- Open Access
Consolidated bioprocessing of cellulose to itaconic acid by a co-culture of Trichoderma reesei and Ustilago maydis
Biotechnology for Biofuels volume 13, Article number: 207 (2020)
Itaconic acid is a bio-derived platform chemical with uses ranging from polymer synthesis to biofuel production. The efficient conversion of cellulosic waste streams into itaconic acid could thus enable the sustainable production of a variety of substitutes for fossil oil based products. However, the realization of such a process is currently hindered by an expensive conversion of cellulose into fermentable sugars. Here, we present the stepwise development of a fully consolidated bioprocess (CBP), which is capable of directly converting recalcitrant cellulose into itaconic acid without the need for separate cellulose hydrolysis including the application of commercial cellulases. The process is based on a synthetic microbial consortium of the cellulase producer Trichoderma reesei and the itaconic acid producing yeast Ustilago maydis. A method for process monitoring was developed to estimate cellulose consumption, itaconic acid formation as well as the actual itaconic acid production yield online during co-cultivation.
The efficiency of the process was compared to a simultaneous saccharification and fermentation setup (SSF). Because of the additional substrate consumption of T. reesei in the CBP, the itaconic acid yield was significantly lower in the CBP than in the SSF. In order to increase yield and productivity of itaconic acid in the CBP, the population dynamics was manipulated by varying the inoculation delay between T. reesei and U. maydis. Surprisingly, neither inoculation delay nor inoculation density significantly affected the population development or the CBP performance. Instead, the substrate availability was the most important parameter. U. maydis was only able to grow and to produce itaconic acid when the cellulose concentration and thus, the sugar supply rate, was high. Finally, the metabolic processes during fed-batch CBP were analyzed in depth by online respiration measurements. Thereby, substrate availability was again identified as key factor also controlling itaconic acid yield. In summary, an itaconic acid titer of 34 g/L with a total productivity of up to 0.07 g/L/h and a yield of 0.16 g/g could be reached during fed-batch cultivation.
This study demonstrates the feasibility of consortium-based CBP for itaconic acid production and also lays the fundamentals for the development and improvement of similar microbial consortia for cellulose-based organic acid production.
Itaconic acid (IA) is a bio-derived platform chemical with various uses ranging from polymer synthesis to biofuel production. At the current selling price of 1500–1700 USD/ton, itaconic acid is already becoming competitive to replace fossil polyacrylic acid in the production of superabsorbent polymers [1, 2]. Still, to access other bulk markets like methyl methacrylate, which is currently produced from acetone cyanohydrin (about 1000 USD/ton), the price of itaconic acid has to drop further. Besides reducing the processing costs, the price of itaconic acid can be further reduced by using cheaper substrates. For comparison, the current sugar prices are about 310 USD/ton while pulp grade wood costs only about 35 USD/ton [3, 4]. The cheap and sustainable production of itaconic acid from cellulosic waste streams is therefore a highly anticipated goal of current research [5, 6].
The biosynthesis of itaconic acid in the filamentous fungus Aspergillus terreus is directly derived from the Krebs cycle, where it is produced from cis-aconitate by decarboxylation via its key biosynthetic enzyme cis-aconitate decarboxylase (Fig. 1) . The yeast Ustilago maydis in contrast, first isomerizes the cis-aconitate to trans-aconitate before decarboxylation . Depending on the production yield and the involved metabolic reactions, the biosynthesis of itaconic acid has different implications on the respiratory quotient, which can be exploited to analyze its production non-invasively via offgas measurements, as described in Fig. 1.
Currently, industrial itaconic acid production is exclusively realized by a fermentation process using the filamentous fungus Aspergillus terreus . However, itaconic acid production with A. terreus is a challenging process that is only efficient if certain prerequisites are fulfilled. These prerequisites are a high initial sugar concentration, a low fermentation pH, a strict manganese deficiency and a non-interrupted oxygen supply [10,11,12]. These prerequisites have been found especially difficult to be fulfilled in the context of cellulose-based itaconic acid production [13, 14]:
The bioconversion of cellulose into itaconic acid as well as other bio-commodities generally involves a hydrolysis of the cellulose into soluble sugars followed by a fermentation of the released sugars into the targeted product. This process configuration is called separate hydrolysis and fermentation (SHF). Recent attempts to produce itaconic acid in an SHF approach failed mainly because of manganese and other impurities contained in both the cellulose feedstock as well as in cellulase enzyme preparations used for hydrolysis . Until now, production of cellulosic itaconic acid had been only proven successful after extensive purification of the cellulose hydrolysate using ion exchangers or activated charcoal [16,17,18], which impacts the economy of the process. Table 1 shows a summary of all known attempts on cellulose-based itaconic acid production available from literature. A strategy that has the potential to substantially increase the process economy is simultaneous saccharification and fermentation (SSF). This concept has the great advantage that the inherent inhibition of the cellulases by their hydrolysis products is completely avoided, since the released sugars are constantly consumed during the process. However, while sugars should not accumulate during SSF to prevent product inhibition of cellulases, high sugar concentrations are a prerequisite for efficient itaconic acid production using A. terreus [10, 13, 15, 19, 20]. Therefore, this process configuration is not suitable with A. terreus as a biocatalyst . Another obstacle for an A. terreus-based SSF is the required low fermentation pH of 3.4–1.8, which is incompatible with the pH activity profile of conventional cellulases (pH 4–6.5).
Ustilago maydis is a promising alternative itaconic acid producer, which is capable of producing itaconate at a more neutral pH range (4.5–6.5) and with lower initial sugar concentrations. Furthermore, U. maydis is completely insensitive to manganese, which renders it much more suitable for the conversion of non-purified cellulose feedstocks. It has a single cell yeast morphology, which improves fermentation broth rheology and thereby facilitates efficient aeration in comparison to shear-sensitive fungi pellets [14, 21]. In addition, in terms of biosafety, U. maydis is classified as biosafety level 1 and can be even consumed as a food delicacy while A. terreus is an opportunistic human pathogen and has recently been classified into biosafety level 2 in some countries, which considerably restricts its use .
U. maydis has already proven suitable for SSF-based itaconic acid production, however reaching only very low yields despite application of high cellulase loadings of 0.1 gProtein/gCellulose or 26 filter paper units (FPU)/gCellulose . Recently, itaconic acid production with U. maydis and other Ustilaginaceae such as U. cynodontis has been improved considerably by genetic engineering [24,25,26,27]. This, along with advances in bioprocess design enabled by the yeast morphology [27,28,29], has considerably enhanced the yield, titer, and rate of itaconic acid production by Ustilago.
A yet unachieved goal is the direct conversion of cellulose into itaconic acid without application of externally produced enzymes in a fully consolidated bioprocess (CBP). Although both A. terreus and U. maydis naturally possess biomass-hydrolysing enzymes [30,31,32], neither of the organisms is known to produce itaconic acid when grown on cellulose. Furthermore, their cellulase activity is far too low for efficient itaconic acid production from cellulose. To realize a CBP, different strategies are possible. One approach that has been realized recently is the genetic modification of a native cellulolytic organism like Neurospora crassa to enable the synthesis of itaconic acid. However, only 0.02 g/L of itaconic acid were produced from 20 g/L corn stover . In general, the recombinant production of itaconic acid in non-native hosts has been proven challenging. Even the conversion of the citric acid producer A. niger, which is closely related to A. terreus, into an effective itaconic acid producer seems to be difficult [34,35,36]. Alternatively, a native itaconic acid producer could be engineered to produce carbohydrate-active enzymes, either by activation of dormant native genes [37, 38], or by heterologous expression . However, this is no straightforward task as it often involves the high-level expression and secretion of multiple enzymes [40, 41]. A third strategy, which has the potential to unite both the benefits of native cellulase producers, and the high production capability of dedicated organisms for the target product synthesis, is co-culture fermentation. Due to synergistic effects of labor division, the performance of a co-culture can even be greater than the sum of the individual sub processes . This strategy has already been proven successful for the production of different bio-commodities such as isobutanol, lactic acid, and fumaric acid [43,44,45]. Therefore, here we aim to establish a CBP by co-cultivating the hyper cellulolytic fungus Trichoderma reesei RUT-C30 (RFP1) with the engineered U. maydis Δcyp3 ΔPria1::Petef Δfuz7 Petef mttA for itaconic acid production.
Results and discussion
Simultaneous saccharification and fermentation (SSF)
As a first step towards consolidated bioprocessing, itaconic acid production was assessed in a SSF setup to evaluate the capability of the engineered U. maydis Δcyp3 ΔPria1::Petef Δfuz7 Petef mttA to produce itaconic acid under glucose-limiting conditions. Thereby, fermentation supernatants of two different cellulolytic fungi (T. reesei RUT-C30 (RFP1) and Penicillium verruculosum (M28-10) were compared as source for cellulases. These fungi have been found compatible with the presence of itaconic acid in a previous screening . Since nitrogen limitation is a prerequisite for itaconic acid production with U. maydis, the residual NH4+-concentration present in the cellulase-containing supernatants had to be monitored . The supernatants were diluted accordingly to reach a final NH4+-concentration equivalent to the 0.8 g/L NH4Cl, typically present in itaconic acid production medium for U. maydis [26, 28, 29]. This resulted in a final cellulase titer of 2.2 FPU/mL for the cultivations containing T. reesei supernatant and 0.6 FPU/mL for the cultivations containing P. verruculosum supernatant. These values corresponded to 18 and 5 FPU/g cellulose, respectively, and are close to the cellulase loading of 10 FPU/g cellulose, typically used for separate cellulose hydrolysis . Since cellulose digestibility has a major impact on cellulose hydrolysis, 120 g/L of highly digestible Sigmacell as well as 120 g/L recalcitrant α-cellulose were tested as substrates . All media were buffered to pH 6.5 using 100 mM MES buffer.
As shown in Fig. 2, both T. reesei and P. verruculosum supernatants enabled itaconic acid production from cellulose by U. maydis during SSF. Using the T. reesei supernatant, similar itaconic acid concentrations as in a reference culture containing 50 g/L of glucose instead of cellulose were reached. The highest itaconic acid concentration achieved during the SSF was 21 g/L using Sigmacell as substrate, which is fourfold higher than previously demonstrated for a SSF using wildtype U. maydis MB215, and close to the values achieved with A. terreus (Table 1). Even using the relatively recalcitrant α-cellulose, a similar titer of 19 g/L itaconic acid was produced. Although the itaconic acid production using the P. verruculosum supernatant was generally lower than using T. reesei supernatant, especially with α-cellulose, the achieved titers were still considerable in relation to the almost fourfold lower cellulase activity of 0.6 FPU/mL. Remarkably, the itaconic acid yield based on the consumed amount of glucose equivalents from cellulose was essentially identical to the yield achieved using glucose in the reference and also comparable to yields achieved with A. terreus using purified cellulose hydrolysate (Table 1).
From the pH profile, it can be seen that in most of the cultures the pH dropped to about 3.5 after 69 h of cultivation. Since it is known that U. maydis stops itaconic acid production at such low pH values , it is possible that higher itaconic acid titers could have been achieved using a higher buffer concentration or active pH control, which would also have further improved the cellulose hydrolysis. This hypothesis was confirmed by comparing the itaconic acid production of glucose-supplemented SSF cultures either buffered with MES or with CaCO3 (Additional file 1: Fig. S1). In case of the MES-buffered culture, itaconic acid production stopped before the exhaustion of glucose when reaching pH 3.5. In contrast, the CaCO3-buffered culture that maintained pH between 6 and 7 continued itaconic acid production after exhaustion of the added glucose and further converted cellulose into itaconic acid. An added benefit of the CaCO3 addition is an in situ precipitation of the product as calcium itaconate, which alleviates product inhibition and facilitates downstream processing . Calcium salt precipitation still belongs to the most mature and widely applied downstream technology for industrial organic acid production [28, 54].
Consolidated bioprocessing (CBP) with co-cultures of T. reesei and U. maydis
As a next step, itaconic acid production was assessed in a CBP setup with a sequential co-culture of U. maydis and T. reesei. First, T. reesei was grown for 1 week in pure culture to produce sufficient cellulase enzymes, whereafter U. maydis was added to an OD of 0.67. To prevent a termination of itaconic acid production due to a decreasing pH, the medium was buffered with 33 g/L CaCO3. The performance of the CBP culture was directly compared to a corresponding SSF culture using undiluted sterile filtered supernatant of the same T. reesei pre-culture used for CBP. A schematic representation of the experimental setup is depicted in Fig. 3.
As can be seen in Fig. 4a, up to 10.5 g/L of itaconic acid was produced in the co-culture CBP. The SSF in contrast produced up to 15.3 g/L of itaconic acid. Thus, the CBP was clearly less effective in producing itaconic acid than the SSF. This could be already expected since two organisms have to share the same resources. The cellulose consumption (Fig. 4e) was clearly higher in the CBP compared to the SSF, especially during the initial 72 h growth phase. Since all conditions are identical between CBP and SSF except for the presence of living T. reesei cells, this increase in cellulose consumption can be clearly attributed to T. reesei. In turn, also the itaconic acid yield was affected by the CBP in comparison to the SSF. While a yield of 0.381 g/g Glucose was reached in the SSF, only 0.134 g/g Glucose were achieved in the CBP.
On the positive side, this increased cellulose consumption also demonstrates an enhanced cellulose hydrolysis performance with increased metabolic substrate demand. A recent publication on cellulosic malic acid production demonstrated that an increase in metabolic activity can drastically enhance cellulose hydrolysis without increasing cellulase concentration . Therefore, the main challenge for optimizing the CBP setup is to channel the substrate consumption towards U. maydis and minimize the activity of T. reesei during the itaconic acid production phase. Still, some low residual activity of T. reesei could be beneficial, since the cellulase activity was more stable in the CBP compared to the SSF (Fig. 4c, d). This was likely due to constant re-synthesis of degraded cellulases by T. reesei.
The population dynamics between U. maydis and T. reesei were not investigated in detail. Still, microscopic examination of the samples suggested a relatively balanced population ratio between T. reesei and U. maydis towards the end of the culture. There were always cells visible from both T. reesei and U. maydis in randomly chosen fields of view (Fig. 5). The nitrogen supply in the cultures had to be limited in order to induce itaconic acid production by U. maydis. As a result of this limited nitrogen availability and competition with cellulase synthesis by T. reesei, both organisms could only grow until the shared nitrogen pool was exhausted. Hence, the U. maydis cell number per field of view was clearly lower in CBP compared to SSF, which might explain the lower itaconic acid productivity. If the nitrogen consumption of T. reesei in the CBP would have been compensated by appropriate addition of NH4+, similar U. maydis cell densities and itaconic acid productivities might have been reached as in the SSF.
The major benefit of CBP in contrast to SSF is that no enzymes had to be added and that cellulose can directly be converted into itaconic acid. Since the targeted substrates are cellulosic waste streams, which have very low cost, the production yield is less important. It has to be evaluated whether the economic benefits of the CBP process can compensate the yield loss. The outcome of this will most likely depend strongly on the price of cellulase enzyme production and cellulosic substrate.
Influence of inoculation time
During the proof of principle CBP described above, T. reesei was cultured for one week in pure culture to produce sufficient cellulase enzymes before adding U. maydis. However, a one week pre-cultivation phase considerably lowers the average productivity of the co-culture compared to the SSF scenario (Table 2). To further optimize the co-culture and increase the productivity, the effect of inoculation delay between T. reesei and U. maydis on the CBP performance was studied. Four different additional inoculation delays were tested: 0 days (direct co-inoculation at the beginning), 3, 4, and 5 days. Because cellulase production by T. reesei usually starts after 2 days, it was expected that preliminary inoculation of U. maydis would strongly affect cellulase production due to competition for nitrogen. Therefore, 1 and 2 days delay were not tested. The experiment was performed in medium containing 5 g/L glucose for initial growth acceleration and 30 g/L α-cellulose. Furthermore, the experiment was carried out as fed-batch with regular feeding of α-cellulose powder for maximization of itaconic acid production.
When T. reesei and U. maydis were co-inoculated, the culture did not produce any cellulase enzymes nor any itaconic acid. Instead, exclusively U. maydis grew and consumed all glucose before T. reesei was able to germinate, thereby preventing the production of cellulases that would have enabled further growth of both organisms on cellulose. Because of the limited initial glucose concentration, a nitrogen limitation could not be reached, which explains the lack of itaconic acid production. Co-inoculation with vital cells of T. reesei instead of T. reesei spores might solve this problem since a starting quantity of cellulases would be present that would allow the co-culture to grow on cellulose instead of collapsing.
When U. maydis was added to the T. reesei culture after cellulase production had already started, itaconic acid production was successful. The influence of the different inoculation delays on both cellulase and itaconic acid production was surprisingly low (Fig. 6). Cellulase production of T. reesei is directly proportional to the available concentration of the nitrogen source. Because of this, it would have been expected that earlier inoculation of U. maydis would reduce cellulase production because of the competition for nitrogen. In this case, due to an earlier limitation of nitrogen also an earlier onset of itaconic acid production would have been expected. However, this was clearly not the case, suggesting only a very low growth and nitrogen consumption by U. maydis. To analyze the growth of U. maydis, a differential fluorescent staining technique was developed to clearly discriminate U. maydis cells from T. reesei and thereby allow for manual cell counting of the U. maydis population (see material and methods). For the cultures with 3 and 4 days inoculation delay, U. maydis only grew very slowly before the first cellulose feed. Starting from an initial inoculation density of 0.8∙107 cells/mL (corresponding to a measured OD of 1.14), only a cell density of 2.7∙107 and 1.7∙107 cells/mL within 46 h and 25 h was reached, respectively, although the medium contained still all nutrients necessary for growth (Fig. 6e–g). The extent of growth inhibition becomes clearer in comparison to the growth of U. maydis in the instantly co-inoculated experiment. Here, U. maydis was able to grow to a cell density of 25∙107 cells/mL in 24 h with just 5 g/L of glucose. For the experiments with inoculation delay, significant growth of U. maydis was only evident after increasing the carbon supply by feeding additional cellulose (Additional file 1: Figure S2). These phenomena may be explained by a higher affinity for sugars of T. reesei compared to U. maydis, enabling the former to out-compete the latter under sugar limitation. For reference, we observed µmax values of 0.17 and 0.21 for T. reesei and U. maydis, respectively, when grown in pure culture at pH 7 in MES-buffered glucose media. Hence, under non-limited conditions U. maydis is the faster growing of both organisms. By feeding cellulose, the sugar concentration is increased, which enabled U. maydis to grow much faster.
Additionally, besides the temporal effect of the inoculation delay, there was also an unexpected viability effect that should have caused a growth benefit for U. maydis in the early inoculated experiments compared to the late inoculated experiments. The U. maydis inoculum was prepared from a YPD medium grown pre-culture that was washed twice with bi-distilled water and then stored as aqueous cell suspension at 0 °C for the different inoculation time points, so that the same stock could be used for all tested conditions. The viability of the aqueous inoculum was monitored for each inoculation time point by always inoculating a YPD medium filled flask in parallel to the CBP cultures and recording growth using online scattered light measurements. By observing an increase in the lag time with the age of the aqueous inoculum, it became clear that the viable cell density dropped significantly over time (Additional file 1: Figure S3). The increase in lag time by more than one doubling time (3.5 h) suggests at least a twofold difference in viable cell density. Despite the drop in viability, there was no impact on CBP performance. Thus, the sugar supply rate was the key factor determining population dynamics and sugar partitioning between T. reesei and U. maydis, while neither the inoculation delay nor inoculation density of U. maydis had a significant effect.
Also regarding itaconic acid productivity, the sugar supply rate (and thus, the cellulose hydrolysis rate) was most likely the limiting factor. For a glucose-based itaconic acid production reference, typically a cell density of 50∙107 cells/mL and a productivity of 0.77 g/L/h are reached under the investigated conditions (Additional file 1: Figure S4). Since the determined U. maydis cell density during CBP ranged from 10∙107 to 30∙107 cells/mL, a theoretical itaconic acid production capacity of 0.16 to 0.46 g/L/h was present in the CBP. The fact that only a maximum productivity of 0.10 g/L/h was reached in the fed-batch CBP indicates that the cells were not producing itaconate at maximum capacity, likely due to the above-mentioned competition for glucose.
As envisaged, the total average productivity (including the cellulase production phase) in this fed-batch experiment was indeed higher than in the previous batch experiment with 7 day inoculation delay (Table 2). However, this effect was not related exclusively to the smaller inoculation delay or an earlier onset of itaconic acid production. Instead, the productivity was generally slightly higher and was sustained for a longer period, so that the influence of the cellulase production phase duration on the total average itaconic acid productivity was minimized. This was due to the regular feeding of cellulose and thus mainly a benefit of fed-batch fermentation in contrast to batch fermentation. The key factor controlling the start of itaconic acid production was the time point of the first cellulose feeding, which in all cases was synchronized to 5 days after start of the experiment and thereby likely also synchronized the itaconic acid production. This feeding regime was chosen because a preliminary mass feeding of cellulose would have compromised cellulase production by T. reesei. An earlier start of itaconic acid production could therefore be at the expense of cellulase activity.
Detailed online process monitoring during co-culture CBP using online respiratory analysis
Up to now, consortium-based CBP has been proven successful only in academic research. One major obstacle for industrial application of such processes is a lack of suitable and established process control techniques. The substrate consumption for example is very difficult to assess in complex cultures containing solid cellulose particles. Here, the respiration rate of the fed-batch CBP was monitored online as a direct measure for microbial activity. As described in earlier studies [49, 56], cellulose consumption and thereby suitable time points for feeding fresh substrate could be estimated online based on the cumulative oxygen consumption. This way, intermittent starvation of the culture could be prevented (Fig. 7a, c).
The use of online respiration measurement further allowed to estimate the product formation online. Assuming the pure aerobic combustion of glucose as only carbon source for maintenance and biomass formation, the respiratory quotient can be considered to be 1 (Fig. 1, pathway C). During phases of significant formation of partially oxidized products such as itaconic acid, which is typically produced at a yield of 0.4 g/g in U. maydis, the RQ should be even below 1. Pure itaconic acid formation would cause an RQ of 0.67 (Fig. 1, pathway a). However, since CaCO3 was used for buffering of the cultures, the production of 1 mol itaconic acid would release an additional mole of CO2 by reacting with the carbonate, thereby increasing the RQ above 1 (Fig. 1, pathways a, b, blue values). This effect is depicted more clearly in Additional file 1: Figure S5, comparing the theoretical RQ in absence or in presence of CaCO3 in relation to the itaconic acid yield. Hence, an RQ above 1 in presence of CaCO3 indicates that itaconic acid production is ongoing, while a drop of RQ close to 1 indicates cessation of itaconic acid production. During the experiment, RQ values well above the theoretically expected values have been measured, because the used strain still produces considerable amounts of reduced by-products such as glycolipids, which result in an increased RQ [25, 57]. An explanation for this phenomenon is illustrated in Figure S5.
The profile of the RQ over time thereby serves as an indicator for the time-resolved itaconic acid yield during the process (Fig. 7b). While the global average itaconic acid yield was only 0.16 g/g, this averaged value likely results from dynamic fluctuations of phases with high yield (0.4 g/g) and phases without itaconic acid production. The data suggest that the actual itaconic acid yield was highly dependent on the cellulose concentration and thus sugar supply rate. After each feeding, the RQ went up to a maximum of about 1.3 before gradually decreasing to values close to or even below 1, where itaconic acid production likely stopped (Fig. 7b). When a surplus of substrate was available after a cellulose pulse, the yield approached values typically observed with glucose based fermentations, but then dropped as the substrate depleted. Thus, when the substrate supply was high, itaconic acid production was the dominant process, while respiration of T. reesei and U. maydis became more dominant with low substrate supply. This implies that a certain threshold substrate supply rate has to be sustained in order to enable itaconic acid production and that the maximum itaconic acid yield is only achieved under carbon non-limited conditions. This observation fits well to the observed influence of sugar supply rate on substrate partitioning and population dynamics between T. reesei and U. maydis observed at the early phase of the fermentation.
Assuming i) a baseline RQ of 1 for both T. reesei and U. maydis; ii) that any surplus CO2 is derived from acid reaction with CaCO3 and iii) that itaconic acid is the only acid formed, the amount of itaconic acid produced can be directly estimated from the difference between cumulated CO2 evolution and the cumulated O2 uptake. Figure 7d shows a comparison of itaconic acid production and online estimation based on respiration measurement. The axes are scaled in a way that 130 g/L itaconic acid equals 1 mol/L CO2 difference, hence 1 mol CO2 per mol itaconic acid (130 g/mol). Although the online estimation did not fit exactly to the HPLC measurements, the method can give an approximation and a clear trend of itaconic acid production. Underestimation can be explained by either production of reduced storage molecules, CO2 fixation or non-respirative oxidation reactions while over-estimation is most likely a result of other organic acid by-products, which have been observed in the CBP cultures but not during itaconic acid production from glucose (Additional file 1: Table S6). The online estimation suggests that the time-resolved itaconic productivity (the slopes in Fig. 7d) reached values up to 2.2 mmol/L/h (or 0.29 g/L/h) after each cellulose feeding, which implies that the actual itaconic acid production potential present in the CPB was considerably higher than the achieved averaged value of 0.07 g/L/h. These data suggest that if the duration of the feeding intervals of the cellulose are reduced, the space–time-yield could be increased up to fourfold, reducing the total process time to 240 h. The best way to optimize the process would be an RQ-controlled automatic feeding of cellulose powder.
Nieder-Heitmann et al. performed a techno-economic analysis to compare sugar cane bagasse-based itaconic acid production via SHF to classical glucose-based production. Assuming an overall conversion yield of cellulose-rich sugarcane bagasse to itaconic acid between 0.086 and 0.188 g/g, a titer of 147 g/L and a productivity of 1.15 g/L/h, cellulosic itaconic acid would be already on-par or superior to glucose based itaconic acid . While the calculated minimum selling price was most sensitive to yield and productivity, the titer was less important. It was shown that major economic burdens of the cellulosic SHF process were the high investment costs related to additional production facilities for separate hydrolysis and enzyme production as well as the energy requirement for the concentration of raw hydrolysates to the high sugar concentrations necessary for efficient itaconic acid production with A. terreus. Both of these major cost drivers were neutralized in the here presented SSF and CBP processes. Additional cost savings can be expected for the downstream processing as the itaconic acid precipitates in situ during fermentation, which makes product isolation less energy intense . While the overall cellulose-to-itaconic acid conversion yield of 0.17 g/g in the fed-batch CBP already fits well into the economically viable scenario of Nieder-Heitmann et al., the productivity still needs to be significantly improved. However, a detailed techno-economic calculation for our case will be necessary to determine the minimum viable productivity, as cost savings from lower energy demand and lower investment costs will likely compensate to some degree for a lower productivity.
The capability of U. maydis to produce itaconic acid under glucose-limiting conditions in an SSF process was verified, achieving a yield of 0.38 g/g using recalcitrant α-cellulose. This yield is the highest ever achieved in an SSF process, and it is comparable to that achieved on glucose (Table 1). The compatibility of U. maydis with a living T. reesei culture was evaluated in a sequential co-culture CBP and compared to an SSF process with undiluted T. reesei supernatant. Although the CBP process was inferior to the SSF configuration, a direct conversion of cellulose to a meaningful quantity of itaconic acid could be demonstrated for the first time. Improvement of substrate allocation to U. maydis will be a key strategy to maximize itaconic acid yield during CBP, with cellulose concentration being the main determining factor. This finding was further corroborated by online analysis of the metabolic processes during fed-batch CBP using online respiration measurements, which indicated that the time-resolved itaconic acid productivity and yield peaked shortly after feeding cellulose and dropped with the depletion of the cellulose. The proposed method for online process monitoring will be a valuable tool for future improvement of the process as the feeding regime can be adjusted precisely to maximize substrate availability and thereby minimize respiration. Another key variable that will be an obvious target for future research is the effect of nitrogen concentration, which ultimately limits cellulase formation as well as the cell density of U. maydis and might therefore significantly improve productivity. A remarkable itaconic acid titer of 33.8 g/L could be reached with the fed-batch CBP strategy, which is on par with current SHF based results (Table1). Overall, this study demonstrates the applicability of U. maydis for consolidated bioprocessing of cellulosic biomass in co-culture, thus further expanding the process window with this organism.
T. reesei RUT-C30 (RFP1) (a red fluorescent protein-labeled clone  of the standard RUT-C30 strain obtained from American Type Culture Collection ATTC 56,765) was propagated at 30 °C on potato extract glucose agar medium (Roth, Karlsruhe, Germany) containing 40 mL/L of carrot juice (BIOBIO, Marken-Discount AG & Co. KG, Germany). P. verruculosum M28-10, kindly gifted by Dr. Gerhard Kerns (Saxon Institute for Applied Biotechnology, Leipzig, Germany), was propagated at 30 °C on medium containing 10 g/L malt extract (Difco; Becton, Dickinson and Company, USA), 40 mL/L carrot juice, 10 g/L wheat bran (Alnatura, Darmstadt, Germany), 10 g/L α-cellulose (Sigma-Aldrich, St. Louis, USA), 30 g/L agar (Difco; Becton, Dickinson and Company, USA). Spores were harvested from agar plates using 10 mL 0.01% (v/v) Tween 80 solution and washed twice with bi-distilled water. The spore concentration was determined in a Neubauer-Improved counting chamber (Superior Marienfeld, Lauda-Königshofen, Germany), adjusted to 109 spores/mL and stored at 4 °C. This 1000 × concentrated stock was used for inoculation all experiments.
U. maydis Δcyp3 ΔPria1::Petef Δfuz7 PetefmttA is a genetically engineered variant of U. maydis MB215 with enhanced itaconate production, reduced by-product formation, and stabilized morphology . This strain was propagated at 30 °C on yeast extract peptone dextrose (YPD) agar plates. Liquid overnight cultures of U. maydis were grown from single agar plate colonies at 30 °C in YPD medium. For inoculation of the experiments, YPD cultures were washed twice with bi-distilled water and used to inoculate the experiments to the final OD as indicated in the figure captions. For the initial SSF and batch CBP experiments, freshly prepared aqueous cell suspensions were used for inoculation. For the fed-batch CBP experiment, the same aqueous cell suspension stock was used for all tested inoculation delays and stored in an ice bath.
Media and cultivation
All experiments were performed in 250-mL Erlenmeyer flasks with 25 mL filling volume at 30 °C, 200 rpm and 50 mm shaking diameter.
The itaconic acid production medium used in the initial SSF experiment was adopted from Geiser et al. . Because the added cellulase-containing fermentation supernatants of the cellulase producers contained already residual NH4+, NH4Cl was omitted. The medium contained 0.2 g/L MgSO4·7H2O, 0.01 g/L FeSO4·7H2O, 0.5 g/L KH2PO4, 1 mL/L vitamin solution, 1 mL/L trace element solution, and as buffer 19.5 g/L (100 mM) 2-(N-morpholino) ethanesulfonic acid (MES) or CaCO3 as indicated in the figure captions. The pH of the MES stock solution was adjusted to 6.5 with 6 M NaOH solution. The trace element solution contained 15 g/L EDTA, 4.5 g/L ZnSO4·7H2O, 1 g/L MnCl2·4H2O, 0.3 g/L CoCl2·6H2O, 0.3 g/L CuSO4·5H2O, 0.4 g/L Na2MoO4·2H2O, 4.5 g/L CaCl2·2H2O, 3 g/L FeSO4·7H2O, 1 g/L H3BO3, and 0.1 g/L KI. The vitamin solution contained 0.05 g/L D-biotin, 1 g/L D-calcium pantothenate, 1 g/L nicotinic acid, 25 g/L myo-inositol, 1 g/L thiamine hydrochloride, 1 g/L pyridoxol hydrochloride and 0.2 g/L para-aminobenzoic acid. The medium was prepared as a 1.43 × concentrated stock solution. The solution was filtered through a 0.2 µm filter for sterilization. Before the experiment, the 1.43 × concentrate was diluted to its original concentration by addition of sterile bidest water and sterile filtered cellulase-containing fermentation supernatants. The cellulase-containing fermentation supernatants of T. reesei RUT-C30 (RFP1) and P. verruculosum M28-10 were produced in a stirred tank fermentation as described in Additional file 1: S7. The necessary amount of cellulose was directly weighted into empty Erlenmeyer flasks (3 g Sigmacell or 3 g α-cellulose) and steam-sterilized at 121 °C as powder before the liquid medium was added. Both types of cellulose were purchased from Sigma-Aldrich (St. Louis, USA). For the single feeding event during the SSF cultivation, 1.5 g the corresponding cellulose was steam-sterilized as powder and added separately to each Erlenmeyer flask.
The medium for the co-culture CBP was based on a medium published by Pakula et al., which was modified for co-culture compatibility with A. terreus, U. maydis and T. reesei, enabling both itaconic acid and cellulase production by the respective organisms [60, 61]. The final medium consisted of (NH4)2SO4 7.6 g/L, KH2PO4 0.8 g/L, MgSO4·7H2O 0.5 g/L, CaCl2·2H2O 0.23 g/L, NaCl 0.05 g/L, 5 g/L CaCO3, glucose 5 g/L, α-cellulose 30 g/L, peptone ex casein 2 g/L (N-Z-Amine® AS, Carl Roth, Karlsruhe, Germany), Tween 80 0.02% (v/v), trace element solution 2.5 mL/L. The main solution without trace elements and cellulose was always prepared as a 2 × concentrated stock solution that was set to pH 5.5 with 5 M NaOH. The solution was filtered through a 0.2 µm filter for sterilization. Before the experiment, the 2 × concentrate was diluted to its original concentration by addition of sterile bidest water and other supplementing solutions such as trace elements or glucose. The trace element solution (400 × concentrated) had the following composition: citric acid 180 g/L, Fe2(SO4)3 2.29 g/L, ZnSO4·7H2O 16 g/L, CuSO4 2.05 g/L, MnSO4·7H2O 1.6 g/L, H3BO3 0.8 g/L, CoCl2·6H2O 2.71 g/L.
For the batch CBP experiment, T. reesei was cultivated at 200 rpm, 50 mm shaking diameter and 30 °C in three 1 L Erlenmeyer flasks with 100 mL filling volume for 7 days in the described co-culture medium buffered with 33 g/L CaCO3. Thereafter, the three cultures were pooled and phosphate and ammonium content of the culture was measured. Residual NH4+ was equivalent to 1.2 g/L NH4Cl and was not necessary to supplement before the inoculation of U. maydis since the NH4Cl concentration in itaconic acid production medium is only 0.8 g/L. Residual KH2PO4 was 0.18 g/L and was supplemented to a final concentration of 0.5 g/L to prevent preliminary phosphate limitation. For the CBP experiment, the T. reesei culture broth was distributed to three replicate Erlenmeyer flasks (25 mL each), for the corresponding SSF experiment, the residual T. reesei culture broth was sterile filtrated and also distributed into three replicate Erlenmeyer flasks (25 mL each). The necessary amount of cellulose and CaCO3 was directly weighted into the empty Erlenmeyer flasks and steam-sterilized at 121 °C as powder before the liquid was added. Thereby, the cultures were supplemented with 120 g/L α-cellulose and 33 g/L CaCO3.
For the fed-batch CBP, the KH2PO4 starting concentration in the co-culture medium was increased to 1.3 g/L to anticipate the KH2PO4 supplementation that was necessary in the batch CBP. CaCO3 was increased to 40 g/L.
The reference cultivation of U. maydis with 50 g/L glucose was performed in in the co-culture medium with only 1.5 g/L NH4SO4, 0.5 g/L KH2PO4, without cellulose and buffered with 40 g/L CaCO3.
1-mL samples were withdrawn from the same Erlenmeyer flasks during the cultivation (no sacrifice flasks). The weight of the Erlenmeyer flasks was determined before every sampling to correct the measured variables for evaporation. When necessary, bi-distilled water was added to compensate for significant evaporation.
Phosphate was determined according a method for orthophosphate determination published by the United states EPA . Ammonium was determined according to a modified version of the Berthelot reaction . The protein concentration of the culture supernatant was determined by a Bradford assay  using Coomassie Plus™ assay reagent (Thermo Scientific, Waltham, USA) and bovine serum albumin as standard. The measurement procedure was performed according to the manufacturer’s manual for microtiter plates. Cellulase activity in the culture supernatant was measured by the standard filter paper activity (FPA) assay according to the method of Ghose  adapted by Xiao . The assay was performed in a 60-µL reaction volume in 96-well conical bottom PCR plates.
Soluble sugars and metabolites including glucose, cellobiose, xylose as well as itaconic acid, citric acid, malic acid and succinic acid were determined via HPLC analysis. To dissolve potentially precipitated calcium itaconate, the broth was diluted 6 × with 0.5 M HCl. After centrifugation of the fermentation samples (16,900 g; 10 min; 4 °C) and a second centrifugation step of the resulting supernatant (3,000 g; 10 min), the supernatant was analyzed by HPLC (Dionex HPLC UltiMate 3000, Thermo Scientific, Waltham, USA) at 65 °C using the following setup: Column: AMINEX Ion Exclusion HPX-87H, 300 × 7.8 mm (Bio-Rad Laboratories GmbH, Munich, Germany); detectors: Dionex™ Ultimate 3000 UV/VIS detector (Thermo Scientific, Waltham, USA) at 210 nm and RI-101 refractory index detector (Shodex, Munich, Germany); mobile phase: 5 mM sulfuric acid; flow rate: 0.7 mL/min.
For the standard determination of CDW in absence of cellulose particles, between 0.75 and 3 mL of sample were filled into pre-weighted conical bottom glass tubes and centrifuged (20 min, 3,000 g, 4 °C). The supernatant was carefully pipetted off for other analytic procedures. The resulting pellet was washed two times by resuspension in 10 mL dest. water with subsequent centrifugation (20 min, 3000 g, 4 °C) and careful removal of the water using a pipette connected via a collecting bottle to a vacuum pump. Thereafter, the washed pellet was dried overnight (at least 12 h) in a Speedvac device under vacuum at 40 °C and 300 g acceleration. Finally, the glass tube containing the dried pellet was weighed on a microbalance and the CDW was calculated by subtracting the empty weight of the tube.
For the determination of CDW and residual cellulose in samples containing cellulose particles, a modified version of the Updegraff method adapted by Ahamed & Vermette was used [67, 68]. First, the total dry weight of all solids (TDW) was determined as described for the standard CDW determination above. The resulting dry pellet was then re-suspended in 3 mL of Updegraff reagent and incubated for 30 min in a boiling water bath with a marble on top of the glass tube to reduce evaporation. Thereby, the Updegraff reagent selectively dissolves the fungal biomass, leaving the cellulose intact. Updegraff reagent is a mixture of 10 mL conc. nitric acid and 100 mL 80% acetic acid. After the incubation, the suspension was mixed with 3 mL 96% ethanol to facilitate sedimentation of the cellulose and centrifuged (20 min, 3000 g, 4 °C). The resulting pellet was washed two times by resuspension in 10 mL dest. water with subsequent centrifugation (20 min, 3000 g, 4 °C) and careful removal of the water using a pipette connected via a collecting bottle to a vacuum pump. Thereafter, the pellet was washed with 1 mL 70% ethanol without subsequent resuspension and dried overnight (at least 12 h) in a Speedvac device under vacuum at 40 °C and 300 g acceleration. Finally, the glass tube containing the dried pellet was weighed on a microbalance and the weight of cellulose was calculated by subtracting the empty weight of the tube. The corresponding CDW was determined by subtracting the weight of cellulose from the TDW.
The offgas analysis was realized using a commercial Transfer-Rate Online Measurement (TOM) system (Kuhner, Birsfelden, Switzerland) equipped with a mass flow controller.
Online scattered light measurements
Online scattered light measurements were performed using the cell growth quantifier (CGQ) system (Aquila biolabs GmbH, Baesweiler, Germany).
Microscopy and U. maydis cell counting
T. reesei and U. maydis were microscopically discriminated by their differing cell wall composition. Therefore, samples were stained with a mixture calcofluor, which predominantly stains β-1,4-glucan and trypan blue, which predominantly stains chitin . The sample suspensions were first diluted 1/10 with bi-distilled water and then 1/10–1/20 with the following staining solution: 10 µg/mL trypan blue and 10 µg/mL calcofluor in 20 mM phosphate–citrate buffer pH 7.4. Finally, 11 µL of the diluted and stained suspension were pipetted into wells of a µ-Slide angiogenesis (ibidi GmbH, Gräfelfing, Germany) and analyzed at 10X magnification (Plan-Apochromat 10X objective with 1X tubelens optovar) by a ZEISS Axio Observer Z1 (Zeiss, Jena, Germany) inverted fluorescence microscope equipped with a Yokogawa CSU-X1 spinning disk unit. Calcofluor fluorescence was recorded with 405 nm laser excitation, RQFT 405/488/568/641 dichroitic mirror and BP 450/50 nm emission filter. Trypanblue fluorescence was recorded with 638 nm laser excitation, RQFT 405/488/568/641 dichroitic mirror and BP 690/50 nm emission filter. Per sample, a total of 8 different field of views were recorded. For extended focus depth, 5 slices covering a Z-dimension range of 32 µm were recorded and processed into a maximum projection image. Besides the differing morphology, U. maydis yeast cells showed stronger trypan blue fluorescence relative to T. reesei hyphae, which allowed manual counting of the yeast cells in the images.
Availability of data and materials
The data generated or analyzed during this study are included in this published article and its supplementary information files. Further datasets used and analyzed during the current study are available from the corresponding author on reasonable request.
Cell dry weight
Cell growth quantifier
Environmental Protection Agency
Filter paper unit
High-pressure liquid chromatography
Optical density at 600 nm
Red fluorescent protein
Separate hydrolysis and fermentation
Simultaneous saccharification and fermentation
Total dry weight
Transfer-rate online measurement
Yeast extract peptone dextrose medium
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We thank Elena Antonov for her former contributions to the project on co-culture-based consolidated bioprocessing itaconic acid within the Cluster of Excellence “Tailor-Made Fuels from Biomass”. We thank Prof. Dr. Gerhard Kerns (Saxon Institute for Applied Biotechnology, Leipzig, Germany) for providing the P. verruculosum M28-10 strain.
Open Access funding enabled and organized by Projekt DEAL. The Clusters of Excellence TMFB 236 “Tailor-Made Fuels from Biomass” and FSC 2186 “The Fuel Science Center”, which are funded by the Excellence Initiative by the German federal and state governments, are gratefully acknowledged for financial support. NW and HT acknowledge funding from the German Federal Ministry of Food and Agriculture (BMEL), through the Agency for Renewable Resources (FNR) as part of the ERA-IB project “TTRAFFIC” (FKZ 22030515).
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Schlembach, I., Hosseinpour Tehrani, H., Blank, L.M. et al. Consolidated bioprocessing of cellulose to itaconic acid by a co-culture of Trichoderma reesei and Ustilago maydis. Biotechnol Biofuels 13, 207 (2020). https://doi.org/10.1186/s13068-020-01835-4
- Consolidated bioprocessing
- Itaconic acid
- Platform chemical
- Microbial consortium
- Mixed culture
- Simultaneous saccharification and fermentation
- Metabolic engineering