1 Introduction

Black liquor is generated in pulp mills and mainly contains pulping chemicals, lignin, and degraded hemicellulose. It is currently combusted in a recovery boiler to recover the cooking chemicals and produce steam for electricity production and meeting heating needs in the plant. Large quantities of hemicellulose are lost in the cooking process to the black liquor stream (see [1] and references therein), and as the heating value of hemicellulose is not very high, extraction and use of this component as an inexpensive raw material for production of green fuels and chemicals, e.g., by fermentation, is an interesting option that may increase the profitability of the mills [2]. It has been shown that it is possible to separate the lignin and hemicellulose from the black liquor, e.g., by precipitating the lignin and use the hemicellulose for biochemical conversion into biofuels and chemicals [3]. In addition, removing lignin from the black liquor will reduce the thermal load on the recovery boiler, which is often the bottleneck for increased pulp production [4].

Recently, there has been a great interest to produce butanol via ABE fermentation using, e.g., the Clostridium acetobutylicum microorganism [5]. Biobutanol may for instance be used as a green gasoline substitute because of its favorable fuel properties [6, 7]. ABE fermentation yields acetone, butanol, and ethanol in the relative composition of ca. 3:6:1 respectively [8]. In addition to acetone, ethanol, and butanol, other components like butyric acid and acetic acid are also present in the fermentation broth. In ABE fermentation, sugars are first converted to acetic acid and butyric acid accompanied by the decrease in culture pH value in an acidogenic stage. In a second solventogenic phase, sugars and some of the acids are converted to acetone, butanol, and ethanol [9]. Kudahettige-Nilsson et al. showed in a recent study that it is possible to run an ABE fermentation using a hydrolyzate obtained from a black liquor precipitate [10]. Further, Mesfun et al. presented a techno-economic assessment for the production of biofuels from black liquor. They showed that with appropriate ABE (acetone, ethanol, and butanol) fermentation yield, biofuel production from this process could be economically feasible for pulping mills [11]. However, a key challenge for making this process feasible is to develop efficient technologies for recovering butanol from the dilute broth. Butanol is slightly toxic to the microorganisms, and therefore, the maximum concentration of butanol in the broth is limited to only 20 g/L [7, 12]. Furthermore, butanol’s higher boiling point compared to water and the presence of azeotropes sets further limits on suitable recovery options. To be able to commercialize this process, it is imperative to find an efficient downstream recovery method. Adsorption has been identified as an energy-efficient separation technique for the recovery of butanol as compared to pervaporation, distillation, gas-stripping, liquid-liquid extraction, and freeze crystallization [13, 14]. In particular, adsorption on hydrophobic adsorbents has been identified as a promising technique for recovering butanol as shown in several recent investigations using both model solutions and real fermentation broths. Hydrophobic adsorbents like high-silica zeolites (including, e.g., the MFI, FER, CHA, and LTA frameworks), activated carbon, and metal organic frameworks, e.g., ZIF-8, have been evaluated for selective recovery of butanol. These adsorbents in general show good selectivities and capacities [15,16,17,18,19,20,21,22]. For example, Abdehagh et al. recently showed that biobutanol can be recovered using F-400 activated carbon from ABE model solutions [15]. Other groups studied recovery of butanol from model ABE solutions using KA-1 and polymeric resins with good outcome [23, 24]. However, most of these studies focused on recovery of butanol and other valuable compounds like butyric acid, etc. from model solutions and very little attention was given to recovery from real fermentation broths. Most studies have been performed on adsorption from liquid phase; however, recently, it was shown that high silica MFI zeolite showed very high butanol selectivity from vapor phase as reported by our group previously [25, 26]. As zeolite MFI is a stable material and strightforward to synthesize in its hydrophobic (high Si/Al ratio) form at relatively low cost, it is one of the most studied materials for recovering butanol from dilute aqueous solutions. Another key challenge for commercialization of the ABE process is the ability to yield high productivity and selectivity starting from inexpensive raw materials. In this respect, the carbohydrates, mainly in the form of hemicellulose, found in the black liquor constitute such an inexpensive source of substrate for the microorganisms. However, recovering butanol from fermentation broths prepared using the hemicellulose fraction from black liquor is an altogether different challenge. Kudahettige-Nilsson et al. recently demonstrated the possibility of utilizing hemicellulose from black liquor as substrate for ABE fermentation [10]. The hydrolyzate was prepared by using a precipitate of Kraft black liquor from a birch pulping line. Noticeably, the hydrolyzate contained phenols in significant amounts (0.75 g/L). Presence of phenols in the fermentation broth may of course adversely affect the recovery of butanol from the fermentation broth. The composition of black liquor is quite complex, and typically, many different phenolic compounds are present; therefore, only the total phenolic content (TPC) is usually reported [10, 27, 28]. However, in a previous study, Löwendahl et al. showed that some of the phenolic compounds present in degraded lignin hydrolyzate are p-coumaric acid, ferulic acid, and syringic acid [29]. The presence of these compounds could potentially affect the adsorption of butanol and butyric acid in hydrophobic adsorbents. Therefore, it is important to identify suitable adsorbents with negligible effects of the phenols on the recovery of butanol from ABE fermentation broths. Many activated carbons are highly selective towards phenols when present in aqueous solutions; thus, this group of adsorbents would not be the first option [30,31,32]. On the other hand, the well-defined pore size of high-silica MFI zeolite (ca 5.5 Å) may be expected to exclude the typical phenolic compounds found in black liquor by molecular sieving. After adsorption, the products may be recovered from the adsorbent by, e.g., thermal desorption, to recover products and the zeolite can be thereafter be reused [19, 20, 33]. In this work, we therefore for the first time present data on the recovery of butanol and butyric acid from real ABE fermentation broths prepared from a black liquor hydrolyzate using a high-silica MFI zeolite adsorbent.

2 Materials and method

2.1 Materials

Commercial high-silica MFI zeolite powder from AkzoNobel, Sweden, with a SiO2/Al2O3 ratio of 230 was used as adsorbent in this study. In addition, binder-free high-silica MFI zeolite beads (G-360) from ACS materials, USA, with a SiO2/Al2O3 ratio of 360 were also used. Sodium hydroxide (99.9%, Merck chemicals) was used for adjusting the pH of the fermentation broth prior to the adsorption experiments when desired. The fermentation broth was prepared in house with details described elsewhere [10]. In brief, a precipitate of Kraft black liquor from a birch pulping line was supplied as filter cake (50–60% dryness) from the Smurfit Kappa Kraftliner mill, in Piteå, Sweden. The precipitate was obtained by sparging carbon dioxide through the black liquor, thus decreasing the pH from ca 12.1 to 7.8, which in turn promotes precipitation of the lignin. The precipitate contained approximately 15 wt% (dry weight) of xylan; the hemicellulose of interest and other components were mainly acetic acid, phenols (acid soluble lignin), solid lignin, and ash. The filter cake was hydrolyzed by adding 2 M sulfuric acid to reach pH < 1, and kept at 121 °C for 60 min. The xylose content in the hydrolyzate was 20–40 g/L. Batch ABE fermentation of the hydrolyzate using the Clostridium acetobutylicum ATCC 824 strain was conducted at 37 °C in an agitated 1-L bioreactor. The pH was controlled to 5.1 using automatic addition of an aqueous ammonium solution during 10 days of cultivation [10]. In addition, butanol (99%) and ethanol (99%) were purchased from Sigma Chemicals, Sweden. Acetone (99%) was purchased from Merck Chemicals, Sweden.

2.2 Experimental methods

Scanning electron microscopy (SEM) images were recorded on a FEI Magellan 400 field emission instrument without coating the samples. X-ray diffraction (XRD) data were recorded using a Panalytical Empyrean diffractometer run in Bragg-Brentano geometry, whereas nitrogen adsorption-desorption data were recorded at 77 K on an ASAP 2020 instrument from Micromeritics. Prior to measurements, the samples were outgassed at 350 °C under vacuum for 10 h. Before the adsorption experiments, the zeolite was activated by calcination in air at 500 °C for 5 h. In addition to the original black liquor fermentation broth (BLFB), another batch of BLFB was prepared by adding acetone, ethanol, and butanol to the original broth. This was done to arrive at two different concentrations of butanol to gain a better understanding of the competitive adsorption between different species in the fermentation broth. The composition of both broths is presented in Tables 1, 2, 3, and 4. The lower concentration (original broth) may be representative for in situ recovery of butanol from the fermentor while operating, whereas the broth with a higher concentration (modified broth) may be representative of a completed fermentation. Batch adsorption experiments with the original fermentation broth were performed three times to gain information on the repeatability of the method. However, due to the limited availability of fermentation broth, only one batch experiment was carried out on the modified broth. Liquid-phase batch adsorption experiments were performed in 50-mL Erlenmeyer flasks at pH 5.2 (original pH of broth) or pH 8. Approximately 40 mL fermentation broth and 1 g zeolite adsorbent were added to the flasks and the mixtures were allowed to equilibrate for 48 h at 25 °C on a shaking table. For the experiments carried out at pH 8, the pH was adjusted by addition of 1 M sodium hydroxide solution prior to equilibration. After equilibration for 48 h, the zeolite was separated from the solution by centrifugation. The supernatant was then filtered using a 0.2-μm PTFE filter and the concentrations of adsorbates in the broth before and after equilibrium with the zeolite were determined by high-pressure liquid chromatography (HPLC, Perkin-Elmer series 200 instrument) equipped with a refractive index detector. The instrument was equipped with a 125–0115 (BioRad) column in hydrogen form and a 0.005 M H2SO4 aqueous solution in water was used as mobile phase at a flow rate of 0.6 mL/min. Additional experiments were conducted to ascertain that the filtration did not affect the composition of the supernatant.

Table 1 Initial concentrations in the original black liquor fermentation broth and amount adsorbed in MFI zeolite at pH 5.2 at 25 °C; values are the average from three experiments with standard deviation indicated
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Table 2 Initial concentrations in the original black liquor fermentation broth and amount adsorbed in MFI zeolite at pH 8.0 at 25 °C; values are the average from three experiments with standard deviation indicated
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Table 3 Initial concentration in the modified black liquor fermentation broth and amount adsorbed in MFI zeolite at pH 5.2 at 25 °C
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Table 4 Initial concentration in the modified black liquor fermentation broth and amount adsorbed in MFI zeolite at pH 8.0 at 25 °C
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A mass balance was used to determine the loading of the adsorbate in the zeolite:

$$ {q}_i=\frac{\left({C}_{i,0}-{C}_i\right).{V}_o\ }{m_{z,0}} $$
(1)

where qi is the mass of adsorbate per unit mass of adsorbent, Ci,0 is the initial concentration of adsorbate in the solution, Ci is the concentration of the adsorbate in the solution at equilibrium, V0 is the volume of solution brought in contact with adsorbent, and mz,0 is the mass of the adsorbent.

The adsorption selectivity was calculated as follows:

$$ {S}_{\frac{i}{j}}=\frac{\raisebox{1ex}{${x}_i$}\!\left/ \!\raisebox{-1ex}{${x}_j$}\right.}{\raisebox{1ex}{${y}_i$}\!\left/ \!\raisebox{-1ex}{${y}_j$}\right.} $$
(2)

where x is the mole fraction in the adsorbed phase and y is the mole fraction in the liquid phase at equilibrium.

3 Results and discussion

The XRD data, shown in Fig. 1, confirmed that both samples consisted of highly crystalline MFI phase. Only reflections originating from the MFI phase were observed in the diffractograms.

Fig. 1
figure 1

X-ray diffractograms of both MFI powder and bead samples as well as a reference pattern for comparison (database reference code: 00-042-0024)

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SEM images of the zeolite MFI powder and binderless beads are shown in Fig. 2 a, b, respectively.

Fig. 2
figure 2

SEM images of the crystals in the powder (a) and in the beads (b)

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For both samples, the crystal sizes vary considerably but are of roughly similar size on the order of 1 μm. The crystal morphologies are slightly different where the crystals making up the beads show a block-like character, whereas the crystals in the powder sample show a spherical or ellipsoidal habit. The crystals in the beads appear quite well packed with relatively small voids between the crystals. However, any difference in crystal size or morphology between the two samples should not have a significant effect on the equilibrium measurements reported in this work. Figure 3 shows the nitrogen adsorption isotherms for both samples. The isotherms are quite similar, especially at lower relative pressures, and typical for microporous material with a rapid increase in the amount adsorbed at low relative pressures. At higher relative pressures, the adsorbed amounts are higher in the powder than in the beads. A hysteresis loop was observed at higher relative pressures in the isotherms of the powder sample, associated to capillary condensation in mesopores between the crystals in the powder.

Fig. 3
figure 3

Nitrogen adsorption/desorption isotherms for both samples determined at 77 K

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The BET-specific surface areas were similar for both samples, i.e., 421 and 407 m2/g for the powder and beads, respectively. On the other hand, the mesopore volume was larger for the powder sample than for the beads as determined by the BJH method using the desorption branch, viz. 0.058 and 0.032 cm3/g, respectively. In our previous work, we reported breakthrough curves for model butanol/water and butanol/ethanol/acetone aqueous solutions using the same beads as in this work (particle size ca 1 μm) and compared those results with that of a structured adsorbent in the form of a ca. 9-μm-thick zeolite MFI films coated on a metal monolith. For both samples, the breakthrough front was quite sharp indicating that intra-crystalline diffusion was not severely limiting the performance of the adsorbents at the conditions studied. However, the breakthrough front from the structured adsorbent was somewhat less sharp, indicating that the resistance to mass transfer was somewhat larger for this sample, as expected [34].

Table 1 shows the concentration of the main products in the ABE fermentation broth. The concentrations of acetone, butanol, and ethanol were 0.39, 2.30, and 0.36 g/L, respectively, in the original fermentation broth.

These concentrations are lower than can be expected in a complete fermentation broth where the concentrations of acetone, butanol, and ethanol are 10, 20, and 5 g/L, respectively. However, these lower concentrations may be typical for the case where it is desirable to remove butanol from the fermentor during the fermentation to prevent the inhibition of production by high concentration of butanol in the fermentor. In a previous study, we showed that even at a butanol concentration of 2 g/L, saturation loading was reached in high-silica MFI zeolite [20]. Consequently, the selectivity towards butanol in the present work should still be high. In addition, to evaluate the performance of the adsorbents also at the concentrations close to those present in an ABE broth run to completion, the original broth was spiked with additional acetone, butanol, and ethanol to arrive at the concentrations of 11.8, 4.7, and 19.9 g/L respectively. The total concentration of phenolic compounds in the fermentation broth was previously determined to 0.75 g/L [10].

Table 1 shows the batch adsorption results for both zeolite powder and for the beads from the original fermentation broth at pH 5.2. The results are quite similar for both the powder and beads. At this pH, the adsorbed loading of butanol and butyric acid in the zeolite was 0.06 and 0.07 g/g zeolite respectively. It should here be pointed out that the saturation loading of butanol or butyric acid in high-silica MFI zeolite is ca 0.12 g/g zeolite [16, 20]. Summing up the adsorbed amounts of butanol and butyric acid yields 0.13 g/g zeolite, i.e., almost the same as the single component saturation capacity for these two compounds. This shows that the zeolite becomes saturated with butanol and butyric acid in this system and that the selectivity towards the C4 compounds is not affected by the presence of phenolic compounds in the broth. According to Kudahettige-Nilsson et al., 95% of the substrate (in this case xylose) was utilized during the fermentation process [10]. Thus, the remaining concentration of xylose was ca. 1.4 g/L. The results obtained however shows that the unreacted substrate present in the broth seemingly did not affect the adsorption of C4 compounds. This is in accordance with previous reports by Ranjan et al. showing that glucose has a very low affinity for high-silica MFI [35]. Furthermore, the amount adsorbed of other components (acetic acid, acetone, and ethanol) is very low. This shows that the only component in this system, which seriously competes with butanol adsorption on high-silica MFI zeolite, is butyric acid. This may not necessarily be a problem as butyric acid has a value of its own and may also be converted into butanol, e.g., by aqueous phase hydrodeoxygenation using a heterogeneous catalyst [36, 37]. As mentioned earlier, Löwendahl et al. showed that some of the cyclic compounds present in a lignin hydrolyzate are p-coumaric acid, ferulic acid, and syringic acid [30]. These structures may be compared to the structure of vanillin and p-xylene [38] (see supplementary material for structures). Vanillin does not adsorb in the MFI framework even at liquid concentrations of 20 g/L, i.e., at concentrations 27 times higher than the total phenolic concentration in this work as demonstrated by Ranjan et al. [35]. The reason most likely being that the vanillin molecule is too large to enter the pores of MFI. p-Xylene has a kinetic diameter of ca. 0.58 nm and may enter the pore system of the MFI zeolite. Thus, p-coumaric acid, which resembles p-xylene, seems small enough to enter the pores. However, ferulic and syringic acids resemble vanillin and should not be able to enter the pores. In any case, these components do not seem to interfere with the adsorption of the C4 compounds; however, the reason is not clear. Perhaps, the concentration of p-coumaric acid is low enough not to interfere with adsorption of the C4 compounds. Further studies would be necessary to unravel this phenomenon. However, other hydrophobic adsorbents proposed for recovery of butanol from ABE broths but with larger effective pore diameters as compared to zeolite MFI, e.g., large pore zeolites, some metal organic frameworks and activated carbon are likely to be more affected by presence of these phenolic compounds in the broth.

We previously showed that the adsorption of butyric acid in high-silica MFI zeolite can be controlled by adjusting the pH of the solutions. Butyric acid is more hydrophobic than the deprotonated butyrate ion and thus shows higher affinity towards hydrophobic high-silica MFI zeolite [20]. By increasing the pH of the fermentation broth well above the pKa value of butyric acid (i.e., 4.82), the adsorption of butyric acid can be reduced, thus increasing the selectivity towards butanol. Table 2 shows the amount adsorbed in zeolite powder and beads from the original fermentation broth at pH 8.0. As expected, at this higher pH, adsorption of butyric acid is considerably lower than that of butanol. At pH 5.2, the original pH of the fermentation broth, the loading of both butanol and butyric acid was approximately 0.06 g/g zeolite, whereas at pH 8, the loading of butanol was four times higher than that of butyric acid. This shows that the adsorption of butyric acid may be suppressed to increase butanol recovery and purity. The total adsorbed amount of C2 and C4 compounds is 0.11 g/g zeolite, which indicates that the zeolite is saturated with these components and that the phenolic compounds present in the fermentation broth are not affecting the adsorption significantly.

Figure 4 shows the butanol selectivity over the other components present in the original fermentation broth at pH 5.2 and 8.0. At pH 5.2, the butanol over butyric and acetic acid selectivities was 3 and 36, respectively. However, at pH 8.0, the butanol selectivity increases significantly as the high-silica MFI zeolite shows less affinity towards the deprotonated carboxylic acids; consequently, the butanol selectivities increased to 190 and 678, over butyric and acetic acid, respectively. However, as the adsorption of the acids is decreased at high pH, the adsorption of acetone increases, whereas adsorption of ethanol decreases. This is expected as acetone shows higher affinity towards high-silica MFI than ethanol [16, 18, 20].

Fig. 4
figure 4

Butanol selectivity over other components present in original black liquor fermentation broth at pH 5.2 (empty bars) and pH 8.0 (filled bars) at 25 °C

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Tables 3 and 4 show the batch adsorption experiment results from modified black liquor fermentation broth at pH 5.2 and 8, respectively. The results are in general very similar to those obtained for the original fermentation broth. At pH 5.2, primarily a mixture of butanol and butyric acid is adsorbed, whereas at pH 8, adsorption of butyric acid is reduced and the adsorbed phase mostly consists of butanol. At both pH values, the sum of the amount adsorbed of butanol and butyric acid is very close to the saturation loading of high-silica MFI zeolite, hence showing again that phenolic compounds are not affecting the adsorption of C4 compounds.

Figure 5 shows the same trend as in Fig. 4; at low pH, the butanol selectivities over acetic and butyric acid were determined to 36 and 0.2, respectively. The low selectivity over butyric acid in this case is due to the fact that even though the concentration of butanol was quite high as compared to butyric acid in the modified fermentation broth, still, butyric acid competes with the butanol for adsorption sites (see Table 3). However, at pH 8.0, butanol selectivity over butyric acid increases slightly, as expected.

Fig. 5
figure 5

Butanol selectivity over other components present in modified black liquor fermentation broth at pH 5.2 (empty bars) and pH 8.0 (filled bars) at 25 °C

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The lower selectivity values observed for the modified broth at pH 8 compared to the corresponding values for the original broth may be explained with that the adsorption of butanol is close to saturation (ca 0.11 g/g) already at the low concentrations found in the original broth. Thus, for the modified solution with higher concentration of butanol in solution, the adsorbed amount will not change to any great extent compared to adsorption from the original broth as the adsorbent is already close to saturation. Instead, the determined selectivity will be reduced as the denominator in Eq. 2 now takes a greater value which results in lower observed selectivities. Several groups have previously reported butanol loading in adsorbents from model solutions and real fermentation broth [6, 15, 16, 19], but to the best of our knowledge, none of these studies reported any selectivity data. However, Cousin Saint Remi et al. reported butanol over ethanol and acetone selectivities of 10.2 and 2.6, respectively, for a ZIF-8 metal organic framework using a model fermentation broth and data from breakthrough [17]. In our previous study, we reported butanol over ethanol and butanol over acetone selectivities of 7.3 and 4.4, respectively, for silicalite-1 beads and breakthrough experiments using model fermentation broths [20]. The differences compared to the results obtained in this work can be ascribed to the different composition of the broth used, mode of measurement, i.e., batch vs breakthrough experiments, and of course the different material used when it comes to comparing with the ZIF-8 material. As pointed out above, this is the first study in which black liquor-derived fermentation broth was used; hence, no data is available in the literature to compare these selectivity values for this particular broth containing relatively high concentrations of phenolic compounds. In addition, to the best of our knowledge, this is the first report presenting results on butanol selectivities over butyric and acetic acid for an ABE fermentation broth.

In this work, we chose to keep the temperature constant but changing the temperature would affect both the adsorption selectivities and the uptake rate. The uptake rate is increasing with increasing temperature, whereas the adsorption selectivity will decrease if the temperature is raised sufficiently, so there is an optimum temperature where the mass transfer is as high as possible while still maintaining a high butanol selectivity. To assure a high butanol concentration in the adsorbent, and thereby in the final product, it is imperative that the concentration of butanol in the adsorbent is close to the saturation concentration; if the temperature is increased too much, this would not be the case. Consequently, to ascertain a high concentration of butanol in the product, there is a maximum temperature above which the butanol selectivity will decrease rapidly; this temperature is of course dependent on the composition of the broth. For example, at the butanol concentrations found in the original broth, increasing the temperature may not be a feasible option, as it would likely compromise the adsorption selectivity as the adsorbed concentration of butanol is close to the concentration in solution where saturation loading is achieved [20]. However, for the composition used in the modified broth with a butanol concentration that is ca. 9 times higher (i.e., ca. 20 g/L), it would likely be possible to increase the temperature somewhat without compromising the adsorption selectivity as at this high concentration of butanol in solution, the adsorbed loadings are far from the point where the adsorbed loadings start decreasing (high up in the flat part of the isotherm). Therefore, when optimizing the temperature, both the effect on the adsorption selectivity and on the uptake rate should be taken into account, e.g., by performing breakthrough experiments at different temperatures, such an optimization is however beyond the scope of the present work.

Recent research shows that the butanol/water adsorption selectivity of a MFI adsorbent may be further increased by decreasing the density of structural defects, in the form of silanol groups, present in the framework [25, 26]. These defects are formed during conventional zeolite synthesis at high pH. The density of structural defects was decreased by synthesizing the zeolite at neutral pH using fluoride ions as mineralizing agent. With a reduced concentration of structural defects, much less water adsorbs in the zeolite which results in an increase in the adsorption selectivity [26, 39, 40]. In future work, it would be interesting to evaluate also these materials as adsorbents in real fermentation broths. Nevertheless, in the present work, we demonstrate that high-silica MFI zeolite shows high adsorption selectivity for butanol against the other main compounds present in real fermentation broths and that the adsorbent is seemingly insensitive to the presence of phenolic compounds in the fermentation broth. However, more studies are needed to confirm or reject any minor adsorption of phenolic acids on high silica MFI zeolite. In addition, future studies should focus on measuring dynamic parameters like uptake rate, flow rate, etc. using breakthrough experiments to further assess the feasibility of implementing this process in biorefineries.

4 Conclusions

In this study, high-silica MFI zeolite was used as adsorbent to recover butanol from ABE fermentation broths derived from a black liquor hydrolyzate, a potential source for inexpensive substrate. The hydrolyzate contained significant amounts of phenolic compounds that potentially could affect the adsorption of the desired C4 products. It was shown that despite the presence of the phenolic compounds in the fermentation broths, the high-silica MFI zeolite adsorbent was very selective towards the C4 products viz. butanol and butyric acid. In addition, by increasing the pH of the fermentation broth, co-adsorption of butyric acid could be suppressed, further increasing butanol selectivity. The selectivity of butanol over acetic acid, butyric acid, acetone, and ethanol was reported at pH 5.2 and pH 8.0 for two broths with different compositions. High-silica MFI zeolite showed higher affinity towards butanol than any other compound present in the fermentation broth. The results presented herein are promising for better utilization of the black liquor stream. However, further studies on the performance under dynamic conditions with, e.g., breakthrough experiments, should be conducted.