Non-catalytic upgrading of fast pyrolysis bio-oil in supercritical ethanol and combustion behavior of the upgraded oil

Prajitno, Hermawan; Insyani, Rizki; Park, Jong–Keun; Ryu, Changkook; Kim, Jaehoon

doi:10.1016/j.apenergy.2016.03.093

Cited by 99 publications

(40 citation statements)

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“…The reductive catalytic fractionations (RCF) of lignocellulosic biomass were performed by using a custom‐built batch reactor, made of SUS 316 stainless steel, with an inner volume of 140 mL, and fitted with a magnetically driven stirrer. A detailed description of the reactor system was included in our previous paper . In each reductive catalytic fractionation reaction, wood sawdust (5 g), solvent mixture (40 mL, EtOH/water/HCOOH) and Ni x –Al/AC catalyst (0.75–1.5 g) were placed in the reactor.…”

Section: Methodsmentioning

confidence: 99%

“…The qualitative analysis of DSO was carried out by using an Agilent Technologies 7890A GC with a time‐of‐flight mass spectrometer (TOF/MS) detector. A detailed description and the measurement conditions of the GC‐TOF/MS are reported elsewhere . The quantification of LDPMs in DSO was carried out by using an Agilent Technologies 6890N GC equipped with an Rxi‐5Sil‐MS capillary column and a flame ionization detector (FID).…”

Section: Methodsmentioning

confidence: 99%

“…The reductive catalytic fractionations (RCF) of lignocellulosic biomass were performed by using ac ustom-built batch reactor,m ade of SUS 316 stainless steel, with an inner volume of 140 mL, and fitted with am agnetically driven stirrer.Adetailed description of the reactor system was included in our previous paper. [34] In each reductive catalytic fractionation reaction, wood sawdust (5 g), solvent mixture (40 mL, EtOH/water/HCOOH) and Ni x -Al/AC catalyst (0.75-1.5 g) were placed in the reactor.T he reactor was closed and purged with N 2 or H 2 gas for 5min, using ap urge line that was dipped into the liquid phase, to remove dissolved oxygen in the liquid phase and the oxygen in the reactor head, and then pressurized at the experimental pressure with N 2 or H 2 .T he reactor was then heated to the experimental temperature (170-230 8C) at a heating rate of approximately 15 8Cmin À1 .A fter reaching the designated reaction temperature, the reaction was allowed to proceed for 1-4 h. After the reaction, the reactor was quickly quenched to 100 8Cb yusing aw ater basket, to prevent further reaction during the cooling period. The reactor pressure was recorded after complete cooling to calculate the quantity of gas produced.…”

Section: Reductive Catalyticfractionationmentioning

confidence: 99%

“…[35] The qualitative analysis of DSO was carried out by using an Agilent Te chnologies 7890A GC with at ime-of-flight mass spectrometer (TOF/MS) detector.A detailed description and the measurement conditions of the GC-TOF/MS are reported elsewhere. [34] The quantification of LDPMs in DSO was carried out by using an Agilent Technologies 6890N GC equipped with an Rxi-5Sil-MS capillary column and af lame ionization detector (FID). For the quantitation of commercially available phenolic monomers (PÀG, P=G, and POHÀG), external standard calibration curves were used, whereas the monomers that are not available in commercial markets (PÀS, P=S, and POHÀS) were quantified by using an effective carbon number method.…”

Section: Characterization Of Productsmentioning

confidence: 99%

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Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al₂O₃ Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

et al. 2019

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Highly dispersed, core–shell Ni@Al2O3 on activated carbon (AC) catalysts were prepared to develop an effective, external‐hydrogen‐free fractionation process for various types of lignocellulosic biomass. In a mixture of formic acid, ethanol, and water at 190 °C, the conversion of oak wood produced 23.4 C% lignin‐derived phenolic monomers (LDPMs) and highly delignified pulp‐rich solid. At an early stage, formic acid acted as a cocatalyst to enhance the delignification by solvolysis, and at a later stage, it acted as a hydrogen source to stabilize the phenolic monomers by hydrodeoxygenation and hydrogenation. Based on the positive correlation between spillover hydrogen on the catalysts and LDPM yields, a new suite of catalyst design criteria was proposed to develop highly active, non‐noble‐metal based catalysts for realizing economically viable biorefineries. Enzymatic saccharification of the pulp‐rich solid indicated that the pulp‐rich solid is an excellent source of fermentable sugars.

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Section: Methodsmentioning

confidence: 99%

Section: Methodsmentioning

confidence: 99%

Section: Reductive Catalyticfractionationmentioning

confidence: 99%

Section: Characterization Of Productsmentioning

confidence: 99%

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Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al₂O₃ Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

et al. 2019

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“…[1,2] Faced with this challenge,n ew types of energy are in demand and the energy structure needs to be changed. [3,4] Biomass has been considered to be one of the most valuable substitutes due to its wide availability and low cost. [5,24] Bamboo,a sa ni mportant part of biomass,i sw idely distributed in China.…”

Section: Introductionmentioning

confidence: 99%

Catalytic Fast Pyrolysis of Bamboo over Micro‐mesoporous Composite Molecular Sieves

Zhong

Zhang

et al. 2018

Energy Tech

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To upgrade biocrude oils from biomass pyrolysis, a novel micro‐mesoporous composite molecular sieve with HZSM‐5 structure as the core and MCM‐41 structure as the shell is synthesized and utilized. The synthesized hierarchical catalyst is characterized using X‐ray diffraction, N2 adsorption–desorption measurements, and transmission electron microscopy. Catalytic fast pyrolysis of bamboo over the composite molecular sieve is implemented using quantitative pyrolysis‐gas chromatography/mass spectrometry (Py‐GC/MS). The experimental results demonstrate that the highest relative content of hydrocarbons (34.41 %) is obtained at 600 °C when bamboo is pyrolyzed by only HZSM‐5, which has significant shape‐selective effect on the products of aromatic hydrocarbons but is easily coked. When a two‐layer catalyst bed of MCM‐41 and HZSM‐5 is used to obtaining higher catalytic activity, the two‐layer catalyst bed is capable of the promotion of hydrocarbon production with a relative content of 41.44 % because the hierarchical catalyst has higher flexibility than the two‐layer catalyst bed. It is found that the concentration of alkali solution used significantly influences the catalytic effects of composite molecular sieve. Additionally, the catalyzed transformation of oxygenated chemicals into hydrocarbons can be facilitated with the utilization of hexadecyl trim‐ethyl ammonium bromide (CTAB) in comparison with NaOH.

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A Two‐Step Approach for the Conversion of Technical Lignins to Biofuels

Figueirêdo

Venderbosch

Deuss

et al. 2020

Advanced Sustainable Systems

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strategies to valorize lignin are required. Depolymerization of lignin has been shown to have considerable potential, [6] leading to innovative lignin-derived biofuels [7,8] or drop-in chemicals. [9] In its native form, lignin consists of a highly crosslinked and methoxylated phenylpropanoid network. The structure of the biopolymer changes during isolation in typical (industrial) processes like the Kraft process used in the pulp and paper industry. [10] These technical lignins are currently produced at large scales (e.g., 50 million tons per year of Kraft lignin [11]) and consist of recalcitrant and remarkably complex structures as a result of their processing. Therefore, depolymerization is highly challenging. Various routes have been explored, and some examples are oxidative and reductive treatments using homogeneous and heterogeneous catalysts. [12] Catalytic hydrotreatment is a well-known reductive upgrading strategy for technical lignins. It involves treatment of lignin with molecular hydrogen (or a hydrogen donor) in the presence of a suitable catalyst. Upon this treatment, hydrodeoxygenation and hydrocracking reactions occur, and a range of valuable monomers can be obtained. [12,13] Interesting results have been reported using different setups, catalysts, reaction conditions, and lignin types (Table 1). Nonetheless, the harsh conditions that typically required cause competitive repolymerization that ultimately leads to char in addition to carbon losses to the gas phase. Altogether, these reactions have a negative impact on the techno-economic viability of the process. Furthermore, due to the presence of stable CC bonds in technical lignins, the yield and quality of the hydrotreated products are yet not optimal for such high end application. [14] Oxidation strategies have been also reported for lignin depolymerization, [12,33-35] from which ozonation stands as a relatively simple treatment for upgrading technical lignins. Ozone was shown to be highly reactive toward phenolic nuclei and CC double bonds at ambient conditions, and neither chemical additives nor catalysts are typically required. [36] It can be easily generated in situ either from oxygen or dry air, and such ozone generation technologies are industrially used [37,38] and thus wellestablished, safe, and available at all scales. Furthermore, ozone has a half-life of <1 h when dissolved, [39] thus any residual ozone in the system quickly decomposes to O 2 , providing an overall clean process with no need of extra separation steps. [40] Previous research has shown that the products obtained by ozonation Lignocellulose is a widely available carbon source and a promising feedstock for the production of advanced second-generation biofuels. Nonetheless, lignin, one of its major components, is largely underutilized and only considered an undesired byproduct. Through catalytic hydrotreatment, the highly condensed lignin can be partially depolymerized into a range of monomers. However, its recalcitrance and the presence of aromatic fragments linked by C...

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Non-catalytic upgrading of fast pyrolysis bio-oil in supercritical ethanol and combustion behavior of the upgraded oil

Cited by 99 publications

References 63 publications

Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al₂O₃ Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al₂O₃ Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

Catalytic Fast Pyrolysis of Bamboo over Micro‐mesoporous Composite Molecular Sieves

A Two‐Step Approach for the Conversion of Technical Lignins to Biofuels

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Non-catalytic upgrading of fast pyrolysis bio-oil in supercritical ethanol and combustion behavior of the upgraded oil

Cited by 99 publications

References 63 publications

Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al2O3 Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al2O3 Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

Catalytic Fast Pyrolysis of Bamboo over Micro‐mesoporous Composite Molecular Sieves

A Two‐Step Approach for the Conversion of Technical Lignins to Biofuels

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Product

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Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al₂O₃ Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source

Fractionation of Lignocellulosic Biomass over Core–Shell Ni@Al₂O₃ Catalysts with Formic Acid as a Cocatalyst and Hydrogen Source