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# A kinetic model for quantitative evaluation of the effect of hydrogen and osmolarity on hydrogen production by *Caldicellulosiruptor saccharolyticus*

*Biotechnology for Biofuels*
**volume 4**, Article number: 31 (2011)

## Abstract

### Background

*Caldicellulosiruptor saccharolyticus* has attracted increased interest as an industrial hydrogen (H_{2}) producer. The aim of the present study was to develop a kinetic growth model for this extreme thermophile. The model is based on Monod kinetics supplemented with the inhibitory effects of H_{2} and osmotic pressure, as well as the liquid-to-gas mass transfer of H_{2}.

### Results

Mathematical expressions were developed to enable the simulation of microbial growth, substrate consumption and product formation. The model parameters were determined by fitting them to experimental data. The derived model corresponded well with experimental data from batch fermentations in which the stripping rates and substrate concentrations were varied. The model was used to simulate the inhibition of growth by H_{2} and solute concentrations, giving a critical dissolved H_{2} concentration of 2.2 mmol/L and an osmolarity of 0.27 to 29 mol/L. The inhibition by H_{2}, being a function of the dissolved H_{2} concentration, was demonstrated to be mainly dependent on H_{2} productivity and mass transfer rate. The latter can be improved by increasing the stripping rate, thereby allowing higher H_{2} productivity. The experimentally determined degree of oversaturation of dissolved H_{2} was 12 to 34 times the equilibrium concentration and was comparable to the values given by the model.

### Conclusions

The derived model is the first mechanistically based model for fermentative H_{2} production and provides useful information to improve the understanding of the growth behavior of *C. saccharolyticus*. The model can be used to determine optimal operating conditions for H_{2} production regarding the substrate concentration and the stripping rate.

## Background

The question of climate change, together with the increasing scarcity and cost of fossil fuels, has triggered research on the sustainable production of energy carriers, such as biofuels. Although a wide spectrum of alternative fuels and processes are available, it is still not known which of them will succeed in replacing fossil fuels in the long term. Processes for producing some biofuels, such as ethanol and methane, are already highly developed for commercial use, while others, including biohydrogen, require more basic research before they can be produced in an economically feasible way [1].

The current major drawbacks of fermentative hydrogen (H_{2}) production are its low yield [2] and the requirement of gas stripping to remove H_{2} from the liquid [3]. Dark fermentation can be performed at either moderate or elevated temperatures: the productivity is generally higher in the former case [4], whereas the latter provides higher yields [5]. However, for an economically sustainable biohydrogen process, high productivity should be accompanied by high yields [2]. One solution is to focus on the process design, such as the optimization of H_{2} removal and substrate concentration [6]. A higher substrate concentration is required to avoid excess amounts of water, since a surplus of process water has a negative effect on both the environmental and economic aspects of the process [7]. It is important to find alternatives to nitrogen (N_{2}) sparging, as this dilutes the H_{2}, leading to a lower-grade product or the need for expensive gas upgrading to remove the N_{2}.

The extreme thermophile *Caldicellulosiruptor saccharolyticus* may be of industrial interest because of its ability to produce high yields of H_{2} from a wide variety of sugars [8, 9], ranging from pentose and hexose monomers [10] to complex (hemi)cellulosic materials [8, 11, 12]. However, the growth of this microorganism, as well as the production of H_{2} and acetic acid, is subject to substrate and product inhibition [13]. In addition, it is sensitive to increased osmotic pressure [14], making it necessary to dilute the substrate. Moreover, *C. saccharolyticus* is inhibited by H_{2} [13], which is a general trait of H_{2}-producing organisms. A high dissolved H_{2} concentration (H_{2aq}) inhibits H_{2}-generating hydrogenases [1, 2], leading to increased nicotinamide adenine dinucleotide, reduced/nicotinamide adenine dinucleotide (NADH/NAD) ratios, resulting in a metabolic shift toward reduced products such as lactate and ethanol [1, 3, 4] and thus decreased H_{2} productivity.

The critical partial H_{2} pressure (${P}_{{H}_{2}}$) is usually the parameter coupled to growth inhibition and lactate formation [5, 13, 15–17], although it has been shown that there are mass transfer limitations that cause the fermentation medium to be supersaturated with H_{2} [18, 19]. Therefore, H_{2aq} should be considered rather than ${P}_{{H}_{2}}$ when discussing inhibition by H_{2}. Stripping with N_{2}, which decreases H_{2aq} [19], can significantly improve the H_{2} yield [3]. Indeed, optimizing the process should consist of a compromise between minimizing the stripping gas flow rate, henceforth called the "stripping rate," and maintaining a suitable H_{2} yield and productivity [20]. However, optimization must take H_{2} productivity into account, since it influences H_{2aq} greatly; otherwise, the optimization will be relevant only to the specific system studied and cannot be applied to other biohydrogen systems. Furthermore, better insight into H_{2} productivity and liquid-to-gas mass transfer will help considerably in finding technical solutions allowing an economical and feasible fermentation process to be designed.

This paper describes the development of a kinetic Monod-based model for cell growth and product formation by *C. saccharolyticus*, which takes the liquid-to-gas mass transfer into consideration. The derived model successfully simulates batch fermentations of *C. saccharolyticus* and predicts the influence of H_{2aq} and osmotic pressure on growth as well as the metabolic shift to lactate production. To the best of our knowledge, this is the first time the inhibitory effects and liquid-to-gas mass transfer of H_{2} and carbon dioxide (CO_{2}) have been included in a model for fermentative H_{2} production. The results obtained with the model are relevant for biohydrogen systems other than that described herein using *C. saccharolyticus*.

## Methods

### Cultivation and fermentation

*C. saccharolyticus* was cultivated in a N_{2} atmosphere in modified DSM640 medium as described previously [9]. Cultures for inocula were grown overnight in 250-mL serum flasks containing 50 mL of modified DSM640 medium, together with a 0.4% carbon source and 0.02% cysteine.

Fermentations were performed in a jacketed 3-L reactor (Applikon, Schiedam, the Netherlands) at a working volume of 1 L. The pH was monitored using an ADI 1025 Bio Console Bio Controller (Applikon) and maintained at pH 6.6 (corresponding to neutral pH at 70°C) by the addition of sodium hydroxide (NaOH). The temperature was thermostatically maintained at 70°C ± 1°C, and the stirring rate was set to 350 rpm. Prior to inoculation, the medium was reduced by the addition of 0.1% cysteine. The fermentor was continuously stripped with N_{2}.

A total of eight experiments were performed, with glucose concentrations of 5 or 10 g/L and stripping rates from 0.78 to 6 L of N_{2}/hour, to estimate the parameters of the kinetic model. The experiments were performed on four different occasions. An overview of the experiments is given in Table 1. The H_{2} productivity and the cumulative H_{2} production were determined as described previously [21].

### Measurement of dissolved hydrogen concentration

The dissolved H_{2} concentration, H_{2aq}, was determined in samples of cell suspensions from the bioreactor in serum flasks. The pressure in the flasks was reduced using a vacuum pump to withdraw the fermentation medium (30 to 40 mL) from the fermentor. The sealed flasks were placed in a water bath (20°C) with magnetic stirring to ensure good mixing. After one hour in the water bath, the pressure in the flasks was rapidly raised to atmospheric pressure by inserting a small needle through the cap, allowing air to enter the flasks. After 12 hours, the H_{2} concentration in the headspace of the serum flasks was measured as described below (Analytical methods). The volume of the collected liquid and the total volume of the individual serum flasks were measured to estimate the original H_{2aq} in the sample.

### Analytical methods

Headspace samples were analyzed for CO_{2} and H_{2} using a Varian CP-4900 Micro GC gas chromatograph (Varian, Inc., Middelburg, the Netherlands) equipped with a thermal conductivity detector (100 mA). The results were analyzed using Galaxie Chromatography Workstation version 1.9.3.2 software (Varian, Inc.). The optical density of aerobic samples was measured at 620 nm using a spectrophotometer (Hitachi U-1100; Hitachi High-Technologies Corp., Tokyo, Japan). Concentrations of acetic acid, lactic acid and ethanol were analyzed using high-pressure liquid chromatography (Waters Corp., Milford, MA, USA). An Aminex HPX-87H ion exchange column (Bio-Rad Laboratories, Hercules, CA, USA) was used at 45°C with a mobile phase of 5 mM H_{2}SO_{4} at a flow rate of 0.6 mL/minute. The chromatograph was equipped with a refractive index detector (RID-6A; Shimadzu, Kyoto, Japan).

### Modeling

The model employed in this study considers the kinetics of growth and product formation, including inhibition, liquid-to-gas mass transfer and the chemical equilibrium of CO_{2} and carbonates. The constants used in the model are listed in Table 2.

#### Growth and product kinetics in C. saccharolyticus

The kinetic model for *C. saccharolyticus* is based on simultaneous solution of the mass balance equations. The following reactions occurring in *C. saccharolyticus* were taken into consideration in the model:

The elemental composition of *C. saccharolyticus* was previously determined by de Vrije *et al*. [21]. The value of the stoichiometric parameter *k* in equation 3 is not known and was therefore estimated (described in detail below, Experimental design and estimation of kinetic parameters). Furthermore, reaction 3 is not balanced, since elements are available in the fermentation medium which were not considered in the model (for example, yeast extract). *C. saccharolyticus* is subject to several inhibiting agents affecting cell growth as well as the production of acetic acid and H_{2}. These include (1) elevated concentrations of dissolved H_{2} and H_{2aq}, and (2) high osmolarity. Osmolarity (named "OSM" in the model) is calculated by summing the molar can be described by the following expression:

where *G*, *Ac* and *Lac* are the concentrations of glucose, acetic acid and lactic acid, respectively, and CO_{2sol} is the concentration of bicarbonate and carbonate, resulting from the CO_{2} produced by the bacterium. The stoichiometric factor 2 arises from the assumption that for each mole of acid produced, one mole of NaOH is added to maintain the pH. The background osmolarity, 0.10 mol/L, resulting from yeast extract and other nutrients was calculated based on osmolarity measurements presented previously [14].

The mass balance for the growth of the cells (in batch fermentation) can be described by the following expression:

where μ, *X* and *r*_{cd} are the specific growth rate, the cell mass concentration and the cell death rate, respectively.

The specific growth rate, μ, is given by Monod kinetics:

Here μ_{max} is the maximum specific growth rate, *G* is the glucose concentration and *K*_{G} is the glucose affinity parameter. *OSM*_{crit}, H_{2aqcrit},${n}_{{H}_{2}}$ and *n*_{μ} are the critical osmolarity, critical dissolved H_{2} concentration and the exponential parameters describing the level of inhibition, respectively. The critical parameters represent the values at which inhibition is 100%. The kinetic inhibition expressions, as presented by Han and Levenspiel [22], are valid only for concentrations of the inhibiting agents (OSM or H_{2aq}) lower than the respective critical concentrations. Elevated osmolarity inhibits the growth of *C. saccharolyticus* [14], which may lead to a metabolic shift toward the production of lactic acid [23].

#### Product formation

The product formation rates were expressed using an adapted form of the Luedeking-Piret equation [24]:

Here, α is a growth-associated constant, and β is a non-growth-associated constant. All products were assumed to be only growth-associated, hence β is zero. This simplification is based on the assumption that other nutrients are in excess. It is further assumed that H_{2} inhibits its own production and thus also that of acetate in both a direct and an indirect way: indirectly through the inhibition of growth, and directly through specifically inhibiting the hydrogenases, which results in an increase in the NADH/NAD ratio in the cell [25]. This in turn induces the activity of the enzyme lactate dehydrogenase, initiating a metabolic shift toward lactate [23]. Besides being activated through H_{2}, lactic acid production is also activated via osmolarity, which at high concentrations inhibits growth [23]. The growth-associated constants (equation 7) for the metabolic products are as follows:

Here *R*_{AcF}, ${{R}_{Lac}}_{F{H}_{2}}$ and R_{LacFOSM} are the factors relating the production rates of acetic acid and lactic acid to the growth rate; INHIB and ACT are the inhibition and activation factors, respectively (see below, Product formation) Y_{GAc} and ${Y}_{GC{O}_{2}}$ are the stoichiometric yield coefficients of the reactions described above (equation 1); and ${Y}_{G{H}_{2}}$ is the estimated H_{2} yield coefficient (mol H_{2}/mol glucose). The following inhibition mechanisms were studied.

Inhibition and activation by dissolved H_{2}:

Activation of lactic acid production by osmolarity:

The mass balances of the products in the liquid phase consist of an accumulation, time-dependent, and a product formation rate, concentration-dependent, term, and, when applicable, a liquid-to-gas mass transfer term.

Here ${K}_{l}{a}_{{H}_{2}}$ is the overall volumetric mass transfer coefficient for H_{2} and ${H}_{2aq}^{*}$ is the H_{2} saturation concentration.

CO_{2}:

where ${K}_{l}{a}_{C{O}_{2}}$ is the overall volumetric mass transfer coefficient for CO_{2}; CO_{2aq} and $C{O}_{2aq}^{*}$ are the concentration of dissolved CO_{2} and the saturation concentration of CO_{2}, respectively; *K*_{1} and *K*_{2} are the dissociation constants; and CO_{2sol} is the total concentration of carbonates. The last two expressions in the CO_{2} mass balance (equation 18) are related to the reaction of CO_{2} with water to form carbonates (see Additional file: Liquid-to-gas mass transfer and chemistry of CO2__Theory_experiments_and_results). The expressions ${K}_{l}{a}_{{H}_{2}}\cdot \left({H}_{2aq}-{H}_{2aq}^{*}\right)$ and ${K}_{l}{a}_{C{O}_{2}}\cdot \left(C{O}_{2aq}-C{O}_{2aq}^{*}\right)$ in equations 17 and 18 describe the liquid-to-gas mass transfer of H_{2} and CO_{2}, respectively (see Additional file: Liquid-to-gas mass transfer and chemistry of CO2__Theory_experiments_and_results).

#### Substrate consumption

The mass balance of glucose can be written as follows:

where *Y*_{GX} is the cell mass yield coefficient parameter (which is the model notation of the constant *k* in equation 3) and *Y*_{GAc} and *Y*_{GLac} are the stoichiometric yield coefficients (mol/mol substrate) describing the theoretical yields of cell mass, acetic acid and lactic acid, respectively.

#### Gas phase balances

The gaseous products are produced in the liquid phase, after which they are transported to the gas phase. The mass balances of the various gaseous compounds comprise an accumulation term and a gas-to-liquid mass transfer term as well as an inflow and an outflow.

Here *V*_{
l
} and *V*_{g} are the liquid and gas volume; *k*_{
l
}*a* is the volumetric mass transfer coefficient for the various compounds; H_{2aq} and CO_{2aq} are the dissolved concentrations of H_{2} and CO_{2}; ${H}_{2aq}^{*}$ and $C{O}_{2aq}^{*}$ are the dissolved concentrations of the compounds at equilibrium; ${F}_{in\phantom{\rule{0.3em}{0ex}}{N}_{2}}$ is the flow rate of N_{2} into the fermentor; and ${F}_{out\phantom{\rule{0.3em}{0ex}}{N}_{2}}$, ${F}_{out\phantom{\rule{0.3em}{0ex}}C{O}_{2}}$ and ${F}_{out\phantom{\rule{0.3em}{0ex}}{H}_{2}}$ are the effluent flow rates of N_{2}, CO_{2} and H_{2}, respectively.

#### Other equations used

The equilibrium between CO_{2}, bicarbonate and carbonate was taken into consideration as follows:

Since the pH was controlled during fermentation, it was kept constant at 6.6 in the model. For more details, see Additional file 1: Liquid-to-gas mass transfer and chemistry of CO2__Theory_experiments_and_results.

Furthermore, the effect of the stripping rate on the volumetric mass transfer coefficients was determined by using the following equation:

where *k*_{
l
}*a*_{
i0
} is the volumetric mass transfer coefficient at a stripping rate of ${F}_{0in\phantom{\rule{0.3em}{0ex}}{N}_{2}}$, *k*_{
l
}*a*_{
i
} is the volumetric mass transfer coefficient at a stripping rate of ${F}_{in\phantom{\rule{0.3em}{0ex}}{N}_{2}}$ and γ is an experimentally determined exponential coefficient.

### Experimental design and estimation of kinetic parameters

The mass transfer parameters (${K}_{l}{a}_{{H}_{2}}$ and ${K}_{l}{a}_{C{O}_{2}}$) and the exponential coefficient (γ) were determined before the parameters for the microbial kinetics were estimated. The mass transfer parameters were estimated using a methodology described by Hill [26]. The volumetric mass transfer coefficient for CO_{2}, ${K}_{l}{a}_{C{O}_{2}}$, was determined and the volumetric mass transfer coefficient for H_{2} (${K}_{l}{a}_{{H}_{2}}$) was calculated using the following relation between *k*_{
l
}*a* values and the diffusion coefficients for the compounds in water [18]:

Here the diffusion coefficients for CO_{2} (${D}_{C{O}_{2}}$) and H_{2} (${D}_{{H}_{2}}$) are 1.98 × 10^{-5} and 4.65 × 10^{-5} cm^{2}/second, respectively, according to Pauss *et al*. [18]. Only the most important results in the estimation of the mass transfer parameters are given here; the detailed results and the methodology can be found in Additional file: Liquid-to-gas mass transfer and chemistry of CO2__Theory_experiments_and_results.

To determine the kinetic parameters, fermentations were performed at two substrate concentrations and various stripping rates (Table 1). The kinetic parameters studied and estimated were *Y*_{GX}, ${Y}_{G{H}_{2}}$, μ_{max}, *R*_{AcF}, ${{R}_{Lac}}_{F{H}_{2}}$, H_{2aqcrit}, ${n}_{{H}_{2}}$, *R*_{LacFOSM}, *OSM*_{crit} and *n*_{μ}. Since the experiments were characterized by different growth rates as well as H_{2} and biomass yields, all parameters except the three related to osmolarity (*R*_{LacFOSM}, *OSM*_{crit} and *n*_{μ}) were estimated simultaneously for each of the 5 g/L experiments (that is, experiments 1 and 3 through 7), giving five parameter sets (Table 3). Experiments 6 and 7 were carried out under almost the same conditions with the same inocula and were thus used together to estimate one parameter set. The effect of osmolarity was assumed to be negligible in these experiments (experiments 1 and 3 through 7). The validity of this assumption was checked and is discussed below (Kinetic parameters: inhibition by osmolarity). An average of all parameters except μ_{max} was then calculated and used to simulate all six experiments. The parameters related to osmolarity were estimated using the 10 g/L experiments (that is, experiments 2 and 8).

Finally, the cell death rate (*r*_{cd}; equation 5), was calculated directly from the experimental data by determining, for each experiment, the slope of the biomass curve as it declined and calculating an average value of the slope based on all experiments. The overall affinity constant (*K*_{G}; equation 6) was taken from the literature on bacteria with the same type of glucose transporter system, that is, the ATP-binding cassette transport system (values are given in Table 2) [10, 27, 28].

The parameters in the model were estimated using a nonlinear least squares method which minimizes the objective function:

where LSQ is the least squares quadratic, that is, the sum of the squared residuals, *Y*_{exp,i,t}and *Y*_{model,i,t}, are the experimental and model values, respectively, at time *t* for each compound *i*, that is, glucose, acetic acid, lactic acid, cell mass and H_{2}. The parameter estimations were carried out and the 95% confidence intervals were calculated using the MATLAB functions *nlinfit* and *nlparci*, respectively (MathWorks, Natick, MA, USA).

## Results and Discussion

The order in which the parameters are estimated is important. Since the mass transfer influences fermentation, and thus the corresponding kinetic parameters, the mass transfer parameters were estimated prior to determining the fermentation-related kinetic parameters.

### Estimation of the volumetric mass transfer coefficient

The estimated overall volumetric mass transfer coefficients for CO_{2} (${K}_{l}{a}_{C{O}_{2}}$) in the fermentation medium were in the range of 3.4 to 7.2/hour for stripping rates ranging from 2.0 to 9.8 L/hour (33 to 164 mL/minute). The ${K}_{l}{a}_{C{O}_{2}}$ values obtained with their respective stripping rates were used to calculate the exponential parameter γ (equation 24), giving a value of 0.46 ± 0.02, which agrees well with previous findings [20, 29]. On the basis of the mass transfer results of CO_{2} and equation 25 ${K}_{l}{a}_{{H}_{2}}$ was determined to be 9.0 ± 0.1/hour at a stripping rate of 6 L/hour (100 mL/minute). This value is consistent with previous results for similar systems with stripping rates between 5 and 2,000 mL/minute, where the *k*_{
l
}*a* values were in the range of 1 to 120/hour [18, 20]. Hence, the expression calculating ${K}_{l}{a}_{{H}_{2}}$ (equation 24) is:

where ${F}_{in\phantom{\rule{0.3em}{0ex}}{N}_{2}}$ is the stripping rate. For more detailed results on mass transfer, see Additional file: Liquid-to-gas mass transfer and chemistry of CO2__Theory_experiments_and_results.

### Fermentation

In fermentation experiments 1 through 7, the glucose was completely consumed and acetic acid, H_{2} and lactic acid were the main products (Figures 1, 2, 3, 4, 5, 6 and 7). In experiment 8, complete glucose consumption was not achieved within 40 hours (Figure 8).

The six 5 g/L experiments (that is, experiments 1 and 3 through 7) differed with respect to growth rate and H_{2} yield (Figures 1, 2, 3, 4, 5 and 6). The reason for the variations is not clear. However, the two sets of experiments, carried out in parallel using inocula from the same preculture (experiments 3 and 4 as well as experiments 5 through 8), showed a strong resemblance. Batch experiments are generally characterized by poor reproducibility, as has also been observed with *Escherichia coli* [30]. Owing to the variations between the experiments, each of the 5 g/L experiments was used separately to estimate all parameters except *OSM*_{crit}, *n*_{μ} and *R*_{LacFOSM}, which were estimated using the 10 g/L experiments (experiments 2 and 8 and Figures 7 and 8). In addition, acetic acid and H_{2} were not produced at a stoichiometric ratio (1:2) in any of the experiments, which is in agreement with prior observations in continuous culture [15, 21] where the H_{2}/acetic acid ratio depended on the dilution rate. Instead, less acetate was produced in relation to H_{2}, and the H_{2} yield was thus considered a parameter in the model. A possible explanation of the nonstoichiometric yield is that acetic acid is used as a building block by the cells.

### Growth rates

The estimated maximum growth rate of *C. saccharolyticus* varied between the different experiments; however, the values were similar for experiments carried out in parallel (that is, experiments 3 and 4 and 5 through 8) (Table 3). The μ_{max} determined for glucose ranged from 0.21 to 0.36/hour and corresponded well with earlier findings, which varied from 0.2 to 0.5/hour [14, 21]. Vrije *et al*. [21] found different values of μ_{max} obtained in washout experiments with *C. saccharolyticus*, depending on the growth history of the culture. The reason for the variation in growth rates has not yet been elucidated, but the quality of the inocula used seems to depend on its growth history. The variation in growth rate was considered in the present model by not using an average value of μ_{max}, while average values were used for all the other parameters (described in more detail below, Kinteic parameters: inhibition by dissolved hydrogen).

Together with changes in the product yields, the variations in growth rates strongly suggest that an as yet unknown factor influences the metabolism. Also, it is likely that the highest value of μ_{max} determined in this study (0.36/hour) is not the true maximum, that is to say, the real μ_{max} that can be achieved for glucose by this organism. This could mean that the growth of *C. saccharolyticus* is normally suppressed, as has been observed for *E. coli* [30]. The cause of the suppression of the growth of *C. saccharolyticus* is not understood and must be further studied to gain a better understanding of the physiology of the microorganism and to improve the model [21].

### Kinetic parameters: inhibition by dissolved hydrogen

As described above (Growth and product kinetics in C. *saccharolyticus*), the effects of two environmental conditions, that is to say, H_{2aq} and osmolarity, on the growth, the production of acetic acid and H_{2}, and the activation of lactic acid production of *C. saccharolyticus* were studied. All parameters except and *R*_{LacFOSM}, *OSM*_{crit} and *n*_{μ} were estimated for each of the experiments with 5 g/L glucose (Table 3), from which their average values were calculated (Table 4). The experimental results are presented in Figures 1, 2, 3, 4, 5, and 6, together with the predictions of the model using the average values of the parameters (except for μ_{max}). The average value of μ_{max} was not used because of the large variation in this parameter; instead, the average within each set of parallel experiments was used. The model then agreed well with the experimental results and also reflected the effect of H_{2aq} on the microorganism. Interestingly, the parameter ${n}_{{H}_{2}}$ has quite a high value (4.5), which indicates a steplike response to the inhibiting agent, H_{2}; that is, at lower concentrations, the inhibition increases only a little with the concentration, whereas at higher concentrations the inhibition increases dramatically with increased concentration. The value of the H_{2} yield coefficient parameter, ${Y}_{G{H}_{2}}$, ranged from 3.7 to 6.2 mol H_{2}/mol glucose. The upper value exceeds the Thauer limit, which is 4 mol H_{2}/mol glucose [31]. However, the observed H_{2} yield obtained in the simulations and in the experiments never exceeded the Thauer limit; that is, the molar ratio of H_{2} produced to glucose consumed is always below 4. The high values of ${Y}_{G{H}_{2}}$ are an effect of the nonstoichiometric ratio between H_{2} and acetic acid seen during the experiments, described as ${Y}_{G{H}_{2}}\u2215{Y}_{GAc}$ in the model (equation 10). The ratios are often above 2 mol H_{2}/mol acetic acid and, in the model, this comes out as a higher H_{2} yield coefficient parameter. The reason for the H_{2} and acetic acid ratio not being equal to 2, as the stoichiometry of reaction 1 shows, might be that some of the acetic acid produced is taken up and utilized by the cell.

### Dissolved hydrogen: degree of supersaturation and its effect

Supersaturation of dissolved H_{2} occurred during fermentation, as measured experimentally and predicted by the model (Table 5), as reported previously [18, 19]. Oversaturation ranged from 4.9 to 52 times the saturation concentration, which corresponds well with the results of other studies [18, 19]. The large deviation in the measured values of H_{2aq} (Table 5) is an effect of the large uncertainties in the measurements. The oversaturation of H_{2aq} can also be clearly seen in Figure 9, where values of H_{2aq} calculated with the model for a few experiments are shown together with the saturation concentration of H_{2} for experiment 6.

The experiment with the lowest stripping rate (experiment 4) showed the highest production of lactic acid (Figure 3). The other two experiments with low stripping rates (experiments 6 and 7) (Figures 5 and 6) showed only a slight increase in lactic acid production compared to the experiments with high stripping rates (experiments 1, 3 and 5) (Figures 1, 2 and 4) and very little lactic acid production compared to experiment 4. This can be explained by the lower growth rates resulting in lower H_{2} productivity, and hence lower values of H_{2aq}, in experiments 5 through 7 (Figures 4, 5 and 6). Experiments 3 and 4 both showed high initial growth rates characterized by a high value of μ_{max} and hence high H_{2} productivity, leading to higher values of H_{2aq}. In experiment 4, with a low stripping rate (0.78 L/hour), H_{2aq} reached a plateau faster than it did in the other experiments (Figure 9). At that stage, the culture reached maximum H_{2} productivity (data not shown), which resulted in linear rates of glucose consumption and H_{2} and acetic acid production (Figure 4). This behavior was reflected by the model (Figure 4) and can be explained by growth inhibition by H_{2}. When H_{2} productivity reaches a critical value in the fermentation system, the cells respond with a reduction in the specific growth rate, and hence a plateau is observed. This plateau was reached much faster in experiment 4 than in the other two low-stripping-rate experiments (experiments 6 and 7), which was due to a combination of the higher initial growth rate and H_{2} productivity and the lower stripping rate (Table 1).

The model with estimated parameters for inhibition by H_{2aq} can be used to indicate how H_{2} productivity, ${P}_{{H}_{2}}$, H_{2aq} and the overall mass transfer coefficient are related (Figure 10). The dissolved H_{2} concentration in experiment 4 reached almost 80% of the value of H_{2aqcrit} (indicated by the red line in Figure 10) after 10 hours, and, Dissolved hydrogen: degree of supersaturation and its effect), H_{2} productivity and hence H_{2aq} were constant until glucose was depleted (Figures 3 and 9). The dissolved H_{2} concentration in experiment 5, on the other hand, was always well above the red line in Figure 10 and also showed little lactic acid production. In experiments 6 and 7, H_{2aq} also ended up near the red line (Figure 10); however, both reached it much later (at 17 hours; that is, only 4 hours before the glucose was depleted). This was due to lower growth rates and slightly higher stripping rates. Finally, H_{2aq} in experiment 1 crossed the red line after 16 hours with little production of lactic acid, which may be due to an exponential increase in H_{2} productivity, and the line was crossed when very little glucose remained; hence almost no substrate was left for lactic acid production (Figure 1).

The organism thus seems to respond to an increase in H_{2aq} by adjusting its growth rate and directing its metabolism toward the production of lactate, thus fine-tuning H_{2} productivity to prevent H_{2aq} values detrimental to the cell. On the basis of both the experimental data and the model, it is clear that dissolved H_{2} has a negative effect on *C. saccharolyticus* and that H_{2} productivity and the stripping rate have a considerable impact on H_{2aq}. This can explain why fermentation with high H_{2} productivity commonly results in low H_{2} yields [15, 21, 32, 33] and why an increase in the stripping rate tends to increase H_{2} yield and productivity [20].

### Predicting the effect of dissolved hydrogen concentration

The dissolved H_{2} concentration can be lowered by stripping with N_{2} gas (Figure 11), which also results in higher H_{2} yields [19, 34–36]. Kraemer and Bagley [20] published details of a study in which they optimized the stripping rate with respect to H_{2} yield and productivity. They concluded that a stripping rate of 12 mL/minute, resulting in a volumetric mass transfer rate of 5/hour, was optimal. However, this was only valid for their particular system and not for systems with higher H_{2} productivity and different liquid-to-gas mass transfer properties. Figure 11 shows H_{2aq} calculated by our model at various stripping rates and H_{2} productivities for the reactor system used herein. It is evident that H_{2aq} is a function of both variables.

Furthermore, the current model cannot simulate a system without sparging, since *k*_{
l
}*a* is based on the stripping rate (equation 24). However, Figure 10 provides an excellent basis for further discussions, since the relation between ${K}_{l}{a}_{{H}_{2}}$, ${P}_{{H}_{2}}$ and H_{2} productivity still holds, even without stripping. For instance, with *C. saccharolyticus* at a total pressure of 1 atm, no stripping, a productivity of 10 mmol H_{2}/L/hour, and a gas composition of 60% H_{2} and 40% CO_{2}, a value of ${K}_{l}{a}_{{H}_{2}}$ of at least 7.5/hour is required to avoid serious H_{2} inhibition (Figure 10).

### Kinetic parameters: inhibition by osmolarity

Experiments 2 and 8 were carried out with almost identical initial conditions, but they progressed quite differently, probably due mainly to different inocula and a slight difference in the initial glucose concentration. It was evident that H_{2aq} as the sole inhibitor could not adequately describe the system at elevated substrate concentrations (Figures 7 and 8). Indeed, the model fitted the data from experiments 2 and 8 very well after introducing growth inhibition by osmotic pressure.

The average value of μ_{max} in experiments 5 through 7, which were carried out using the same inocula as experiment 8, was used for experiment 8. However, since no experiments were carried out using the same inocula as experiment 2, together with a low glucose concentration, the value of μ_{max} for experiment 2 is not known. Instead, the average value of μ_{max} for the three sets of 5 g/L experiments (experiment 1, experiments 3 and 4, and experiments 5 through 7) was assumed (0.27/hour) when estimating the inhibition parameters for osmolarity, that is, *R*_{LacFOSM}, *OSM*_{crit} and *n*_{μ} (Table 6). Applying this extended model to the experiments with lower glucose concentrations confirmed that the osmolarity had a minor influence on the outcomes of the fermentations under those conditions. To estimate the three parameters describing the inhibition by osmolarity, μ_{max} for experiment 2 had to be assumed. This assumption mainly affects the value of the exponential factor, *n*_{μ}, and not *R*_{LacFOSM} or *OSM*_{crit} (Table 5). This strongly indicates that *OSM*_{crit} for *C. saccharolyticus* is in the range of 0.27 to 0.29 mol/L, a range that is in agreement with previous results of a study by Willquist *et al*. [14].

Although this rather simple model describes the effect of osmolarity well, some aspects of it cannot be reproduced by this type of unstructured, mechanistic model. It is evident from Figure 8 that the growth rate, and hence the glucose consumption and acetic acid production rates, are not affected at the initiation of growth, since the model excluding inhibition by osmolarity fits the first three points perfectly. However, at an osmolarity of about 0.2 mol/L, there is a shift toward a reduction in the growth rate, glucose consumption, and acetic acid production rate, as well as an increase in lactic acid production, rapidly at first, followed by a slow decline of all of them. It is not possible to model this effect, that is, a rapid shift followed by a slow gradual decrease, using a simple inhibition expression. One could assume a very high exponential factor, but that would predict only the beginning of the experiment; however, as inhibition came into effect, the decrease in the growth rate to zero would not be slow and gradual, but very considerable and rapid.

## Conclusions

Batch fermentations of *C. saccharolyticus* on glucose were successfully simulated using Monod kinetics extended to include liquid-to-gas mass transfer and inhibition by H_{2aq} and osmolarity. In agreement with previous measurements [18, 19], the model predicted high oversaturation of H_{2} in the liquid, which was also confirmed experimentally.

To the best of our knowledge, we have demonstrated for the first time the possibility of predicting H_{2aq} and its effect on the fermentation in a laboratory-scale bioreactor as a function of stripping rate and productivity using the derived model. With this tool, it was possible to conclude that the inhibition of growth and H_{2} production depend on both H_{2aq} and osmolarity. The model described the inhibition by both H_{2aq} and osmolarity satisfactorily and can hence be used to predict the optimal stripping rate and substrate concentration. It also shows how *C. saccharolyticus* responds to increased osmolarity and H_{2aq}. In addition, the modeled relationship between mass transfer, H_{2} productivity and H_{2aq} is not specific to *C. saccharolyticus*, but can also be applied to other systems. To widen the applicability of the model even further, future studies should aim at incorporating the effect of the stirrer speed and the absence of stripping on the liquid-to-gas mass transfer.

### Nomenclature

Ac: acetic acid concentration (mol/L); CO_{2aq}: CO_{2} concentration in the liquid phase (mol/L); $C{O}_{2aq}^{*}$: saturation concentration (mol/L); CO_{2sol}: solubilized CO_{2} (mol/L); ${F}_{out\phantom{\rule{0.3em}{0ex}}C{O}_{2}}$: flow rate of CO_{2} out of the fermentor (L/hour); ${F}_{out\phantom{\rule{0.3em}{0ex}}{H}_{2}}$: flow rate of H_{2} out of the fermentor (L/hour); ${F}_{in\phantom{\rule{0.3em}{0ex}}{N}_{2}}$: flow rate of N_{2} into the fermentor (L/hour); ${F}_{out\phantom{\rule{0.3em}{0ex}}{N}_{2}}$: flow rate of N_{2} out of the fermentor (L/hour); *G*: substrate concentration (mol/L); H_{2aq}: H_{2} concentration in the liquid phase (mol/L); H_{2aqcrit}: critical H_{2} concentration in the liquid phase (mol/L); ${H}_{2aq}^{*}$: saturation concentration (mol/L); ${H}_{{H}_{2}}$: Henry's constant for H_{2} (L atm/mol); ${H}_{C{O}_{2}}$: Henry's constant for CO_{2} (L atm/mol); *K*_{1}: dissociation constant for CO_{2} into bicarbonate; K_{2}: dissociation constant for bicarbonate into carbonate; ${K}_{l}{a}_{{H}_{2}}$: mass transfer coefficient for H_{2} (per hour); ${K}_{l}{a}_{C{O}_{2}}$: mass transfer coefficient for CO_{2} (per hour); *K*_{G}: saturation constant (mol/L); Lac: lactic acid concentration (mol/L); *n*_{μ}: inhibition coefficient for inhibition by osmolarity; ${n}_{{H}_{2}}$: inhibition coefficient for inhibition by H_{2}; *OSM*: osmolarity parameter (mol/L); *OSM*_{crit}: critical osmolarity parameter (mol/L); ${P}_{{H}_{2}}$: partial pressure of H_{2} (Pa); ${p}_{{H}_{2}crit}$: critical partial pressure of H_{2} (Pa); *P*_{tot}: total pressure (Pa); PPi: pyrophosphate; LSQ: least squares quadratic; *R*: gas constant (L atm/K/mol); *R*_{AcF}: maximum Ac production rate (mol/g cell mass/hour); ${{R}_{Lac}}_{F{H}_{2}}$: maximum Lac production rate caused by H_{2} (mol/g cell mass/hour); *R*_{LacFOSM}: maximum Lac production rate caused by osmotic pressure (mol/g cell mass/hour); *r*_{cd}: death rate of cells (per hour); *T*: temperature (Kelvin); *V*_{g}: gas volume in liquid (L); *V*_{l}: liquid volume in reactor (L); *X*: cell mass concentration (mol/L); *Y*_{GAc}: stoichiometric acetic acid yield (mol acetic acid/mol substrate); ${Y}_{GC{O}_{2}}$: stoichiometric CO_{2} yield (mol CO_{2}/mol substrate); ${Y}_{G{H}_{2}}$: stoichiometric H_{2} yield (mol H_{2}/mol substrate); *Y*_{GLac}: stoichiometric lactic acid yield (mol lactic acid/mol substrate); *Y*_{GX}: biomass yield (mol cell mass/mol substrate); α: cell-growth-associated constant; α_{Ac}: cell-growth-associated constant for Ac production rate (mol Ac/mol cells); ${\alpha}_{C{O}_{2}}$: cell growth-associated constant for CO_{2} production rate (mol CO_{2}/mol cells); ${\alpha}_{{H}_{2}}$: cell growth-associated constant for H_{2} production rate (mol H_{2}/mol cells); α_{Lac}: cell-growth-associated constant for Lac production rate (mol Lac/mol cells); β: non-cell-growth-associated constant; γ: exponential coefficient for mass transfer correlation; μ: specific growth rate (per hour); μ_{max}: maximum specific growth rate (per hour).

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## Acknowledgements

The authors gratefully acknowledge the Commission of the European Communities, Sixth Framework Programme, Priority 6, Sustainable Energy Systems (019825 HYVOLUTION), as well as the Swedish Energy Agency for their financial support.

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### Competing interests

The authors declare that they have no competing interests.

### Authors' contributions

ML developed the model, carried out the parameter estimations and planned as well as performed the mass transfer experiments. ML also wrote the main part of the manuscript and took part in the planning and execution of the fermentation experiments. KW took part in the development of the model, planned and carried out the main part of the fermentation experiments, analyzed the results and assisted in the mass transfer experiments. KW also wrote parts of the manuscript. GZ and EVN participated in the coordination of the study and reviewed the manuscript. All authors read and approved the final manuscript.

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### 13068_2011_110_MOESM1_ESM.DOCX

Additional file 1: Liquid-to-gas mass transfer and chemistry of CO2__Theory_experiments_and_results. This file contains information on the estimation of the mass transfer parameters as well as the set-up of the mass transfer experiments. The file also contains more detailed information concerning the theory behind the chemistry of carbon dioxide and liquid-to-gas mass transfer. (DOCX 40 KB)

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### Cite this article

Ljunggren, M., Willquist, K., Zacchi, G. *et al.* A kinetic model for quantitative evaluation of the effect of hydrogen and osmolarity on hydrogen production by *Caldicellulosiruptor saccharolyticus*.
*Biotechnol Biofuels* **4, **31 (2011). https://doi.org/10.1186/1754-6834-4-31

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### Keywords

- Fermentation
- Lactic Acid Production
- Biohydrogen
- Volumetric Mass Transfer Coefficient
- Mass Transfer Parameter