Food Technology and Biotechnology

INTRODUCTION

Lactic acid is a well-established bio-based chemical, which can be produced using renewable resources by various wild-type strains. Traditionally, lactic acid is synthesized via the chemical hydrolysis of lactonitrile, a process that leads to the production of a racemic mixture of d(-)- and l(+)-lactic acid. In contrast to the petrochemical route, biotechnological production of lactic acid has various advantages such as high enantiomeric purity, utilization of inexpensive substrates and environmentally benign processes (1). The industrial production of lactic acid is mainly based on its fermentative route since it is estimated that about 90% is produced microbiologically (1).

Global lactic acid production is approx. 270 000 t per year, as it presents a broad range of applications in food industry, cosmetics and also in pharmaceuticals (2). Its market demand presents an annual growth rate of 10%, which is mainly attributed to the utilization of lactic acid for the synthesis of polylactic acid (PLA) (3). PLA is a biodegradable polymer used in the production of food packaging materials such as containers, wraps, single use trays, but also mulch films and garbage bags (3). In Europe, the demand for PLA accounts for 25 000 t per year, and it is expected to reach 650 000 t by 2025 (3).

Enantiomeric ratio and polymerization process are the two key parameters affecting the properties of PLA (2, 4, 5). The polymer produced from a racemic mixture of l- and d-lactic acid (PDLLA) is both thermally and mechanically unstable, also with a short shelf life. PLA produced from pure l- (PLLA) or d-lactic acid (PDLA) possesses better properties (higher melting point), but still its application is hindered due to its thermal instability. Recent research on PLA properties has shown that both thermal and mechanical stability are enhanced when an isotactic stereocomplex of PLLA and PDLA is formed (4). The chemical stabilization of the polymer chains is achieved via hydrogen and van der Waals bonding (2, 6). With this technique, the melting temperature of the polymer is 230 instead of 60 °C of the PLLA (4).

The fermentative production of l-lactic acid of high optical purity has been extensively studied using different strains and substrates such as municipal solid wastes, lignocellulosic hydrolysates and food wastes (7, 8). Its industrial production has also been reported since 1881, and many companies or pilot plants are operating on l-lactic acid production using renewable resources such as Corbion (Amsterdam, The Netherlands), Galactic (Celles, Belgium), and NatureWorks LLC (Minnetonka, MN, USA) (1). Among these companies, only Corbion had launched PDLA in its portfolio.

This review aims to provide an overview of the current research on d-lactic acid production from renewable resources. Additionally, three experimental case studies dealing with the valorization of acid whey, coffee mucilage and rice husks will be presented and discussed as alternative feedstocks for d-lactic acid production.

d-LACTIC ACID PRODUCERS

Highly pure l-lactic acid can be produced by a broad range of microorganisms, such as bacteria, fungi, algae and cyanobacteria. On the other hand, most of d-lactic acid-producing microorganisms produce either the racemic mixture or other organic acids, such as acetic acid or succinic acid (9). For efficient fermentative production of d-lactic acid, it is crucial to identify or even engineer the adequate strain. Moreover, since the cost of the substrate plays an important role for the economic feasibility of the process, the utilized strain needs to be able to consume pentoses, which are mainly present in lignocellulosics, the emerging renewable resource.

The most well-known wild-type d-lactic acid-producing strains include Lactobacillus delbrueckii and Sporolactobacillus sp. (9, 10). These microorganisms are characterized as Gram--positive, facultative anaerobic, mesophilic and catalase negative. The optimum temperatures for the growth of Lactobacillus delbrueckii range between 45 and 47 °C, whereas the strains belonging to Sporolactobacillus sp. prefer lower temperatures, in the range of 20–45 °C (9). Lactic acid production occurs either through homofermentative or heterofermentative pathway. Homofermentative strains, such as L. delbrueckii, produce only lactic acid as end-product of their metabolism, via the Embden-Meyerhof-Parnas pathway in the presence of glucose as carbon source (11). d-lactic acid production is catalyzed by the enzyme d-lactate dehydrogenase (d-LDH), and theoretically 1 g of lactic acid can be produced from 1 g of glucose (12). However, homofermentative strains cannot assimilate pentoses, such as xylose and arabinose, which are the main sugars present in lignocellulosic hydrolysates. Heterofermentative strains, such as L. brevis and L. pentosus, are able to consume pentoses through the phosphoketolase (PK) pathway, producing lactic acid as the main end product and acetic acid, ethanol and/or formic acid as byproducts (13). Therefore, the theoretical d-lactic acid yield in this case is 0.5 g/g from glucose (hexoses) and 0.6 g/g from xylose (pentoses) (9).

High d-lactic acid concentrations of more than 200 g/L have already been demonstrated from commercial glucose, by employing Sporolactobacillus inulinus. Wang et al. (14) reported the production of 207 g/L of d-lactic acid of high optical purity (99.3%) from glucose with peanut meal as nitrogen source in a fed-batch fermentation. In the recent work of Klotz et al. (2), product concentrations up to 222 g/L were achieved with S. inulinus DSM 20348 in a fed-batch fermentation, in which amino acids and vitamins were also added.

Recombinant strains of Escherichia coli, Bacillus coagulans, Corynebacterium glutamicum and Bacillus licheniformis have also been evaluated for d-lactic acid production. In the study of Awasthi et al. (10), a thermotolerant B. subtilis derivative was metabolically engineered to produce d-lactic acid via insertion of five heterologous IdhA (d-LDH) genes. The authors cloned two genes responsible for d-lactic acid from an engineered B. coagulans strain; an altered glycerol (polyol) dehydrogenase (gldA101) and IdhA. The results indicated that neither the insertion of the gene encoding gldA101 nor IdhA had a positive effect on d-lactic acid production by the engineered strains. Three IdhA genes from three different L. delbrueckii strains were also tested, since this microorganism can grow in a wide range of temperatures. The d-LDH from L. delbrueckii ssp. bulgaricus was more stable at 50 °C than the ones from L. delbrueckii ssp. lactis, so these genes were chosen for engineering B. subtilis. The engineered strain produced approx. 1 M d-lactic acid in batch fermentation mode, with a yield of 0.98 g/g on consumed glucose.

An alkaliphilic Bacillus sp. was also engineered by deletion of the Idh gene and insertion of the IdhA gene from L. delbrueckii. At the same time, for enhanced d-lactic acid, the gene encoding exopolysaccharide biosynthesis (epsD) was disrupted. The strain produced almost 144 g/L of optically pure d--lactic acid (99.85%), with a yield of 0.96 g/g and productivity of 1.67 g/(L·h), in a fed-batch fermentation using peanut meal as nitrogen source and commercial glucose as carbon source (15).

Even though there are some studies reporting l-lactic acid fermentation from renewable resources on a pilot or technical scale, the information for d-lactic acid is quite limited. The most representative work so far is the publication of Liu et al. (16) that demonstrated d-lactic acid production from a genetically engineered E. coli strain on a pilot scale using a working volume of 3 t. Glucose was the sole carbon source together with various mineral salts, and Ca(OH)₂ was used as neutralizing agent. Operating in batch mode, the authors obtained a final d-lactic acid value of 126 kg/t, with a yield of 0.97 g/g and productivity of 6 kg/(t·h). The optical purity of the derived lactic acid was 99.5%.

d-LACTIC ACID PRODUCTION FROM RENEWABLE RESOURCES

The efficient production of d-lactic acid from commercial glucose has already been demonstrated in the previous section. However, the main challenge nowadays lies in developing efficient bioprocesses based on renewable resources. Table 1 (13, 17-34) lists recent publications dealing with the utilization of alternative substrates for d-lactic acid production using wild-type or engineered strains. Lignocellulosic biomass constitutes one of the most promising substrates, since it is abundant, inexpensive, and rich in structural polysaccharides (cellulose, hemicellulose) that after pretreatment and hydrolysis can be converted to value-added products and chemicals (7, 35). d-lactic acid production from lignocellulosic hydrolysates has not been extensively studied. Hama et al. (18) employed a metabolically engineered L. plantarum for simultaneous saccharification and fermentation (SSF) of hardwood pulp. Hardwood pulp is a byproduct of the pulp and paper industry, generated after biomass fractionation. The engineered strain L. plantarum 8826 ΔldhL1::PxylAB-Δxpk1::tkt-Δxpk2::PxylAB was able to utilize both glucose and xylose, resulting in 102.3 g/L d-lactic acid with high optical purity (99.2%), a yield on total sugars of 0.879 g/g, and a productivity of 2.29 g/(L·h).

Corncob residues and cottonseed meal were evaluated by Bai et al. (22) for d-lactic acid production using the strain S. inulinus YBS1-5. The hemicellulosic part of corncobs was utilized for the production of xylitol and furfural, leaving the cellulosic stream as a waste residue. The pretreatment required for hemicellulose exploitation renders cellulose more susceptible to enzymatic hydrolysis. Lactic acid is produced with a growth-associated mechanism, meaning that the selection of an adequate nitrogen source is also of major importance in order to achieve efficient cell growth. To this end, the authors studied four alternative nitrogen sources: cottonseed meal, soybean meal, peanut meal and corn wine dregs. Their screening revealed that among the different agro-industrial residues, cottonseed meal gave the most promising results, since it is found to be rich in proteins and vitamins. In order to facilitate the utilization of the proteins in cottonseed meal by the strain, enzymatic hydrolysis was carried out with neutral proteases. When the hydrolysates from two different streams were combined in a fed-batch fermentation, the strain produced 107 g/L lactic acid, with a yield and productivity of 0.85 g/g and 1.2 g/(L·h), respectively. The resulting d-lactic acid was of high enantiomeric purity (99.2%); however, xylose accumulation was observed.

Besides lignocellulosics, other waste or byproduct streams have been suggested as alternative carbon and/or nitrogen sources for d-lactic acid production. Reddy Tadi et al. (20) achieved high d-lactic acid concentrations (189 g/L) by combining sugars derived from Borassus flabellifer with whey protein hydrolysate and employing S. inulinus NBRC 13595. Zhao et al. (29) achieved a final concentration of 145.8 g/L from corn flour hydrolysate using S. inulinus Y2-8. When S. inulinus cells were immobilized in a fibrous bed reactor, final d-lactic acid concentration was enhanced by 37.67%.

Production of d-lactic acid from a L. bulgaricus strain using renewable inulin was also reported by Xu et al. (30). Inulin is a naturally occurring polysaccharide, serving as energy storage for many plants such as chicory, Jerulasem artichoke and dahlia among others, mainly found in their roots or tubers (36). It is a fructose polymer, having glucosyl moieties at the end-chains. Enzymatic or acidic hydrolysis of inulin leads to the production of feedstock rich in fructose and glucose. The strain performed better when operating under SSF, since fructose inhibition was prevented. Under these conditions the strain was able to produce 123.6 g/L of optically pure d-lactic acid (>99.9%).

Recently, Liu et al. (32) suggested cheese whey powder as a complete feedstock for d-lactic acid production employing L. bulgaricus. Neutral protease was selected for the hydrolysis of the protein content in cheese whey powder, in order to facilitate their assimilation by the microorganism. Their results indicated that the addition of a small amount of yeast extract significantly enhanced the final d-lactic acid concentration. Finally, 113.18 g/L of d-lactic acid was produced in a fed-batch fermentation, with a productivity of 2.36 g/(L·h).

Beitel et al. (31) reported a d-lactic acid concentration of 112.93 g/L using the strain S. nakayamae and commercial sucrose and peanut flour as carbon and nitrogen sources, respectively. The authors initially tested the effect of different inexpensive carbon sources (molasses, commercial sucrose, sugarcane juice and whey) on lactic acid production, yield and productivity. The strain grew poorly on molasses and whey, but it was able to produce high amounts of lactic acid from sucrose and sugarcane juice. Using commercial sucrose as carbon source, the authors subsequently evaluated the effect of different nitrogen sources. Among corn steep liquor, Proflo, peanut flour, soybean flour and urea, Proflo and peanut flour led to the highest lactic acid production (more than 50 g/L) and productivities of more than 1 g/(L·h). Liu et al. (32) also achieved high d-lactic acid concentration of 113.18 g/L by employing cheese whey as carbon and nitrogen source combined with 9 g/L of yeast extract.

B. coagulans is a very attractive l-lactic acid producer since it is able to ferment pentoses, making it an excellent candidate for fermentation of lignocellulosic hydrolysates (14). Moreover, its thermotolerant nature (50–55 °C) minimizes the need for sterilized conditions. This strain has already been reported for efficient l-lactic acid fermentation from renewable resources like coffee pulp (37), coffee mucilage (8) and corn stover (38). Deletion of both Idh and alsS (acetolactate synthase), with subsequent growth-based selection, led to the development of the mutant strain QZ19, which could accumulate 90 g/L of optically pure d-lactic acid (14). The strain was also tested on sorghum juice, resulting in almost 125 g/L d-lactic acid, with a productivity of 5 g/(L·h). An engineered L. plantarum strain was also evaluated for fermentation of corn stover and soybean meal extract to d-lactic acid. Genes encoding xylose isomerase and xylulokinase were inserted, giving the recombinant strain L. plantarum NCIMB 8826 DldhL1-pLEM-xylAB, which was able to ferment the renewable resources (containing both glucose and xylose), resulting in 61.4 g/L lactic acid, with a yield of 0.77 g/g in a fed-batch fermentation (13).

CO-CULTIVATION STRATEGIES

The efficiency of upstream process strongly depends on the fermentability of the substrate. Unconsumed sugars lead to low product yields and at the same time impede the purification of lactic acid. Mixed cultures or co-cultivation (cofermentation) strategies could be employed aiming to increase the fermentability of the lignocellulose-derived substrates. This strategy is based on the utilization of a homofermentative and a heterofermentative strain either simultaneously or sequentially. The homofermentative strain converts glucose into highly pure d-lactic acid, and the heterofermentative one consumes the pentoses. This approach leads to better substrate utilization and a controlled byproduct formation from the heterofermentative strain. A mixed culture of L. rhamnosus and L. brevis was tested for the fermentation of corn stover hydrolysate, increasing the conversion of substrate to lactic acid for almost 30%, in comparison to pure cultures (26). Zhang and Vadlani (25) accomplished an enhanced fermentability of poplar and corn stover hydrolysates by sequential cofermentation of L. brevis and L. plantarum. L. brevis was added after 20 h of fermentation, when poplar hydrolysate was employed, leading to a 13% increased yield, but with only 50% optical purity. When corn stover was used as fermentation substrate, a simultaneous saccharification and fermentation strategy was followed. The authors utilized Cellic® CTec2 (Novozymes Inc., Franklinton, NC, USA) for sugar monomer release from the substrate. When all glucose was depleted by L. plantarum, L. brevis was added for xylose consumption. Final lactic acid concentration was 31.2 g/L, but also 6.3 g/L of acetic acid was produced, and the optical purity was only 43.2%.

ACID TOLERANCE

The optimum pH for most lactic acid microorganisms ranges between 5.0 and 6.0, values above the pK_a of the acid (pK_a=3.8). At pH values higher than the pK_a, the acid is mainly found at its dissociated form, greatly incommoding its separation from the fermentation medium. For its efficient separation and purification, lactic acid needs to be in its free acid form, meaning that further addition of chemicals and purification steps is required (section DOWNSTREAM PROCESSING). The development of robust strains towards acidic pH would decrease the downstream costs and minimize waste generation. Genetic engineering of the strains has been proposed in order to achieve acid tolerance, since free lactic acid is highly inhibitory towards the fermenting microorganisms (1, 12, 39). The mechanism of inhibition is mainly described as increased proton transfer through the plasma membrane, causing a disturbance of intracellular pH (40). Decrease in intracellular pH, which is supposed to be neutral, has a linearly decreasing effect on cell propagation (40).

Zheng et al. (41) applied genome shuffling in S. inulinus ATCC 15538, aiming to enhance the strain’s tolerance to d-lactic acid, and at the same time to increase the productivity. After three rounds of genome shuffling, the mutant strain produced 119% more d-lactic acid than the wild-type in a fed-batch fermentation with glucose as carbon source, operating at pH=5. At the same time, the viability of the mutant strains at acidic pH values was enhanced, since they were able to grow at pH=4, when their optimum was pH=6.5.

Yeast strains have also been used for d-lactic acid production, due to their ability to grow at lower pH values than bacteria. Baek et al. (42) combined metabolic engineering and adaptive evolution of the strain Saccharomyces cerevisiae in order to induce d-lactic acid production and tolerance of glucose. A fed-batch fermentation resulted in 112 g/L of d-lactic acid in shake flasks with yield and productivity of 0.80 g/g and 2.2 g/(L·h), respectively. In a recent study of Park et al. (43), a newly isolated Pichia kudriavzevii strain was engineered to enhance lactic acid production and at the same time it was adapted to tolerate high acid concentrations. Another interesting feature of the strain was the fact that it was able to grow at low pH conditions. Operating in fed-batch fermentation mode with glucose as carbon source, the strain was able to produce 154 g/L of d-lactic acid at pH=4.7, while it was also possible to accumulate lactic acid up to 135 g/L at pH=3.6. The yeast strain Kluyveromyces marxianus was metabolically engineered by redirection of its metabolic pathway from ethanol to lactic acid (44). The recombinant strain could ferment Jerusalem artichoke tuber powder (inulin-rich) at pH=6, resulting in the production of 122 g/L lactic acid with an optical purity of more than 99%.

DOWNSTREAM PROCESSING

An efficient upstream process must be coupled with a cost-efficient and environmentally benign downstream separation method. The steps required for the separation and purification of lactic acid from the fermentation broth are crucial for the final quality of the product (9). The cost of the downstream process can account for 50% of the costs (9).

In general, the same downstream process that needs to be followed for l-lactic acid must also be utilized for d-lactic acid. Currently, the industrial process for separation of lactic acid from the fermentation broth involves its precipitation with calcium hydroxide or calcium carbonate. Before precipitation, biomass is separated via filtration. Lactic acid is then separated from the fermentation broth as a precipitate, and it is recovered with excess of sulphuric acid. The main drawback of this process is the generation of high amounts of gypsum that are considered a waste stream (45). Research has been focusing on finding more environmentally friendly alternatives; however, they have been tested only on laboratory or pilot scales.

Alternative separation technologies involve reactive extraction, membrane separation or in situ recovery via solvent extraction. Chromatography using cation- or/and anion-exchange resins has been reported as efficient purification method, mainly due to its selectivity, low waste generation and operational effectiveness (35). Another industrially attractive process is reactive distillation, in which lactic acid is esterified to an alcohol and then the ester is hydrolysed to give free lactic acid (46, 47).

Beitel et al. (31) attempted to separate and purify d-lactic acid from the fermentation broth. The medium contained 88.27 g/L of d-lactic acid and 13.5 g/L of residual sugars. Cell biomass was removed via centrifugation, and then the supernatant was filtered through activated carbon and Celite twice. The filtrate was subsequently treated with the cation exchange resin Amberlite IRA 120. The recovery yield of lactic acid from the fermentation broth was 79%, while 98% of the remaining sugars were removed.

TECHNO-ECONOMIC ASSESSMENT OF d-LACTIC ACID PRODUCTION

The success of the biotechnological production of d-lactic acid from renewable resources is strongly affected by the sustainability issues as well as the cost-competiveness of the individual process parameters and operations. Environmental and socio-economic aspects should be also taken into account (48). The most recent studies on techno-economic analysis of l-lactic acid production from various renewable resources are summarized in the review article of Alves de Oliveira et al. (1). The use of lignocellulosic biomass requires pretreatment before fermentation. The type of pretreatment contributes significantly to the overall cost of the process as well as the environmental impact, especially when chemicals are utilized. The nitrogen source is another major cost contributor. Then, downstream process steps also require careful selection, since high purity is required with minimum use of chemicals and waste generation.

The complexity of such a process is described in the work of Gezae Daful and Görgens (49), in which six different scenarios for the biotechnological production of l-lactic acid from sugarcane bagasse and leaves were proposed and discussed in terms of cost efficiency and environmental impact. Biomass pretreatment was based on steam explosion, leading to the formation of a hemicellulose-rich liquid fraction and a cellulignin one. The authors decided to investigate the production of lactic acid either from C5 or C6 sugars and couple its production with other fuels and chemicals. The use of Ca(OH)₂ or Mg(OH)₂ (coupled with recycling of Mg(OH)₂) or an acid-tolerant thermophilic Bacillus coagulans were other process parameters under investigation. Reactive distillation was the selected downstream separation process. The scenarios in which the cellulose fraction was selected as a carbon source were more profitable than hemicellulose-based ones. The selected strain, a genetically engineered E. coli WL204, was able to produce l-lactic acid of high purity from both glucose and xylose. This process resulted in 7–10% increase in total capital investment, 58–86% increase in operating cost and 12–18% revenue increase in comparison to the other studied scenarios. Higher environmental impact was observed when Ca(OH)₂ and H₂SO₄ were utilized due to the formation of gypsum. According to that study, the production of 1 t of lactic acid is accompanied by the generation of 1 t of gypsum as solid waste. The use and recycling of Mg(OH)₂ was more favourable both in terms of economic feasibility and environmental impact.

Sikder et al. (50) evaluated the economic feasibility of a membrane-integrated bioreactor system, in which lactic acid was produced from sugarcane juice. The individual processing steps involved sterilization, fermentation, microfiltration, nanofiltration and vacuum evaporation. Raw material and yeast extract were the two largest cost contributors, accounting for about 6 and 87% of the total operating cost, respectively. Approximately 36% of the total fixed capital cost was attributed to the fermentation step, whereas the membrane units were responsible for only 2%. Total product cost of this process was calculated at 3.15 US$/kg for 80% (m/m) concentrated lactic acid with 95% purity. The authors concluded that product cost could be further reduced if alternative and cheaper nitrogen sources were applied.

Techno-economic analyses of d-lactic acid from renewable resources are scarce in the literature. De la Torre at al. (34) calculated the cost contribution of the nitrogen source. The authors carried out fermentations to test yeast extract, malt extract and corn steep liquor. An amount of 2.64 g/L of nitrogen was found regardless of the source, which resulted in d-lactic acid yield of about 80%. However, the cost varies significantly among the different sources, with malt extract being the most expensive one. More specifically, the authors reported that when malt extract was selected as nitrogen source, the cost was up to 3482 US$/t of d-lactic acid, when its industrial price was 1300 US$/t. When using yeast extract, the cost was calculated up to 500 US$/t of d-lactic acid, while for corn steep liquor the cost was only 90.78 US$/t. The researchers concluded that even when corn steep liquor needs to be added at higher amount than malt and yeast extracts, its cost is still significantly lower than of the other two nitrogen sources.

Since nutritional requirements can be different for the d-lactic acid-producing strains, more studies of the techno-economic assessment that are more product-specific need to be carried out. Techniques like co-cultivation, which are not attractive in the case of l-lactic acid, are quite promising for d-lactic acid and this scenario should also be investigated in terms of economic viability. If wild-type strains are used, some byproducts like acetic acid and ethanol might also be co-produced, and the efficiency of the downstream separation steps must be studied as well, and subsequently these steps will also affect both the economics of the process and the environmental impact.

CASE STUDIES

Acid whey

Whey is the main byproduct derived from the dairy industry, and it is divided into two categories: sweet and acid whey. Sweet whey is generated from the production of cheese, whereas acid whey is the byproduct stream of acid-coagulated dairies like yoghurt (51). Sweet whey is processed mainly via spray drying to whey powder or whey protein concentrate and sold for various food applications (51). Acid whey is rich in lactic acid, making the powder too hygroscopic, resulting in agglomeration, which is quite problematic for spray dryers (52). Consequently, acid whey is either used as animal feed or discarded, causing serious environmental problems. The worldwide production of fresh dairy products in 2016 was more than 400 million tonnes, of which almost 80 million tonnes were in Europe (53). It is quite obvious that whey is produced in vast amounts and none of the current handling practices are effective enough for its exploitation or even valorisation (54).

Acid whey is rich in lactose (4.3%), proteins (0.5%), minerals (mainly calcium at 0.09%) and lactic acid (0.7%). The presence of lactic acid is the major drawback for valorisation of this byproduct stream, negatively affecting lactose crystallization and at the same time acting as an antimicrobial agent for the fermentation of whey into value-added products. Membrane separation has been proposed in the literature as a promising unit operation for the removal of lactic acid from acid whey (51, 55). Chandrapala et al. (51) coupled nanofiltration with diafiltration and removed almost 66% lactic acid from acid whey. Ultrafiltration followed by electrodialysis led to 90% demineralization of acid whey, corresponding to almost 80% lactic acid removal in the study of Chen et al. (55).

For this case study, acid whey (Glanbia Ingredients Ireland, Ballyragget, Ireland) was also nanofiltered in order to achieve higher lactose and at the same time lower lactic acid concentrations in the fermentation medium. The details of the nanofiltration will not be presented here, since the emphasis is given on the lactic acid fermentation. After nanofiltration, acid whey contained almost 100 g/L lactose and a small amount of galactose (1.2 g/L), while initial lactic acid concentration was 1.2 g/L. Yeast extract and MRS salts (in g/L: K₂HPO₄ 2, MgSO₄ 0.1 and MnSO₄ 0.05) were also added to the medium to support the growth of Lactobacillus coryniformis subsp. torquens (DSM 20005; DSMZ – German Collection of Microorganisms and Cell Cultures, Leibniz Institute, Braunschweig, Germany). Sugar consumption, organic acid formation and the number of viable cells expressed as colony forming units (CFU) per L are presented in Fig. 1. L. coryniformis subsp. torquens is an interesting strain that has not yet been fully studied in the literature. Even though it is classified as facultative heterofermentative, many researchers have reported its ability to produce d-lactate exclusively (56, 57). Studies of the strain L. coryniformis subsp. torquens DSM 20004^T have shown that the strain can also produce acetate either under glucose limitation, or due to the presence of pentoses in the substrate (57).

Fig. 1

Sugar consumption, organic acid production and microbial growth in batch fermentation on technical scale (72-litre BIOSTAT UD bioreactor; B-Braun Biotech, Melsungen, Germany) using acid whey as feedstock, V=50 L. L. coryniformis subsp. torquens was used as the microbial biocatalyst. Fermentation was carried out at 30 °C and 200 rpm, and pH was adjusted to 6.0 by the addition of 20% (m/m) NaOH. Inoculum volume was 6% (V/V)

In this experiment, acetic acid production was also observed, mainly during exponential growth phase (6–10 h), and its formation almost ceased during stationary phase. The strain was able to utilize the lactose present in the substrate, eliminating the need for prior hydrolysis. Fermentation lasted 46 h and 64.2 g/L of optically pure (99%) d-lactic acid was produced with a yield of 0.78 g/g based on total sugars and an average productivity of 1.40 g/(L·h). The final concentration of acetic acid was 2.4 g/L, while less than 1 g/L of lactose was left unconsumed. Juodeikiene et al. (52) tested d- and l-lactic acid production from hydrolysed cheese whey by employing the strains L. bulgaricus and P. acidilactici, respectively. The strain L. bulgaricus produced almost 57 g/L of optically pure d-lactic acid after 48 h of fermentation. The authors highlighted the use of CaCO₃ as neutralizing agent in these experiments that is supposed to decrease the inhibitory effect of the produced lactic acid towards the microorganism. In a recent study of Liu et al. (32), cheese whey powder was hydrolysed using commercial proteases and utilized as a sole substrate for d-lactic acid production with the bacterial strain L. bulgaricus CGMCC 1.6970. Final d-lactic acid concentrations reached 70.7 and 113.2 g/L in batch and fed-batch mode, respectively. These results indicate that different waste streams from the dairy industry could be exploited for the production of d-lactic acid of high purity.

Coffee mucilage

Coffee mucilage consists of the inner mesocarp of the bean, which is removed either by natural fermentation of the bean inside the tanks or mechanically (58). This waste material has already been considered as a potential substrate for bioconversion, since it is rich in reducing sugars (accounting for 63% m/m), proteins and pectins (59). Neu et al. (8) reported the production of more than 40 g/L of l-lactic acid of high purity from mucilage supplemented with 5 g/L yeast extract using a B. coagulans isolate. The production of d-lactic acid from coffee mucilage has not yet been reported in the literature. As in the case study using acid whey, the strain L. coryniformis subsp. torquens was evaluated for its ability to grow and produce d-lactic acid of high optical purity. Coffee mucilage was supplied by Cenicafé, the National Coffee Research Center in Manizales, Colombia. The composition of the material was (in %): dry matter 83.3, cellulose 4.7, hemicellulose 2.7, lignin 2.9, total sugars 40.7 (glucose 9.5, xylose/fructose/galactose 13, sucrose 18.2) and total Kjeldahl nitrogen 1.5. Mucilage was supplemented with 5 g/L yeast extract and also MRS salts. At the beginning of the fermentation, the substrate contained 23.4 g/L of glucose, 20 g/L of sucrose and 23 g/L of other monosaccharides. Due to analytical restrictions, it is not possible to determine the presence of either fructose or galactose or xylose, since they elute at the same time during HPLC analysis. The results are presented in Fig. 2. The strain showed a clear preference for glucose, since it was completely depleted after around 12 h. The consumption rate of both sucrose and the residual monosaccharides was slower at the beginning of the fermentation, but after glucose consumption, the other monosaccharides were also rapidly fermented. d-lactic acid accumulation initiated after 6 h and at the end of the fermentation (54 h), it reached a value of 39.7 g/L, with an optical purity of 99%. The yield on total sugars was 0.89 g/g, and the productivity was 0.74 g/(L·h). The production of acetic acid started when glucose was completely depleted (24 h) and when the concentration of the residual monosaccharides (xylose/fructose/galactose) also became limiting, formic acid was also produced (30 h). These results are in accordance with previous studies in which formic and acetic acids were produced by homofermentative strains due to different pyruvate metabolism, triggered either by a specific carbon source limitation, or by the assimilation of other sugars rather than glucose (57). Yáñez et al. (57) reported the consumption of hemicellulosic sugars when cardboard hydrolysate was utilized as substrate in simultaneous saccharification and fermentation. However, hemicellulosic sugars consist of both pentoses (xylose, arabinose) and hexoses (galactose, mannose), meaning that there is not yet enough information that the strain is actually able to assimilate pentoses.

Fig. 2

Sugar consumption, organic acid production and microbial growth in batch fermentation (2-litre bioreactor; Sartorius AG, Göttingen, Germany) using acid coffee mucilage as feedstock, V=1 L. L. coryniformis subsp. torquens was used as the microbial biocatalyst. Temperature was set at 30 °C, stirring at 400 rpm and the pH was adjusted to 6.0 by the addition of 20% (m/m) NaOH. Inoculum volume was 10% (V/V)

At the end of the process, around 9 g/L of sucrose were still left unconsumed as well as 0.4 g/L of monosaccharides. Final concentrations of formic and acetic acids were 1.3 and 2.5 g/L, respectively. Comparing these results to the ones obtained when acid whey was employed as fermentation substrate, lactic acid yield was 14% higher, even though its average productivity decreased by 47%. It seems that the strain was able to consume lactose faster than sucrose, and also sucrose consumption possibly induced formic acid production (Fig. 2). Since this strain has not yet been fully explored, more research should be carried out in order to elucidate the different pathways involved during mixed sugar fermentation.

Rice husks

During rice milling, the main byproduct streams include the husks and the bran. The first step of puddy rice processing involves the removal of the outer layer of the seed, which is called the rice husk. The processing of 1 kg of paddy rice generates approx. 0.2–0.33 kg husks (60). In 2017, 506 million tonnes of rice were estimated to have been harvested, meaning that rice husk generation was more than 100 million tonnes (53). Rice husks are rich in silica (90% of its ash content), which can be recovered and utilized (61). Many studies also deal with the hydrolysis of the hemicellulose and cellulose fraction for the production of bioethanol (60, 62, 63). Different pretreatment and hydrolysis methods have been suggested in the literature for the production of fermentable sugars (64, 65).

In this case study, the details of the hydrolysis will not be described since this is not within the scope of the current review. However, after adequate pretreatment and hydrolysis (provided by Green Sugar AG, Meißen, Germany), a sugar-rich hydrolysate with 42.7 g/L total sugars was produced. The main carbohydrate present was possibly xylose at 28 g/L, followed by glucose (11 g/L) and lower amounts of cellobiose (3.7 g/L). A Leuconostoc sp. isolate (strain A15, available at Leibniz Institute for Agricultural Engineering and Bioeconomy, Potsdam, Germany) was selected for d-lactic acid production from this lignocellulosic substrate. Leuconostoc sp. is well-known heterofermentative LAB found in dairy (66) and other fermented products (67), but it has not yet been tested on a renewable substrate.

The strain was able to utilize the sugars found in the hydrolysate, resulting in the production of approx. 27 g/L of d-lactic acid, with an optical purity of 97% (Fig. 3). As with the majority of strains, glucose was the first sugar to be consumed, but xylose was also depleted after 22 h of fermentation (Fig. 3). At this point the strain started to utilize cellobiose, but the consumption rate was too low and even after 49 h, only 1.4 g/L cellobiose was consumed. Lactic acid yield on total sugars was 0.74 g/g, and productivity was 0.88 g/(L·h). The main disadvantage of this process was that high concentrations of acetic acid were also formed (14.4 g/L). Further strain optimisation is required in order to achieve higher concentration of lactic acid compared to acetic acid.

Fig. 3

Sugar consumption and organic acid production in batch fermentation (2-litre bioreactor; Sartorius AG, Göttingen, Germany) using rice husk hydrolysate as feedstock. A Leuconostoc sp. isolate was used as the microbial biocatalyst. Temperature was set at 30 °C, stirring at 400 rpm and the pH was adjusted to 6.0 by the addition of 20% (m/m) NaOH. Inoculum volume was 10% (V/V)

CONCLUSIONS

The biotechnological production of d-lactic acid from renewable resources is currently in the spotlight due to its significance in the production of polylactic acid. A wide variety of wild-type or genetically engineered LAB are able to produce high concentrations of optically pure d-lactic acid, but there is still need for research, especially in terms of utilization of lignocellulosic materials as fermentation feedstocks. Co-cultivation strategies could be an alternative for high d-lactic acid enantiomeric purity obtained via fermentation of mixtures of pentoses and hexoses. Genetically engineered strains could also be implemented, which will be able to produce lactic acid from hemicellulose following a homofermentative pathway. Our case studies showed that the strain Lactobacillus coryniformis subsp. torquens is an efficient d-lactic acid producer when cultivated in whey or in hydrolysates from coffee residues where no significant amounts of pentoses are present. Leuconostoc spp. is able to grow on lignocellulosic hydrolysates rich in pentoses, but further optimisation is required in order to minimize acetic acid formation.