**About the Editors**

**Tae Hyun Kim** is currently a professor of the Department of Materials Science & Chemical Engineering at Hanyang University, and he was formerly a faculty member at Iowa State University and Kongju National University. He received his B.S. degree in Chemical Engineering from Hanyang University in 1994. He received his Ph.D. degree in Chemical Engineering in 2004. He has worked at two companies, namely Samsung Engineering and LG Chemical, and at USDA-ARS-ERRC.

**Chang Geun Yoo** is currently an assistant professor in the Department of Chemical Engineering at State University of New York College of Environmental Science and Forestry. He received his B.S. and M.S. degrees in Chemical Engineering from Hanyang University and received his Ph.D. degree in Agricultural and Biosystems Engineering from Iowa State University in 2012. After graduation, he worked as a postdoc research associate at the University of Wisconsin–Madison and Oak Ridge National Laboratory. He started his current position at SUNY ESF in 2018.

### *Editorial* **Advancements in Catalytic Conversion of Biomass into Biofuels and Chemicals**

**Chang Geun Yoo 1,\* and Tae Hyun Kim 2,\***


Received: 13 October 2020; Accepted: 14 October 2020; Published: 19 October 2020

**Abstract:** The shortage of resources and increasing climate changes have brought the need for sustainable and renewable resources to people's attention. Biomass is an earth-abundant material and has great potential as a feedstock for alternative fuels and chemicals. For the effective utilization of biomass, this biopolymer has to be depolymerized and transformed into key building blocks and/or the targeted products, and biological or chemical catalysts are commonly used for the rapid and energy-efficient reactions. This Special Issue introduces recent advances in the catalytic conversion of biomass into biofuels and value-added products.

**Keywords:** biomass; catalysts; solvents

Over the past several decades, petroleum has been used as an essential resource in our lives. However, the rapid increase in the consumption of petroleum-based resources and environmental issues such as greenhouse gas emissions and climate change demand the use of alternative resources. Compared to other renewable sources, such as solar, wind, hydro, and geothermal, biomass has a broader spectrum of applications (e.g., biofuels, biochemicals, biomaterials). However, in order to utilize biomass, its rigid cell wall structures need to be deconstructed and selectively fractionated in advance. The cell walls of biomass are mainly composed of cellulose, hemicellulose, and lignin with other minor components such as extractives, ash, and protein. Recalcitrance factors, including crystalline cellulose, acetylated xylan, lignin, lignin-carbohydrate complex, and inorganic components, must be removed or at least reduced to some extent for effective biomass conversion [1,2].

Pretreatment is designed to eliminate these factors using various solvents and catalysts. Hydrothermal, acid, alkaline, organosolv and other methods have been applied to improve the biological conversion of cellulose and hemicellulose into biofuels and biochemicals [3–6]. Notable enhancements in enzymatic hydrolysis and fermentation were reported with these pretreatments. In addition, robust and effective biocatalysts (i.e., enzymes) and microorganisms have solved many technical problems. Unfortunately, due to the low price of petroleum-based resources these days, these bio-products are not cost-competitive by themselves.

Further enhancement of the efficiency of biomass conversion process and valorization of by-products such as lignin are the possible solutions to overcome this challenge. Several solvents, such as ionic liquids, deep eutectic solvents, molten salt hydrates, and cellulose-derived solvents, have been designed to improve the biomass conversion [7–10]. These solvents provided similar or better biomass conversion under milder conditions compared to the traditional pretreatments. Many catalysts were also designed for improving other key reactions such as hydrolysis, isomerization, hydrogenation, and oxidation of carbohydrates and lignin [11–14]. In particular, solid heterogeneous

catalysts have much better catalyst recyclability and product separation than homogeneous catalysts and biocatalysts [15,16].

Fractionation strategies for co-utilizing hemicellulose and lignin have also been studied. The fractionation process aims to separate the unnecessary components from the main product stream with high purity and yield. Therefore, finding and applying a selective as well as an effective catalyst and solvent are crucial. A biphasic solvent system [10] or co-solvent system mixed with an organic and aqueous solution [17] specifically increased the recovery of hydrophobic components (e.g., lignin) and degradation products (e.g., furfural and HMF) by preventing unwanted side reactions in aqueous environments. In addition to the high separation efficiency of each component, fractionation can preserve the quality of the separated components by minimizing their condensation and formation of pseudo-lignin.

Both solvents and catalysts play an important role in biomass conversion. This Special Issue introduces a recent catalytic biomass conversion and upgrade approaches. The published articles provide a clue to solve the technical and economic challenges in biomass utilization.

**Funding:** This article received no external funding.

**Conflicts of Interest:** The authors declare no conflict of interest.

#### **References**


**Publisher's Note:** MDPI stays neutral with regard to jurisdictional claims in published maps and institutional affiliations.

© 2020 by the authors. Licensee MDPI, Basel, Switzerland. This article is an open access article distributed under the terms and conditions of the Creative Commons Attribution (CC BY) license (http://creativecommons.org/licenses/by/4.0/).

## *Article* **Improvement of Organosolv Fractionation Performance for Rice Husk through a Low Acid-Catalyzation**

#### **Tae Hoon Kim 1,2, Hyun Jin Ryu <sup>1</sup> and Kyeong Keun Oh 1,3,\***


Received: 18 April 2019; Accepted: 9 May 2019; Published: 11 May 2019

**Abstract:** For the effective utilization of rice husk, organosolv fractionation was investigated to separate three main components (glucan, xylose, and lignin) with low acid concentration. Reaction temperatures of 170–190 ◦C, ethanol concentrations of 50%–70% (*v*/*v*), and sulfuric acid concentrations of 0%–0.7% (*w*/*v*) were investigated, with the reaction time and liquid-to-solid ratio kept constant at 60 min and 10, respectively. The fractionation conditions for the efficient separation into the three components of rice husk were determined to be 180 ◦C, 60% (*v*/*v*) of ethanol, and 0.25% (*w*/*v*) of sulfuric acid. Under these fractionation conditions, 86.8% of the xylan and 77.5% of the lignin were removed from the rice husk, and xylose and lignin were obtained from the liquid in 67.6% and 49.8% yields, respectively. The glucan digestibility of the fractionated rice husk was 85.2% with an enzyme loading of 15 FPU (filter paper unit) of cellulase per g-glucan.

**Keywords:** biomass; xylan; lignin; cellulose; pretreatment

#### **1. Introduction**

World rice production is 685 million tons per year, and 137 million tons of rice husk (RH) is generated [1]. Despite the enormous amount of RH, most of it is burned or buried in the ground because of lax environmental standards and technological limitations [2]. However, researchers have been attempting to develop efficient uses for RH. Because of its high ash content, RH has been studied in fields such as absorbents, coatings, pigments, the cement industry, insulators, rubber, and electronics [3]. However, these studies have focused only on the ash content of RH, which cannot be considered an efficient use. The composition of RH differs by location but typically includes 49.5% to 64.2% carbohydrates, including cellulose and hemicellulose, and 13.5% to 40.2% lignin [4]. In general, carbohydrates and lignin are sources of high-value-added materials in the biorefinery field. For example, pure cellulose can be converted into fibers or energy and hemicellulose can be converted into high-value-added materials such as furfural, succinic acid, and xylooligosaccharide [5]. Lignin can be used as phenolic platform chemicals such as catechols, cresols, or hydrocarbon precursors [6]. Therefore, the fractionation of lignocellulosic biomass into major components such as cellulose, hemicellulose, and lignin is an effective method to use RH [5].

Different catalysts, including acids, alkalis, organic solvents, and ionic liquids, have been used to separate the major components of lignocellulosic biomass [7]. Among these chemicals, organic solvents offer numerous advantages. Organic solvent (organosolv) fractionation can separate RH into three major components in a single process and therefore assist downstream processing, e.g., enzymatic hydrolysis [8]. When ethanol (EtOH) is used as an organic solvent, it can dissolve hemicellulose and lignin in the liquid hydrolyzate while leaving a high content of cellulose in the residual solid. The removal of hemicellulose and lignin from biomass improves the enzymatic digestibility of cellulose by increasing enzyme accessibility [9]. The lignin extracted into the liquid can be easily precipitated by exploiting the difference in EtOH solubility, and high-quality, high-purity lignin is precipitated [10]. Additional advantages of organosolv-precipitated lignin include a low molecular weight, uniform molecular weight distribution, hydrophobicity, and a low glass transition temperature, which makes the precipitated lignin easy to use in various applications, as previously mentioned [11]. Furthermore, EtOH can be easily recovered and recycled, which is economically advantageous [12]. Although EtOH is known to exhibit high solubilization of lignin, it is generally used in conjunction with an added acid catalyst. The use of an acid catalyst not only leads to a mild reaction but also decomposes the carbohydrate-lignin complex more easily than when an acid catalyst is not used [9,13]. Therefore, the use of an appropriate acid catalyst can improve the efficiency of the fractionation process.

The purpose of this study is to effectively extract xylose and lignin from RH and to improve the enzymatic digestibility of fractionated solids. The EtOH organosolv process was evaluated at various independent variables (reaction temperatures, EtOH concentrations, and sulfuric acid (SA) concentrations). The effects of independent variables were determined in order to selectively extract the desired component in one stage process. In addition, the chemical characteristics of acid-free and acid-catalyzed organosolv precipitated lignin were compared.

#### **2. Results and Discussion**

#### *2.1. Organosolv Fractionation of RH*

#### 2.1.1. Organosolv Fractionation with Reaction Temperature and EtOH Concentration

Figure 1 presents the compositions of fractionated solid after organosolv fractionation (acid-free) under various reaction conditions. The effects of different reaction temperatures (170–190 ◦C) and EtOH concentrations (50%–70%) were investigated. As shown in Figure 1, the glucan and xylan contents in the fractionated solid were better retained at high EtOH concentrations (70%) than at low EtOH concentration (50%) at all of the investigated reaction temperatures (170–190 ◦C). This phenomenon is attributed to the hydrolysis reaction of water at different EtOH–water ratios. That is, a low EtOH concentration means a high concentration of hydronium ions, which would increase the reaction severity [14,15]. The pH at initial EtOH concentrations of 50%, 60%, and 70% were 6.24, 6.25, and 6.25, respectively; however, after reaction (170 ◦C, 60 min, liquid-to-solid (L/S) ratio of 10), the pH levels of 50%, 60%, and 70% EtOH solutions were 3.32, 4.12, and 4.89, respectively. These results are consistent with the results of the liquid hydrolyzate analysis shown in Figure 2. As the EtOH concentration (50%–70%) and reaction temperature (170–190 ◦C) were increased, smaller amounts of sugars (glucose and xylose) and byproducts (formic acid, acetic acid, levulinic acid, 5-HMF, and furfural) were released in the liquid hydrolyzate. As byproducts (except for acetic acid) are produced by the decomposition of cellulose and hemicellulose, they are generally used as an indicator of reaction severity [16]. In particular, the 5-HMF was generated under the most severe reaction conditions (190 ◦C, 50%) via hexose decomposition. Under these conditions (190 ◦C, 50%), the lignin extraction yield was only 46.0%; thus, large amounts of lignin remained in the solids.

**Figure 1.** Effects of reaction temperature and EtOH concentration on the chemical compositions of the raw and fractionated solids of rice husk: (**a**) 170 ◦C, (**b**) 180 ◦C, and (**c**) 190 ◦C. Note: reaction conditions: 170–190 ◦C, 50%–70% EtOH concentration.

**Figure 2.** Effects of reaction temperature and EtOH concentration on the sugar extraction yield and byproducts concentration of liquid hydrolyzate: (**a**) 170 ◦C, (**b**) 180 ◦C, and (**c**) 190 ◦C. Note: reaction conditions: 170–190 ◦C, 50%–70% EtOH concentration.

The SA was added as an acid catalyst to improve the organosolv fractionation performance. Figure 3 presents the effects of reaction temperature (180 ◦C, 190 ◦C) and EtOH concentration (50%–70%) on the chemical composition of the fractionated solid. As shown in Figure 3, the xylan content decreased under all of the investigated reaction conditions. In particular, xylan was not detected under the conditions of 190 ◦C and 50% or 60% EtOH concentration. However, as shown in Figure 4, xylose extracted from the RH was not present in the liquid hydrolyzate. The formation of furfural indicates decomposition of the pentose sugar (xylose), which in turn indicates an increase in the severity of the reaction conditions. As shown in Figure 4, the xylose extraction yield of liquid hydrolyzate was greater at 180 ◦C than at 190◦C, which means that xylose was decomposed into furfural because of the severe conditions (190 ◦C). However, as shown in Figure 3, the glucan content (88.4%–90.3%) was well preserved in the fractionated RH at 180 ◦C but was somewhat lower (76.1%–77.4%) at 190 ◦C. As previously mentioned, glucose was considered to be decomposed into byproducts such as formic acid, levulinic acid, and 5-HMF because of the severe reaction conditions at 190 ◦C (Figure 4).

**Figure 3.** Effects of reaction temperature and EtOH concentration on the chemical compositions of raw and fractionated solid of rice husk: (**a**) 180 ◦C and (**b**) 190 ◦C. Note: reaction conditions: 180–190 ◦C, 50%–70% EtOH concentration, 0.25% (*w*/*v*) H2SO4 concentration.

**Figure 4.** Effects of reaction temperature and EtOH concentration on the sugar extraction yield and the byproducts concentration of liquid hydrolyzate: (**a**) 180 ◦C and (**b**) 190 ◦C. Note: reaction conditions: 180–190 ◦C, 50%–70% EtOH concentration, 0.25% (*w*/*v*) H2SO4 concentration.

The delignification yield tended to increase with increasing EtOH concentration. In general, a high EtOH concentration increases the lignin solubility; however, Ni and Hu reported that lignin exhibited maximal solubility at an EtOH concentration of 70% [17]. If the EtOH concentration exceeds 70%, the lignin solubility decreases slightly. Therefore, the appropriate EtOH concentration for delignification is likely in the range from 60% to 70%.

#### 2.1.2. Acid-Catalyzed Organosolv Fractionation for Xylose and Lignin Extraction

The effect of acid concentration in the organosolv fractionation is shown in Figure 5. As the SA concentration was increased from 0.15% to 0.7%, the glucan and xylan contents of the fractionated solid decreased (Figure 5a). At an SA concentration of 0.7%, xylan was not present and the amount of glucan was substantially decreased. The difference in SA concentration was confirmed more clearly in the hydrolyzate results in Figure 5b. The xylose extraction yield increased with increasing SA concentration from 0.15% to 0.25%. However, the highest xylose extraction yield (67.5%) was observed at 0.25% and tended to decrease with increasing SA concentration as the SA concentration was progressively increased to 0.7%. When hexose sugar (mainly glucose) is degraded under severe conditions, it is converted into formic acid, levulinic acid, and 5-HMF. A large amount of formic acid, levulinic acid, and 5-HMF were produced at SA concentrations of 0.35% and 0.7%, accompanied by a substantial decrease of the glucan content in the fractionated RH (Figure 5b). However, the change in lignin was inconsequential as the SA concentration was increased from 0.25% to 0.7%. This result means that an improvement of the delignification effect should not be expected at SA concentrations above a certain concentration. In the present system, the optimal SA concentration was determined to be 0.25%.

**Figure 5.** Effects of reaction temperature and H2SO4 concentration on (**a**) the chemical compositions of raw and fractionated solids of rice husk and (**b**) the sugar extraction yield and concentration of byproducts of liquid hydrolyzate. Note: reaction conditions: 180–190 ◦C, 60% EtOH concentration, 0.15%–0.7% (*w*/*v*) H2SO4 concentration.

2.1.3. Comparison with Acid-Free and Acid-Catalyzed Organosolv Fractionation

The chemical compositions of raw and fractionated RH and the extraction yields of glucose and xylose (under acid-free and acid-catalyzed conditions) are compared in Figure 6. The reaction temperature, reaction time, and EtOH concentration were fixed at 180 ◦C, 60 min, and 60% (*v*/*v*), respectively. As shown in Figure 6a, the glucan content did not show a dramatic difference under acid-free and acid-catalyzed conditions. By contrast, the xylose and lignin extraction yields were dramatically improved under acid catalysis. In addition, the xylose extraction yield under acid catalysis was also improved more than twofold (Figure 6b). Thus, in organosolv fractionation, SA can improve the xylose and lignin extraction yields.

**Figure 6.** Comparison of acid-free and acid-catalyzed organosolv fractionations: (**a**) chemical composition of the fractionated RH and (**b**) the extraction yield of sugars. Note: reaction conditions: acid free: 180 ◦C, 60% EtOH concentration; acid catalyzed: 180 ◦C, 60% EtOH concentration, 0.25% H2SO4 (*w*/*v*) concentration.

#### 2.1.4. Enzymatic Hydrolysis Tests

The enzymatic hydrolysis tests were performed with raw and fractionated RH; the results are present in Figure 7. The acid-catalyzed organosolv-fractionated RH showed 80.1% enzyme digestibility in 24 h, and the maximum digestibility was 85.2% at 72 h. By contrast, the acid-free organosolv-fractionated RH showed only 32.5% enzyme digestibility at 72 h and showed no appreciable difference in enzyme digestibility from the raw RH (24.5%). This lack of improvement in enzyme digestibility is attributed to xylan and phenolic compounds (lignin), which were insufficiently removed, interfering with cellulase access to the fractionated RH.

**Figure 7.** Enzymatic digestibility profiles of raw and fractionated RH; acid free: 180 ◦C, 60% EtOH concentration; acid catalyzed: 180 ◦C, 60% EtOH concentration, 0.25% H2SO4 (*w*/*v*) concentration. Note: enzymatic hydrolysis conditions: 15 FPU of Cellic® CTec2/g-glucan, pH 4.8, 50 ◦C, and 150 rpm.

#### *2.2. Chemical Characteristics of Organosolv-Fractionated Lignin*

The hydroxyl groups, which include aliphatic hydroxyl groups, phenolic hydroxyl groups (*p*-hydroxyphenyl units, guaiacyl units, and syringyl units), and carboxyl groups of lignin, were analyzed by 31P NMR. The amounts of hydroxyl groups were calculated on the basis of an internal standard (cyclohexanol); the respective integrated peak areas are presented in Table 1. The *M*n, *M*w, and PD of lignin were determined by GPC; the results are presented in Table 1. As shown in Table 1, the acid-catalyzed organosolv-fractionated lignin contained higher concentrations of phenolic hydroxyl groups and carboxyl groups compared with the acid-free organosolv-fractionated lignin. This result is related to the severity of the reaction. In general, the β-aryl ether linkage is known to occupy 50% of the lignin structure [18]. With increasing reaction severity, phenolic hydroxyl and carboxyl groups generate more aromatic monomers through cleavage of the β-O-4 linkage [19]. Furthermore, cleaving β-O-4 linkages causes a decrease in lignin molecular weight [20]. These results are consistent with the molecular-weight results shown in Table 1, where the molecular weight of acid-catalyzed organosolv-fractionated lignin was higher than that of acid-free organosolv-fractionated lignin


**Table 1.** Hydroxyl groups and molecular weight of acid-free and acid-catalyzed organosolv precipitated lignin from RH.

<sup>1</sup> Number-average molecular weight, <sup>2</sup> Weight-average molecular weight, <sup>3</sup> Polydispersity index (*Mw*/*Mn*).

The previously presented results indicate that the acid-catalyzed organosolv-fractionated lignin has a low molecular weight, uniform molecular weight distribution, and a high concentration of phenolic hydroxyl groups. The phenolic hydroxyl groups increase the reactivity of lignin toward formaldehyde when aromatic polymers are used in phenolic resin formulations [21,22]. Therefore, lignin with these characteristics would be suitable for application in the biorefinery field.

#### *2.3. Overall Fractionation Yield and Total Mass Balance*

The extraction mass balance (EMB) of raw and fractionated RH was present in Table 2. In the acid-free organosolv fractionation, 91.8% of glucan was preserved from the fractionated RH and 31.6% of xylose and 11.0% of lignin were obtained from the liquid hydrolyzate. By contrast, in the acid-catalyzed organosolv fractionation, 89.9% of glucan was preserved from the fractionated RH and 67.6% of xylose and 49.8% of lignin were obtained from the liquid hydrolyzate. As the P lignin shown in Table 2 was lignin precipitated from liquid hydrolyzate, conclusively, three main components (glucan, xylose, and lignin) of RH were separated. Therefore, the acid-catalyzed organosolv pretreatment is a valuable process to fractionate three main components for RH in the biorefinery field.

**Table 2.** Extraction mass balance of sugars and lignin with acid-free acid acid catalyzed orgarnosolv fractionation of RH.


Fractionation conditions: Acid-free: 180 ◦C, 60 min, 60% (*v*/*v*) EtOH; acid catalyzed: 180 ◦C, 60 min, 60% (*v*/*v*) EtOH, 0.25% (*w*/*v*) H2SO4. <sup>1</sup> Extraction mass balance (EMB) = ( - *CLi* + - *CSi*)/( - *CRi*), where *Ci* is the mass of each component as *CLi*, as determined through HPLC chromatography. The subscripts *L*, *S*, and *R* refer to the extracted liquid, fractionated solids, and raw fractions respectively. <sup>2</sup> Precipitated lignin from liquid hydrolyzate. <sup>3</sup> Data are based on the oven-dried raw biomass.

The simplified flowchart and an overall mass balance of the acid-catalyzed organosolv fractionation and consecutive enzymatic hydrolysis are summarized in Figure 8. Most of the hemicellulose and lignin were separated from the RH by organosolv fractionation with SA. Under the optimized conditions, approximately 49.9 g of the mass fraction was solubilized into liquid hydrolysate, which involved discharging 11.8 g of xylan, 17.6 g of lignin, and 4.7 g of glucan (based on 100 g of raw RH) from the

reactor for recovery of lignin by the precipitation method. The residual solid, i.e., 50.1 g of acid-catalyzed fractionated RH, was subjected to consecutive enzymatic hydrolysis. The liquor resulting from the enzymatic hydrolysis had a sugar fraction including 30.0 g of glucose and 1.5 g of xylose, which could be easily used for microbial fermentation. The acid-catalyzed organosolv fractionation was assumed to have greatly increased the cellulase effectiveness through the removal of hemicellulose and lignin.

**Figure 8.** Overall mass balance of the organosolv fractionation process of RH under optimal conditions.

#### **3. Materials and Methods**

#### *3.1. Materials*

RH was harvested at Gimpo-si, Gyeonggi-do, Korea and collected in 2017. The RH was ground with a blend mill (Blender 7012s, Waring Commercial, Stamford, CT, USA) and then sieved to a nominal size of 14–45 mesh (from 0.36 to 1.4 mm). The ground RH was placed in a convection oven at 45 ± 5 ◦C for 48 h and then stored in an automatic dehumidification desiccator until used. The average moisture content of the dried RH was 4.3% during the experiment. The composition of the RH was determined by the National Renewable Energy Laboratory (NREL, Golden, CO, USA) Laboratory Standard Procedure (LAP) [23–28]. The chemical composition of the raw RH was 35.6% glucan, 13.6% xylan, 1.7% arabinan, 22.7% acid insoluble lignin (AIL), 0.7% acid-soluble lignin (ASL), 1.2% EtOH extractives, 6.6% water extractives, and 15.7% ash (*n* = 3, standard deviations < 0.8).

EtOH (cat. no. E7023), sodium azide (cat. no. S2002), tetrahydrofuran (THF, cat. no. 401757), pyridine (cat. no. 270970), chloroform-d (cat. no. 151858), cyclohexanol (cat. no. 105899), chromium(III) acetylacetonate (cat. no. 574082), 2-chloro-4,4,5,5-tetramethyl-1,2,3-dioxaphospholane (TMDP, cat. no. 447536), and cellulase enzyme Cellic® CTec2 (Novozymes, A/S Bagsvaerd, Denmark) were purchased from Sigma-Aldrich Korea.

#### *3.2. Experimental Setup and Operation*

The batch reactor used for the organosolv fractionation process consisted of reaction baths (a molten salt bath and a silicone oil bath) and a cooling bath (water bath). The temperatures of the molten salt bath and the silicone oil bath could be driven to 250 ◦C and 200 ◦C, respectively. The molten salt bath was used for preheating to the target temperature, the silicone oil bath was used for maintaining the reaction temperature, and the water bath was used for cooling. The average preheating time was less than 1.0 min under all of the investigated reaction temperature conditions. The fractionation reactor, a bomb tubular reactor, was constructed of SS-316L tubing with a 10.9 mm ID and a 150 mm length (14.0 cm3 internal volume). The temperatures of the reaction baths and fractionation reactors were measured continuously with high-temperature thermocouples (catalog number HY-72D, Hanyoung Nux, Incheon, Korea). The timer and movement controller were set up to control the reaction time and movement of the fractionation reactors, respectively.

When the reaction was completed, the liquid samples were removed from the reactor, diluted threefold with deionized (DI) water to precipitate the lignin, and then evaporated in a drying oven at 55 ◦C for 4 h. The liquid samples were analyzed to determine their concentrations of carbohydrates (i.e., glucose, xylose, and arabinose) and byproducts. The fractionated solids discharged from the reactor were separated into two portions. One portion was dried using a convection oven for weight-loss measurement and composition analysis. The other portion was subjected to an enzymatic digestibility test in the wet state.

#### *3.3. Enzymatic Digestibility Tests*

The enzymatic digestibility test of raw and fractionated RH was determined according to the NREL LAP [27]. The tests were conducted under the following conditions: 50 ◦C, pH 4.8 (0.05 M sodium citrate buffer), 150 rpm in a shaking incubator (model VS-8480SFN, Vision Scientific Co., Bucheon, Korea) and 15 FPU g-glucan enzyme loadings. The average activity of the cellulase was measured to be 119.4 FPU/mL. The initial glucan concentration was 1.0% (*w*/*v*) based on 100 mL of total liquid in a 250 mL Erlenmeyer flask. To prevent microbial contamination, 1.0 mL of 20 mg/mL sodium azide was added. Samples were collected periodically at appropriate sampling times (6, 12, 24, 48, and 72 h) and analyzed for hydrolyzed glucose using a high-performance liquid chromatography (HPLC) system.

#### *3.4. Composition Analysis of Raw and Fractionated RH*

The chemical compositions of the solid and liquid samples were determined according to the procedures of the NREL-LAP [24,25,28]. The extractives process was carried out in two steps using water and EtOH consecutively. For the composition analysis of extractives-free and fractionated solids, two-step acid hydrolysis was carried out.

An HPLC system (LC-10A, Shimadzu Inc., Kyoto, Japan) with a refractive index (RI) detector (RID-10A, Shimadzu Inc., Kyoto, Japan) was used to determine the carbohydrate and organic acid components of the samples. For analysis of monomeric sugars from the raw and fractionated RH samples, a carbohydrate column (Aminex HPX-87P, Bio-Rad Inc., Hercules, CA, USA) was used; HPLC-grade water was used as the mobile phase with a volumetric flow rate of 0.4 mL/min. The samples were neutralized with calcium carbonate and filtered (0.2 μm pore size) before analysis. The operating temperature of the column was 80 ◦C. The liquid hydrolysis samples and enzymatic hydrolysis samples were analyzed using an organic acid column (Aminex HPX-87H, Bio-Rad Inc., Hercules, CA, USA); 5 mM SA was used as a mobile phase with a volumetric flow rate of 0.5 mL/min. These samples were also neutralized with calcium carbonate and filtered (0.4 μm pore size) before analysis. The operating temperature of the column was 65 ◦C.

#### *3.5. Chemical Characterization of Organosolv Fractionated Lignin*

The number-average molar mass (*M*n), weight-average molar mass (*M*w), and polydispersity (PD) of the organosolv fractionated lignin samples were determined by gel permeation chromatography (GPC, Ultimate 3000, Thermo Fisher Scientific Inc., Waltham, MA, USA). For molecular-weight determination, 3 mg of an acetylated lignin sample was dissolved in 2 mL of THF and filtered with a 0.45 μm polytetrafluoroethylene (PTFE) syringe filter to remove impurities. The GPC system was equipped with a Shodex column (KF-806L with Shodex KF-G guard column, Showa Denko, Tokyo, Japan) and an RI detector (Refracto Max 520, Thermofisher Scientific Korea Ltd, Seoul, Korea); THF was used as the mobile phase (1.0 mL/min); the injection volume was 20 μL.

31P NMR (Avance 600, Bruker, Billerica, MA, USA) spectra were recorded at 242.88 MHz and 256 scans with a 2 s pulse delay. For quantitative 31P NMR analysis, 20 mg of lignin sample was accurately weighed and dissolved in 400 μL of solution A and 150 μL of solution B in a 5 mL vial. Solution A was a mixture of pyridine and chloroform-d (CDCl3) at a ratio of 1.6:1 (*v*/*v*). Solution B was a mixture of solution A (25 mL), cyclohexanol (100 mg), and chromium(III) acetylacetonate (90 mg). The dissolved

liquid was vortexed for 5 min, 70 μL of TMDP was added to the solution, and the resultant mixture was analyzed with the 31P NMR system.

Fourier transform infrared (FTIR) spectroscopy (IRSpirit-L/T, Shimadzu Inc., Kyoto, Japan) was used to determine the characteristic absorption peaks of the chemical functional groups in the organosolv-fractionated lignin via the attenuated total reflectance (ATR) technique. Mid-IR spectra were collected by averaging 40 scans collected at a resolution of 1 cm−<sup>1</sup> over the wavenumber region from 4000 to 500 cm<sup>−</sup>1.

#### **4. Conclusions**

The results of this work indicate that acid-catalyzed organosolv fractionation using a low reaction severity (i.e., low acid concentration) is a worthwhile process in the field of biorefinery. Very pure lignin fractions were recovered, and the resulting hydrolyzate, xylose-rich liquid fraction can potentially be used for xylose-uptaking fermentations; similarly, the insoluble residue, the cellulose-rich solid fraction, could potentially be readily hydrolyzed at a low enzyme loading into glucose. These findings strongly suggest that a biorefinery procedure is required prior to a five-carbon fermentation process, as well as catalytic conversion of fractionated lignin, for full valorization of the cellulosic biomass.

**Author Contributions:** T.H.K., H.J.R., and K.K.O. contributed equally to this work. T.H.K. contributed to the experimental process for RH Fractionation and T.H.K. contributed to the project administration and experimental design. And H.J.R. contributed to providing the methodology and data validation. All of the authors contributed to the writing and review of this document.

**Funding:** This work was supported by the R and D program of Korea Institute of Energy Technology Evaluation and Planning (KETEP) grant funded by the Ministry of Trade, Industry and Energy (MOTIE), the Republic of Korea (No. 20183030091950).

**Conflicts of Interest:** The authors declare no conflict of interest.

#### **References**


© 2019 by the authors. Licensee MDPI, Basel, Switzerland. This article is an open access article distributed under the terms and conditions of the Creative Commons Attribution (CC BY) license (http://creativecommons.org/licenses/by/4.0/).

*Article*
