Open Access

Facile isothermal solid acid catalyzed ionic liquid pretreatments to enhance the combined sugars production from Arundo donax Linn.

  • Tingting You1,
  • Lupeng Shao1,
  • Ruizhen Wang1,
  • Liming Zhang1 and
  • Feng Xu1Email author
Biotechnology for Biofuels20169:177

https://doi.org/10.1186/s13068-016-0589-8

Received: 3 May 2016

Accepted: 15 August 2016

Published: 24 August 2016

Abstract

Background

Solid acid catalyzed inexpensive ionic liquid (IL) pretreatment is promising because of its effectiveness at decreasing biomass recalcitrance to subsequent enzymatic hydrolysis or in situ hydrolysis of carbohydrate oligomers. However, the conventional strategy was limited by the complex non-isothermal process and considering only one aspect of sugar recovery. In this study, facile isothermal pretreatments using Amberlyst 35DRY catalyzed 1-n-butyl-3-methylimidazolium chloride ([C4mim]Cl) at mild conditions were developed on bioenergy crop Arundo donax Linn. to enhance the combined sugars released. The physicochemical differences, enzymatic digestibility, and sugars released in situ were evaluated and compared to define the best set of conditions.

Results

The optimized isothermal pretreatment (110 °C, IL for 3 h, Amberlyst for 1 h) resulted in significant enhancement in combined sugars released (58.4 g/100 g raw materials), recovering 85.0 % of the total reducing glycan in the raw biomass. This remarkable improvement could be correlated to cellulose crystallinity reduction, crystalline conversion, and partial removal of the main chemical components caused by the pretreatment. Particularly, solubilization of hemicelluloses and partial depolymerization of cellulose contributed to the synergetic improvement of sugars production in enzymatic hydrolysis and in situ. Irrespective of the generous differences in mass recovery, the highest cellulose digestibility of 90.2 % and sugar released of 43.0 % (based on initial materials) in the pretreatment liquor were obtained. Interestingly, lignin (0.8–6.1 %) and sugars derived lactic acid (4.70–5.94 %) were produced without any notable deleterious effects.

Conclusions

Isothermal [C4mim]Cl-Amberlyst pretreatment was a highly effective, simple, and convenient process that produced high yields of fermentable sugars from recalcitrant biomass by in situ hydrolysis of soluble biomass and enhancement of cellulose digestibility of the regenerated biomass. Relatively high amount of new revenues beyond sugars of this pretreatment could promote the commercial viability.

Keywords

Arundo donax Linn. Acid enhanced ionic liquid pretreatment Enzymatic hydrolysis Total reducing sugars

Background

The world’s ever-growing energy demands and concerns over the shortage of oil reserves accompanying with its detrimental effects on climate change have garnered interest in the research for alternative renewable sources for the sustainable production of fuels and petroleum based products [1]. Dedicated bioenergy crops, such as switchgrass, miscanthus, and reed are renewable and present in great abundance that can be converted to transportation fuels and commodity chemicals [2, 3]. A perennial grass Arundo donax Linn. is a promising candidate when compared to other bioenergy crops because of its high biomass production, plant adaptability, and low input required for its cultivation [2]. Studies investigating the conversion of this biomass to fermentable sugars would bring economic and ecological benefits. Due to the naturally rigid and complex submicroscopic structure of plant, pretreatment is a pre-requisite step to modify the physical and chemical properties and to enhance enzymes accessibility to achieve high yields of fermentable sugars [4].

Ionic liquids (ILs) have held great promise as powerful green solvents for pretreatment and dissolution of biomass with improved yields of reducing sugars [59]. This process has certain advantages such as environmentally benign, feedstock agnostic, and short processing time demanded to convert pretreated biomass to high yields of fermentable sugars [5, 1012]. However, the high cost of IL impedes the industrial investment of this technology. Up to now, combinatorial pretreatments involving ILs and other chemicals have been developed to cut down the high cost of ILs whist boosting the sugars production [1315]. Among them, acid in inexpensive prototype 1-n-butyl-3-methylimidazolium chloride ([C4mim]Cl) pretreatments have been considered as cost-effective alternatives to the expensive IL to disrupt the physical and biochemical barriers for enzymatic hydrolysis [15]. In the earlier works, in situ hydrolysis of carbohydrate oligomers that dissolved in IL to monomers with acid catalysts was proposed [16, 17]. Nevertheless, there exists a void of explicit knowledge regarding the promotion to the combined sugars production by in situ hydrolysis of IL-soluble biomass and enhancement of cellulose digestibility of regenerated biomass after pretreatment across techniques. For instance, Sun and coworkers [17] have tended to focus only on the production and extraction of sugars produced in IL. The evaluation of the potential sugar production from regenerated solids was ignored after the pretreatment.

Maximizing valorization of lignocellulosic biomass can be achieved by neoteric methods using ILs and acid catalysts [18]. Fractionation of biomass with ionic liquid-acid systems to cellulose-rich fractions is believed to facilitate cellulose conversion [15]. Compared to the liquid acids, solid acids such as nafion, Amberlyst resins, and zeolites are less toxic, easy to recycle, and substantially mitigating the undesired degrading compounds in pretreatment liquors [19]. Moreover, a few compounds of commercial interest, such as phenolic acid and lactic acid can be directly accessible from biomass by using heterogeneous solid acid in ILs [2022]. For instance, da Costa Lopes and coworkers [21] used acid resin Amberlite XAD-7 to extract phenolic compounds that dissolved after a complete fractionation of biomass by IL. In our previous research, a two-step solid acid catalyzed [C4mim]Cl pretreatment has been developed to open the rigid structure of plants [23]. Accordingly, 5.21-fold enhancement of fermentable sugars yield from A. donax could be gained by enzymatic hydrolysis. More recently, new acidic ILs have been therefore designed to efficiently separate cellulose-rich fractions from lignocellulosic biomass to enhance the cellulose digestibility [6, 7, 9].

However, there are still some limitations inherent for the practical application of IL-solid acid pretreatments despite satisfactory sugars yields have been obtained. The previous proposed procedures [15, 23] required a comparatively high temperature (160 °C) in the first IL pretreated step, which was higher than the maximum operating temperatures of most resins. Therefore, additional cooling apparatus was demanded to cool down the system before adding any acid resins. The extra procedure makes the pretreatment more complex and poses pivotal equipment cost and energy challenge when considering as part of a practical, large-scale biomass pretreatment process. In addition, chloride based ILs were reported to show signs of decomposition at temperatures of 160 °C [24]. The high temperature used in the state-of-the-art methods might deteriorate ILs quality for reuse. Furthermore, the in situ sugars production directly during the pretreatment was out of consideration when evaluated the effectiveness of pretreatments. To advance the pretreatment technology, we describe a facile isothermal pretreatment that used Amberlyst 35DRY catalyzed [C4mim]Cl to achieve high combined fermentable sugars yields from bioenergy crops A. donax at mild conditions. The effects of pretreatments on the chemical composition, cellulose digestibility, structural features, and reducing sugars released in pretreatment liquors were detected and compared to find out the optimal condition. Other value-added chemicals were observed as the new revenues beyond sugars. The in-depth knowledge of this approach will be beneficial for raising the profitability of the entire biorefinery.

Results and discussion

Biomass isothermal pretreatment and dry mass recovery

A facile isothermal protic acid resin catalyzed ionic liquid pretreatment was utilized to deconstruct A. donax cell wall. To define the best set of conditions for pretreatment, A. donax was processed using different pretreatment combination of temperature and acid reaction time and the yields of recovered samples are compared in Table 1.
Table 1

Mass recovery and crystallinity of the raw and pretreated A. donax under different conditions

Samples

Pretreatment conditions

Recovered A. donax (%)

CrI (%)

LOI

[C4mim]Cl

Amberlyst 35DRY

Raw

Untreated

Untreated

100

36.0

1.43

R90-1.0

90 °C 3 h

90 °C 1.0 h

95.4

29.4

0.93

R100-1.0

100 °C 3 h

100 °C 1.0 h

78.4

31.4

0.58

R110-1.0

110 °C 3 h

110 °C 1.0 h

58.0

24.7

0.63

R120-0.5

120 °C 3 h

120 °C 0.5 h

66.1

23.2

0.53

R120-1.0

120 °C 3 h

120 °C 1.0 h

46.7

25.8

1.03

R120-1.5

120 °C 3 h

120 °C 1.5 h

31.7

27.3

0.56

R130-0.5

130 °C 3 h

130 °C 0.5 h

53.5

25.2

0.86

R140-0.5

140 °C 3 h

140 °C 0.5 h

28.2

25.8

1.15

R150-0.5

150 °C 3 h

150 °C 0.5 h

25.8

16.5

13.78

Temperatures of 90–150 °C and acid reaction time intervals of 0.5–1.5 h (Table 1) were used to avoid the degradation of Amberlyst 35DRY while reducing biomass recalcitrance. As expected, the dry mass recovery decreased gradually with increasing temperature and prolonging acid reaction time, ranging from 95.4 % for the R90-1 sample to 25.8 % for the R150-0.5 sample. After pretreatment at 90 °C and Amberlyst catalyzed for 1.0 h (R90-1.0), only 4.6 % biomass was consumed by the system, but more than 70 % biomass was lost after pretreatment at 150 °C and acid catalyzed for 0.5 h (R150-0.5). It is probably the consequences of severe degradation of carbohydrates and partial removal of lignin by IL-acid at high temperatures. Moreover, the A. donax pretreated at high temperatures likely reacted with the ionic liquid and formed a highly viscous paste that could increase the mass loss. It is interesting to note that the mass loss of R130-0.5 sample is lower than that of R120-1.0 and R120-1.5 samples. These values differed from those described in the literature by Trinh et al. [12], which indicated that the pretreatment of softwood at 130 °C in [C4mim]Cl resulted in considerable decrease in the solid yields than that at 120 °C. Rinaldi and coworkers [16, 25] reported that Amberlyst released hydronium ions (H3O+) in IL progressively to selectively cleave the longer cellulose chain and other soluble compounds to oligomers and sugars. Amberlyst reaction time was therefore suggested to be the main controlling factor at a high incubation temperature for mass recovery from A. donax.

Chemical composition of pretreated Arundo donax

Chemical composition determination is of vital importance to understand the biomass conversion. The chemical compositions of raw A. donax and of samples submitted to IL-Amberlyst pretreatments are illustrated in Table 2. As can be seen, the raw A. donax used in this study presents cellulose (44.59 %), hemicellulose (17.15 %), and lignin (20.54 %) composition similar to those reported in the literature for the same material, whose values vary from 29.2–42.15 % for cellulose, 19.2–32 % for hemicellulose and 19.20–24.3 % for lignin [2, 26]. Significant differences in chemical compositions were observed in the IL-Amberlyst pretreated samples.
Table 2

Chemical composition of the raw and pretreated A. donax obtained after isothermal [C4mim]Cl-Amberlyst 35DRY pretreatments

Samples

Cellulose

Hemicelluloses

AILa

ASLb

Ash

Acetyl

Raw

44.59 (44.59)c

17.52 (17.52)

19.15 (19.15)

1.39 (1.39)

0.81 (0.81)

4.91 (4.91)

R90-1.0

44.77 (42.71)

17.15 (16.36)

18.19 (17.35)

1.2 (1.14)

1.09 (1.04)

4.70 (4.49)

R100-1.0

52.38 (41.07)

15.7 (12.31)

19.06 (14.94)

1.25 (0.98)

1.11 (0.87)

4.89 (3.84)

R110-1.0

56.56 (32.80)

11.21 (6.50)

23.27 (13.50)

1.32 (0.77)

1.66 (0.96)

4.22 (2.45)

R120-0.5

51.39 (33.97)

14.13 (9.34)

22.73 (15.02)

1.17 (0.77)

1.23 (0.81)

4.24 (2.79)

R120-1.0

47.43 (22.15)

11.65 (5.44)

25.35 (11.84)

1.03 (0.48)

1.72 (0.80)

4.31 (2.01)

R120-1.5

42.99 (13.63)

9.51 (3.01)

34.46 (10.92)

1.06 (0.34)

1.81 (0.57)

3.99 (1.27)

R130-0.5

54.24 (29.02)

13.85 (7.41)

23.72 (12.69)

1.21 (0.65)

1.57 (0.84)

4.64 (2.48)

R140-0.5

46.14 (13.01)

8.6 (2.43)

39.22 (11.06)

1.12 (0.32)

2.6 (0.73)

4.84 (1.36)

R150-0.5

23.62 (6.09)

10.19 (2.63)

46.99 (12.12)

1.03 (0.27)

2.00 (0.52)

4.77 (1.23)

Data refer to the samples, in terms of cellulose, hemicellulose, AIL, ASL, ash, and acetyl contents (w/w, dry weight basis). Data are means of three replicates

aacid insoluble lignin

bacid soluble lignin

crelative content (mass recovery × relative content)

Ionic liquid typically with 1,3-dialkylimidazolium cations can liquefy both lignin and polysaccharides in plant cell wall and then can be reprecipitated from solutions by adding anti-solvents, for examples, water and ethanol [27, 28]. During the selective regeneration, the major cell wall components were partially separated. Table 2 shows that the isothermal [C4mim]Cl-Amberlyst pretreatments contributed to the removal of hemicellulose in A. donax. The hemicellulose percentage decreased with elevated temperature and prolonged time of acid reaction. R140-0.5 sample displayed the lowest hemicellulose content of 8.60 % (2.43 %) after the isothermal IL-Amberlyst pretreatment at 140 °C and acid catalyzed for 0.5 h. This is primarily because both the acid and ionic liquid pretreatment at a high temperature favor the solubilization and chemical degradation of hemicellulose [29]. In an earlier work, the effect of [C4mim]Cl-hydrochloric acid pretreatment on grass samples was investigated (5 % solid loading, at 160 °C for 1.5 h followed by 15 min aicdolysis by 4 M HCl) [17]. They also reported that IL-acid pretreatment had a major effect on hemicellulose and a xylan content of 1.1 % was reported for the solid residue. Moreover, the acetyl contents in the pretreated samples were slightly decreased (Table 2), which may facilitate the enzymatic hydrolysis.

Cellulose was more susceptible to the high pretreatment temperature and long acid reaction time. The isothermal pretreatments resulted in 1.88–38.5 % cellulose removal. Cellulose in the pretreated A. donax samples was gradually decreased with increasing pretreatment temperature and acid reaction time, reaching a minimum of 6.09 % at 150 °C, acid catalyzed for 0.5 h. The noticeable degradation of cellulose may ascribe to severe cellulose depolymerization at high temperature in IL-acid system [25]. Irrespective of mass loss, the relative content of cellulose in samples considering the same acid reaction time (1.0 or 0.5 h), was firstly increased, and then decreased as the temperature increased with peak values of 56.56 % at 110 °C, acid catalyzed for 1.0 h and 54.24 % at 130 °C, acid catalyzed for 0.5 h (Table 2). It is noted that the low relative contents of cellulose are found in R90-1.0, R120-1.0, R120-1.5, R140-0.5, and R150-0.5 samples.

Lignin in biomass was partially removed by IL with evidence of decreased lignin amount in the regenerated residues (11.26–18.49 %, including AIL and ASL fractions). The dissolution of hemicellulose into IL-acid system contributed to a more efficient removal of lignin. A similar tendency of lignin removal to hemicellulose solubilization could be detected as lignin was covalently linked to hemicellulose to some extent. However, the relative content of lignin in pretreated samples was only slightly decreased in R90-1.0 and R100-1.0 samples but obviously increased (23.90–48.02 %) in the others. Relative contents of lignin in R90-1.0 and R100-1.0 samples were similar to those reported previously using a two-steps IL (160 °C)-Amberlyst (90 °C) pretreatment [23]. The highest relative content of lignin was observed in R150-0.5 sample, accompanying the lowest cellulose content. We attribute this high lignin content to the comprehensive functions of cellulose hydrolysis, hemicellulose solubilization, lignin redistribution, and the possible formation of insoluble substrates from carbohydrate conversion during acid pretreatment at high temperature [16, 30, 31]. Further examinations are needed to find out the dominating determinant.

Enzymatic digestibility of pretreated Arundo donax

Figure 1 presents the temporal profiles of cellulose conversion from raw and pretreated A. donax samples under various pretreatment conditions. Since IL in substrate showed toxic or inhibitory effects on microorganisms’ growth, all the samples were washed thoroughly before enzymatic hydrolysis [32]. Enzymatic saccharification assays were conducted under the same conditions to ensure the validity of comparison. As can be seen, A. donax substrates originating from IL-Amberlyst pretreatments were readily degraded by enzymes when compared to raw materials-enzymatic digestibilities were significantly enhanced and high cellulose conversion and high hydrolysis rate were observed.
Fig. 1

Cellulose conversions of raw and pretreated A. donax. by enzymatic saccharification. Cellulose conversions expressed as percentage of the theoretical glucose in pretreated samples. a Effect of solid acid reaction time (0.5, 1.0, and 1.5 h) on enzymatic hydrolysis, b Effect of low pretreatment temperature (90, 100, and 110 °C) on enzymatic hydrolysis, and c effect of high pretreatment temperature (130, 140, and 150 °C) on enzymatic hydrolysis. Error bars indicate standard deviation of triplicate determinations. Sample code with definition is in Table 1

Our results showed evidences that enzymatic saccharification enhancement depends on the Amberlyst reaction time considering the same temperature at 120 °C (Fig. 1a). The digestibilities of samples exposed to water pretreatments of the same temperature profiles were also evaluated as the heat alone might increase the cellulose digestibility. As can be seen from Additional file 1, A. donax subjected to IL-Amberlyst pretreatment displayed an increase of 5.32, 5.58, 6.25 folds in cellulose digestibility compared to the corresponding water pretreated samples after 0.5, 1.0, and 1.5 h of Amberlyst pretreatment, respectively. The highest cellulose conversion was obtained for A. donax pretreated at 120 °C and acid catalyzed for 1.5 h. After 72 h of enzymatic hydrolysis, the glucose yield was reached up to 90.2 % relative to initial level in the corresponding pretreated biomass (Fig. 1b). This was consistent with previous observations employed [C4mim]Cl at a long pretreatment time or dilute acid at high temperature [12, 29]. For example, studies conducted by Trinh and coworkers [12] obtained ~90 % cellulose digestion when the wood materials were pretreated with [C4mim]Cl at 120 °C for 24 h. Nevertheless, Uppugundla and coworkers [29] achieved nearly 100 % glucan conversion for corn stover pretreated with 1-ethyl-3-methylimidazolium acetate ([C2mim][OAc]) for 3 h at 140 °C. As the cost of IL and pretreatment temperature are very important parameters for an economic analysis of IL pretreatment, the comparatively low price of [C4mim]Cl (approximately 1/60th of [C2mim][OAc]) and depressed temperature used in the present study may compensate the glucose release [18, 33].

Samples pretreated at higher temperature with shorter acid reaction time or lower temperature with longer acid reaction time showed similar enhanced cellulose digestibilities [34]. It is interesting to note that the cellulose digestibility increases dramatically with temperature increases from 90 to 110 °C, whereas decreased increments are detected when the temperature increases from 130 to 150 °C (Fig. 1b, c). According to literature, the presence of lignin in biomass hinders the enzymatic hydrolysis by nonproductive binding of cellulase to its surface [35]. High relative content of lignin in R150-0.5 sample (Table 2) could be the major factor that restricted the augment of cellulose conversion.

All of these pretreated A. donax showed a rapid response to enzyme addition, as seen in Fig. 1. As expected, the glucose released during enzymatic hydrolysis rose rapidly within the first 24 h, with a slowly released afterwards. Nevertheless, as can be seen from Table 3 that the initial rates (defined as sugar released within the first 3 h) of glucose released for samples pretreated at lower temperatures were between 60 and 92 g/kg/h compared to 92–226 g/kg/h for samples pretreated at higher temperatures. These initial rates were apparently higher than that of switchgrass subjected to ammonia fibre expansion pretreatment conducted by Bals and coworkers [36]. In addition, a number of detectable xylose was released during the saccharification for these samples (Additional file 2). Aside from the comparatively high yields of glucose and xylose, the high mass recovery at lower pretreatment temperatures resulted in higher monomeric sugars released in pretreated samples (Table 1, Fig. 2). Both R110-1.0 and R120-0.5 samples have significantly increased total sugars recovery (29.5 and 30.9 g total sugar per 100 g starting biomass) in the enzymatic hydrolysates as compared to the 8.3 and 8.4 g total sugars per 100 g starting biomass from the corresponding water pretreated samples (Table 3, Additional file 1), which was higher than those of Arabidopsis pretreated with [C2mim][OAc] at 140 °C for 3 h [37].
Table 3

Enzymatic saccharification and products in pretreatment liquor of raw and pretreated A. donax

Samples

Enzymatic hydrolysis

Pretreatment liquora

Initial enzymatic rate (g/kg/h)b

Reducing sugar (g/100 g)c

Cellulose digestibility (%)d

TRS (%)

ASL (%)

Lactic acid (%)

Acetic acid (%)

Formic acid (%)

HMF (%)

FF (%)

Raw

17

9.7

12.5

R90-1.0

87

24.6

36.7

2.9

0.8

4.98

NDe

ND

ND

ND

R100-1.0

57

25.7

41.9

5.1

1.4

4.90

ND

ND

ND

ND

R110-1.0

92

29.6

66.7

28.8

2.6

4.70

ND

ND

ND

ND

R120-0.5

146

30.9

66.7

18.1

2.4

4.96

ND

ND

ND

ND

R120-1.0

167

21.9

73.2

31.8

3.7

4.96

ND

ND

ND

ND

R120-1.5

226

15.3

90.2

43.0

5.8

5.94

ND

ND

ND

ND

R130-0.5

149

26.4

65.2

23.5

3.3

5.06

ND

ND

ND

ND

R140-0.5

177

11.5

69.6

40.4

5.8

5.72

ND

ND

ND

ND

R150-0.5

92

3.9

41.0

35.2

6.1

5.56

ND

ND

ND

ND

All data are means of three replicates

aData referred to the products in pretreatment liquor are based on dry raw materials

bSugar released within the first 3 h based on dry pretreated sample

cSum of glucose and xylose released in the enzymatic hydrolysates based on dry raw materials

dData are calculated after 72 h of enzymatic hydrolysis at 48 °C

eNo detectable levels (below 0.1 % based on dry raw materials)

Fig. 2

Comparison of total glucose and xylose recovery of raw and pretreated A. donax. after enzymatic saccharification. The sugars were recovered after 72 h of enzymatic hydrolysis at 48 °C and 150 rpm and expressed as percentage of the original biomass. Error bars indicate standard deviation of triplicate determinations. Sample code with definition is in Table 1

Structural analysis in the pretreated Arundo donax

As is well known, the cellulose digestibility is closely connected to the physicochemical characteristics of biomass. Morphological, chemical, and structural changes of biomass were occurred during the pretreatments to facilitate the biomass more susceptible to cellulase. Detailed analysis was conducted to compare the inherent features of the raw and differently pretreated substrates.

Modification of the gross morphology of the A. donax samples was analyzed by scanning electron microscopy (SEM) (Additional file 3). Results show that the raw A. donax had a densified smooth surface and intact fibers arranged in bundles, which prevented the accessibility of cellulase to substrates. The isothermal IL-Amberlyst pretreatment variables resulted in considerable damage in structure, exposing more cellulosic materials and contributed to high cellulose digestibility. The images of samples pretreated at low temperatures showed reversible swelling of cellulose with evidence of the twisting of separated fibres and rough surface with some cracks and fragmentations appearing when the pretreatment temperatures increased to 110 °C (Additional files 3, 4). A possible reason was the incipient disruption of hemicellulose and the onset of the delignification during the pretreatment. Re-deposition of polymers on the surface of fibre was observed in samples pretreated at high temperatures similar to those seen on wheat straw pretreated by thermal autoclaving and alkaline peroxide pretreatments [38]. When prolonging the acid reaction time, rougher and porous surfaces were visualized due to re-deposition of polymers, hemicellulose solubilisation, and lignin delignification. The increasing roughness and porosity improved the accessibility of the enzyme to fibres as reported in the previous literature [35]. Under harsher conditions (150 °C, 0.5 h), the SEM image shows disaggregation of cell bundles and the formation of sheet-like structure with large amount of re-deposited polymers on the surface of fibres (Additional file 3). These polymers were insoluble in acid solution and added to acid insoluble lignin in R150-0.5 sample. The resulted high insoluble polymers in R150-0.5 sample evidently impeded the effective enzymatic hydrolysis (Fig. 1).

Fourier transform infrared spectroscopy (FTIR) was applied to probe the chemical differences among the raw and pretreated A. donax (Additional file 5). When compared with the raw materials, the absorption bands at 1735 and 1240 cm−1 which are assigned to C=O stretching vibration in acetyl groups and C–O stretching of hemicelluloses [39], respectively, were broaden in the isothermal pretreated samples. The decline of the intensities of these two bands indicated the partial removal of hemicellulose. It is clearly discernible that the intensities of bands at 1600, 1510, 1460, and 834 cm−1 that associated with lignin [40] increase especially in samples of R120-1.5, R140-0.5, and R150-0.5 samples, which are consistent with the increased relative contents of lignin (Table 2). Moreover, characteristic assignments of cellulose at 1635, 1424, 1155, 1038, and 896 cm−1 were observed.

The changes in the crystallinity of cellulose in the untreated and pretreated materials could be established by FT-IR analysis [41, 42]. The band at 1424 cm−1 is considered as typical of cellulose I, whereas the absorbance at 896 cm−1 represents cellulose II and the amorphous regions [43]. The absorbance ratio (lateral order index, LOI) of these two bands reflects the cellulose I fraction in cellulose structures. The increased intensity in band at 896 cm−1 in the pretreated samples (except that of R150-0.5 sample) with decreased LOI values ranging from 0.56 to 1.15 (Table 1) indicated that the cellulose I was transformed to cellulose II to some extent. Interestingly, R150-0.5 sample had LOI value as high as 13.78. It suggested that cellulose I structure may be found in cellulose of R150-0.5 sample and the amorphous regions could almost be broken under the given condition.

X-ray diffraction (XRD) analyses were employed to further monitor the cellulose crystalline structural changes upon the pretreatment conditions varied as a whole. The crystallinity index (CrI) values were calculated (Table 1), and their XRD patterns are shown in Fig. 3. As presented, the CrI value of raw A. donax was 36.0 %, containing large proportions of crystalline cellulose. For pretreated samples, the CrI values were decreased to 16.5–31.4 %. After pretreatments at low temperatures, the decreased CrI values with increasing pretreatment temperatures were caused by the progressively increased swelling of cellulose in samples by IL [44]. The CrI values of samples pretreated at 120 °C successively slightly increased with increasing acid reaction time, which could be originated from the progressive degradation of amorphous hemicellulose and hydrolysis of amorphous cellulose. Further increase in the pretreatment temperature to 150 °C, highly amorphous with a minor crystalline component (CrI = 16.5 %) were noted which primary ascribed to further depolymerization of crystalline cellulose. According to Morais and coworkers, a perfect linear relationship between the CrI values and cellulose contents was found for wheat straw pretreated by imidazole [42]. However, no obvious relationship existed between cellulose content and crystallinity (both CrI and LOI values) in the present study, which may owe to the synergistic effects of ionic liquid and solid acid on A. donax.
Fig. 3

X-ray diffractograms of the raw and pretreated A. donax. Sample code with definition is in Table 1

The regeneration processes of IL based pretreatments can change the cellulose crystal structures by disrupting inter- and intra-chain hydrogen bonding of the cellulose fibrils in the native state. The diffraction patterns of the raw biomass exhibited typical diffractions of cellulose Ι and only the decreasing in magnitudes were detected in samples pretreated at 90–100 °C. When the samples pretreated at temperatures higher than 100 °C (excepted that of R150-0.5 sample), the peak at 22.6° shifted to lower angles and the composite peak at around 15.5° became vanishingly small. Moreover, a small shoulder peak at around 12.5° (reflection 1 1 0, cellulose II) was also observed (Fig. 3), indicating cellulose I lattice was severely distorted and partially transferred to cellulose II in these samples [44]. These results supported the observation made by FTIR analysis. It is noteworthy that samples pretreated at 120 °C, 1.5 h and 140 °C, 0.5 h displayed striking diffractions of cellulose II at 12.5°, 20.5°, and 22.1° (Fig. 3). According to Chundawat and coworkers [45] and Wada and coworkers [46], the cellulose crystal structure transformation from cellulose I to cellulose II or IIII increases its enzymatic hydrolysis by decreasing the number of cellulose intra-sheet hydrogen bonds. The conversion of cellulose I to expended cellulose I and II definitely increased the cellulose digestibility (Fig. 1).

Evaluation of total reducing sugars and inhibitors in pretreatment liquor

Total reducing sugars (TRS) released during the pretreatments were determined in the IL liquors and the results are present in Fig. 4. The percentage of TRS in the IL-water phase was found to rely on the pretreatment conditions. At temperatures less than or equal to 100 °C and acid catalyzed for 1 h, only about 5 % of TRS was observed based on the starting A. donax, primary resulting from hemicellulose degradation. Comparatively, approximately 30 % of TRS was obtained when at an elevated temperature (110 °C). It is confirmed that the high temperature shortened the incubation period of solid acid reaction [25]. It is worth noted that there may be a strong positive correlation (R 2 = 0.99) between the acid reaction time and TRS released when the pretreatment temperature is 120 °C (Additional file 6). The highest TRS yield of 43.0 % based on starting materials was found in the IL liquor of acid catalyzed for 1.5 h. This value was comparable to that obtained in the hydrolysate by pretreated the switchgrass with [C4mim]Cl at 160 °C for 1.5 h, followed by acidolysis by 4 M HCl at 105 °C for 2.5 h [17] and pretreated the bermuda grass with dilute acid at 121 °C for 1 h [47]. Despite similar sugars yields could be achieved by other IL based and traditional dilute acid pretreatments, this process provides a convenient, mild, and recyclable alternative method for in situ sugars production. However, a slight decrease of TRS yield in R150-0.5 sample was probably due to the decomposition of TRS to form insoluble substrates at high temperature, such as humins.
Fig. 4

Effect of isothermal pretreatment conditions on TRS and ASL released. TRS in pretreatment liquor was measured by the DNS method. ASL in pretreatment liquor was detected at 320 nm on a UV2300 spectroscopy. The yields expressed as percentage of the original biomass. Error bars indicate standard deviation of triplicate determinations. Sample code with definition is in Table 1

It is known that cellulose dissolved in [C4mim]Cl releases reducing sugars in the presence of solid acid catalysts. Our results corroborate those of other studies, such as Rinaldi and coworkers [16], Zhang and coworkers [48], Yamaguchi and coworkers [49], and Guo and coworkers [50]. They also reported that cellulose can be hydrolysed by solid acid catalysts, such as a carbon material bearing SO3H (100 °C, 3 h), zeolites (100 °C, 6 h) and magnetic solid acid (150 °C, 2 h). A comparatively high TRS released was detected in the IL liquors of R120-1.0, R120-1.5, R140-0.5, and R150-0.5 samples (31.8–43.0 %). Taking into account the low cellulose content (Table 2), it was demonstrated that cellulose depolymerization was the determining factor of TRS released at temperatures higher than 120 °C. It is not surprising that the relative contents of lignin increase in samples pretreated at high temperature due to the cellulose hydrolysis (Table 2). Sun and coworkers [17] have reported that sugars in IL can be extracted by a biphasic system. The recovery of sugars in [C4mim]Cl provides higher combined monomeric sugars released from the starting A. donax (Table 3).

Acid pretreatment is recognized to produce by-products considered inhibitory to microbial fermentation from carbohydrates [51, 52]. However, a quite different by-product distribution was obtained by Brønsted acid pretreatment in the present study. As can be seen from Table 3, no detectable levels (below 0.1 % based on dry raw materials) of routine inhibitors were found in any of the hydrolysates; whereas 4.7–5.94 % of lactic acid was obtained based on the dry raw materials. The lactic acid concentration obtained here was higher than that produced after 3 months of incubation by lactic acid bacteria during the solid state fermentation of forage rice round bales [53]. It was reported that cellulose can be converted to lactic acid in the presence of solid Lewis acids in water or solid Brønsted acid [20, 22]. Despite relatively high amount of lactic acid was produced during the pretreatment; this output had little effect on the further processes [52]. Lignin can also act as an inhibitor for fermentation. In terms of acid soluble lignin (ASL), 0.78–6.10 % of starting material was detected in pretreatment liquors and a similar tendency of lignin solubilizing to TRS released was seen (Table 3; Fig. 4). Regeneration of these soluble lignins from liquors is believed to reduce the inhibitory. The recovery of lactic acid and acid soluble lignin during IL-Amberlyst pretreatment may offset the high cost of IL.

Process mass balance

In this study, the maximum TRS yield and enzymatic saccharification were achieved at 120 °C and acid catalyzed for 1.5 h, whereas the comparatively high total glucose and xylose yields in enzymatic hydrolysates were obtained at 120 °C and acid catalyzed for 0.5 h and 110 °C and acid catalyzed for 1.0 h. Therefore, process mass balances of the isothermal pretreatments were developed for these three conditions (Fig. 5). All data were based on experimental results starting from 100 g of raw A. donax. The pretreatments used 1900 g of IL and 20 g of Amberlyst 35DRY per 100 g of the materials. About 96 % of IL can be recycled by an aqueous biphasic system, following distillation of residual water for further reuse [54], and the solid acid resins were recovered by sieving the solid fractions.
Fig. 5

Mass balance of [C4mim]Cl-Amberlyst 35DRY isothermal pretreatment for the selected conditions. a IL pretreated at 110 °C, following by solid acid Amberlyst 35DRY catalyzed for 1.0 h, b IL pretreated at 120 °C, following by solid acid Amberlyst 35DRY catalyzed for 0.5 h, and c IL pretreated at 120 °C, following by solid acid Amberlyst 35DRY catalyzed for 1.5 h. Mass balanced adjusted to 100 g starting biomass. Values presented ±SD

Taking into account the cellulose conversion and mass recovery, maximum glucose and xylose produced in enzymatic hydrolysates were 24.9 and 6.0 g when biomass pretreated at 120 °C and acid catalyzed for 0.5 h. A similar glucose (24.2 g) and xylose (5.4 g) production was found at 110 °C and acid catalyzed for 1.0 h. As the TRS released increased with increasing acid reaction time, a higher combined sugars yield was obtained for the latter one. In the case of pretreatment at 110 °C and acid catalyzed for 1.0 h, 85.0 % of total reducing glycan (glucan, xylan, arabinan, and galactan) in raw materials was obtained, higher than 76 % of recovery from corn stover subjected to dilute acid pretreatment carried by Uppugundla and coworkers [29]. 4.7 g of lactic acid and 2.6 g of acid soluble lignin were produced during this pretreatment. Despite highest cellulose conversion for R120-1.5 (Fig. 1), only 32 g biomass was recovered, resulting in the low total glucose and xylose yields in enzymatic hydrolysates. However, prolonged acid reaction time enhanced the sugar released during the pretreatment. It was found that 43.0 g of TRS could be obtained in this way. Considering the enzymatic hydrolysis, it was possible to convert 84.9 % of initial total reducing glycan. Reduction of the costly hydrolytic enzymes for sugar released suggests that this process may offer compelling economic advantages. Addition to the sugars recovery, 5.9 g of lactic acid and 5.8 g of soluble lignin byproducts were also obtained which will further reduce the cost of pretreatment. Therefore, this process provides an alternative way to produce fermentable sugars cost-effectively.

Conclusions

In this work, energy favorable facile isothermal [C4mim]Cl-Amberlyst 35DRY pretreatment was proposed to enhance the combined sugars yields in enzymatic hydrolysates and pretreatment liquors. During the pretreatments, it was found that hemicellulose removal, cellulose hydrolysis, crystalline conversion, and polymer re-deposition were dependent on pretreatment conditions since the liberation of H3O+ into IL were temperature- and time-dependent. Under the optimal condition IL pretreated at 110 °C for 3.0 h and subsequent acid reaction for 1.0 h, 24.2 g glucose and 5.4 g xylose in enzymatic hydrolysate and 28.8 g TRS in pretreatment liquor were produced without any notable deleterious effects. This process could potentially recover 85.0 % of the total reducing glycan in the untreated A. donax under a moderate temperature. Moreover, the production of lactic acid and lignin by-products will especially increase the economic prospects. Clearly, the facile isothermal [C4mim]Cl-Amberlyst 35DRY pretreatment provides an emerging strategy for fermentable sugars production and new revenues energy-efficiently which make IL technology a serious candidate for an industrially based biorefinery process.

Methods

Arundo donax preparation

One-year-old A. donax was spring harvested and kindly provided by the Beijing Academy of Agriculture and Forestry Sciences, China. The foliage was removed, and the dried stems were knife-milled and passed through 0.3 mm screen. These lignocellulosic materials were then exhaustively extracted with toluene/ethanol (2:1, v/v) in a Soxhlet apparatus, oven-dried at 40 °C for 16 h, and stored in a sealed bag at room temperature for further use. The dry matter content in biomass was 97 % (w/w).

Ionic liquid-Amberlyst pretreatment

1-butyl-3-methylimidazolium chloride, [C4mim]+Cl with stated purity ≥98.5 %, was purchased from Lanzhou Institute of Chemical Physics of the Chinese Academy of Sciences (Lanzhou, China) and used as the IL for all pretreatments. The water content in IL was 960 ppm as determined by a volumetric Karl-Fischer titration. Solid acid Amberlyst 35DRY was acquired from the Dow Chemical Company (Michigan, America) and sieved to 20 mesh (0.425–0.850 mm). The isothermal pretreatments were performed in a 250 mL dried three-neck flask. Firstly, 5.0 g of A. donax was pretreated with 95.0 g of [C4mim]Cl at 90, 100, 110, 120, 130, 140, and 150 °C with stirring at 100 rpm for 3 h, respectively. Then 1 g of Amberylst catalyst was isothermally added to the corresponding slurry and kept at 90, 100, or 110 °C for 1.0 h, 120 °C for different periods (0.5, 1.0, or 1.5 h), or 130, 140, or 150 °C for 0.5 h with stirring at 100 rpm. After reaction time was completed, 300 mL of deionized water was added whilst stirring vigorously to precipitate the biomass. The mixture of IL, water, biomass, and solid resin was centrifuged to separate the liquid (IL and water) and solid (regenerated biomass and resin) phases. The recovered solids were washed thoroughly with hot water for 4–6 times to remove residual IL and freeze-dried. The pretreated A. donax samples were then gained by passing through a 0.425 mm sieve and used for analysis. Water pretreatments following the same temperature and time profiles were conducted to compare the cellulose digestibility.

Compositional analysis

The chemical composition and acetyl content of raw and pretreated A. donax samples were determined according to analytical procedures established by NREL [55, 56]. More details were described in the literature [26]. All assays were performed in triplicate.

Enzymatic saccharification

The enzymatic saccharification of raw and pretreated A. donax samples was performed in a 0.05 M sodium acetate buffer with a pH of 4.8 at a biomass loading of 2 % (w/v) in an air-shaking incubator at 48 °C and 150 rpm for 72 h. For hydrolysis reaction, 25 mg protein/g substrate of cellulase cocktail (Novozyme) was used to reach an enzyme loading of 20 filter paper units (FPU)/g substrate. To monitor hydrolysis kinetics, 100 μL of hydrolyzed slurry was taken periodically (0, 0.5, 3, 6, 12, 24, 48, and 72 h). The hydrolysis reaction was terminated by boiling the hydrolyzed slurry for 5 min. After cooling, the hydrolyzed slurry was centrifuged at 10,000g for 5 min and then the supernatant was collected and filtered through a 0.45 μm syringe filter for HPAEC analysis. Results are presented as percentage of the corresponding theoretical glucose yield of each sample. All assays were performed in triplicate.

Fourier transform infrared spectroscopy

FTIR spectra of samples were obtained with a Thermo Scientific Nicolet iN 10 FTIR Microscopy (Madison, America) equipped with a liquid nitrogen cooled MCT detector. Spectra were collected from 1800 to 800 cm−1 at room temperature. 32 scans were taken for each sample and the distinguishability was 4 cm−1. The FTIR absorption spectra of raw and pretreated A. donax were baseline correction and normalized to the highest peak [40].

X-ray diffraction

Crystallinity of raw and pretreated A. donax samples was analyzed by powder X-ray diffraction in a D8 Advance instrument (Bruker AXS) employing Ni-filtered Cu Kα radiation (wavelength = 0.154 nm) at 40 kV and 30 mA. Scans were obtained from 5º to 35º 2θ (Bragg angle) at 0.03º per second of scanning rate and at room temperature. Sample was packed into an aluminum sample holder and run as received for data collection. Sample crystallinity, as expressed by crystallinity index (CrI) was measured from the XRD data and calculated with the following formula proposed by Segal et al. [57]:
$${\text{CrI}} = \frac{{I_{ 0 0 2} - I_{\text{am}} }}{{I_{ 0 0 2} }} \times 1 0 0$$
in which I 002 is the scattered intensity of 002 peak (cellulose I) at about 2θ = 22.5°, and I am is the scattered intensity of peak in the amorphous phase at about 2θ = 18.5°.

Scanning electron microscopy

The morphology of raw and pretreated A. donax samples was examined by scanning electron microscopy. The SEM images were recorded with a Hitachi S-3400 N scanning electron microscope operated at 10 kV acceleration voltages. All the samples were spread on a metal-cylinder plate with a carbon tape and coated with gold prior to examination.

Analysis of pretreatment liquors

Total reducing sugars in ionic liquid solution were colorimetrically measured at 540 nm on a UV spectrophotometer using the DNS method [58]. D-glucose was applied as a standard and the concentration of TRS was calculated based on a standard curve obtained with D-glucose (A = 0.1404c−0.0888, R2 = 0.9994). For acid soluble lignin determination, the ionic liquid solution was diluted to bring the absorbance at 320 nm into the range of 0.7–1.0. Inhibitors (lactic acid, acetic acid, HMF, formic acid, and furfural) in ionic liquid solution were analyzed using an Agilent 1200 high performance liquid chromatography (HPLC) instrument equipped with a Bio-Rad HPX-87P ion-exclusion column. Degassed 0.01 N dilute H2SO4 solution was used as the mobile phase with a flow rate of 0.6 ml/min, while the temperature in the column was kept constant at 50 °C. All assays were carried out in triplicate.

Abbreviations

IL: 

ionic liquid

[C4mim]Cl: 

1-n-butyl-3-methylimidazolium chloride

[C2mim][OAc]: 

1-ethyl-3-methylimidazolium acetate

TRS: 

total reducing sugars

AIL: 

acid insoluble lignin

ASL: 

acid soluble lignin

FF: 

furfural

HMF: 

5-hydroxymethyl furfural

SEM: 

scanning electron microscopy

FTIR: 

Fourier transform infrared spectroscopy

XRD: 

X-ray diffraction

CrI: 

crystallinity index

Declarations

Authors’ contributions

TTY participated in the design of the study, carried out the pretreatments, enzymatic hydrolysis, FTIR, XRD, and SEM, analyzed the data and drafted the manuscript. LPS participated in the determination of chemical composition in pretreated samples and helped to interpret the data. RZW participated in the TRS and ASL determination in pretreatment liquor. LMZ participated in the materials preparation. FX conceived of the study, coordinated the overall study, participated in the analysis of the results and their discussion, and revised the manuscript critically before submission. All authors read and approved the final manuscript.

Acknowledgements

The authors thank the Beijing Academy of Agriculture and Forestry Sciences for providing the raw A. donax. They would also like to thank the reviewers for positive criticism to improve the quality of the manuscript.

Competing interests

The authors declare that they have no competing interests.

Availability of supporting data

All data supporting our findings can be found in the Additional files 1, 2, 3, 4, 5, and 6.

Funding

This study was funded by the Fundamental Research Funds for the Central Universities (No. 2015ZCQ-CL-03) and the Chinese Ministry of Education (113014A).

Open AccessThis article is distributed under the terms of the Creative Commons Attribution 4.0 International License (http://creativecommons.org/licenses/by/4.0/), which permits unrestricted use, distribution, and reproduction in any medium, provided you give appropriate credit to the original author(s) and the source, provide a link to the Creative Commons license, and indicate if changes were made. The Creative Commons Public Domain Dedication waiver (http://creativecommons.org/publicdomain/zero/1.0/) applies to the data made available in this article, unless otherwise stated.

Authors’ Affiliations

(1)
Beijing Key Laboratory of Lignocellulosic Chemistry, Beijing Forestry University

References

  1. Claassen P, Van Lier J, Contreras AL, Van Niel E, Sijtsma L, Stams A, et al. Utilisation of biomass for the supply of energy carriers. Appl Microbiol Biotechnol. 1999;52(6):741–55.View ArticleGoogle Scholar
  2. Corno L, Pilu R, Adani F. Arundo donax L.: a non-food crop for bioenergy and bio-compound production. Biotechnol Adv. 2014;32(8):1535–49.View ArticleGoogle Scholar
  3. David K, Ragauskas AJ. Switchgrass as an energy crop for biofuel production: a review of its ligno-cellulosic chemical properties. Energ Environ Sci. 2010;3(9):1182–90.View ArticleGoogle Scholar
  4. Sousa LD, Chundawat SPS, Balan V, Dale BE. ‘Cradle-to-grave’ assessment of existing lignocellulose pretreatment technologies. Curr Opin Biotechnol. 2009;20(3):339–47.View ArticleGoogle Scholar
  5. Mora-Pale M, Meli L, Doherty TV, Linhardt RJ, Dordick JS. Room temperature ionic liquids as emerging solvents for the pretreatment of lignocellulosic biomass. Biotechnol Bioeng. 2011;108(6):1229–45.View ArticleGoogle Scholar
  6. Soudham VP, Raut DG, Anugwom I, Brandberg T, Larsson C, Mikkola JP. Coupled enzymatic hydrolysis and ethanol fermentation: ionic liquid pretreatment for enhanced yields. Biotechnol Biofuels. 2015;8(1):135–47.View ArticleGoogle Scholar
  7. George A, Brandt A, Tran K, Zahari SMS-NS, Klein-Marcuschamer D, Sun N, et al. Design of low-cost ionic liquids for lignocellulosic biomass pretreatment. Green Chem. 2015;17:1728–34.View ArticleGoogle Scholar
  8. da Costa Lopes AM, Bogel-Łukasik R. Acidic ionic liquids as sustainable approach of cellulose and lignocellulosic biomass conversion without additional catalysts. Chem Sus Chem. 2015;8:947–65.View ArticleGoogle Scholar
  9. Achinivu EC, Howard RM, Li G, Gracz H, Henderson WA. Lignin extraction from biomass with protic ionic liquids. Green Chem. 2014;16(3):1114–9.View ArticleGoogle Scholar
  10. Bose S, Armstrong DW, Petrich JW. Enzyme-catalyzed hydrolysis of cellulose in ionic liquids: a green approach toward the production of biofuels. J Phys Chem B. 2010;114(24):8221–7.View ArticleGoogle Scholar
  11. Li CL, Tanjore D, He W, Wong J, Gardner JL, Thompson VS, et al. Scale-up of ionic liquid-based fractionation of single and mixed feedstocks. Bioener Res. 2015;8(3):982–91.View ArticleGoogle Scholar
  12. Trinh LTP, Lee YJ, Lee JW, Lee HJ. Characterization of ionic liquid pretreatment and the bioconversion of pretreated mixed softwood biomass. Biomass Bioenerg. 2015;81:1–8.View ArticleGoogle Scholar
  13. Fu DB, Mazza G. Aqueous ionic liquid pretreatment of straw. Bioresour Technol. 2011;102(13):7008–11.View ArticleGoogle Scholar
  14. Weerachanchai P, Lee JM. Effect of organic solvent in ionic liquid on biomass pretreatment. Acs Sustain Chem Eng. 2013;1(8):894–902.View ArticleGoogle Scholar
  15. Groff D, George A, Sun N, Sathitsuksanoh N, Bokinsky G, Simmons BA, et al. Acid enhanced ionic liquid pretreatment of biomass. Green Chem. 2013;15(5):1264–7.View ArticleGoogle Scholar
  16. Rinaldi R, Palkovits R, Schüth F. Depolymerization of cellulose using solid catalysts in ionic liquids. Angew Chem Int Ed. 2008;47(42):8047–50.View ArticleGoogle Scholar
  17. Sun N, Liu H, Sathitsuksanoh N, Stavila V, Sawant M, Bonito A, et al. Production and extraction of sugars from switchgrass hydrolyzed in ionic liquids. Biotechnol Biofuels. 2013;6(1):39–52.View ArticleGoogle Scholar
  18. Tadesse H, Luque R. Advances on biomass pretreatment using ionic liquids: an overview. Energ Environ Sci. 2011;4(10):3913–29.View ArticleGoogle Scholar
  19. Harmer MA, Sun Q. Solid acid catalysis using ion-exchange resins. Appl Catal Gen. 2001;221(1):45–62.View ArticleGoogle Scholar
  20. Chambon F, Rataboul F, Pinel C, Cabiac A, Guillon E, Essayem N. Cellulose hydrothermal conversion promoted by heterogeneous Brønsted and Lewis acids: remarkable efficiency of solid Lewis acids to produce lactic acid. Appl Catal B-Environ. 2011;105(1–2):171–81.View ArticleGoogle Scholar
  21. da Costa Lopes AM, Brenner M, Falé P, Roseiro LB, Bogel-Łukasik R. Extraction and purification of phenolic compounds from lignocellulosic biomass assisted by ionic liquid, polymeric resins, and supercritical CO2. ACS Sus Chem Eng. 2016. doi:https://doi.org/10.1021/acssuschemeng.5b01600.Google Scholar
  22. Holm MS, Saravanamurugan S, Taarning E. Conversion of sugars to lactic acid derivatives using heterogeneous zeotype catalysts. Science. 2010;328(5978):602–5.View ArticleGoogle Scholar
  23. You T, Zhang L, Zhou S, Xu F. Protic acid resin enhanced 1-butyl-3-methylimidazolium chloride pretreatment of Arundo donax Linn. Bioresour Technol. 2014;167:574–7.View ArticleGoogle Scholar
  24. Meine N, Benedito F, Rinaldi R. Thermal stability of ionic liquids assessed by potentiometric titration. Green Chem. 2010;12(10):1711–4.View ArticleGoogle Scholar
  25. Rinaldi R, Meine N, Stein J, Palkovits R, Schuth F. Which controls the depolymerization of cellulose in ionic liquids: the solid acid catalyst or cellulose. Chemsuschem. 2010;3(2):266–76.View ArticleGoogle Scholar
  26. You T, Mao J, Yuan T, Wen J, Xu F. Structural elucidation of the lignins from stems and foliage of Arundo donax Linn. J Agric Food Chem. 2013;61(22):5361–70.View ArticleGoogle Scholar
  27. da Costa Lopes AM, João KG, Rubik DF, Bogel-Łukasik E, Duarte LC, Andreaus J, et al. Pre-treatment of lignocellulosic biomass using ionic liquids: wheat straw fractionation. Bioresour Technol. 2013;142:198–208.View ArticleGoogle Scholar
  28. Lan W, Liu CF, Sun RC. Fractionation of bagasse into cellulose, hemicelluloses, and lignin with ionic liquid treatment followed by alkaline extraction. J Agric Food Chem. 2011;59(16):8691–701.View ArticleGoogle Scholar
  29. Uppugundla N, Sousa LD, Chundawat SPS, Yu XR, Simmons B, Singh S, et al. A comparative study of ethanol production using dilute acid, ionic liquid and AFEX() pretreated corn stover. Biotechnol Biofuels. 2014;7:72–85.View ArticleGoogle Scholar
  30. Sievers C, Musin I, Marzialetti T, Olarte MBV, Agrawal PK, Jones CW. Acid-catalyzed conversion of sugars and furfurals in an ionic-liquid phase. Chemsuschem. 2009;2(7):665–71.View ArticleGoogle Scholar
  31. Cortez D, Roberto I, Barbosa M, Milagres A. Evaluation of cellulosic and hemicellulosic hydrolysate fermentability from sugarcane bagasse hybrids with different compositions. Biomass Conv Biorefin. 2014;4(4):351–6.View ArticleGoogle Scholar
  32. Turner MB, Spear SK, Huddleston JG, Holbrey JD, Rogers RD. Ionic liquid salt-induced inactivation and unfolding of cellulase from Trichoderma reesei. Green Chem. 2003;5:443–7.View ArticleGoogle Scholar
  33. Klein-Marcuschamer D, Simmons BA, Blanch HW. Techno-economic analysis of a lignocellulosic ethanol biorefinery with ionic liquid pre-treatment. Biofuels Bioprod Biorefin. 2011;5(5):562–9.View ArticleGoogle Scholar
  34. Rajan K, Carrier DJ. Effect of dilute acid pretreatment conditions and washing on the production of inhibitors and on recovery of sugars during wheat straw enzymatic hydrolysis. Biomass Bioenerg. 2014;62:222–7.View ArticleGoogle Scholar
  35. Kumar R, Wyman CE. Access of cellulase to cellulose and lignin for poplar solids produced by leading pretreatment technologies. Biotechnol Progr. 2009;25:807–19.View ArticleGoogle Scholar
  36. Bals B, Rogers C, Jin MJ, Balan V, Dale B. Evaluation of ammonia fibre expansion (AFEX) pretreatment for enzymatic hydrolysis of switchgrass harvested in different seasons and locations. Biotechnol Biofuels. 2010;3:1–11.View ArticleGoogle Scholar
  37. Scullin C, Cruz AG, Chuang YD, Simmons BA, Loque D, Singh S. Restricting lignin and enhancing sugar deposition in secondary cell walls enhances monomeric sugar release after low temperature ionic liquid pretreatment. Biotechnol Biofuels. 2015;8:95–106.View ArticleGoogle Scholar
  38. Toquero C, Bolado S. Effect of four pretreatments on enzymatic hydrolysis and ethanol fermentation of wheat straw. Influence of inhibitors and washing. Bioresour Technol. 2014;157:68–76.View ArticleGoogle Scholar
  39. Labbe N, Rials TG, Kelley SS, Cheng ZM, Kim JY, Li Y. FT-IR imaging and pyrolysis-molecular beam mass spectrometry: new tools to investigate wood tissues. Wood Sci Technol. 2005;39(1):61–76.View ArticleGoogle Scholar
  40. Faix O. Classification of lignins from different botanical origins by FT-IR spectroscopy. Holzforschung. 1991;45(s1):21–8.View ArticleGoogle Scholar
  41. Siroky J, Blackburn RS, Bechtold T, Taylor J, White P. Attenuated total reflectance Fourier-transform infrared spectroscopy analysis of crystallinity changes in lyocell following continuous treatment with sodium hydroxide. Cellulose. 2010;17(1):103–15.View ArticleGoogle Scholar
  42. Morais ARC, Pinto JV, Nunes D, Roseiro LB, Oliveira MC, Fortunato E, et al. Imidazole: prospect solvent for lignocellulosic biomass fractionation and delignification. ACS Sus Chem Eng. 2016;4(3):1643–52.View ArticleGoogle Scholar
  43. Kuo CH, Lee CK. Enhancement of enzymatic saccharification of cellulose by cellulose dissolution pretreatments. Carbohyd Polym. 2009;77(1):41–6.View ArticleGoogle Scholar
  44. Zhang JF, Wang YX, Zhang LY, Zhang RH, Liu GQ, Cheng G. Understanding changes in cellulose crystalline structure of lignocellulosic biomass during ionic liquid pretreatment by XRD. Bioresour Technol. 2014;151:402–5.View ArticleGoogle Scholar
  45. Chundawat SP, Bellesia G, Uppugundla N, da Costa Sousa L, Gao D, Cheh AM, et al. Restructuring the crystalline cellulose hydrogen bond network enhances its depolymerization rate. J Am Chem Soc. 2011;133(29):11163–74.View ArticleGoogle Scholar
  46. Wada M, Ike M, Tokuyasu K. Enzymatic hydrolysis of cellulose I is greatly accelerated via its conversion to the cellulose II hydrate form. Polym Degrad Stab. 2010;95(4):543–8.View ArticleGoogle Scholar
  47. Sun Y, Cheng JJ. Dilute acid pretreatment of rye straw and bermudagrass for ethanol production. Bioresour Technol. 2005;96(14):1599–606.View ArticleGoogle Scholar
  48. Zhang ZH, Zhao ZBK. Solid acid and microwave-assisted hydrolysis of cellulose in ionic liquid. Carbohydr Res. 2009;344(15):2069–72.View ArticleGoogle Scholar
  49. Yamaguchi D, Kitano M, Suganuma S, Nakajima K, Kato H, Hara M. Hydrolysis of cellulose by a solid acid catalyst under optimal reaction conditions. J Phys Chem C. 2009;113(8):3181–8.View ArticleGoogle Scholar
  50. Guo H, Lian Y, Yan L, Qi X, Smith RL. Cellulose-derived superparamagnetic carbonaceous solid acid catalyst for cellulose hydrolysis in an ionic liquid or aqueous reaction system. Green Chem. 2013;15(8):2167–74.View ArticleGoogle Scholar
  51. Larsson S, Palmqvist E, Hahn-Hägerdal B, Tengborg C, Stenberg K, Zacchi G, et al. The generation of fermentation inhibitors during dilute acid hydrolysis of softwood. Enzyme Microb Technol. 1999;24(3):151–9.View ArticleGoogle Scholar
  52. Graves T, Narendranath NV, Dawson K, Power R. Effect of pH and lactic or acetic acid on ethanol productivity by Saccharomyces cerevisiae in corn mash. J Ind Microbiol Biot. 2006;33(6):469–74.View ArticleGoogle Scholar
  53. Horita M, Kitamoto H, Kawaide T, Tachibana Y, Shinozaki Y. On-farm solid state simultaneous saccharification and fermentation of whole crop forage rice in wrapped round bale for ethanol production. Biotechnol Biofuels. 2015;8:9–18.View ArticleGoogle Scholar
  54. Shill K, Padmanabhan S, Xin Q, Prausnitz JM, Clark DS, Blanch HW. Ionic liquid pretreatment of cellulosic biomass: enzymatic hydrolysis and ionic liquid recycle. Biotechnol Bioeng. 2011;108(3):511–20.View ArticleGoogle Scholar
  55. Sluiter A, Hames B, Ruiz R, Scarlata C, Sluiter J, Templeton D et al. Determination of structural carbohydrates and lignin in biomass. National Renewable Energy Laboratory, Golden CO. 2008; Technical Report NREL/TP-510-42618.Google Scholar
  56. Sluiter A, Hames B, Ruiz R, Scarlata C, Sluiter J, Templeton D. Determination of ash in biomass. National Renewable Energy Laboratory, Golden CO. 2008; Technical Report NREL/TP-510-42622.Google Scholar
  57. Segal L, Creely J, Martin A, Conrad C. An empirical method for estimating the degree of crystallinity of native cellulose using the X-ray diffractometer. Text Res J. 1959;29(10):786–94.View ArticleGoogle Scholar
  58. Miller GL. Use of dinitrosalicylic acid reagent for determination of reducing sugar. Anal Chem. 1959;31(3):426–8.View ArticleGoogle Scholar

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