- Open Access
Integrating enzyme fermentation in lignocellulosic ethanol production: life-cycle assessment and techno-economic analysis
Biotechnology for Biofuels volume 10, Article number: 51 (2017)
Cellulase enzymes have been reported to contribute with a significant share of the total costs and greenhouse gas emissions of lignocellulosic ethanol production today. A potential future alternative to purchasing enzymes from an off-site manufacturer is to integrate enzyme and ethanol production, using microorganisms and part of the lignocellulosic material as feedstock for enzymes. This study modelled two such integrated process designs for ethanol from logging residues from spruce production, and compared it to an off-site case based on existing data regarding purchased enzymes. Greenhouse gas emissions and primary energy balances were studied in a life-cycle assessment, and cost performance in a techno-economic analysis.
The base case scenario suggests that greenhouse gas emissions per MJ of ethanol could be significantly lower in the integrated cases than in the off-site case. However, the difference between the integrated and off-site cases is reduced with alternative assumptions regarding enzyme dosage and the environmental impact of the purchased enzymes. The comparison of primary energy balances did not show any significant difference between the cases. The minimum ethanol selling price, to reach break-even costs, was from 0.568 to 0.622 EUR L−1 for the integrated cases, as compared to 0.581 EUR L−1 for the off-site case.
An integrated process design could reduce greenhouse gas emissions from lignocellulose-based ethanol production, and the cost of an integrated process could be comparable to purchasing enzymes produced off-site. This study focused on the environmental and economic assessment of an integrated process, and in order to strengthen the comparison to the off-site case, more detailed and updated data regarding industrial off-site enzyme production are especially important.
With second generation biofuels comes an increased potential for bioenergy worldwide as well as new challenges related to efficient conversion of woody biomass and environmental sustainability. The use of residual lignocellulosic material as feedstock for biofuels has been suggested as a way to avoid potentially negative effects of land use change and competition with human food production [1, 2], which has previously generated concern and debate. Spruce is the most abundant wood species in Sweden, and in several studies it has been shown to be a suitable raw material for bioethanol production [3–6]. The cost and environmental impact of lignocellulosic bioethanol, most notably in terms of greenhouse gases (GHG) emitted, have been assessed in various studies giving results with significant variations [7–23].
Life-cycle assessment (LCA) has become a widespread tool for performing such analyses of the environmental performance of a product by mapping the resource use and emissions related to its life cycle. Thus, LCA is a potential tool for comparing and analysing different pathways for lignocellulosic ethanol as well as finding hot spots for future improvements. Several LCA studies of lignocellulosic ethanol have found the production of enzymes to contribute significantly to environmental impacts, including GHG emissions [7–12]. Enzymes have also been identified as an important factor in total ethanol production costs. Liu et al.  calculated costs up to 0.82 EUR L−1 ethanol, depending on the price of cellulase enzymes used in enzymatic hydrolysis. Earlier studies reported production costs from approximately 0.10 to 0.59 EUR L−1 ethanol, depending on the choice of process design and the assumptions used in the studies [14–23]. The cost of cellulases not only represents a significant part in the overall production costs in current systems, but it is also one of the most uncertain parameters in the evaluations , and many have used assumptions based on future prices for manufactured enzyme products [14, 19, 20, 24–28]. Furthermore, the lack of transparency and the difference in the way enzyme dosages are reported hinder comparisons between studies .
A potential alternative to purchasing manufactured enzymes is an integrated process of enzyme and ethanol production. By using whole, crude fermentation broths containing fungal cells and substrate residues, the processes of cell removal, enzyme concentration and purification steps could be avoided. Hypercellulolytic mutants of Trichoderma reesei, the most widely used fungus for cellulase production, have been reported to grow well and secrete large amounts of cellulolytic enzymes on steam-pretreated spruce [30, 31] and could thus be assessed for an integrated process design . Integrated production entails using part of the wood feedstock for growing T. reesei, reducing the fraction of wood available for ethanol conversion, but using the whole fermentation broth could also improve saccharification and ethanol yields due to the effect of mycelium-bound enzymes [33–36]. Some LCA studies have taken steps towards investigating the potential environmental benefits of co-locating and partly integrating enzyme production with ethanol conversion [10–12], but the full potential of an integrated process approach, using part of the lignocellulosic feedstock for enzyme production, has only recently been addressed [37, 38]. Janssen et al.  showed that an integrated process could potentially halve GHG emissions from high-gravity ethanol production and significantly improve the performance in other environmental impact categories. In terms of economics, several studies presume that on-site or integrated production of enzymes on cheap lignocellulosic raw materials will be desirable to reduce ethanol costs [13, 21, 29, 39–44].
The aim of the present study was to investigate GHG emissions, primary energy use and the production cost for ethanol made from spruce logging residues in Sweden, using two different process designs for integrated cellulase enzyme and ethanol production. Integrated enzyme production in a full-scale bioethanol plant was modelled together with the whole ethanol production process using the commercial software Aspen Plus. GHG emissions and primary energy balances were assessed in a life-cycle perspective using two standardized calculation frameworks to illustrate the sensitivity of the results to different assumptions made in the LCA method. Ethanol production cost was assessed as minimum ethanol selling price (MESP), meaning the ethanol price at the break-even point where the annual cost and the annual income are equal, as also the annual costs and revenues. The results for the integrated process designs were compared to an off-site case, where enzymes were assumed to be purchased from an off-site facility. The enzyme production in the off-site case was based on existing data for current industrial production reported in previous LCAs of lignocellulosic ethanol [7, 9], and potential improvements and uncertainties regarding GHG emissions, energy and cost performance of off-site enzyme production were assessed in sensitivity analyses. The focus in these sensitivity analyses was on critical factors affecting the comparison between the modelled integrated cases developed in this paper and the off-site case.
The model of bioethanol production is based on previously published research by Barta et al.  and will be introduced here only briefly. For the integrated cases, the entire ethanol plant with integrated enzyme production was modelled. For the off-site case, the ethanol plant was modelled without the external enzyme production facility. The purchased enzymes are added to the modelled ethanol plant according to available information and data regarding industrial enzyme production today. Due to the aggregated nature of such information and data presented in the existing scientific literature, it was not possible to analyse off-site enzyme production in the same level of detail as the modelled integrated production. Thus, there is a difference in the assessment performed in this paper between the cases, where the integrated cases are analysed in more detail than the off-site case.
The dry spruce chips were assumed to contain 37.9% glucan, 9.9% mannan, 1.8% galactan, 4.3% xylan, 1.3% arabinan, and 28.0% lignin . Cellulases were assumed to be produced using a mutant of T. reesei, employing the whole crude fermentation broth of the fungus in the saccharification step. Figure 1 shows the process schematically. A pretreated liquid fraction and a pretreated liquid fraction supplemented with molasses were evaluated as feed for integrated enzyme production. As reference case, ethanol production without integrated enzyme production was modelled, and enzymes were assumed to be purchased from an external enzyme production facility. The latter is the off-site case. In all the scenarios, the conversion factors for some reactions were the following : (1) in steam pretreatment glucan to glucose 0.185, glucan to hydroxymethylfurfural 0.007, xylan to xylose 0.792, xylan to furfural 0.083, water-insoluble lignin to water-soluble lignin 0.037 and (2) in SSF (simultaneous saccharification and fermentation) glucan to glucose 0.91, xylan to xylose 0.8, glucose to ethanol 0.92, glucose to glycerol 0.035. Further details regarding the ethanol production design can be found in the Additional files 1, 2, and in .
Integrated enzyme fermentation
Two configurations, denoted A and B, were investigated in the model of integrated enzyme fermentation (Fig. 2). They differed in the carbon source: in configuration A, part of the liquid fraction of the diluted slurry was used, while in configuration B the liquid fraction was supplemented with molasses to increase the sugar content. The enzyme dosage of simultaneous saccharification and fermentation was ten filter paper units (FPU) g−1 water-insoluble solid.
Assumptions regarding enzyme dosage in the integrated cases were based on confirmed laboratory-scale results. These results were based on an integrated process setup, and thus impacts on ethanol yields from diversion of part of the hydrolysate for growing T. reesei, and the toxicity of the hydrolysate in the cellulase enzyme fermentation, are taken into account (for further discussion of these parameters, see Barta et al. ). To illustrate a future scenario, two cases A+ and B+ were included, which use the same setup as A and B, respectively, but with increased enzyme activity. In the cases annotated by “+”, the specific activity of the soluble proteins was enhanced 1.5-fold, resulting in an increase of 50% in the productivity in terms of enzyme activity, while protein and mycelium yields remained the same.
Off-site enzyme production
In the off-site case, enzymes were assumed to be purchased from an external production facility and added directly to the SSF in the ethanol plant model. In general, the steps in off-site enzyme production are as follows: (i) production by microorganisms using inputs of carbohydrates, protein, mineral salts and vitamins followed by (ii) the recovery of the enzyme liquor and (iii) formulation of the enzyme product . For the purpose of this study, the important differences between off-site and integrated enzyme production are the treatment steps in (ii) and (iii) applied to refine and stabilize the enzymes intended for use elsewhere (see e.g. ), as well as feedstock material. However, since no cost breakdown is available for the current industrial production of enzymes, and environmental data based on industrial scale production are aggregated in the existing scientific literature [see e.g. 7, 9, 45], no detailed data for the different processes of off-site enzyme production can be presented, and therefore off-site enzyme production is analysed in less detail.
The enzyme preparation purchased in the off-site case was based on existing data for the commercially available cellulase cocktail Cellic CTec3 from Novozymes A/S. Assuming 213 FPU mL−1 for the cocktail [46, 47] and a density of 1.1 g mL−1 (valid for CTec2, the predecessor product) , enzyme dosage was calculated to be 30.4 g enzyme cocktail kg−1 DM (dry matter) wood. This dosage is used for the base case scenario, but as it is a crucial factor for the resulting costs and GHG emissions, alternative assumptions were tested in sensitivity analyses (see “Alternative enzyme data for sensitivity analyses” section).
The model in Barta et al.  was updated mainly regarding capital and enzyme costs. Mass and energy balances were solved using the commercial flow sheeting program Aspen Plus V8.0 (Aspen Technology, Inc., Cambridge, MA). The important results of mass and energy balances used as inputs for the life-cycle assessment are included in the Additional file 1 for all the modelled cases of ethanol production. Fixed capital investment (FCI) costs were estimated either with Aspen Process Economic Analyzer V8.0 (Aspen Technology, Inc.) or from vendor quotation (see Additional file 3). To obtain the annual FCI, an annuity factor of 0.11 was used, corresponding to a depreciation period of 15 years and an interest rate of 7%. Working capital investment (WCI) was calculated according to the recommendations in the literature . Annual WCI was calculated by multiplying the WCI by the interest rate.
All costs were calculated in Swedish kronor (SEK) but are presented here in Euros (EUR, 1 US$ ≈ 1.1 EUR, 1 EUR ≈ 9.3 SEK). In the off-site case, the purchase price of enzyme was 3.55 EUR per million FPU, which was obtained by updating the estimate of a previous study . Purchase prices of raw material, nutrients, chemicals, and utilities, costs of labour, insurance, maintenance and selling prices of co-products are found in the Additional file 1, with further economic data presented in the Additional file 3.
Focusing on the comparison between off-site and integrated enzyme production, MESP is calculated in the economic analysis. As the enzyme price is uncertain to a great extent, sensitivity analysis of MESP was performed in the off-site case: MESP was plotted as a function of enzyme price in EUR MFPU−1 (Fig. 3). Using the equation of the fitted curve (Fig. 3), the MESP of the off-site case can easily be adjusted to other enzyme prices and compared to integrated cases at any enzyme price.
Annual cash flows show the difference between the annual cost and annual income, and illustrate the distribution of costs and revenues for the ethanol production systems studied. As an illustration, the annual cash flows were calculated using an ethanol selling price of 0.59 EUR L−1 (5.5 SEK L−1, based on ). The results can be found in the Additional file 1.
Two calculation approaches for LCA were applied: one following the standardized methodology of ISO 14040 and 14044 [50, 51] and the other following the method presented in the EU renewable energy directive (RED) . Where the ISO method offers a frame and structure for LCA with recommendations regarding method considerations, the RED method goes further by stating how the environmental impact in terms of GHG emissions from biofuel systems is to be calculated . The RED method is designated for calculations of GHG emissions, but for the purpose of this study, RED method assumptions are also applied to calculate primary energy efficiency. Both methods were applied in a well-to-gate analysis, meaning that the environmental life cycle of ethanol was followed from cradle to factory gate.
LCA results for biofuels have proved to be generally affected by methodological choices such as the allocation procedure and the handling of different co-products [53–56]. Both ISO and RED methods call for sensitivity analyses in which the sensitivity of the results to changes of different parameters is tested, and thus applying two calculation approaches can in itself serve as this analysis. As the focus of this study was primarily on the assessment of new integrated process designs, and secondly on a comparison to an off-site case with purchased enzymes, the main objects for scrutiny in the sensitivity analyses were the input data and the assumptions made for enzyme production and utilization. As a result, choices regarding system expansion and crediting co-products in the ISO method are discussed only briefly. Furthermore, this study cannot answer questions concerning an optimized, overall process design for a lignocellulosic ethanol biorefinery, but focuses on one aspect of such an environmentally sustainable and commercially viable design.
Functional unit and system boundaries
According to RED, the functional unit (FU) to which environmental impact is related is 1 MJ (LHV) of fuel . For the purpose of comparison, the FU was 1 MJ bioethanol (LHV) in both ISO and RED calculations. GHG performance was calculated as global warming potential (GWP) with a 100-year time-frame. Emissions of CO2, CH4 and N2O were taken into account, where 1 g of CH4 and N2O was regarded as 34 and 298 g CO2-eq., respectively .
In the RED methodology, wastes and agricultural crop residues used as feedstock in biofuel production are free from GHG emissions from activities prior to their collection . RED also states that CO2 uptake during cultivation and CO2 emissions from combustion of biofuels are to be excluded from the calculations. For the ISO method, CO2 uptake during biomass growth was assumed to be equal to CO2 emissions stemming from the biomass in the fermentation process and from ethanol combustion. No environmental impact from forestry was allocated to forest residues, other than from the collection and transportation of residues. However, the collection of residues may affect soil carbon content as biomass is removed from the forest (see e.g. ). Nutrient balances can also be affected negatively, though ash recovery can reduce such issues . These aspects were excluded from the present calculations due to the study focus here being on the potential for integrated enzyme production, but effects on soil carbon are included in a sensitivity analysis.
Multi-functionality and allocation
The ethanol systems studied are multi-functional and deliver electricity and lignin solid fuel as co-products. According to the ISO order of priority, expansion of the system to include co-products is preferred prior to the allocation of environmental burden based on physical or economic relationships . For the ISO method we applied substitution, a form of system expansion where co-products are assumed to substitute corresponding products. Electricity was assumed to be delivered to the grid, replacing the regional electricity mix. Avoided environmental impacts from substituted products were credited to ethanol.
In the RED method, environmental impacts are allocated to co-products based on lower heating value (LHV) . The RED guidelines state that electricity is regarded as a co-product if generated from by-products or waste at the plant, and in other scenarios it is assumed to substitute grid electricity . Here electricity was regarded as co-product for RED calculations.
Table 1 shows GHG and primary energy data for nutrients, chemicals, enzymes, electricity mixes and fuels included in the assessment.
Collection and transportation of feedstock
We assumed that the forest residues were collected as loose logging residues (tops and branches) after final felling of spruce stands. Collection, forwarding, loading, unloading, comminution and transport of feedstock were assumed to be conducted as in Lindholm et al. [58, 69]. Feedstock was collected as loose residues in northern Sweden where transportation distance was estimated, on average, to be 138 km.
Based on LHV of 19.2 MJ kg−1 DM for forest residues, GHG emissions related to harvest and transport activities were 65 and 42 g CO2-eq. kg−1 DM collected, respectively . Energy input was 0.25 MJ kg−1 DM for harvest and 0.25 MJ kg−1 DM for transport .
Enzyme and nutrients
For integrated cases, primary energy input and GHG emissions for chemicals and nutrients shown in Table 1 were included in the calculations. Regarding the energy content of the products, only the energy content of molasses (13.6 MJ kg−1 DM based on Aspen modelling) and purchased enzymes (assuming 10% protein concentration and 11.2 MJ kg−1 protein, based on Aspen modelling) were taken into account.
As described in the previous sections, the off-site production of purchased enzymes was not modelled, in contrast to the integrated enzyme production cases, and thus life-cycle data are based on the existing scientific literature and other available information. For the off-site case, GHG emission data for the Novozymes A/S Cellic CTec3 enzyme product were based on previously used data [7, 9] that were updated based on personal communication with Novozymes A/S (personal communication with Kløverpris, J. H., Novozymes A/S, February 2015). The data refer to aggregated GHG emissions from the production at the company site in North Carolina, United States, which amount to 5.5 kg CO2-eq. kg−1 product. No further breakdown of GHG emissions was available but alternative data for production of the purchased enzymes were tested in the sensitivity analyses, and thus making possible more thorough comparisons of the integrated and off-site cases.
Previously released data from Novozymes A/S contained information on the aggregated input of fossil primary energy in the production process. As presented in , fossil primary energy input was 100 MJ kg−1 formulated product based on aggregated data from 2012, where the corresponding data for GHG emissions were 8 kg CO2-eq. kg−1 product. For the purpose of this study, assumptions regarding primary energy input in off-site enzyme production were necessary:
The source of electricity in the off-site enzyme production was natural gas (personal communication with Kløverpris, J. H., Novozymes A/S, February 2015), while the source of heat is unknown. Total primary energy input was therefore assumed to correspond to the reported input of fossil primary energy.
The update of the Cellic CTec3 carbon footprint data from 8 to 5.5 kg CO2-eq. kg−1 of product corresponds to a reduction by 31%. An update of fossil primary energy input was assumed to follow the reduction of the carbon footprint, resulting in 69 MJ kg−1 of enzyme product.
The above assumptions and updated data were used to calculate the GHG emissions and primary energy balance for the off-site case, in order to enable a justified comparison to the integrated process designs.
Alternative enzyme data for sensitivity analyses
Impacts of off-site enzyme production could potentially be reduced, for instance by developing higher enzyme activity, enhancing energy efficiency or using a higher proportion of renewable energy. The size of potential improvements related to different measures and time horizons entails large uncertainties, and a detailed assessment was further complicated by scarce and aggregated data. In an attempt to relate to and discuss our results, we present GWP results for off-site enzyme production using the following alternative data and assumptions leading to various potential improvements.
For the sensitivity analysis, off-site enzyme dosage data were adapted from  (12.4 g enzyme cocktail kg−1 DM) and alternative GHG data for enzymes from  and  (16 and 2.3 kg CO2-eq. kg−1 enzyme, respectively). Using alternative GHG data for enzyme production required a different method to decide enzyme dosage: we assumed 65 FPU g−1 of whole, purchased enzyme preparation containing 10% enzyme protein according to . Furthermore, we tested assumptions of a 50% increase in enzyme activity based on previous improvements from earlier generations of the Novozymes A/S Cellic CTec product (personal communication with Kløverpris, J. H., Novozymes A/S, February 2015). Lastly, an assumption of Swedish electricity mix for the production was tested to exemplify a scenario with a larger share of renewable electricity. For this purpose, a rough estimation of electricity use in off-site enzyme production was based on general data for industrial enzyme production : electricity was estimated to contribute to roughly 40% of GHG emissions from the enzyme production. Replacing natural gas-based electricity  with the Swedish electricity mix was estimated to reduce GHG emissions by 70% kWh−1 electricity, thus reducing total GHG emissions from enzyme production by roughly one-third.
Electricity and fuels
The electricity and fuel data used in the calculations of GWP and primary energy input are presented in Table 1. Natural gas-based electricity was included in aggregated, off-site enzyme production data. Because of the aggregated nature of these data, combined with a lack of information or alternative data regarding a more detailed breakdown of primary energy and GWP, assumptions regarding electricity and fuels in off-site enzyme production were necessary. The procedure for such assumption is described in the “Enzyme and nutrients” section. For the integrated cases, assumptions regarding electricity and fuels are mainly based on the geographic location. As the proposed ethanol plant was assumed to be located in Sweden, electricity supply in case A, which is the only case requiring input of grid electricity for the bioethanol production, was assumed to be the average Swedish grid electricity. For the same reason exported electricity was assumed to substitute the Swedish electricity mix in all ISO calculations. In the sensitivity analysis, grid electricity was assumed to be natural gas-based electricity. Assuming competing interests for forest residues for biofuel and bio-based heat , lignin solid fuel was assumed to replace wood-based pellets. In the sensitivity analysis, lignin pellets were assumed to substitute hard coal for heating.
Results and discussion
Minimum ethanol selling price
Results for MESP in EUR L−1 ethanol were as follows: off-site 0.581, A 0.622, A+ 0.595, B 0.586 and B+ 0.568. Figure 3 shows the MESP of ethanol with off-site enzyme production, plotted as a function of enzyme price, and MESP for each of the integrated cases. In regard to MESP, case B+ was the most favourable. Furthermore, this was the only case with integrated enzyme production in which the MESP was lower than that in the off-site case with purchased enzymes. The off-site case, case B and case B+, result in MESPs below the estimated average ethanol selling price of 0.59 EUR L−1, thus resulting in positive annual cash flows (see Additional file 1).
In the off-site case, we calculated an approximate enzyme cost of 0.078 EUR L−1 ethanol (39 MSEK year−1 for the production of 6760 L ethanol h−1 for 8000 h year−1). In a previous statement from Novozymes A/S, the predecessor product to Cellic CTec3 was said to cost just under 0.5 USD gallon−1 lignocellulosic ethanol , corresponding to approximately 0.1 EUR L−1 (using 2010 exchange rates, 1 EUR ≈ 1.3 USD). Our cost estimate could thus be reasonably close to that of the more recent Cellic CTec3 enzyme product. In the study by Liu et al. , an enzyme cost of 0.5 USD gallon−1 ethanol from corn stover was the basis for enzyme case 3, which was the intermediate scenario investigated. Thus, the estimated cost of enzymes in the off-site case presented here appears to compare reasonably well with the previous studies and available information, though the raw material and enzyme dosage underlying the calculated costs in  are unknown.
Factors other than enzyme cost affect the MESP and economics of the systems studied. An example is the selling prices of co-products, though in this case annual cash flows show that ethanol is the most important source of income (see Additional file 1). The cash flows are calculated on an ethanol selling price of 0.59 EUR L−1 but actual market prices for ethanol vary over time. In Sweden, the yearly average consumer price of E85, an ethanol blend fuel of 15% gasoline, varied by 5% above and below the average price in the years 2010–2015 .
Greenhouse gas emissions
The results for GWP of ethanol using the ISO and RED calculation methods are presented in Figs. 4 and 5, respectively. In the base case scenario, the off-site case resulted in significantly higher GWP than the integrated cases and case B+ showed the lowest GWP (Figs. 4, 5). The purchased enzymes contributed with 18 and 30 g CO2-eq. MJ−1 ethanol in the base case (RED and ISO methods, respectively). Since these results show that off-site enzyme production could be a major contributor to the GHG emissions of ethanol in the off-site case, alternative data and assumptions are tested in sensitivity analyses, where the GWP of off-site enzyme production was reduced by 13–88%. Implications to the comparison between off-site and integrated cases are illustrated in Figs. 4 and 5. It should also be noted that GWP results are generally lower using the RED method (Fig. 5) than the ISO method (Fig. 4), which is explained by the difference in LCA method choices.
With the GHG emissions value 16 kg CO2-eq. kg−1 enzyme protein from , which is based on Aspen modelling of an off-site scenario, the GWP of the off-site case was still higher than those in all other cases (Figs. 4, 5). Assuming 2.3 kg CO2-eq. kg−1 enzyme protein as in , the GWP of the off-site case was reduced significantly, and was roughly equal to the GWP of case A using both calculation methods. In , co-location of enzyme and ethanol production was assumed, using part of the hydrolysate from ethanol conversion from switchgrass to grow T. reesei for cellulase production. Thus, this scenario presents an on-site case, partly integrated with ethanol production.
Applying the enzyme dosage from  (12.4 g enzyme cocktail kg−1 DM) to the off-site case (which assumes a dosage of 30.4 g enzyme cocktail kg−1 DM) gave a 73% reduction of the base case enzyme GHG emissions (Figs. 4, 5). The total GWP of the off-site case was still higher than the GWP of the integrated cases, but the difference between them was reduced significantly. The dosage in  was based on a Novozymes A/S dosage data sheet for cellulose conversion in corn stover.
Assumptions of 50% increased enzyme activity and a Swedish electricity mix both reduced the GHG emissions from enzyme production by roughly 30%. If these improvements were assumed simultaneously, the GWP from purchased enzymes would be reduced by approximately half, leading to roughly a 30% reduction of the total GWP in the off-site case. Total GHG emissions were still higher in the off-site case than in cases with integrated enzyme and ethanol production (Figs. 4, 5).
Various input data available regarding the GHG emissions from off-site enzyme production [10, 11] indicate the significant uncertainties in the estimation of total emissions of ethanol. The dosage of purchased enzymes in lignocellulosic ethanol production was a significant uncertainty in assessing the total GHG emissions, as illustrated by adopting dosage data from . The base case scenario illustrated the current state of enzyme production, using GHG emission data based on actual plant performance, and enzyme activity of a purchased cellulase cocktail as reported in the literature. The lower GWP results obtained when using data from  can be explained by the future and partly integrated scenario used in which enzyme activity is higher and GHG emissions are lower. On the other hand, enzyme dosage as calculated in  did not make any assumptions on future improvements, but nevertheless resulted in a significant reduction of the total GWP of the off-site case compared to the base case scenario.
It is thus difficult to draw general conclusions regarding both the current state of off-site enzyme production, as well as its future improvement potential. Nevertheless, the cases and results presented in this study indicate that an integrated process design could provide lower GHG emissions for lignocellulosic ethanol production. For instance, the replacement of natural gas-based electricity with renewable alternatives did lower the GHG emissions of off-site enzyme production, but based on the estimation made, the integrated cases result in even lower GHG emissions for ethanol (Figs. 4, 5). In order to improve the comparison between emerging integrated production designs and existing off-site enzyme production systems, further studies are, however, needed to provide a more detailed analysis of off-site enzyme production, including potential improvements.
The results for GWP were also tested with alternative assumptions for substituted products and changes in soil organic carbon (SOC) levels due to the recovery of logging residues in spruce stands. Table 2 shows that the ISO GWP results are sensitive to assumptions regarding substituted products. Assuming substitution of natural gas-based electricity decreases total GWP by 0–18% for different cases, and when solid fuel was assumed to replace coal for heating all cases resulted in negative GWP values. All cases were affected (except case A for substituted electricity) and the results of the comparison between off-site and integrated cases did not change significantly.
Including potential effects on SOC levels according to  significantly increased GHG emissions in all cases. Cases with integrated enzyme production use more feedstock per MJ ethanol produced, and were thus affected to a greater extent than the off-site case. Changes in SOC levels differ between the northern and southern Sweden, with biogenic CO2 emissions in the north of the country approximately twice the magnitude of those in the south in the long term. Here we chose an average case to illustrate the potential magnitude of the results for Swedish spruce residues. Because the degradation of biomass in the forest is time-dependent, results are affected by the time horizon chosen, where shorter time spans increase the impact of SOC changes significantly.
Assuming a long-term scenario of two to three rotation periods (231 and 240 years in southern and northern Sweden, respectively ) for changes in SOC, GHG emissions increased by approximately 54–126% using the ISO method and by 50–104% using the RED method. The off-site case still resulted in higher GWP than the integrated cases. Assuming one rotation period (77 and 120 years in southern and northern Sweden ), ISO GWP results were above or at the same level as the RED fossil fuel reference of 83.8 g CO2-eq. MJ−1, still with the off-site case causing the highest emissions. With a time horizon of only 20 years, all GWP results increased drastically, with results of up to 710 and 510 g CO2-eq. MJ−1 ethanol for the ISO and RED methods, respectively. On this assumption, the off-site case had a lower GWP than case A but higher than case B, with both calculation methods.
Primary energy balance
Case B+ showed the lowest primary energy input per MJ of ethanol, and the off-site case showed the highest (Fig. 6). Feedstock energy was the main contributor to primary energy input for all cases.
Using the ISO method and the RED method (in parentheses), primary energy efficiency, expressed as primary energy output over input, was as follows: off-site 36% (49%), A 37% (50%), A+ 38% (51%), B 39% (52%) and B+ 39% (53%). The efficiency was slightly lower in the off-site case, with 3% units between the highest and lowest result using the ISO method, and 6% units using the RED method.
The sensitivity of primary energy balances was tested in relation to dosage of purchased enzymes and lignin solid fuel substitution (Table 3). As feedstock was the main contribution to primary energy input, the parameters tested had limited impact on the results (4–10% change from the base case scenario). However, with alternative assumptions regarding enzyme dosage, the primary energy balance of the off-site case was approximately equal to that of case B+. In general, the difference between an integrated and an off-site approach regarding primary energy efficiency did not appear significant enough to justify drawing any definite conclusions, considering the aggregation and uncertainty of the input data.
This study assessed the economic and environmental aspects of integrated enzyme production in lignocellulosic ethanol production. An LCA compared the modelled integrated cases to an off-site case regarding emissions of GHG and primary energy balance, and a techno-economic analysis compared the cost performance.
The results show that a new integrated process design for ethanol and enzyme production could lower GHG emissions from lignocellulosic ethanol, compared to existing ethanol production with purchased enzymes. Regarding primary energy efficiency, no significant difference was identified in this study. The LCA results are sensitive to assumptions regarding the production and utilization of purchased enzymes, e.g. dosage needed and energy sources utilized in production. Although the GHG emissions of off-site enzyme production could be lowered, for instance by replacing fossil energy sources, drawbacks are the refining and stabilization processes not needed in an integrated process design. It is possible that separated processes could provide other benefits that have not been investigated here, where focus was on the potential of an integrated process. Thus, updated and more detailed studies are required for off-site enzyme production systems.
Within LCA, assumptions regarding crediting co-products and system expansion, especially the inclusion of effects on soil organic carbon levels from logging residue recovery, were crucial to the end result for the GHG performance of ethanol. However, in most cases, such assumptions did not significantly affect the comparison of the integrated production approaches to the off-site case with off-site enzyme production.
The economic feasibility of integrating enzyme production in the lignocellulosic ethanol process depends on the price of the full-scale commercial preparation of cellulase enzyme. In this study, off-site production resulted in the lowest MESP with the exception of one integrated case (case B+). This implies that integrated enzyme production can potentially be an alternative strategy considering process economics, provided that higher enzyme productivity and yield can be achieved than those presented in the laboratory trials.
To strengthen the comparison between off-site and integrated production, more detailed and updated data for off-site enzyme production are needed, as also further upscaling and implementation of both off-site and integrated processes.
cellulase enzyme fermentation
fixed capital investment
filter paper unit
global warming potential
minimum ethanol selling price
renewable energy directive
soil organic carbon
simultaneous saccharification and fermentation
working capital investment
Searchinger T, Heimlich R, Houghton RA, Dong F, Elobeid A, Fabiosa J, et al. Use of US croplands for biofuels increases greenhouse gases through emissions from land-use change. Science. 2008;319:1238–40.
Fargione J, Hill J, Tilman D, Polasky S, Hawthorne P. Land clearing and the biofuel carbon debt. Science. 2008;319:1235–8.
Alkasrawi M, Rudolf A, Liden G, Zacchi G. Influence of strain and cultivation procedure on the performance of simultaneous saccharification and fermentation of steam pretreated spruce. Enzyme Microb Technol. 2006;38:279–86.
Galbe M, Zacchi G. A review of the production of ethanol from softwood. Appl Microbiol Biotechnol. 2002;59:618–28.
Rudolf A, Alkasrawi M, Zacchi G, Liden G. A comparison between batch and fed-batch simultaneous saccharification and fermentation of steam pretreated spruce. Enzyme Microb Technol. 2005;37:195–204.
Stenberg K, Bollok M, Reczey K, Galbe M, Zacchi G. Effect of substrate and cellulase concentration on simultaneous saccharification and fermentation of steam-pretreated softwood for ethanol production. Biotechnol Bioeng. 2000;68:204–10.
Karlsson H, Börjesson P, Hansson P-A, Ahlgren S. Ethanol production in biorefineries using lignocellulosic feedstock—GHG performance, energy balance and implications of life cycle calculation methodology. J Clean Prod. 2014;83:420–7.
Börjesson P, Ahlgren S, Barta Z, Björnsson L, Ekman A, Erlandsson P, et al. Sustainable performance of lignocellulose-based ethanol and biogas co-produced in innovative biorefinery systems. Report 87. Lund University; 2013. http://www.f3centre.se/sites/default/files/f3_lth_report_2013-87_co-produced_ethanol_and_biogas_130827.pdf. Accessed 24 June 2015.
Liptow C, Tillman A-M, Janssen M, Wallberg O, Taylor GA. Ethylene based on woody biomass—what are environmental key issues of a possible future Swedish production on industrial scale. Int J Life Cycle Assess. 2013;18:1071–81.
Hong Y, Nizami A-S, Bafrani MP, Saville BA, MacLean HL. Impact of cellulase production on environmental and financial metrics for lignocellulosic ethanol. Biofuels Bioprod Biorefin. 2013;7:303–13.
MacLean HL, Spatari S. The contribution of enzymes and process chemicals to the life cycle of ethanol. Environ Res Lett. 2009. doi:10.1088/1748-9326/4/1/014001.
Slade R, Bauen A, Shah N. The greenhouse gas emissions performance of cellulosic ethanol supply chains in Europe. Biotechnol Biofuels. 2009;2:15.
Liu G, Zhang J, Bao J. Cost evaluation of cellulase enzyme for industrial-scale cellulosic ethanol production based on rigorous Aspen Plus modeling. Bioprocess Biosyst Eng. 2016;39:133–40.
Aden A, Ruth M, Ibsen K, Jechura J, Neeves K, Sheehan J, et al. Lignocellulosic biomass to ethanol process design and economics utilizing co-current dilute acid prehydrolysis and enzymatic hydrolysis for corn stover. Report NREL/TP-510-32438. National Renewable Energy Laboratory; 2002. http://www.nrel.gov/docs/fy02osti/32438.pdf. Accessed 14 July 2016.
Bohlmann GM. Process economic considerations for production of ethanol from biomass feedstocks. Ind Biotechnol. 2006;2:14–20.
Galbe M, Sassner P, Wingren A, Zacchi G. Process engineering economics of bioethanol production. In: Olsson L, editor. Biofuels. 2007. p. 303-27.
Hamelinck CN, van Hooijdonk G, Faaij APC. Ethanol from lignocellulosic biomass: techno-economic performance in short-, middle- and long-term. Biomass Bioenergy. 2005;28:384–410.
Lynd LR, Elander RT, Wyman CE. Likely features and costs of mature biomass ethanol technology. Appl Biochem Biotechnol. 1996;57:741–61.
Sassner P, Galbe M, Zacchi G. Techno-economic evaluation of bioethanol production from three different lignocellulosic materials. Biomass Bioenergy. 2008;32:422–30.
Wingren A, Galbe M, Zacchi G. Techno-economic evaluation of producing ethanol from softwood: comparison of SSF and SHF and identification of bottlenecks. Biotechnol Prog. 2003;19:1109–17.
Wooley R, Ruth M, Sheehan J, Ibsen K, Majdeski H, Galvez A. Lignocellulosic biomass to ethanol process design and economics utilizing co-current dilute acid prehydrolysis and enzymatic hydrolysis. Current and futuristic scenarios. Report NREL/TP-580-26157. National Renewable Energy Laboratory; 1999. http://digital.library.unt.edu/ark:/67531/metadc624334/m2/1/high_res_d/12150.pdf. Accessed 14 July 2016.
So KS, Brown RC. Economic analysis of selected lignocellulose-to-ethanol conversion technologies. Appl Biochem Biotechnol. 1999;77–9:633–40.
Eggeman T, Elander RT. Process and economic analysis of pretreatment technologies. Bioresour Technol. 2005;96:2019–25.
Gregg D, Saddler JN. Bioconversion of lignocellulosic residue to ethanol: process flowsheet development. Biomass Bioenergy. 1995;9:287–302.
Gregg DJ, Boussaid A, Saddler JN. Techno-economic evaluations of a generic wood-to-ethanol process: effect of increased cellulose yields and enzyme recycle. Bioresour Technol. 1998;63:7–12.
Sassner P, Zacchi G. Integration options for high energy efficiency and improved economics in a wood-to-ethanol process. Biotechnol Biofuels. 2008;1:1–11.
Wingren A, Galbe M, Roslander C, Rudolf A, Zacchi G. Effect of reduction in yeast and enzyme concentrations in a simultaneous-saccharification-and-fermentation-based bioethanol process. Appl Biochem Biotechnol. 2005;122:485–99.
Wingren A, Galbe M, Zacchi G. Energy considerations for a SSF-based softwood ethanol plant. Bioresour Technol. 2008;99:2121–31.
Johnson E. Integrated enzyme production lowers the cost of cellulosic ethanol. Biofuels Bioprod Biorefin. 2016;10:164–74.
Juhasz T, Szengyel Z, Reczey K, Siika-Aho M, Viikari L. Characterization of cellulases and hemicellulases produced by Trichoderma reesei on various carbon sources. Process Biochem. 2005;40:3519–25.
Szengyel Z, Zacchi G, Varga A, Reczey K. Cellulase production of Trichoderma reesei Rut C 30 using steam-pretreated spruce: hydrolytic potential of cellulases on different substrates. Appl Biochem Biotechnol. 2000;84–86:679–91.
Barta Z, Kovacs K, Reczey K, Zacchi G. Process design and economics of on-site cellulase production on various carbon sources in a softwood-based ethanol plant. Enzyme Res. 2010. doi:10.4061/2010/734182.
Kovacs K, Szakacs G, Zacchi G. Comparative enzymatic hydrolysis of pretreated spruce by supernatants, whole fermentation broths and washed mycelia of Trichoderma reesei and Trichoderma atroviride. Bioresour Technol. 2009;100:1350–7.
Kovacs K, Szakacs G, Zacchi G. Enzymatic hydrolysis and simultaneous saccharification and fermentation of steam-pretreated spruce using crude Trichoderma reesei and Trichoderma atroviride enzymes. Process Biochem. 2009;44:1323–9.
Schell DJ, Hinman ND, Wyman CE, Werdene PJ. Whole broth cellulase production for use in simultaneous saccharification and fermentation. Appl Biochem Biotechnol. 1990;24–5:287–97.
Xia LM, Shen XL. High-yield cellulase production by Trichoderma reesei ZU-02 on corn cob residue. Bioresour Technol. 2004;91:259–62.
Janssen M, Xiros C, Tillman AM. Life cycle impacts of ethanol production from spruce wood chips under high-gravity conditions. Biotechnol Biofuels. 2016;9:53.
Lever M. Modelling the energy performance of a farm-scale cellulose to ethanol process with on-site cellulase production and anaerobic digestion. Renew Energy. 2015;74:893–902.
Singhania RR, Saini R, Adsul M, Saini JK, Mathur A, Tuli D. An integrative process for bio-ethanol production employing SSF produced cellulase without extraction. Biochem Eng J. 2015;102:45–8.
Barta Z, Sassner P, Zacchi G, Reczey K. Techno-economic aspects of on-site cellulase production. Hung J Ind Chem. 2008;36:5–9.
Frederick WJ Jr, Lien SJ, Courchene CE, DeMartini NA, Ragauskas AJ, Iisa K. Production of ethanol from carbohydrates from loblolly pine: a technical and economic assessment. Bioresour Technol. 2008;99:5051–7.
Merino ST, Cherry J. Progress and challenges in enzyme development for biomass utilization. In: Olsson L, editors. Biofuels. 2007. p. 95–120.
Nguyen QA, Saddler JN. An integrated model for the technical and economic evaluation of an enzymatic biomass conversion process. Bioresour Technol. 1991;35:275–82.
Wooley R, Ruth M, Glassner D, Sheehan J. Process design and costing of bioethanol technology: a tool for determining the status and direction of research and development. Biotechnol Prog. 1999;15:794–803.
Nielsen PH, Oxenboll KM, Wenzel H. Cradle-to-gate environmental assessment of enzyme products produced industrially in Denmark by Novozymes A/S. Int J Life Cycle Assess. 2007;12:432–8.
Li J, Li S, Han B, Yu M, Li G, Jiang Y. A novel cost-effective technology to convert sucrose and homocelluloses in sweet sorghum stalks into ethanol. Biotechnol Biofuels. 2013;6:174.
Zhang J, Laguna A, Clemons C, Wolcott MP, Gleisner R, Zhu JY, et al. Effect of hot-pressing temperature on the subsequent enzymatic saccharification and fermentation performance of SPORL pretreated forest biomass. Bioenergy Res. 2015;8:464–70.
Benjamin Y, Garcia-Aparicio MP, Goergens JF. Impact of cultivar selection and process optimization on ethanol yield from different varieties of sugarcane. Biotechnol Biofuels. 2014;7:60.
Peters MS, Timmerhaus KD. Plant design and economics for chemical engineers. 3rd ed. New York: McGraw-Hill; 1980.
International Organization of Standardization. Environmental management—life cycle assessment—principles and framework (ISO 14040:2006). 2006.
International Organization of Standardization. Environmental management—life cycle assessment—requirements and guidelines (ISO 14044:2006). 2006.
European Commission. Directive 2009/28/EC of the European Parliament and of the Council of 23 April 2009 on the Promotion of the Use of Energy from Renewable Sources and Amending and Subsequently Repealing Directives 2001/77/EC and 2003/30/EC. 2009.
Luo L, van der Voet E, Huppes G, de Haes HAU. Allocation issues in LCA methodology: a case study of corn stover-based fuel ethanol. Int J Life Cycle Assess. 2009;14:529–39.
Pourbafrani M, McKechnie J, Shen T, Saville BA, MacLean HL. Impacts of pre-treatment technologies and co-products on greenhouse gas emissions and energy use of lignocellulosic ethanol production. J Clean Prod. 2014;78:104–11.
Sunde K, Brekke A, Solberg B. Environmental impacts and costs of woody biomass-to-liquid (BTL) production and use—a review. Forest Policy Econ. 2011;13:591–602.
Wiloso EI, Heijungs R, de Snoo GR. LCA of second generation bioethanol: a review and some issues to be resolved for good LCA practice. Renew Sustain Energy Rev. 2012;16:5295–308.
Myhre G, Shindell D, Bréon F-M, Collins W, Fuglestvedt J, Huang J, et al. Anthropogenic and natural radiative forcing. In: Stocker TF, Qin D, Plattner G-K, Tignor M, Allen SK, Boschung J, Nauels A, Xia Y, Bex V, Midgley PM, editors. Climate change 2013: the physical science basis. Contribution of working group I to the fifth assessment report of the intergovernmental panel on climate change. Cambridge: Cambridge University Press; 2013. p. 659–740.
Lindholm E-L, Stendahl J, Berg S, Hansson P-A. Greenhouse gas balance of harvesting stumps and logging residues for energy in Sweden. Scand J For Res. 2011;26:586–94.
Hellsten S, Akselsson C, Olsson B, Belyazid S, Zetterberg T. Effekter av skogsbränsleuttag på markförsurning, näringsbalanser och tillväxt—Uppskalning baserat på experimentella data och modellberäkningar som grund för kartläggning av behov av askåterföring. Report B1798. IVL Swedish Environmental Research Institute; 2008. http://www3.ivl.se/rapporter/pdf/B1798.pdf. Accessed 19 Feb 2015.
Weidema BP, Bauer C, Hischier R, Mutel C, Nemecek T, Reinhard J, et al. Overview and methodology. Data quality guideline for the ecoinvent database version 3. Report 1 (v3). The ecoinvent Centre; 2013.
BIOGRACE. Harmonised calculations of biofuel greenhouse gas emissions in Europe. 2012. http://www.biograce.net. Accessed 15 Oct 2014.
BYK-Chemie GmbH: Environmental Product Declaration for BYK®-023. Issue 10/2011. 2011. www.byk.com/en/additives/additives-by-name/byk-023.php. Accessed 15 Oct 2014.
Evonik Industries AG: Life Cycle Assessment Data of TEGO® Foamex 1488. 2014. http://www.tego.de/sites/dc/Downloadcenter/Evonik/Product/Tego/de/Sonstiges/lca-foamex-1488.pdf. Accessed 15 Oct 2014.
Adom F, Dunn JB. Material and energy flows in the production of macro and micronutrients, buffers, and chemicals used in biochemical processes for the production of fuels and chemicals from biomass. Lemont: Argonne National Laboratory; 2015. https://greet.es.anl.gov/publication-fuel-chemicals-biomass. Accessed 15 July 2016.
Flysjö A, Cederberg C, Strid I. LCA-databas för konventionella fodermedel—miljöpåverkan i samband med produktion. Version 1.1. Report 772. The Swedish Institute for Food and Biotechnology SIK; 2008.
GREET. Argonne National Laboratory. 2015. https://greet.es.anl.gov/net. Accessed 5 July 2016.
Gode J, Martinsson F, Hagberg L, Öman A, Höglund J, Palm D. Miljöfaktaboken 2011. Uppskattade emissionsfaktorer för bränslen, el, värme och transporter. Report 1183. Värmeforsk; 2011.
Uppenberg S, Almemark M, Brandel M, Lindfors LG, Marcus HO, Stripple H, et al. Miljöfaktabok för bränslen. Del 1: Huvudrapport. Report B1334A-2. IVL Swedish Environmental Research Institute; 2001.
Lindholm EL, Berg S, Hansson PA. Energy efficiency and the environmental impact of harvesting stumps and logging residues. Eur J For Res. 2010;129:1223–35.
Tromborg E, Bolkesjo TF, Solberg B. Second-generation biofuels: impacts on bioheat production and forest products markets. Int J Energy Sect Manag. 2013;7:383–402.
Novozymes A/S: New enzymes turn waste into fuel. 2010. http://www.novozymes.com/en/news/news-archive/2010/02/45713. Accessed 5 July 2016.
Svenska Petroleum och Biodrivmedel Institutet (SPBI): Priser & skatter. http://spbi.se/statistik/priser/. Accessed 17 Aug 2016.
JO carried out the LCA, analysed results and wrote most of this paper under the guidance and supervision of PB. ZB performed the Aspen modelling and analysed the techno-economic results. OW was project leader and contributed to the study design and the analysis of the results. All authors read and approved the final manuscript.
We gratefully acknowledge the provision by Novozymes A/S of LCA data on the cellulase cocktail, and the funding from the Swedish Knowledge Centre for Renewable Transportation Fuels, f3, and the Swedish Energy Agency, as well as the Hungarian National, Research, Development and Innovation Office (NKFIH) and the New Hungary Development Plan. We also thank the two anonymous reviewers for constructive comments which improved this work.
The authors declare that they have no competing interests.
Availability of data and materials
The datasets supporting the conclusions of this article are included within the article (and its additional files).
The authors gratefully acknowledge funding from the Swedish Knowledge Centre for Renewable Transportation Fuels, f3, and the Swedish Energy Agency, as well as the Projects OTKA PD-108389 and PD-121024 of the Hungarian National, Research, Development and Innovation Office (NKFIH) and the New Hungary Development Plan (Project ID: TÁMOP-4.2.1/B-09/1/KMR-2010-0002).
Mass balances, annual costs and revenues, and techno-economic details for the ethanol production systems studied. The file contains the mass balances and the economic data that were used to produce the results of this study. The file also contains annual cash balances for the ethanol production systems studied, providing further information on the implications of the results in the techno-economic analysis, and a process flow diagram and additional details for one of the studied systems.
Aspen Plus data for the results of mass and energy balances. The overall process is shown in the first Excel sheet, and the hierarchies (PRETREAT, YC-E-SSF, DISTILL, EVP-SEP, DRYING, COMBUST) are in the subsequent sheets.
Aspen Process Economic Analyzer data for the equipment cost and the total direct cost (in SEK). The quoted items (e.g. steam pretreatment unit) are not included in the list, as we do not have permission to present the quoted prices in details.
About this article
Cite this article
Olofsson, J., Barta, Z., Börjesson, P. et al. Integrating enzyme fermentation in lignocellulosic ethanol production: life-cycle assessment and techno-economic analysis. Biotechnol Biofuels 10, 51 (2017). https://doi.org/10.1186/s13068-017-0733-0
- Second generation (2G)
- Process economics
- Greenhouse gases