4/kgVS&#160;at mesophilic AD for a 200 days of continuous operation (Figure 4). Those performance values have been calculated from the quantitative and qualitative analysis of the biogas related to the dry feedstock basis.
The biomethane potential for the wheat straw was determined (following VDI Guideline 4630) to be 304.3&#160;LCH4/kgVS&#160;for thermophilic and 244.2 LCH4/kgVS&#160;for mesophilic operation, respectively, and presented in Figure 5&#160;21. In terms of quality, biogas produced by UASS contained between 41% and 61% of methane (Figure 5).
HTC of digestate
Figure 6 shows dry straw, dry digestate derived from straw by AD, and HTC biochar derived from dry digestate by HTC. Dry digestate looks similar to the dry straw, which is only a bit darker in color. For this work, digestate from thermophilic conditions were considered for HTC. As shown in Table 1, 63% of the total mass remains in the digestate (Table 1). Dry HTC biochar is lighter than dry raw straw, probably due to the degradation of monomers and simple polymers by thermophilic microorganisms during AD.
Figure 7 shows the hydrophobic behavior, and softness of HTC biochar. During HTC, the fibrous crystalline structures are destroyed and produce a soft amorphous carbon-rich HTC biochar16,17,28. It can be seen from Table 1 that the mass yield of digestate and raw straw derived HTC biochar are 43.4%, and 38.3%, respectively. The solid product, HTC biochar is very hydrophobic12; it can stay in contact with water for a prolonged time13. Also it is very soft, as it barely requires any pressure to pulverize it. For coal-to-power industry, maintaining softness of the feedstock is very important, as this can eliminate the expansive pulverizing steps.
Elemental analysis
From elemental compositions presented in Table 1, it can be seen that elemental carbon and hydrogen remain the same in the solid throughout the anaerobic digestion. Elemental carbon increases and hydrogen decreases during HTC. Most of the elemental nitrogen remains in the solid since the elemental nitrogen content is increased during both digestion and HTC processes. Since sulfur in wheat straw is trace, the concentration of elemental sulfur is not presented in the results. Elemental oxygen content was calculated by subtracting C, H, and N from 100% and also presented in Table 1, assuming the feedstock consists of CHONS only. The oxygen concentration decreased dramatically during HTC, while it remains similar during digestion.
<img alt="Figure 1" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig1highres.jpg" width="500" /> 
Figure 1. Basic concept and steps of anaerobic digestion. This figure describes the basic concepts of anaerobic digestion. In this figure, four general steps (hydrolysis, acedogenesis, acetogenesis, and methanogenesis) of anaerobic digestion are presented
<img alt="Figure 2" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig2highres.jpg" width="500" /> 
Figure 2: Schematic diagram of the laboratory scale UASS reactor for anaerobic digestion. This is the schematic of UASS reactor system. Here the UASS reactor and anaerobic filter (AF) are shown connected by a liquid stream, where fatty acids produced in the UASS reactor come to AF and methane is produced. From the bottom of the AF, another liquid stream is drawn to UASS, where microorganisms are going from AF to UASS reactor.
<img alt="Figure 3" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig3highres.jpg" width="500" /> 
Figure 3. (top) Concept of HTC of lignocellulosic biomass, (bottom) integration concept of anaerobic digestion and HTC *cellulose will be partially reacted24 . In this block diagram, it can be seen that different fiber components come into contact with subcritical water and are converted into HTC biochar (Coal type).
<img alt="Figure 4" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig4highres.jpg" width="500" /> 
Figure 4.&#160;Methane production from UASS reactor in both thermophilic and mesophilic conditions with the anaerobic filter. These are experimental results of UASS reactor for 210 days of operation for both thermophilic and mesophilic conditions. The X-axis is days of operation, while the Y-axis is the methane yield (LCH4/kgVS) compared to volatile solid (VS).
<img alt="Figure 5" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig5highres.jpg" width="500" /> 
Figure 5.&#160;Methane fraction of biogas from UASS reactor in both thermophilic and mesophilic conditions. These are experimental results of UASS reactor for 210 days of operation under both thermophilic and mesophilic conditions. The X-axis is days of operation, while Y-axis is the methane fraction (%) in the biogas. Values given are averages from duplicates.
<img alt="Figure 6" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig6highres.jpg" width="500" /> 
Figure 6.&#160;(Left to right) Dry wheat straw, dry wheat straw digestate, and HTC biochar of wheat straw digestate. This is the real time image of the different states of wheat straw. Here in this figure, the effect of anaerobic digestion (AD) and HTC can be visible. The fiber structure is still visible in the digestate, while it becomes powdery after HTC.
<img alt="Figure 7" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig7highres.jpg" width="500" /> 
Figure 7.&#160;Hydrophobicity of the HTC biochar (left), friability of the HTC biochar (right). This is again the real time image of hydrophobicity and friability of HTC biochar. In the first image, HTC biochar is sunk under the water, while the next two images the condition of biochar before and after hard-crushing are shown.
<img alt="Figure 8" fo:content-width="5in" src="/files/ftp_upload/51734/51734fig8highres.jpg" width="500" /> 
Figure 8.&#160;(top) Bioenergy potential by anaerobic digestion (AD) from 1 kg of raw wheat straw and (bottom) bioenergy potential by integrating AD-HTC from 1 kg of dry wheat straw. This is a figure to evaluate the necessity of combination concepts. The block diagram shows how much energy is extracting by AD and HTC from the feedstock.
<img alt="Table 1" fo:content-width="7in" src="/files/ftp_upload/51734/51734table1v2.jpg" width="700" /> 
Table 1.&#160;Elemental analysis, HHV, mass yield, and fiber analysis of raw wheat straw, digestate (thermophilic), and corresponding HTC biochar. HHV is calculated from CHNS composition as shown in literature18,24.&#160;Table 1 is the experimental results of elemental analysis, and mass yield after AD and HTC. Lignin, cellulose and hemicellulose are measured by van Soest fiber analysis [12]. Note: n.a is not analyzed. <a href="https://jove.unicartagenaproxy.elogim.com/files/ftp_upload/51734/51734table1.jpg" target="_blank">Please click here to view a larger version of this table.</a>

Watch this Scientific Journal Video about Evaluation of Integrated Anaerobic Digestion and Hydrothermal Carbonization for Bioenergy Production at JoVE.com

Evaluation of Integrated Anaerobic Digestion and Hydrothermal Carbonization for Bioenergy Production

A novel Upflow Anaerobic Solid State (UASS) reactor was used for biogas production from fibrous feedstock. Digestate from UASS reactor was hydrothermally carbonized into HTC biochar in a pressurized batch reactor. The integration of the two bioenergy concepts was applied in this study to increase overall bioenergy production.

Lignocellulosic biomass is one of the most abundant yet underutilized renewable energy resources. Both anaerobic digestion (AD) and hydrothermal ...

evaluation-integrated-anaerobic-digestion-hydrothermal-carbonization

Universidad de Cartagena UDEC

Research

JoVE Journal

Environment

25.5K Views.  Leibniz Institute for Agricultural Engineering. A novel Upflow Anaerobic Solid State (UASS) reactor was used for biogas production from fibrous feedstock. Digestate from UASS reactor was hydrothermally carbonized into HTC biochar in a pressurized batch reactor. The integration of the two bioenergy concepts was applied in this study to increase overall bioenergy production.

Video: Evaluation of Integrated Anaerobic Digestion and Hydrothermal Carbonization for Bioenergy Production

Biomass Conversion to Produce Hydrocarbon Liquid Fuel Via Hot-vapor Filtered Fast Pyrolysis and Catalytic Hydrotreating

Lignocellulosic biomass conversion to produce biofuels has received significant attention because of the quest for a replacement for fossil fuels. Among the various thermochemical and biochemical routes, fast pyrolysis followed by catalytic hydrotreating is considered to be a promising near-term opportunity. This paper reports on experimental methods used 1) at the National Renewable Energy Laboratory (NREL) for fast pyrolysis of lignocellulosic biomass to produce bio-oils in a fluidized-bed reactor and 2) at Pacific Northwest National Laboratory (PNNL) for catalytic hydrotreating of bio-oils in a two-stage, fixed-bed, continuous-flow catalytic reactor. The configurations of the reactor systems, the operating procedures, and the processing and analysis of feedstocks, bio-oils, and biofuels are described in detail in this paper. We also demonstrate hot-vapor filtration during fast pyrolysis to remove fine char particles and inorganic contaminants from bio-oil. Representative results showed successful conversion of biomass feedstocks to fuel-range hydrocarbon biofuels and, specifically, the effect of hot-vapor filtration on bio-oil production and upgrading. The protocols provided in this report could help to generate rigorous and reliable data for biomass pyrolysis and bio-oil hydrotreating research.

Experimental methods for fast pyrolysis of lignocellulosic biomass to produce bio-oils and for the catalytic hydrotreating of bio-oils to produce fuel range hydrocarbons are presented. Hot-vapor filtration during fast pyrolysis to remove fine char particles and inorganic contaminants from bio-oil was also assessed.

Lignocellulosic biomass conversion to produce biofuels has received significant attention because of the quest for a replacement for fossil fuels. Among ...

Biochemistry

Transcript and Metabolite Profiling for the Evaluation of Tobacco Tree and Poplar as Feedstock for the Bio-based Industry

The global demand for food, feed, energy, and water poses extraordinary challenges for future generations. It is evident that robust platforms for the exploration of renewable resources are necessary to overcome these challenges. Within the multinational framework MultiBioPro we are developing biorefinery pipelines to maximize the use of plant biomass. More specifically, we use poplar and tobacco tree (Nicotiana glauca) as target crop species for improving saccharification, isoprenoid, long chain hydrocarbon contents, fiber quality, and suberin and lignin contents. The methods used to obtain these outputs include GC-MS, LC-MS and RNA sequencing platforms. The metabolite pipelines are well established tools to generate these types of data, but also have the limitations in that only well characterized metabolites can be used. The deep sequencing will allow us to include all transcripts present during the developmental stages of the tobacco tree leaf, but has to be mapped back to the sequence of Nicotiana tabacum. With these set-ups, we aim at a basic understanding for underlying processes and at establishing an industrial framework to exploit the outcomes. In a more long term perspective, we believe that data generated here will provide means for a sustainable biorefinery process using poplar and tobacco tree as raw material. To date the basal level of metabolites in the samples have been analyzed and the protocols utilized are provided in this article.

Plant biomass offers a renewable resource for multiple products, including fuel, feed, food, and a variety of materials. In this paper we investigate the properties of tobacco tree (Nicotiana glauca) and poplar as suitable sources for a biorefinery pipeline.

The global demand for food, feed, energy, and water poses extraordinary challenges for future generations. It is evident that robust platforms for the ...

Integrated Field Lysimetry and Porewater Sampling for Evaluation of Chemical Mobility in Soils and Established Vegetation

Potentially toxic chemicals are routinely applied to land to meet growing demands on waste management and food production, but the fate of these chemicals is often not well understood. Here we demonstrate an integrated field lysimetry and porewater sampling method for evaluating the mobility of chemicals applied to soils and established vegetation. Lysimeters, open columns made of metal or plastic, are driven into bareground or vegetated soils. Porewater samplers, which are commercially available and use vacuum to collect percolating soil water, are installed at predetermined depths within the lysimeters. At prearranged times following chemical application to experimental plots, porewater is collected, and lysimeters, containing soil and vegetation, are exhumed. By analyzing chemical concentrations in the lysimeter soil, vegetation, and porewater, downward leaching rates, soil retention capacities, and plant uptake for the chemical of interest may be quantified. Because field lysimetry and porewater sampling are conducted under natural environmental conditions and with minimal soil disturbance, derived results project real-case scenarios and provide valuable information for chemical management. As chemicals are increasingly applied to land worldwide, the described techniques may be utilized to determine whether applied chemicals pose adverse effects to human health or the environment.

Field lysimetry and porewater sampling allow researchers to evaluate the fate of chemicals applied to soils and established vegetation. The goal of this protocol is to demonstrate how to install required instrumentation and collect samples for chemical analysis during integrated field lysimetry and porewater sampling experiments.

Potentially toxic chemicals are routinely applied to land to meet growing demands on waste management and food production, but the fate of these chemicals ...

Development of Sulfidogenic Sludge from Marine Sediments and Trichloroethylene Reduction in an Upflow Anaerobic Sludge Blanket Reactor

The importance of microbial sulfate reduction relies on the various applications that it offers in environmental biotechnology. Engineered sulfate reduction is used in industrial wastewater treatment to remove large concentrations of sulfate along with the chemical oxygen demand (COD) and heavy metals. The most common approach to the process is with anaerobic bioreactors in which sulfidogenic sludge is obtained through adaptation of predominantly methanogenic granular sludge to sulfidogenesis. This process may take a long time and does not always eliminate the competition for substrate due to the presence of methanogens in the sludge. In this work, we propose a novel approach to obtain sulfidogenic sludge in which hydrothermal vents sediments are the original source of microorganisms. The microbial community developed in the presence of sulfate and volatile fatty acids is wide enough to sustain sulfate reduction over a long period of time without exhibiting inhibition due to sulfide. 
This protocol describes the procedure to generate the sludge from the sediments in an upflow anaerobic sludge blanket (UASB) type of reactor. Furthermore, the protocol presents the procedure to demonstrate the capability of the sludge to remove by reductive dechlorination a model of a highly toxic organic pollutant such as trichloroethylene (TCE). The protocol is divided in three stages: (1) the formation of the sludge and the determination of its sulfate reducing activity in the UASB, (2) the experiment to remove the TCE by the sludge, and (3) the identification of microorganisms in the sludge after the TCE reduction. Although in this case the sediments were taken from a site located in Mexico, the generation of a sulfidogenic sludge by using this procedure may work if a different source of sediments is taken since marine sediments are a natural pool of microorganisms that may be enriched in sulfate reducing bacteria.

Microbial sulfate reduction is a process of great importance in environmental biotechnology. The success of the sulfidogenic reactors depends among other factors on the microbial composition of the sludge. Here, we present a protocol to develop sulfidogenic sludge from hydrothermal vents sediments in a UASB reactor for reductive dechlorination purposes.

The importance of microbial sulfate reduction relies on the various applications that it offers in environmental biotechnology. Engineered sulfate ...

Continuously-stirred Anaerobic Digester to Convert Organic Wastes into Biogas: System Setup and Basic Operation

Anaerobic digestion (AD) is a bioprocess that is commonly used to convert complex organic wastes into a useful biogas with methane as the energy carrier 1-3. Increasingly, AD is being used in industrial, agricultural, and municipal waste(water) treatment applications 4,5. The use of AD technology allows plant operators to reduce waste disposal costs and offset energy utility expenses. In addition to treating organic wastes, energy crops are being converted into the energy carrier methane 6,7. As the application of AD technology broadens for the treatment of new substrates and co-substrate mixtures 8, so does the demand for a reliable testing methodology at the pilot- and laboratory-scale.
Anaerobic digestion systems have a variety of configurations, including the continuously stirred tank reactor (CSTR), plug flow (PF), and anaerobic sequencing batch reactor (ASBR) configurations 9. The CSTR is frequently used in research due to its simplicity in design and operation, but also for its advantages in experimentation. Compared to other configurations, the CSTR provides greater uniformity of system parameters, such as temperature, mixing, chemical concentration, and substrate concentration. Ultimately, when designing a full-scale reactor, the optimum reactor configuration will depend on the character of a given substrate among many other nontechnical considerations. However, all configurations share fundamental design features and operating parameters that render the CSTR appropriate for most preliminary assessments. If researchers and engineers use an influent stream with relatively high concentrations of solids, then lab-scale bioreactor configurations cannot be fed continuously due to plugging problems of lab-scale pumps with solids or settling of solids in tubing. For that scenario with continuous mixing requirements, lab-scale bioreactors are fed periodically and we refer to such configurations as continuously stirred anaerobic digesters (CSADs).
This article presents a general methodology for constructing, inoculating, operating, and monitoring a CSAD system for the purpose of testing the suitability of a given organic substrate for long-term anaerobic digestion. The construction section of this article will cover building the lab-scale reactor system. The inoculation section will explain how to create an anaerobic environment suitable for seeding with an active methanogenic inoculum. The operating section will cover operation, maintenance, and troubleshooting. The monitoring section will introduce testing protocols using standard analyses. The use of these measures is necessary for reliable experimental assessments of substrate suitability for AD. This protocol should provide greater protection against a common mistake made in AD studies, which is to conclude that reactor failure was caused by the substrate in use, when really it was improper user operation 10.

Laboratory-scale anaerobic digesters allow scientists to research new ways of optimizing existing applications of anaerobic biotechnology and to evaluate the methane producing potential of various organic wastes. This article introduces a generalized model for the construction, inoculation, operation, and monitoring of a laboratory-scale continuously stirred anaerobic digester.

Anaerobic digestion (AD) is a bioprocess that is commonly used to convert complex organic wastes into a useful biogas with methane as the energy carrier ...

Bioengineering

Reducing Willow Wood Fuel Emission by Low Temperature Microwave Assisted Hydrothermal Carbonization

Biomass is a sustainable fuel, as its CO2 emissions are reintegrated in biomass growth. However, the inorganic precursors in the biomass cause a negative environmental impact and slag formation. The selected short rotation coppice (SRC) willow wood has a high ash content (<img alt="Equation 1" src="/files/ftp_upload/58970/58970eq1.jpg" /> = 1.96%) and, therefore, a high content of emission and slag precursors. Therefore, the reduction of minerals from SRC willow wood by low temperature microwave assisted hydrothermal carbonization (MAHC) at 150 &#176;C, 170 &#176;C, and 185 &#176;C is investigated. An advantage of MAHC over conventional reactors is an even temperature conductance in the reaction medium, as microwaves penetrate the whole reactor volume. This allows a better temperature control and a faster cooldown. Therefore, a succession of depolymerization, transformation and repolymerization reactions can be analyzed effectively. In this study, the analysis of the mass loss, ash content and composition, heating values and molar O/C and H/C ratios of the treated and untreated SCR willow wood showed that the mineral content of the MAHC coal was reduced and the heating value increased. The process water showed a decreasing pH and contained furfural and 5-methylfurfural. A process temperature of 170 &#176;C showed the best combination of energy input and ash component reduction. The MAHC allows a better understanding of the hydrothermal carbonization process, while a large-scale industrial application is unlikely because of the high investment costs.

A protocol for the emission precursor depletion from low quality biomass by low temperature microwave assisted hydrothermal carbonization treatment is presented. This protocol includes the microwave parameters and the analysis of the biocoal product and process water.

Biomass is a sustainable fuel, as its CO2 emissions are reintegrated in biomass growth. However, the inorganic precursors in the biomass cause a negative ...

Chemistry

Carbon Sequestration and Soil Enhancement Through Onsite Biochar Production

Producing, Characterizing and Quantifying Biochar in the Woods Using Portable Flame Cap Kilns

One of the biggest challenges in utilizing non-commercial forest biomass is its widely distributed nature. The best solution to the biomass problem, to avoid expensive and carbon-intensive processing (chipping) and transportation costs, is to process it onsite. However, conventional burn piles have destructive impacts on forest soil and provide no benefits other than fuel reduction. Converting forest slash to biochar onsite has many ecological advantages over the current practice of slash disposal by incineration in burn piles, including reduced soil heating and particulate emissions, along with multiple benefits of the biochar to forest soil health and water holding capacity when left in place. Making biochar onsite in the woods is a way to return a pyrogenic carbon component to forest soils that has been missing due to the recent history of fire suppression. Biochar is also a leading method of carbon removal and sequestration for climate change mitigation. In this study, we document a method for making biochar using a portable biochar kiln. This low-cost method utilizes hand crews equipped with water for quenching kilns before the biochar burns to ash. Simple techniques for quantifying and characterizing the biochar produced are incorporated into the method for the purpose of measuring impact and qualifying for carbon removal certificates to help pay for the cost of the work. We describe the CM002 Component Methodology that provides standardized procedures for the quantification of GHG benefits during three stages of the process: waste biomass sourcing, biochar production, and biochar soil application. The CM002 Methodology is based on international best practices, including the most recent VCS methodology VM0044 Standards and EBC C-Sink Artisan Standards. Reliable quantification methods utilizing appropriate safety factors are the first essential step toward eligibility for carbon removal finance.

Author Spotlight: On-Site Biochar Production for Woody Debris Incineration in Forestry 

New methods for disposing of forestry slash piles in place produce pyrogenic carbon for restoring forest soil health and for carbon removal and sequestration. Here, we present a biochar production method integrating a new carbon removal accounting methodology and a digital application.

One of the biggest challenges in utilizing non-commercial forest biomass is its widely distributed nature. The best solution to the biomass problem, to ...

Microalgal Cultivation for Biomethane Obtention from Swine Waste Biogas

Biogas Purification through the use of a Microalgae-Bacterial System in Semi-Industrial High Rate Algal Ponds

In recent years, a number of technologies have emerged to purify biogas into biomethane. This purification entails a reduction in the concentration of polluting gases such as carbon dioxide and hydrogen sulfide to increase the content of methane. In this study, we used a microalgal cultivation technology to treat and purify biogas produced from organic waste from the swine industry to obtain ready-to-use biomethane. For cultivation and purification, two 22.2 m3 open-pond photobioreactors coupled with an absorption-desorption column system were set up in San Juan de los Lagos, Mexico. Several recirculation liquid/biogas ratios (L/G) were tested to obtain the highest removal efficiencies; other parameters, such as pH, dissolved oxygen (DO), temperature, and biomass growth, were measured. The most efficient L/Gs were 1.6 and 2.5, resulting in a treated biogas effluent with a composition of 6.8%vol and 6.6%vol in CO2, respectively, and removal efficiencies for H2S up to 98.9%, as well as maintaining O2 contamination values of less than 2%vol. We found that pH greatly determines CO2 removal, more so than L/G, during cultivation because of its participation in the photosynthetic process of microalgae and its ability to vary pH when solubilized due to its acidic nature. DO, and temperature oscillated as expected from the light-dark natural cycles of photosynthesis and the time of day, respectively. Biomass growth varied with CO2 and nutrient feeding as well as reactor harvesting; however, the trend remained primed for growth.

Author Spotlight: Scaling Microalgal Biotechnology for Enhanced Biomethane Production 

Air pollution impacts the quality of life of all organisms. Here, we describe the use of microalgae biotechnology for the treatment of biogas (simultaneous removal of carbon dioxide and hydrogen sulfide) and the production of biomethane through semi-industrial open high-rate algal ponds and subsequent analysis of treatment efficiency, pH, dissolved oxygen, and microalgae growth.

In recent years, a number of technologies have emerged to purify biogas into biomethane. This purification entails a reduction in the concentration of ...

Respirometry Protocol for Anaerobic Digestion of Food Waste and Sludge

Measuring Biomethane Potential of Food Scrap Waste Anaerobically Co&#45;Digested with Waste&#45;Activated Sludge Using Respirometry

The use of respirometry to study the biokinetics of microbiota treating wastewater or digesting wastewater sludges has become more prevalent over the last few decades. The use of respirometry to examine the biokinetics of anaerobic microbiota co-digesting organic waste streams such as wastewater sludge and food scrap is an area of active research. To date, no visualized protocol has been published on the topic. Accordingly, in this protocol, we configured a respirometer to measure methane production and flow rate over time using three different food-to-microorganism (F:M) ratios and food scrap waste and waste-activated sludge as substrates. The resulting data, coupled with substrate utilization measurements, provides the basis for understanding how different substrate concentrations influence the rate at which anaerobic microbiota produce methane. Additionally, this protocol presents a method to develop biokinetic parameters (e.g., methane production rate constant and yield). Others can use this respirometry protocol to examine organic degradation under anaerobic conditions and develop microbial parameters.

Author Spotlight: Advancing Anaerobic Microbiota Research Using a Novel Respirometry Protocol

This protocol describes a best practice for determining methane production and microbial kinetic parameters using respirometry for anaerobic microbiota co-digesting food scrap waste and waste-activated sludge.

The use of respirometry to study the biokinetics of microbiota treating wastewater or digesting wastewater sludges has become more prevalent over the last ...

Transformation of Organic Household Leftovers into a Peat Substitute

A two-step procedure is described for the synthesis of a carbon material with a similar composition and properties as peat. The produced hydrochar is made suitable for agricultural applications by removing plant growing inhibitory substances. Wet household waste such as fruit peel, coffee grounds, inedible vegetable parts, or wet lignocellulosic material in general, are treated in presence of water at 215 &#x00B0;C and 21 bar in an autoclave, i.e., by hydrothermal carbonization. All these leftovers have a considerable water content of up to 90 weight % (wt%). Adding water extends the procedure to drier materials such as nutshells or even garden prunings and compostable polymers, i.e., the plastic bag for collection of the leftovers.
Usually, the resulting carbon material, called hydrochar, produces a negative effect on plant growth when added to soil. It is supposed that this effect is caused by adsorbed phytotoxic compounds. A simple post-treatment under inert atmosphere (absence of oxygen) at 275 &#x00B0;C removes these substances. Therefore, the raw hydrochar is placed on a glass frit of a vertical tubular quartz reactor. A nitrogen gas flow is applied in down-flow direction. The tube is heated to the desired temperature by means of a heating mantle for up to one hour.
The success of the thermal treatment is easily quantified by thermogravimetry (TG), carried out in air. A weight loss is determined when the temperature of 275 &#x00B0;C is reached, since volatile content is desorbed. Its amount is reduced in the final material, in comparison to the untreated hydrochar.
The two-step treatment converts household leftovers, including compostable bags employed for their collection, into a carbon material that may serve as plant growth promoter and, at the same time, as a carbon sink for climate change mitigation.

A protocol for hydrothermal carbonization of vegetable food waste in an autoclave is presented, with subsequent dry thermal treatment at 275 &#x00B0;C in a continuous flow reactor desorbing volatile organic substances. The aim is to produce a carbon material suitable as soil amendment product or substrate component.

A two-step procedure is described for the synthesis of a carbon material with a similar composition and properties as peat. The produced hydrochar is made ...