Name: fast pyrolysis of biomass residues in a twin-screw mixing reactor
Uploaded: 2016-09-09T14:00:00.000+00:00
Duration: 7 min 30 s
Description: Watch this Scientific Journal Video about Fast Pyrolysis of Biomass Residues in a Twin-screw Mixing Reactor at JoVE.com

The authors thank Melanie Frank, Pia Griesheimer, Jessica Henrich, Petra Janke, Jessica Maier, and Norbert Sickinger for technical and analytical support of this work.
Financial support provided within the BioBoost project is greatly acknowledged. BioBoost is a European R&#38;D project co-funded under contract 282873 within the Seventh Framework Programme by the European Commission (www.bioboost.eu).

1. Start-up
<ol>
	<li>Activate the whole pyrolysis and condensation system by starting the auxiliary N2 supply and the pyrolysis gas fan. Flush the pyrolysis test rig with 500 L hr-1 of nitrogen during standby. Regulate the fan by opening the fan&#39;s menu in the process control and adjusting its nominal volumetric flow such that the pressure in the reactor is 3-8 mbar above ambient pressure. 
	Caution: Especially during start-up, there is an increased risk of build-up of explosive atmospheres. The system must be completely inert in order to mitigate this risk.</li>
	<li>Fill the bio-oil cycle (i.e., organic-rich condensate) with an appropriate amount of ethylene glycol as the starting medium for the quenching system to allow safe operation of the pump and homogenizer (e.g., 15 kg in the example given). Record the weight of the starting material.</li>
	<li>Fill the aqueous condensate cycle with an appropriate amount of water to allow safe operation of the pump (e.g., 7 kg in the example given). Record the weight of starting material.</li>
	<li>Heat up the system, including the heat carrier heater and all auxiliary heaters, by opening their menus in the process control and entering the desired values (e.g., around 500 &#176;C). Auxiliary heating is recommended for the reactor itself and the connecting pipes up to the first condenser in order to prevent uncontrolled condensation of vapors.</li>
	<li>Start the cooling cycle for the heat exchangers in both condensation cycles by switching on the cooler.</li>
	<li>Start the pumps of both condensation cycles by opening their menus in the process control and click on activate. Use the same menus to adjust the mass flow to provide enough cooling power. For example, recirculate the bio-oil at a rate of around 350 kg hr-1 and cool it down to 80 &#176;C before spraying it into the quenching vessel. Recirculate the aqueous condensate at a rate of around 600 kg hr-1 and, in addition, supply cooling water at a rate of 300 kg hr-1 at 8 &#176;C.</li>
	<li>Switch on the electrostatic precipitator.</li>
	<li>After both condensation cycles have run for 10-20 min, check the nozzles of the quenching system for blocking and remove any blockage present.</li>
	<li>Start the heat carrier loop by opening the menu of the bucket elevator and the heat carrier feeding screw in the process control and click on activate. Set the heat carrier temperature to a value above the desired reactor temperature in order to allow a smoother start-up by accounting for the heat requirements for the pyrolysis reaction. For example, supply the heat carrier with a mass flow of 1,000 kg hr-1 at a temperature of 520 &#176;C during operation, but heat to 545 &#176;C before starting the biomass feed. 
	Caution: Make sure that the twin-screws of the reactor are started automatically once the heat carrier feeding screw is activated. Otherwise there is the risk of blocking and even damage to the feeding system.</li>
	<li>After the system (i.e., all temperatures) has reached the set values, start feeding biomass by filling the biomass storage with the desired feedstock. Subsequently, open the lock hopper and start the biomass feeding screw by clicking on activate in their menus in the process control. Slowly increase the feed rate in order to prevent excessive pressure fluctuations.</li>
</ol>
2. Steps and Observations Continuously Required during Operation
<ol>
	<li>Record the amount of biomass fed in order to account for balancing and take appropriate samples.</li>
	<li>Check for the desired reactor temperature (exit temperature of the heat carrier) and regulate the heating of the heat carrier loop accordingly.</li>
	<li>Regulate the fan by adjusting its nominal volumetric flow to keep the desired reactor pressure.</li>
	<li>Check for blocking in the nozzles of the quenching system (drop in mass flow and/or increase in quenching temperature).</li>
	<li>Observe the pressure drop across the cyclones and the quenching system in order to detect excessive scaling early enough. Install appropriate measures to be able to remove excessive scaling during operation, especially at the point of the first temperature drop of the pyrolysis vapors (usually the inlet of the quenching system).
	<ol>
		<li>For example, clean the tube&#39;s cross section by using a rod to remove scaling mechanically. Seal the rod with a gasket to prevent intake of air into the quenching system. Install a ball valve at the inlet point of the rod to further decrease air leakage if the cleaning is not in operation. 
		Caution: Cleaning the inlet of the quenching system by inserting a rod leads to temporary blockage of the gas removal from the reactor. Biomass feeding must be stopped if it cannot be assured that the cleaning is performed in &#60;10 sec.</li>
	</ol>
	</li>
	<li>Monitor the condensation temperatures of both condensation cycles and adapt the temperature set-points of the process thermostats if necessary.</li>
	<li>Remove condensate from cycles as soon as 80% of the maximum allowable filling level has been reached (depending on the size of the buffer tanks and the amount and type of biomass fed).</li>
	<li>Conduct measurements of the gas phase. Measure the amount of gas as well as its composition (see details in step 4.5). 
	NOTE: Primary gaseous compounds include N2, CO, CO2, CH4, O2, and H2. Additional compounds are to be expected, such as C2H4, C2H6, and C3H8. An example of a gas measurement system is described below (see step 4.5). 
	Caution: If parts of the pyrolysis unit are operated under pressure, leakage of air may lead to the development of an explosive atmosphere. It is highly recommended to closely observe the amount of oxygen in the pyrolysis gas.</li>
</ol>
3. Shutdown
<ol>
	<li>To stop the experiment, simply turn off the biomass feed and regulate the fan to keep the desired reactor pressure.</li>
	<li>Allow the system (heat carrier loop and condensation cycles) to run for another 30-40 min to ensure that all remainders are pyrolyzed and the products recovered.</li>
	<li>Turn off the heating of the heat carrier loop.</li>
	<li>Turn off the pumps of both condensation cycles and the electrostatic precipitator.</li>
	<li>Empty both condensate cycles and record the weight of each condensate. Subtract the amount of starting material (see steps 1.2 and 1.3) before setting up the balances.</li>
	<li>Allow the containers for char collection to cool down to room temperature in an inert atmosphere. Weigh the amount of char. 
	Caution: The char may exhibit pyrophoric characteristics, and specific care should be taken when handling this material.</li>
	<li>Clean the bio-oil cycle with fresh ethylene glycol and the aqueous condensate cycle with a 1:1 mixture of water and ethanol. Fill with appropriate amounts (see steps 1.2 and 1.3) and allow to run for 30-40 min.</li>
</ol>
4. Required Analyses for Setting up &#39;Dry&#39; and &#39;Elemental Carbon&#39; Balances
<ol>
	<li>Perform the following feedstock analyses (examples for applicable standards are given in parentheses):
	<ol>
		<li>Determine the water content17.</li>
		<li>Determine the ash content18.</li>
		<li>Determine the elemental carbon, hydrogen, and nitrogen contents19. 
		NOTE: It is highly recommended to analyze the water content each experimental day because differences in weather conditions might affect the moisture content of the feedstock. Depending on the size of the lot, several samples are required to reliably characterize the feedstock. Additional analyses such as fiber analysis and higher heating value are recommended but not mandatory for setting up the above-mentioned balances.</li>
	</ol>
	</li>
	<li>Perform the following char powder analyses (examples of applicable standards are given in the references):
	<ol>
		<li>Determine the water content17.</li>
		<li>Determine the ash content18.</li>
		<li>Determine the elemental carbon, hydrogen, and nitrogen contents19. 
		NOTE: It is assumed that char has no moisture content when leaving the process for setting up the balances. Moisture take-up may occur during the course of analyses, and the water content is required for the correction of the other two analyses.</li>
	</ol>
	</li>
	<li>Perform the following bio-oil analyses (examples of applicable standards or other recommended methods are given in parentheses):
	<ol>
		<li>Determine the water content by volumetric Karl-Fischer titration according to standard protocols. Dissolve a sample in dry methanol and titrate it with a mixture of a base, SO2, and a known concentration of I2 (detailed examples of materials are given in the material list). Each mole of water reacts with one mole of I2.</li>
		<li>Determine the solids content by taking a 3,040 g sample of FPBO and dissolve it in methanol to a final solution volume of about 100 ml. Stir the solution for 10 min at room temperature. Filter the solution through cellulose filter at particle retention of 2.5 &#181;m and rinse the residue thoroughly with methanol until a clear filtrate is obtained. Dry the solid residue at 105 &#176;C overnight and determine the residual weight.</li>
		<li>Determine the elemental carbon, hydrogen, and nitrogen contents19.</li>
		<li>Determine the ethylene glycol content by 1H NMR analysis according to standard protocols. Dissolve an FPBO sample in a solution of deuterated methanol with 3-(trimethylsilyl)propionic-2,2,3,3-d4 acid sodium salt (TMSP) as reference material (approximately 0.1 g FPBO in 0.8 g solution). For example, the solution may contain 44 g methanol and 0.1 g TMSP. Centrifuge the dissolved sample in order to remove solids. Analyze the sample by 1H nuclear magnetic resonance spectroscopy (NMR). The hydroxy groups of ethylene glycol show a peak at 3.55&#8211;3.65 ppm. The reference peak of TMSP appears around 0 ppm and is used to quantify the ethylene glycol content. 
		NOTE: Start-up with pure ethylene glycol leads to a dilution of the condensate in the first condenser. This needs to be considered in the calculation of mass and energy balances and for the presentation of the results. It is highly desirable to identify individual chemical compounds. Such an analytical method is very complex due to the vast number of different compounds and the nature of the condensate matrix. A description of such analyses is outside the scope of this paper. It should also be pointed out that the above-mentioned analyses are merely required for setting up balances and are not sufficient for describing the bio-oil as a product. Standards that cover FPBO applications are in preparation.</li>
	</ol>
	</li>
	<li>Perform the following aqueous condensate analyses (examples of applicable standards are given in parentheses):
	<ol>
		<li>Determine the water content by volumetric Karl-Fischer titration (see 4.3.1).</li>
		<li>Determine the total organic carbon as non-purgeable organic carbon20. 
		NOTE: Start-up with pure water leads to a dilution of the condensate in the second condenser. This needs to be considered in the calculation of mass and energy balances and for the presentation of the results.</li>
	</ol>
	</li>
	<li>Monitor the gas composition throughout the experiment because composition varies considerably with time. For example, analyze the product gas during the experiments presented here in a process gas chromatograph every 30-60 min. Analyze the following gas species: Ne, H2, CO, CO2, N2, O2, CH4, and alkane/alkene C2-C5 components.
	<ol>
		<li>Inject a constant gas flow of Ne into the reactor as a reference. Calculate the mass of each gas species based on the reference volumetric flow, the average gas composition ratio, the duration of the experiment, and the density of the species. In order to determine the water content of the pyrolysis gas, assume saturated conditions at the outlet temperature of the last condenser.</li>
	</ol>
	</li>
</ol>

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M. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=The+effect+of+lignin+and+inorganic+species+in+biomass+on+pyrolysis+oil+yields,+quality+and+stability.">The effect of lignin and inorganic species in biomass on pyrolysis oil yields, quality and stability.</a> Fuel. 87, 1230-1240 (2008).</li><li>Oasmaa, A., Solantausta, Y., Arpiainen, V., Kuoppala, E., Sipil&#228;, K. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=Fast+Pyrolysis+Bio-Oils+from+Wood+and+Agricultural+Residues.">Fast Pyrolysis Bio-Oils from Wood and Agricultural Residues.</a> Energ. &amp; Fuels. 24, 1380-1388 (2010).</li><li>DIN German Institute for Standardization. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=.">.</a> DIN EN ISO 18134-3 Solid biofuels - Determination of moisture content - Oven dry method - Part 3: Moisture in general analysis sample. , (2015).</li><li>DIN German Institute for Standardization. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=.">.</a> DIN EN ISO 18122 Solid biofuels - Determination of ash content. , (2016).</li><li>DIN German Institute for Standardization. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=.">.</a> Institute for Standardization. DIN EN ISO 16948 Solid biofuels - Determination of total content of carbon, hydrogen and nitrogen. , (2015).</li><li>DIN German Institute for Standardization. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=.">.</a> Institute for Standardization. DIN EN 1484 Water analysis - Guidelines for the determination of total organic carbon (TOC) and dissolved organic carbon (DOC). , (1997).</li><li>DIN German Institute for Standardization. <a target="_blank" href="http://www.ncbi.nlm.nih.gov/entrez/query.fcgi?db=PubMed&cmd=Search&doptcmdl=Citation&defaultField=Title+Word&term=.">.</a> ESO 16993: Solid biofuels - Conversion of analytical results from one basis to another. , (2015).</li><li>Bridgwater, A. 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The authors have nothing to disclose.

For all experiments, process conditions such as size of the feedstock material, feed rate, pressure, reaction temperature, condensation temperatures, and flow rates of both the heat carrier and the condensate cycle were the same. Naturally, variations within defined limits cannot be avoided. For a test plant such as the process development unit presented here, the acceptable ranges of fluctuation and required times of operation for reproducible experiments need to be calculated and/or determined by experience. For example, the reactor temperature, which is indicated by the temperature of the heat carrier leaving the reactor, is controlled with a standard deviation of 35 &#176;C over the entire course of the reaction from the start of the reaction at full biomass capacity to the stop of biomass feeding (typically around 4 hr). The pressure in the reactor is controlled with a standard deviation of 300&#8211;500 Pa. Peaks in pressure are likely to occur due to fluctuations in biomass feeding. It is recommended to adjust the feeding screw system to the biomass material under consideration in order to minimize such fluctuations and ensure a constant biomass flow. The condensation temperature in the first and second condensers was maintained at a standard deviation of 3 &#176;C and 1 &#176;C, respectively.
It should be noted at this point that all experiments presented were conducted at the same reactor temperature (500 &#176;C). This temperature does not necessarily reflect the optimum fast pyrolysis temperature which exists for each specific feedstock22. A variation of the reactor temperature could lead to an optimized pyrolysis temperature with even higher organic oil yields.
The choice of balancing method is not trivial for fast pyrolysis of biomass, especially when applying fractionated condensation and when using biomass with high ash content. Three different types of balancing have been presented in the previous section. Reporting the yields of product fractions on an &#39;as received&#39; basis is advantageous for practical considerations such as the design of apparatuses and storage capacities as it reports the actual product distribution to be expected. However, these values are obscured by the water and ash contents of the feedstock. Especially for residual biomass &#8212; e.g., straw, forestry and pruning residues and biogenic &#39;waste&#39; &#8212; this is an issue as these feedstocks have a wide range of water and inorganic contents, see Table 1.
The common balancing method for biomass processes on a &#39;dry basis&#39; is in most cases useful for comparisons between different studies as it eliminates the effect of different moisture contents of the feedstock. However, it should be pointed out that these calculated values from experiments with a specific moist feedstock do not necessarily reflect the behavior and yields of this specific feedstock if it was completely dried by physical means prior to the experiment. It is known that moisture affects the yield distribution of pyrolysis23 and this should be kept in mind when evaluating and comparing &#39;dry&#39; balances.
Furthermore, mass balances on a &#39;dry basis&#39; are inappropriate for feedstocks with high ash content because minerals end up primarily in the char and obscure the results similarly to the initial moisture content. Similarly to water, minerals affect the actual pyrolysis reaction network because they promote secondary pyrolysis reactions, leading to higher char and lower bio-oil yields. Such effects can only be evaluated on a scientific basis if balances are corrected for the ash content. One way to achieve this is by setting up carbon balances. From the comparison of Figure 2 and Figure 4 it can be seen that the increased solids yield observed after pyrolysis of wheat straw as compared to miscanthus is not only due to inorganic material that is recovered with the char, but also due to an increased fraction of organic solids that were formed during the process.
Another advantage of elemental carbon balances is to show the fate of biogenic carbon, i.e., its distribution in the recovered product fractions. This is important for the evaluation of more complex conversion chains &#8212; e.g., pyrolysis, gasification, and synthesis as in the case presented here &#8212; because the biogenic carbon should be used as efficiently as possible. One of the most important roles of biomass in a future bio-based economy is to provide biogenic carbon for a wide range of commodities, thus replacing carbon from fossil resources.
The presented protocol for fast pyrolysis in a twin-screw mixing reactor can be realized on different scales with some adjustments. The presented case of a unit with a feed capacity of 10 kg hr-1 has proven to be a feasible compromise between operational complexity and meaningful results for process behavior. It can be applied both for screening of different types of biomass and optimization of process conditions. Testing a specific biomass feedstock is crucial because certain feedstock characteristics might lead to unfavorable process operation if coarse solid residues accumulate in the heat carrier cycle. Such accumulation was not observed for the biomass presented in the results section, but it has been observed for very hard biogenic material with large particle size (&#62;1 mm) which limits the applicability of the presented process. This problem could be reduced with a different design of the heat carrier loop, e.g., by pneumatic transport of the heat carrier with simultaneous partial combustion.

The use of biomass as an alternative to fossil carbon sources is becoming increasingly important for reducing the effect of societal activity on the earth&#39;s climate. There exist other renewable energy sources such as wind and solar, but biomass represents the only renewable carbon source to date. Consequently, the most efficient use of biomass is in the production of chemicals and specialized liquid fuels. Residual biomass should be used in order to reduce competition between feed, food, and chemicals/fuel production. These residues often have low bulk density, thus presenting a logistical challenge for industrial scale applications.
To address these challenges, the bioliq concept has been developed at the Karlsruhe Institute of Technology1. It features a decentralized first step to convert residual biomass into an energy dense intermediate (bioslurry), a subsequent conversion in a central gasification unit to synthesis gas and a final synthesis to the desired product(s). The gasification and synthesis unit can be designed on the required industrial scale at the same site to achieve commercial operation. The concept allows for different products, ranging from drop-in fuels to specialized fuel additives and bulk chemicals2-5. This paper presents the first step in which fast pyrolysis is used to convert residual biomass to the intermediate bioslurry. Fast pyrolysis is characterized by rapid heating of biomass in an inert atmosphere to a reaction temperature of typically 450-500 &#176;C with a residence time of the produced pyrolysis vapors of &#60;2 sec6. Most commonly, fluidized bed reactors are used for performing fast pyrolysis but there also exist different reactor designs specifically adapted to optimize reaction conditions7. The work presented in the following has been conducted with a twin-screw mixing reactor. It presents a robust technology that has already been applied on an industrial scale for pyrolysis of coal and on a pilot scale for oil sands8.
The purpose of the twin-screw mixing reactor is to mix the solid biomass feed with a solid, pre-heated heat carrier. Mixing needs to be sufficiently thorough in order to achieve the heating rate that is necessary for converting the biomass under fast pyrolysis conditions. Additionally, the size of both the biomass and heat carrier particles needs to be small to achieve a high heat transfer coefficient and a short particle heating period. At the Institute of Catalysis Research and Technology (IKFT) of the Karlsruhe Institute of Technology (KIT), a process development unit with a biomass input capacity of 10 kg hr-1 has been operational for more than a decade. It uses steel balls as the heat carrier, which is recirculated internally with a bucket elevator and re-heated with an electrical heating system. Its main purpose was the investigation of a unique product recovery technology that was adapted to the use of the product in a gasifier and the validation of its suitability for a broad range of feedstocks9-11. A larger pilot plant was built in parallel to these studies with a biomass input capacity of 500 kg hr-1, which has been operational for five years. It utilizes sand as the heat carrier, which is recirculated pneumatically by a hot lift gas and additionally heated by partial combustion of entrained char particles1,12. The following description of the experimental method is based on the smaller process development unit after its product recovery section was refurbished to better resemble the pilot plant design13. A flow scheme of this experimental setup is illustrated in Figure 1.
It is important to note that product requirements for fast pyrolysis bio-oil (FPBO) for use in gasifiers are different to those developed for conventional FPBO, which is usually intended for direct fuel applications14. Most importantly, the solids content of the FPBO does not have to be very low. In fact, it is desirable to mix the FPBO produced with the char obtained from the conversion process in order to increase the amount of carbon available for gasification and subsequent synthesis of drop-in fuels. These facts are important for understanding the differences in the design of the experimental setup presented here and fast pyrolysis experiments published elsewhere. Another important difference is the fact that the biomass conversion concept under investigation was specifically designed for agricultural residues such as wheat straw. Typically, this kind of feedstock contains a large fraction of ash. Ash is known to significantly influence the product distribution of fast pyrolysis. It leads to a decrease of organic condensate (OC) and an increase in both solid and gaseous products10,15,16. These facts are accounted for both in the design of the experimental setup presented here and the overall process chain. Most industrial installations run on wood with low ash content and simply burn the solids internally. This leads to additional production of heat for external use. When using feedstocks with high ash content, char is a significant by-product that should be used efficiently13.

<table><tbody><tr><td>Wheat straw</td><td>D&amp;ouml;rrmann Kraichtal-M&amp;uuml;nzesheim</td><td>n/a</td><td>&lt;em&gt;Triticum aestivum L.&lt;/em&gt;</td></tr><tr><td>Scrap wood</td><td>Rettenmeier Holding AG</td><td>n/a</td><td>According to class A2 of the German scrap wood decree (AltholzV &amp;sect;2): glued, coated, painted, or otherwise treated scrap wood without organic halogen compounds and wood preservatives</td></tr><tr><td>Miscanthus</td><td>Hotel-Heizungsbau Kraichgau-Odenwald</td><td>n/a</td><td>&lt;em&gt;Miscanthus x giganteus&lt;/em&gt;</td></tr><tr><td>Ethylene glycol</td><td>H&amp;auml;ffner GmbH &amp;amp; Co KG</td><td>1042090220600</td><td></td></tr><tr><td>Ethanol</td><td>H&amp;auml;ffner GmbH &amp;amp; Co KG</td><td>1026800150600</td><td>Grade 99.9%</td></tr><tr><td>Nitrogen</td><td>KIT</td><td>n/a</td><td>Supplied by internal nitrogen pressure system.</td></tr><tr><td>Pyrolysis test rig</td><td>self-built</td><td>n/a</td><td>Flow scheme is illustrated in manuscript.</td></tr><tr><td>&lt;strong&gt;Name&lt;/strong&gt;</td><td>&lt;strong&gt;Company&lt;/strong&gt;</td><td>&lt;strong&gt;Catalog Number&lt;/strong&gt;</td><td>&lt;strong&gt;Comments&lt;/strong&gt;</td></tr><tr><td>&lt;strong&gt;Analyses:&lt;/strong&gt;</td><td></td><td></td><td></td></tr><tr><td>Gas chromatograph Daniel 700</td><td>Emerson Process Management</td><td>n/a</td><td>Designed for this specific application by Emerson; two 20% SF 96 columns, two HAYESEP N columns, and one MS-5A washed column; carrier gas is helium</td></tr><tr><td>Helium</td><td>Air Liquide</td><td>P0252L50R2A001</td><td>Grade 6.0</td></tr><tr><td>Gas mixture for calibration</td><td>basi Sch&amp;ouml;berl GmbH &amp;amp; Co. KG</td><td>FG 10002</td><td>Specified gas composition: 5% Ne, 2% O&lt;sub&gt;2&lt;/sub&gt;, 20% CO, 30% CO&lt;sub&gt;2&lt;/sub&gt;, 5% CH&lt;sub&gt;4&lt;/sub&gt;, 5% H&lt;sub&gt;2&lt;/sub&gt;, 2% C&lt;sub&gt;2&lt;/sub&gt;H&lt;sub&gt;6&lt;/sub&gt;, 0.5% C&lt;sub&gt;3&lt;/sub&gt;H&lt;sub&gt;8&lt;/sub&gt;, 0.5% C&lt;sub&gt;4&lt;/sub&gt;H&lt;sub&gt;10&lt;/sub&gt;, 0.5% C&lt;sub&gt;5&lt;/sub&gt;H&lt;sub&gt;12&lt;/sub&gt;, remainder N&lt;sub&gt;2&lt;/sub&gt;.</td></tr><tr><td>Neon</td><td>Air Liquide</td><td>P0890S10R2A001</td><td>Grade 4.0; used as fixed reference gas flow; not necessarily required and is only given as an example for quantifying the pyrolysis gas flow.</td></tr><tr><td>Elementaranalysator CHN628</td><td>Leco Instrumente GmbH</td><td>622-000-000</td><td></td></tr><tr><td>TGA701</td><td>Leco Instrumente GmbH</td><td>n/a</td><td></td></tr><tr><td>DIMATOC 2000</td><td>Dimatec</td><td>n/a</td><td></td></tr><tr><td>Hydranal methanol dry</td><td>Sigma Aldrich</td><td>34741</td><td></td></tr><tr><td>Hydranal composite V</td><td>Sigma Aldrich</td><td>34805</td><td></td></tr><tr><td>841 Titrando</td><td>Deutsche Metrohm GmbH &amp;amp; Co. KG</td><td>2.841.0010</td><td></td></tr><tr><td>774 Oven Sample Processor</td><td>Deutsche Metrohm GmbH &amp;amp; Co. KG</td><td>2.774.0010</td><td></td></tr><tr><td>800 Dosino</td><td>Deutsche Metrohm GmbH &amp;amp; Co. KG</td><td>2.800.0010</td><td></td></tr><tr><td>801 Stirrer</td><td>Deutsche Metrohm GmbH &amp;amp; Co. KG</td><td>2.801.0010</td><td></td></tr><tr><td>Methanol</td><td>Carl Roth GmbH &amp;amp; Co KG</td><td>83884</td><td>99% for synthesis</td></tr><tr><td>Whatman cellulose filter grade 42</td><td>Sigma Aldrich</td><td>WHA1442090</td><td></td></tr><tr><td>Methanol-D&lt;sub&gt;4&lt;/sub&gt;</td><td>Sigma Aldrich</td><td>151947</td><td></td></tr><tr><td>3-(Trimethylsilyl)propionic-2,2,3,3-d&lt;sub&gt;4&lt;/sub&gt; acid sodium salt</td><td>Sigma Aldrich</td><td>269913</td><td></td></tr><tr><td>BZH&amp;nbsp;250&amp;nbsp;MHz</td><td>Bruker</td><td>n/a</td><td></td></tr></tbody></table>

fast pyrolysis of biomass residues in a twin-screw mixing reactor

Fast pyrolysis is being increasingly applied in commercial plants worldwide. They run exclusively on woody biomass, which has favorable properties for conversion with fast pyrolysis. In order to increase the synergies of food production and the energetic and/or material use of biomass, it is desirable to utilize residues from agricultural production, e.g., straw. The presented method is suitable for converting such a material on an industrial scale. The main features are presented and an example of mass balances from the conversion of several biomass residues is given. After conversion, fractionated condensation is applied in order to retrieve two condensates &#8212; an organic-rich and an aqueous-rich one. This design prevents the production of fast pyrolysis bio-oil that exhibits phase separation. A two phase bio-oil is to be expected because of the typically high ash content of straw biomass, which promotes the production of water of reaction during conversion.
Both fractionated condensation and the use of biomass with high ash content demand a careful approach for establishing balances. Not all kind of balances are both meaningful and comparable to other results from the literature. Different balancing methods are presented, and the information that can be derived from them is discussed.

Various types of biomass were successfully pyrolyzed in the pyrolysis unit at IKFT/KIT with the current setup. For example, three different feedstocks (wheat straw, miscanthus, and scrap wood) were compared concerning their properties and yields after pyrolysis following the procedure described. Different kinds of balancing methods are shown and discussed in regard to their applicability towards ash-rich feedstock. It is important to note that the balances have been calculated and summarized according to the state of aggregation of each fraction. The bio-oil recovered in the first condenser still contains solids, which have not been removed by the cyclones. These are marked separately in the balances. For comparison and statistical evaluation, the solids content of the bio-oil was added to the char fraction recovered from the cyclones.
On an &#39;as received&#39; basis, the solids yield, i.e., char recovered via cyclones and char present in the bio-oil, is in the range from 14-25% by weight for the investigated feedstocks. Total condensate yields recovered in the two condensers range from 53-66% by weight, whereas gas yields are relatively similar (around 20%) for all 3 biomasses (see Figure 2). These &#39;as received&#39; values give practical information on the actual amount of product fractions to be expected in fast pyrolysis installations of this kind.
However, total liquid organic yields in the literature are most commonly reported on a dry basis, i.e., excluding moisture and water of reaction in the condensate and in the feed. The advantage of this kind of balance is the fact that initially present moisture of the biomass does not affect the results. This moisture content would artificially increase the condensate yield in an &#39;as received&#39; balance. For reasons of comparability, Figure 3 shows organic oil yield and reaction water on a dry basis. In this study, organic oil yields increase (35 - 46 - 50% by weight) with decreasing ash contents (9.2 - 2.7 - 1.5% by weight) of the feedstocks wheat straw - miscanthus - scrap wood (see Table 1). This is in line with observations from other studies10,15,16. Yields of water of reaction are in a comparatively narrow range from 12-14% by weight.
Mass balances on a dry basis are still directly affected by the ash content of the feedstocks. Minerals contained in the biomass material will artificially increase the yield of solids in both &#39;as received&#39; and &#39;dry&#39; balances. Consequently, elemental carbon balances were determined because they appear to be more suitable for evaluating differences in thermochemical conversion reactions of biomass (see Figure 4). It becomes evident that the larger part of carbon is recovered in the bio-oil (44-54% by weight) and only a mass fraction of 24-32% in solid form as pyrolysis char. About 16-19% by weight of the carbon is not recovered in solid or liquid form and leaves the plant with the pyrolysis gas. In a commercial plant, this gas would be recycled for reasons of energy recovery in an internal combustion device. A mass fraction of only about 3-4% of carbon is recovered in the aqueous condensate, which has a water content of around 80% by weight. This validates the effectiveness of the fractionated condensation setup presented here.
<table border="1" fo:keep-together.within-page="1" fo:keep-with-next.within-page="always">
	<tbody>
		<tr>
			<td></td>
			<td>Wheat straw</td>
			<td>Miscanthus</td>
			<td>Scrap wood</td>
		</tr>
		<tr>
			<td>Water, ar</td>
			<td>9.6</td>
			<td>10.1</td>
			<td>15.2</td>
		</tr>
		<tr>
			<td>Ash, d</td>
			<td>9.2</td>
			<td>2.7</td>
			<td>1.5</td>
		</tr>
		<tr>
			<td>Carbon, d</td>
			<td>46.1</td>
			<td>48.6</td>
			<td>49.8</td>
		</tr>
		<tr>
			<td>Hydrogen, d</td>
			<td>5.7</td>
			<td>5.9</td>
			<td>6.1</td>
		</tr>
		<tr>
			<td>Nitrogen, d</td>
			<td>&#60;0.5</td>
			<td>&#60;0.5</td>
			<td>&#60;0.5</td>
		</tr>
		<tr>
			<td colspan="4">ar: as received, d: dry basis21</td>
		</tr>
	</tbody>
</table>
Table 1. Selected properties of the different feedstocks used. All values represent mass fractions (%).
<img alt="Figure 1" src="/files/ftp_upload/54395/54395fig1.jpg" /> 
Figure 1. Flow diagram of the experimental setup. 1) Biomass storage. 2) Lock hopper system. 3) Biomass dosing. 4) Twin-screw mixing reactor. 5) Bucket elevator. 6) Heater for heat carrier. 7) Cyclone for solids removal. 8) Char storage. 9) Spray quenching. 10) Bio-oil storage tank. 11) Homogenizer and pump. 12) Heat exchanger for cooling of recirculated condensate. 13) Electrostatic precipitator. 14) Aqueous condensate storage tank. 15) Pump for recirculating aqueous condensate. 16) Heat exchanger for cooling of recirculated condensate. 17) Condenser for aqueous condensate. 18) Fan for removing gas/vapors. <a href="https://www.jove.com/files/ftp_upload/54395/54395fig1large.jpg" target="_blank">Please click here to view a larger version of this figure.</a>
<img alt="Figure 2" src="/files/ftp_upload/54395/54395fig2.jpg" /> 
Figure 2. Mass balances of experiments. Balances are reported on an &#39;as received&#39;21 basis of the feedstock and products. All values are expressed as mass fractions. Three different types of biomass have been used and all experiments were conducted at least in triplicates13. The solids content in the bio-oil is reported separately for illustration purposes. The error bars indicate standard deviations of experiments with one type of feedstock. <a href="https://www.jove.com/files/ftp_upload/54395/54395fig2large.jpg" target="_blank">Please click here to view a larger version of this figure.</a>
<img alt="Figure 3" src="/files/ftp_upload/54395/54395fig3.jpg" /> 
Figure 3. Total organic oil yields and water of reaction. All values are presented on a dry21 feed basis and are expressed as mass fractions. The solids content of the condensate has been excluded from the organic oil yield13. The error bars indicate standard deviations of experiments with one type of feedstock. <a href="https://www.jove.com/files/ftp_upload/54395/54395fig3large.jpg" target="_blank">Please click here to view a larger version of this figure.</a>
<img alt="Figure 4" src="/files/ftp_upload/54395/54395fig4.jpg" /> 
Figure 4. Carbon balances. All values are reported as mass fractions of the biomass carbon input. Three different types of biomass have been used and all experiments were conducted at least in triplicates13. The solids content in the bio-oil is reported separately for illustration purposes. The error bars indicate standard deviations of experiments with one type of feedstock. <a href="https://www.jove.com/files/ftp_upload/54395/54395fig4large.jpg" target="_blank">Please click here to view a larger version of this figure.</a>

Watch this Scientific Journal Video about Fast Pyrolysis of Biomass Residues in a Twin-screw Mixing Reactor at JoVE.com

Fast Pyrolysis of Biomass Residues in a Twin-screw Mixing Reactor

A procedure for thermochemical conversion of biomass residues is presented that aims at maximizing the yield of liquid products (fast pyrolysis). It is based on a technology proven on an industrial scale and especially suitable for treating a straw type of biomass.

Fast pyrolysis is being increasingly applied in commercial plants worldwide. They run exclusively on woody biomass, which has favorable properties for ...

fast-pyrolysis-of-biomass-residues-in-a-twin-screw-mixing-reactor

Research

JoVE Journal

Bioengineering

27.6K Views.  Karlsruhe Institute of Technology (KIT). A procedure for thermochemical conversion of biomass residues is presented that aims at maximizing the yield of liquid products (fast pyrolysis). It is based on a technology proven on an industrial scale and especially suitable for treating a straw type of biomass.

Video: Fast Pyrolysis of Biomass Residues in a Twin-screw Mixing Reactor

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.

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Biochemistry

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.

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 ...

Environment

Method to Produce Durable Pellets at Lower Energy Consumption Using High Moisture Corn Stover and a Corn Starch Binder in a Flat Die Pellet Mill

A major challenge in the production of pellets is the high cost associated with drying biomass from 30 to 10% (w.b.) moisture content. At Idaho National Laboratory, a high-moisture pelleting process was developed to reduce the drying cost. In this process the biomass pellets are produced at higher feedstock moisture contents than conventional methods, and the high moisture pellets produced are further dried in energy efficient dryers. This process helps to reduce the feedstock moisture content by about 5-10% during pelleting, which is mainly due to frictional heat developed in the die. The objective of this research was to explore how binder addition influences the pellet quality and energy consumption of the high-moisture pelleting process in a flat die pellet mill. In the present study, raw corn stover was pelleted at moistures of 33, 36, and 39% (w.b.) by addition of 0, 2, and 4% pure corn starch. The partially dried pellets produced were further dried in a laboratory oven at 70 &#176;C for 3-4 hr to lower the pellet moisture to less than 9% (w.b.). The high moisture and dried pellets were evaluated for their physical properties, such as bulk density and durability. The results indicated that increasing the binder percentage to 4% improved pellet durability and reduced the specific energy consumption by 20-40% compared to pellets with no binder. At higher binder addition (4%), the reduction in feedstock moisture during pelleting was &#60;4%, whereas the reduction was about 7-8% without the binder. With 4% binder and 33% (w.b.) feedstock moisture content, the bulk density and durability values observed of the dried pellets were &#62;510 kg/m3 and &#62;98%, respectively, and the percent fine particles generated was&#160;reduced to &#60;3%.

In this study, a protocol was developed to produce good quality pellets using a flat die pellet mill at reduced specific energy consumption testing high-moisture corn stover and a starch based binder. The results indicated that adding a corn starch binder improved the pellet durability, reduced percent fines and decreased specific energy consumption.

A major challenge in the production of pellets is the high cost associated with drying biomass from 30 to 10% (w.b.) moisture content. At Idaho National ...

Laboratory Production of Biofuels and Biochemicals from a Rapeseed Oil through Catalytic Cracking Conversion

The work is based on a reported study which investigates the processability of canola oil (bio-feed) in the presence of bitumen-derived heavy gas oil (HGO) for production of transportation fuels through a fluid catalytic cracking (FCC) route. Cracking experiments are performed with a fully automated reaction unit at a fixed weight hourly space velocity (WHSV) of 8 hr-1, 490-530 &#176;C, and catalyst/oil ratios of 4-12 g/g. When a feed is in contact with catalyst in the fluid-bed reactor, cracking takes place generating gaseous, liquid, and solid products. The vapor produced is condensed and collected in a liquid receiver at -15 &#176;C. The non-condensable effluent is first directed to a vessel and is sent, after homogenization, to an on-line gas chromatograph (GC) for refinery gas analysis. The coke deposited on the catalyst is determined in situ by burning the spent catalyst in air at high temperatures. Levels of CO2 are measured quantitatively via an infrared (IR) cell, and are converted to coke yield. Liquid samples in the receivers are analyzed by GC for simulated distillation to determine the amounts in different boiling ranges, i.e., IBP-221 &#176;C (gasoline), 221-343 &#176;C (light cycle oil), and 343 &#176;C+ (heavy cycle oil). Cracking of a feed containing canola oil generates water, which appears at the bottom of a liquid receiver and on its inner wall. Recovery of water on the wall is achieved through washing with methanol followed by Karl Fischer titration for water content. Basic results reported include conversion (the portion of the feed converted to gas and liquid product with a boiling point below 221 &#176;C, coke, and water, if present) and yields of dry gas (H2-C2's, CO, and CO2), liquefied petroleum gas (C3-C4), gasoline, light cycle oil, heavy cycle oil, coke, and water, if present.

This paper presents an experimental method to produce biofuels and biochemicals from canola oil mixed with a fossil-based feed in the presence of a catalyst at mild temperatures. Gaseous, liquid, and solid products from a reaction unit are quantified and characterized. Conversion and individual product yields are calculated and reported.

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Chemistry

Utilization of Stop-flow Micro-tubing Reactors for the Development of Organic Transformations

A new reaction screening technology for organic synthesis was recently demonstrated by combining elements from both continuous micro-flow and conventional batch reactors, coined stop-flow micro-tubing (SFMT) reactors. In SFMT, chemical reactions that require high pressure can be screened in parallel through a safer and convenient way. Cross-contamination, which is a common problem in reaction screening for continuous flow reactors, is avoided in SFMT. Moreover, the commercially available light-permeable micro-tubing can be incorporated into SFMT, serving as an excellent choice for light-mediated reactions due to a more effective uniform light exposure, compared to batch reactors. Overall, the SFMT reactor system is similar to continuous flow reactors and more superior than batch reactors for reactions that incorporate gas reagents and/or require light-illumination, which enables a simple but highly efficient reaction screening system. Furthermore, any successfully developed reaction in the SFMT reactor system can be conveniently translated to continuous-flow synthesis for large scale production.

A protocol for organic reaction screening using stop-flow micro-tubing (SFMT) reactors employing gaseous reactants and/or visible-light mediated reactions is presented.

A new reaction screening technology for organic synthesis was recently demonstrated by combining elements from both continuous micro-flow and conventional ...

Combustion Chemistry of Fuels: Quantitative Speciation Data Obtained from an Atmospheric High-temperature Flow Reactor with Coupled Molecular-beam Mass Spectrometer

This manuscript describes a high-temperature flow reactor experiment coupled to the powerful molecular beam mass spectrometry (MBMS) technique. This flexible tool offers a detailed observation of chemical gas-phase kinetics in reacting flows under well-controlled conditions. The vast range of operating conditions available in a laminar flow reactor enables access to extraordinary combustion applications that are typically not achievable by flame experiments. These include rich conditions at high temperatures relevant for gasification processes, the peroxy chemistry governing the low temperature oxidation regime or investigations of complex technical fuels. The presented setup allows measurements of quantitative speciation data for reaction model validation of combustion, gasification and pyrolysis processes, while enabling a systematic general understanding of the reaction chemistry. Validation of kinetic reaction models is generally performed by investigating combustion processes of pure compounds. The flow reactor has been enhanced to be suitable for technical fuels (e.g. multi-component mixtures like Jet A-1) to allow for phenomenological analysis of occurring combustion intermediates like soot precursors or pollutants. The controlled and comparable boundary conditions provided by the experimental design allow for predictions of pollutant formation tendencies. Cold reactants are fed premixed into the reactor that are highly diluted (in around 99 vol% in Ar) in order to suppress self-sustaining combustion reactions. The laminar flowing reactant mixture passes through a known temperature field, while the gas composition is determined at the reactors exhaust as a function of the oven temperature. The flow reactor is operated at atmospheric pressures with temperatures up to 1,800 K. The measurements themselves are performed by decreasing the temperature monotonically at a rate of -200 K/h. With the sensitive MBMS technique, detailed speciation data is acquired and quantified for almost all chemical species in the reactive process, including radical species.

An investigation of the oxidative combustion chemistry of novel biofuels, fuel components, or jet fuels by comparison of quantitative speciation data is presented. The data can be used for kinetic model validation and enables fuel assessment strategies.This manuscript describes the atmospheric high-temperature flow reactor and demonstrates its capabilities.

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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.

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Air Curtain Burners and Biochar &#8211; Advancing Forest Health and Carbon Capture

Continuous In-woods Production of Biochar Using a Trailer-Mounted Air Curtain Burner

Fuel treatments and other forest restoration thinning practices aim to reduce wildfire risk while building forest resilience to drought, insects, and diseases and increasing aboveground carbon (C) sequestration. However, fuel treatments generate large amounts of unmerchantable woody biomass residues that are often burned in open piles, releasing significant quantities of greenhouse gases and particulates, and potentially damaging the soil beneath the pile. Air curtain burners offer a solution to mitigate these issues, helping to reduce smoke and particulates from burning operations, more fully burn biomass residues compared to pile burning, and eliminate the direct and intense fire contact that can harm soil beneath the slash pile. In an air curtain burner, burning takes place in a controlled environment. Smoke is contained and recirculated by the air curtain, and therefore burning can be conducted under a variety of climatic conditions (e.g.,&#160;wind, rain, snow), lengthening the burning season for disposal of slash material. The mobile pyrolysis unit that continuously creates biochar was specifically designed to dispose of residual woody biomass at log landings, green wood at landfills, or salvaged logged materials and create biochar in the process. This high-carbon biochar output can be used to enhance soil resilience by improving its chemical, physical, and biological properties and has potential applications in remediating contaminated soils, including those at abandoned mine sites. Here, we describe the general use of this equipment, appropriate siting, loading methods, quenching requirements, and lessons learned about operating this new technology.

Author Spotlight: Advancing Place-Based Biochar Production for Ecosystem Restoration and Soil Health

We describe the use of a place-based mobile pyrolysis unit equipped with an air curtain to continuously create biochar. The technology reduces the need for open slash pile burning, which results in lower emissions and fewer soil impacts. The protocol includes guidelines for site selection, loading, and quenching.

Fuel treatments and other forest restoration thinning practices aim to reduce wildfire risk while building forest resilience to drought, insects, and ...

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 ...

Twin-Screw Extrusion Process to Produce Renewable Fiberboards

A versatile twin-screw extrusion process to provide an efficient thermo-mechano-chemical pre-treatment on lignocellulosic biomass before using it as source of mechanical reinforcement in fully bio-based fiberboards was developed. Various lignocellulosic crop by-products have already been successfully pre-treated through this process, e.g., cereal straws (especially rice), coriander straw, shives from oleaginous flax straw, and bark of both amaranth and sunflower stems.
The extrusion process results in a marked increase in the average fiber aspect ratio, leading to improved mechanical properties of fiberboards. The twin-screw extruder can also be fitted with a filtration module at the end of the barrel. The continuous extraction of various chemicals (e.g., free sugars, hemicelluloses, volatiles from essential oil fractions, etc.) from the lignocellulosic substrate, and the fiber refining can, therefore, be performed simultaneously.
The extruder can also be used for its mixing ability: a natural binder (e.g., Organosolv lignins, protein-based oilcakes, starch, etc.) can be added to the refined fibers at the end of the screw profile. The obtained premix is ready to be molded through hot pressing, with the natural binder contributing to fiberboard cohesion. Such a combined process in a single extruder pass improves the production time, production cost, and may lead to reduction in plant production size. Because all the operations are performed in a single step, fiber morphology is better preserved, thanks to a reduced residence time of the material inside the extruder, resulting in enhanced material performances. Such one-step extrusion operation may be at the origin of a valuable industrial process intensification.
Compared to commercial wood-based materials, these fully bio-based fiberboards do not emit any formaldehyde, and they could find various applications, e.g., intermediate containers, furniture, domestic flooring, shelving, general construction, etc.

A versatile twin-screw extrusion process to provide an efficient thermo-mechano-chemical pretreatment on lignocellulosic biomass was developed, which leads to an increased average fiber aspect ratio. A natural binder can also be added continuously after fiber refining, leading to bio-based fiberboards with improved mechanical properties after hot pressing of the obtained extruded material.

A versatile twin-screw extrusion process to provide an efficient thermo-mechano-chemical pre-treatment on lignocellulosic biomass before using it as ...