Production of spiculisporic acid by Talaromyces trachyspermus in fed-batch bioreactor culture

Spiculisporic acid (SA) is a fatty acid-type biosurfactant with one lactone ring and two carboxyl groups. It has been used in metal removers and cosmetics, because of its low propensity to cause irritation to the skin, its anti-bacterial properties, and high surface activity. In the present study, we report an effective method for producing SA by selecting a high-producing strain and investigating the effective medium components, conditions, and environments for its culture. Among the 11 kinds of Talaromyces species, T. trachyspermus NBRC 32238 showed the highest production of a crystalline substance, which was determined to be SA using NMR. The strain was able to produce SA under acidic conditions from hexoses, pentoses, and disaccharides, with glucose and sucrose serving as the most appropriate substrates. Investigation of nitrogen sources and trace metal ions revealed meat extract and FeCl3 as components that promoted SA production. Upon comparing the two types of cultures with glucose in a baffle flask or aeration bioreactor, SA production was found to be slightly higher in the flask than in the reactor. In the bioreactor culture, sucrose was found to be an appropriate substrate for SA production, as compared to glucose, because with sucrose, the lag time until the start of SA production was shortened. Finally, fed-batch culture with sucrose resulted in 60 g/L of SA, with a total yield of 0.22 g SA/g sucrose and a productivity of 6.6 g/L/day.


Introduction
Surfactants are among the most versatile chemicals used in a variety of industries, including detergents, paints, paper products, pharmaceuticals, cosmetics, petroleum, food, and water treatment (Elazzazy et al. 2015;Mahamallik and Pal 2017;Varjani and Upasani 2017). At present, domestic annual surfactant production in Japan is more than 1.1 million tons, a number that is increasing year by year (Chemical Industry Statistics 2019). Commercially available surfactants can be synthesized from petrochemicals, animal fats, plants, and microorganisms; however, most surfactant production relies on petrochemicals (Ru no et al. 2014;Melo et al. 2015;De Almeida et al. 2016). An increase in the amount of oil chemicals causes two phenomena: an increase in environmental pollution, which affects public health, and depletion of oil production within the next few decades (Frumkin et al. 2009). Sustainable social growth demands the development of new strategies to replace fossil fuel products with renewable and biodegradable materials. For the same reason, surfactants made from natural resources using biotechnology, known as biosurfactants, are being focused on to replace synthetics derived from petroleum. Biosurfactants produced by the metabolism of organisms are characterized by low toxicity, bioavailability, biodegradability, high effervescence, and environmental friendliness, and can be widely used in foods, pharmaceuticals, cosmetics, etc (Ahmadi-Ashtiani et al. 2020). These have been developed and used as multifunctional agents, such as stabilizers, wetting agents, anti-bacterial agents, humectants, emulsi ers, and anti-adhesion agents (Banat et al. 2000;Vijayakumar and Saravanan 2015). However, the mass production of many biosurfactants is di cult and expensive because of the low productivity of microorganisms and low availability of raw materials (Santos et al. 2016).
Spiculisporic acid (4,5-dicarboxy-4-pentadecanolide, SA) is a fatty acid-type biosurfactant (Ishigami et al. 2013). The tricarboxylic-type surfactant structure has recently received attention as a commercially available biosurfactant and a new biomaterial owing to its safety for human health and the environment. It contains 2-3 carboxylic acids and the physiological properties of a surfactant. SA was discovered as a metabolite from Penicillium spiculisporum, which was isolated from the precipitate crystallized in the acidi ed culture broth of the fungus (Percival Walter Clutterbuck 1931). Isotope uptake studies and enzyme puri cation showed that SA biosynthesis involves the condensation of lauroyl-CoA and 2-oxoglutarate (Måhlén 1971(Måhlén , 1973. The reaction is catalyzed by decylhomocitrate synthase. Enantioselective synthesis of SA has also been reported (Brandänge et al. 1984;Brown et al. 2003). SA is used in commercial applications to prepare new emulsion-type organogels, super ne microcapsules (vesicles or liposomes), heavy metal sequestrants, and in many other applications in specialty chemicals and biotechnology (Hong et al. 1998;Pekdemir et al. 2000). The raw material has low surface activity, which increases in the derivatives (Yamazaki et al. 1983;Choi et al. 1993). The derivatives promote transdermal absorption of the moisturizer. Due to their physiological properties, these have potential use as new bioactive substances in the pharmaceutical, cosmetic, agricultural, and biotechnology industries.
Talalomyces trachyspermus is the perfect state teleomorph of P. spiculisporum. The genus Talalomyces was rst introduced by Benjamin in 1955 as teleomorphs of the Penicillium species, with woven hyphae and soft cleistothecia ascomata (Benjamin 1955). It was rede ned by Stolk andSamson in 1971 (Stolk andSamson 1971;Fennell 1973). T. trachyspermus are characterized by conspicuously spindle-shaped, elliptical ascospores, and a clear ascotic covering. T. trachyspermus has been found to produce a fatty acid surfactant, trachyspic acid [2-(carboxymethyl)-8-nonyl-9-oxo-1,6-dioxaspiro[4.4]non-7-ene-2,3-dicarboxylic acid], which inhibits heparanase (Shiozawa et al. 1995). Since the structure of the product is similar to that of SA produced by P. spiculisporum, the strain was predicted to produce SA. Its derivatives are found in T. trachyspermus and Aspergillus candidus cultures (Wang et al. 2012(Wang et al. , 2015Kumla et al. 2014). While various reports have shown SA production and characterization, its industrial production is limited. It is manufactured in Japan by only a single source, Iwata Chemical Industry Co. Ltd., which has established a manufacturing method for it. Annual production is estimated to be 4-5 tons. Mass production and scale-up have inevitable problems in trying to achieve low production costs, low environmental pollution, and advanced innovation in the industrial production of fermented products (Chakravarty et al. 2017). Fed-batch (semi-batch) operation is a practical cultivation technology to overcome the various problems that are faced when performing batch and continuous operation (El Moslamy 2019).
In this study, the effective production of SA by T. trachyspermus was investigated by changing the medium composition and culture conditions. In the shake ask scale step, the microbial response to medium components (carbon sources, nitrogen sources, and trace metals) and pH conditions was assessed for SA production. Scaled-up cultivation was attempted in an aeration and stirring bioreactor, to achieve high SA productivity. The utility of two types of culture was evaluated: normal batch culture and fed-batch culture, in which two substrates of glucose or sucrose solution were added to the culture medium.

Batch ask culture
Cultivations using 13 types of lamentous fungi were performed in an Erlenmeyer ask, as follows: hyphae piece ~ 1 cm 2 grown on the pre-culture PDA plate was inoculated in a 500 mL Erlenmeyer ask with 3 ba es containing 100 mL of the medium. The asks were cultured with shaking on a rotary shaker at 28°C and 140 rpm for 7 d.
After cultivation, the mycelium and SA were separated from the culture solution using a lter paper (Advantec® No. 131, 110 mm, ADVANTEC Toyo Kaisha, Ltd., Tokyo, Japan). The ltrate was analyzed using HPLC. The solid phase on the lter was washed several times with distilled water. After removing the water, ethanol was poured above the lter paper to dissolve the SA, followed by collection of the ltrate. The solution containing SA was evaporated at 50°C for 24 h, and the weight of the product was measured. After washing with ethanol, the residue was dried in an oven at 90°C for 24 h, to estimate the growth of fungi in terms of dry cell weight (DCW).

Bioreactor culture
An aeration stirring-type bioreactor with a volume of 2 L was used (Sakura Seiki Co., Nagano, Japan). Batch cultures were performed in 1 L of the medium with glucose or sucrose in the bioreactor, which was autoclaved at 121°C for 45 min. The cultivation was started with the mycelium of T. trachyspermus inoculated into the bioreactor under aseptic conditions. It was controlled at 28°C and 700 rpm, with an aeration rate of 0.5 vvm for 11-19 d.
Fed-batch cultures were performed in the same reactor with either glucose or sucrose. During the culture, 200 mL of 500 g/L sterilized sugar solution was added from the insertion port of the bioreactor, at 6 and 11 d for glucose, and at 4 and 8 d for sucrose.

HPLC assay
Culture broth samples ltered with lter paper were analyzed using HPLC (LC-10 system: Shimadzu Co., Kyoto, Japan) using a refraction detector (RID-10A, Shimadzu Co.) at 40°C with 1.25 mM sulfuric acid as the mobile phase, at a ow rate of 0.6 mL/min. The column used was an IC Sep WA1 Wine Analysis Column (Transgenomic Co., NE, USA).

NMR analysis
The re ned product was analyzed using NMR, to identify the crystals secreted from T. trachyspermus. The recrystallized SA was analyzed using 1 H and 13 C-NMR (400 MHz, JNM-ECS400, JEOL Ltd., Tokyo, Japan) after evaporation of ethanol from the SA solution recovered from the culture. The solvent used was 99.5% ethanol-d6, and the inner standard was 0.005 v/v% tetramethylsilane.

Results And Discussion
Screening for a biosurfactant-producing strain Eleven strains of Talaromyces were compared for SA production, to select for the high-producing strains. These were cultured with 100 g/L glucose in a ba e ask at pH 3.0, 28°C for 7 d. The pre-experiment showed that the strains produced SA under conditions of high substrate concentration and low pH, under adequate aeration. T. trachyspermus was able to produce SA, whereas T. assiutensis only grew (Fig. 1). SA dispersed into the culture medium in a crystalline form as soon as it was produced, because it is hardly soluble in water. The medium became cloudy in the later stage of the culture. T. trachyspermus NBRC 32238 produced the highest SA yield of 11.3 g/L, while the others produced a slight amount of SA, of no more than 3 g/L. The yield of NBRC 32238 (based on sugar consumption) was 0.333 g SA/g glucose, while the productivity was 0.012 g/L/d. The T. trachyspermus NBRC 32238 was selected as the most e cient SA-producing strain and used in the subsequent studies.
Identi cation of the T. trachyspermus product using NMR SA is a white crystal with the molecular formula C 17 H 28 O 6 and molecular weight 328.405 g/mol. It is a needle-like crystal with extremely high solubility in ethanol and poor solubility in water. A photograph of the SA crystal is shown in Fig. 2. NMR analysis was performed to verify that the substance secreted from T. trachyspermus NBRC 32238 was indeed SA. The 1 H-NMR spectrum displayed signals corresponding to 26 aliphatic protons (Fig. 3a). The 13 C-NMR spectrum showed three carbonyl carbons at δC 178.5, 175.5, and 174.2; one oxygen-bearing quaternary carbon at δC 88.2; one methine carbon at δC 52.5; one methyl carbon at δC 13.4; and 11 aliphatic carbons at δC 31.8 to 22.5 (Fig. 3b). The spectra of the products from P. spiculisporum and T. trachyspermus were compared (Table 1). The structural information for the product was determined from a series of 2D NMR analyses, including DEPT90, DEPT135, 1 H-1 H COSY, and HMQC spectra (data not shown). The 1 H-1 H COSY revealed a correlation between H-2 (δH 2.60) and H-3 (δH 2.49).
Correlations between the methylene protons H-6a (δH 1.85) and H-5 [δH 3.01 (br d, J = 9.2 Hz)] were observed in the 1 H-1 H COSY spectrum. DEPT90 and DEPT135 con rmed the carbon series, and the HMQC spectrum showed correlation between the directly bound 1 H and 13 C. Structure of the T. trachyspermus product was determined based on these observations (Fig. 4). From the various NMR analyses, the substance secreted by T. trachyspermus NBRC 32238 was con rmed to have the same structure as that of SA. Effect of initial pH The effect of initial pH on SA production was investigated because the selected strain of T. trachyspermus NBRC 32238 produced the substance in a low pH medium. The medium was prepared at an acidic pH of 2.0-4.0, and the strain was cultured in the medium with 100 g/L glucose at 28°C for 7 d. Glucose consumption by the strain increased with increasing pH up to a pH of 4.0 (Fig. 5). When the initial pH was 3.0, a maximum SA amount of 11.2 g/L was produced, without linking the glucose assimilation behavior.
Low pH operation can avoid contamination problems in a scale-up culture during on-site manufacturing. The strain produced the crystalline form SA at acidic pH. This phenomenon protects its own cell from the adverse effects of SA as a surfactant, because the solubility of this substance increases with environmental pH.
Moreover, the salt changes the state of molecular aggregation in response to environmental pH: vesicles are formed at pH in the range of approximately 5.8-6.2, lipid particles at pH in the range of 6.3-6.6, and micelles at pH 6.8 or higher (Yamazaki et al. 1983;Ishigami et al. 2000;Kunieda and Sakamoto 2010).
Substrate speci city SA production by T. trachyspermus NBRC 32238 upon using eight types of sugars (glucose, sucrose, galactose, arabinose, xylose, lactose, fructose, and maltose) as carbon sources was assessed. It was cultivated for 7 d in basic medium containing 100 g/L of each sugar.
The strain assimilated and metabolized various carbohydrates (hexoses, pentoses, and disaccharides) (Fig. 6). SA was produced from all the sugars at concentrations in the range of 2.5-11.9 g/L. The highest SA yield of 11.9 g/L was produced upon use of glucose; the yield and productivity were 0.14 g SA/g glucose and 1.7 g/L/d based on sugar consumption, respectively. Sucrose was the most consumed carbon source and had the largest DCW, with similar SA production as the glucose culture. The strain secretes acid-resistant invertase to decompose sucrose into glucose and fructose.
Sugars, as energy sources, are involved in substance conversion along metabolic pathways for cell growth.
Adequate substrates are essential for both fatty acid synthesis and promotion of the TCA cycle, since SA biosynthesis is a condensation reaction between lauroyl-CoA and 2-oxoglutarate.

Selection of nitrogen sources
Page 7/22 The basic medium culture containing (NH 4 ) 2 SO 4 and CSL resulted in a yield of at most 2.2 g/L of SA, as described in the previous section. Nitrogen sources affect the production of many materials as substrates of enzymes and substances involved in the different processes in microorganism cells. SA production was evaluated upon using 10 alternate nitrogen sources for (NH 4 ) 2 SO 4 in the medium. T. trachyspermus NBRC 32238 was cultured for 7 d with these nitrogen sources (5 g/L) in a ba e ask containing 100 g/L glucose.
The strain grew and produced SA with each nitrogen source (Fig. 7a). When inorganic sources were used, glucose consumption was poor and SA production was approximately 0.5-15.0 g/L. Natural nitrogen sources improved glucose consumption and led to relatively high DCW and SA amounts. Meat extract induced the highest SA production of 22.2 g/L. It is essential to determine which components of the meat extract affect SA synthesis; however, this is challenging since the components in the extract are private.
Different meat extract concentrations (0-5 g/L) were investigated for SA production in basic medium with 100 g/L glucose at 28°C for 7 d. SA production increased with increasing meat extract up to 4.5 g/L and reached a highest value of 23.3 g/L (Fig. 7b). The SA yield and productivity were 0.29 g SA/g glucose and 3.3 g/L/d, respectively.
The amount of the target substance depends on the type of nitrogen source to be added or the product lot.
This induces a large change in production, or, in some cases, no production of the target substance. SA synthesis requires lipid production, the formation of 2-oxoglutarate in the TCA cycle, and expression of enzymes involved in these formations because it is produced by a condensation reaction with lipids and organic acids. The formation of these enzymes necessitates the use of appropriate nitrogen sources.

Effect of trace metal ions
The effects of metal ions involved in SA production were examined to improve the production e ciency. Eleven types of metal salts were added to the basal medium at a concentration of 5 mg/L, and T. trachyspermus NBRC 32238 was cultured with 100 g/L glucose for 7 d.
The strain produced 5.2 g/L of SA in the control case without the metal salts (Fig. 8a). Culture with the addition of metal salts such as FeSO 4 , Fe 2 (SO 4 ) 3 , FeCl 3 , MnSO 4 , and NiCl 2 promoted SA production to 2-3 times higher than that without addition. FeCl 3 increased the glucose consumption to 10-fold, as compared to the control culture, whereas the DCW was not different (data not shown). This resulted in the induction of the highest concentration of SA (15.0 g/L). The addition of iron-containing salt to the medium signi cantly affected the glucose consumption and SA production. The trivalent chloride iron, especially, plays a positive role in the metabolism involved in SA production in T. trachyspermus because only FeCl 3 promoted both glycolysis and SA production, while FeCl 2 , FeSO 4 , and Fe 2 (SO 4 ) 3 did not.
The effects of addition of different concentrations of FeCl 3 to the medium (0-50 mg/L) were investigated.
Cultivation was performed under the same conditions as described above. The produced SA increased with increasing concentration of FeCl 3 , from 0 to 5 mg/L, and then decreased upon further addition (Fig. 8b). The strain was able to grow with 50 mg/L of FeCl 3 , but SA was not produced at this concentration. The highest amount of SA (18.6 g/L) was produced by the strain at 5 mg/L of FeCl 3 .
Trace mineral components are required in the culture medium for many physiological activities in the production of useful substances by microorganisms, for example, as an enzyme cofactor that acts on sugar metabolism, substance production, substance synthesis, and cell retention. Iron ions play an important role in energy acquisition by repeated oxidation and reduction on the electron transport chain in the inner mitochondrial membrane downstream of the TCA cycle. The trivalent chloride iron has a positive effect on the SA-producing strain. FeCl 3 enhances the expression level of related enzymes in SA production, to increase the accumulation of fatty acids-CoA and 2-oxoglutarate generated in the TCA cycle and downstream.

Batch culture in ask or bioreactor
The selected media components were used in T. trachyspermus NBRC 32238 culture, to prove the effectiveness of SA production. This strain was cultivated in a ask with three ba es containing 100 g/L glucose at 28°C and 140 rpm for 9 d. The nitrogen source and trace metal compound used were 4.5 g/L meat extract and 5.0 g/L FeCl 3 . Glucose consumption started from day 3 and was almost depleted at day 7, and correspondingly, the cells grew with the progress of culture and reached a DCW of 12.7 g/L at day 7 (Fig. 9a).
The maximum amount of SA was 29.0 g/L, which was 2.4-fold higher than that of the basic medium culture.
In terms of pH behavior, SA production started after the pH fell below 2.4, at day 3. The produced SA decreased after a maximum amount, either because the strain assimilated the product post glucose decrease, or because it dissolved in the produced ethanol, to be ltered through the lter paper. However, because the product is crystalline in low pH conditions, the reason for this phenomenon is unclear. From the results of the ask batch culture, the growth of the mycelium cells became constant after 4 d because of the decrease in the pH of the medium. SA production stopped with glucose depletion on day 7. A scale-up of batch equipment is necessary to make the process continuous and to produce the product stably and e ciently.
A bioreactor culture of T. trachyspermus NBRC32238 was performed in a 1 L working volume with 100 g/L glucose. The culture was carried out for 11 d at 28°C and 700 rpm with an aeration rate of 0.5 vvm. The strain assimilated the substrate for 7 d and the DCW was almost constant at approximately 11.2 g/L after 10 d (Fig. 9b). SA production started on day 4 and reached a value of 25.3 g/L at day 8, which was lower than that in the ask culture. It also decreased after glucose depletion, similar to that in the ask culture. In the glucose culture using both ask and bioreactor, the strain requires 3-4 d to decrease the pH to 2.4 and start producing SA. Scale-up of the aerobic processes often reduces the biomass yield and production of the target substance. The use of lamentous fungi is particularly problematic because of the entanglement of hyphae with the equipment. Dispersion is an important factor for substrates, cells, and oxygen supply in bioprocesses using aerobic microorganisms. Optimization of these conditions improves the production of the target substance.
SA production using fed-batch culture One of the major causes of decreased SA production was substrate depletion in the batch culture. A fedculture was performed to improve the SA production, with the stepwise supply of an additional medium containing glucose to the bioreactor. The productivity of SA was improved upon supplying su cient oxygen and a carbon source to the cells.
A fed-batch culture was performed with T. trachyspermus NBRC 32238 and glucose. Fermentation was rst started with 100 g/L of substrate, under the same conditions as the batch culture using the bioreactor. After incubation for 6 d, and then subsequently, again at the interval of 6 d, 200 mL of 500 g/L glucose was added directly to the bioreactor at the point at which SA production stagnates. The residual glucose concentration decreased to 19.5 g/L and the cell grew to a DCW of 4.3 g/L in the early 6 d of cultivation (Fig. 10a). At the same time, the produced SA was only 0.66 g/L and hardly increased, although the strain was growing by consuming glucose in the culture. After the addition of glucose, the sugar gradually decreased at the same rate as the rst batch term, with increasing DCW; in addition, SA production increased drastically with growth and reached 39.5 g/L on day 11. It further increased to 53.2 g/L on day 12, but still the DCW hardly increased after glucose was added again, because the mycelia amount in the reactor was limited. The productivity of the fed-batch culture was 4.1 g/L/d on day 12. It was constant at 47-55 g/L from day 12 to 19; however, glucose was slowly consumed for maintenance of the mycelia. The product reached its limit because of the spatial inhibition in the reactor and other biochemical reasons of the strain, such as product inhibition and toxicity. SA also did not decrease as in the batch culture because adequate sugar remained around the mycelium in the fed-culture. The strain can consume su cient sugar in this culture in the late term, while the depletion of glucose results in SA consumption in the batch culture.
Sucrose fed-batch culture was attempted using stepwise addition with T. trachyspermus NBRC32238, as the strain can produce SA from sucrose. The culture was performed using the same equipment and conditions, with the replacement of glucose with sucrose at a concentration of 100 g/L. The substrate was fed on days 4 and 8, which were the timings of growth and stagnation of SA production, respectively. The residual sucrose decreased to 58 g/L with the growth of the cells to a DCW of 12.6 g/L at day 4 (Fig. 10b). After the two additions, the growth of the mycelium remained almost constant from day 4 until the end of the culture (15 d). The growth of the strain was promoted by sucrose, as evidenced by the observation that the maximum growth was 5 days faster than that with glucose. The SA yield was 12.1 g/L in the sucrose culture at only day 4, although it was hardly produced in the early term with glucose. Only 42 g/L of sucrose consumption resulted in a DCW of 12.6 g/L and an SA amount of 12.1 g/L. After the rst addition, sucrose was rapidly consumed, from 179 g/L to 74 g/L, and simultaneously, SA amount increased to 44.7 g/L from day 4 to day 8 of the culture. Upon adding the sucrose solution again on the eighth day, the SA yield reached 59.7 g/L and remained almost constant (56-60 g/L). Sucrose was consumed only to maintain the cells. The productivity of the sucrose fed-batch culture was 6.6 g/L/d on day 9, which was 1.6-fold higher than that of the glucose culture. The rapid growth and SA production indicated that sucrose is a better carbon source than glucose in fed-batch SA production. Using sucrose for the manufacture of a compound has the advantage that raw materials are easily available, which keeps the unit cost relatively low. A further increase in SA production is expected upon carrying out continuous culture, which involves partially extracting the culture solution or sedimentation and separation of the product during the culture.
The fed-batch culture process is usually a step in an R&D program that leads to large-scale industrial production by fermentation. The operation of a fed-batch system for improving the productivity of a product is often governed by a number of important engineering considerations, such as improving the culture equipment and conditions. This process has the following effects: 1) decreases the viscosity of the culture solution; 2) increases the density of the cells; 3) compensates for water loss; 4) extends the production time; 5) suppresses the Crabtree effect for high-concentration production; 6) suppresses catabolite repression in secondary metabolite production; and 7) controls the expression of genes with repressible promoters. Fedbatch culture is desirable for a variety of industries that deal with living organisms, such as the production of secondary metabolites, large-scale chemicals, and pharmaceuticals that are produced by overexpressing recombinant or natural strains (Elsayed et al. 2015;Krause et al. 2016).

Conclusion
In the present study, we found that among 11 related strains of Talaromyces, the novel ascomycetes T. trachyspermus NBRC 32238 had the highest production capability for SA, a biosurfactant with multivalent carboxyl groups. The strain can produce SA effectively from glucose and sucrose at low pH (no more than 3.0). Low pH culture is an advantage that avoids contamination in bioprocesses using microorganisms.
Nitrogen sources and metals in the medium affect the production of secondary metabolites, including glycolytic and metabolic pathways, redox reactions, and secretion of enzymes. The SA yield was improved upon in the sequential identi cation of an optimum nitrogen source and trace metal component in the medium. Meat extract and FeCl 3 were found to be the appropriate components for this production. The factor of a positive interaction becomes clear by examining the detailed composition of the components and the metabolism when they are added. A typical problem faced in the scale-up of fermentation processes is that even though the cells continue to grow, the products hardly appear. Reactor culture is different from that carried out in a ask, in terms of aeration, distribution, shear force, etc. The reactor culture of SA production reproduced the ask culture at the same level. In this experimental system, the strain used the substrate for simultaneous cell growth and SA production. To improve the yield, fed-batch fermentation was applied as a continuous production system. Periodic addition of substrate increased the nal SA amount and prevented product consumption. Sucrose culture enhanced SA production by T. trachyspermus. A remarkable SA of 60 g/L was achieved using the fed-batch process. The fed-batch strategy is a promising, time-saving strategy from a long-term perspective, because the process can produce a high amount of substance in one tank. SA is expected to be widely used in cosmetics, food, medical materials, etc. In the near future, we hope that industrially produced SA using these strains is of application in many elds.

Declarations
Ethics approval and consent to participate Not applicable.

Consent for publication
All authors agreed with this publication.

Availability of data and materials
The dataset (graphs and tables) supporting the conclusions of this article are available.  Figure 1 Screening for an spiculisporic acid-producing fungus from the Talaromyces species. Cultivation was performed in a ba e ask for 7 d. The medium volume was 100 mL, containing 100 g/L glucose. The culture conditions were pH 3.0 and a temperature of 28°C.

Figure 2
Page 17/22 A photograph of spiculisporic acid crystals. The product was puri ed from T. trachyspermus NBRC 32238 using ethanol elution and recrystallization.

Figure 3
Analysis of the product from T. trachyspermus NBRC32238 using NMR. Spectrum data of a 1H NNR b 13C NMR (b). The solvent used was 99.5% ethanol-d6, and the inner standard was 0.005 v/v% tetramethylsilane.

Figure 5
Effect of initial pH on spiculisporic acid production by T. trachyspermus NBRC32238. The medium was adjusted to an initial pH of 2.0-4.0, and the strain was cultured with 100 g/L glucose at 28°C for 7 d. Error bars indicate standard deviations from three independent experiments.

Figure 7
Effect of nitrogen source on spiculisporic acid production by T. trachyspermus NBRC32238. a Comparison of spiculisporic acid production with various nitrogen sources. b Spiculisporic acid production with meat extract at concentrations of 0-5 g/L. Cultivation was carried out with 100 g/L glucose at 28°C for 7 d. Error bars indicate standard deviations from three independent experiments.

Figure 9
Batch fermentation pro les for spiculisporic acid production with different culture equipment. a Flask culture with three ba es containing 100 mL medium with 100 g/L glucose at 28°C for 9 d. b Bioreactor culture by an aeration stirring-type reactor containing 1 L medium controlled at 28°C and 700 rpm with an aeration rate of 0.5 vvm for 10 d. The cultivation was carried out with 100 g/L glucose, 4.5 g/L meat extract, and 5.0 g/L FeCl3. Error bars indicate standard deviations from three independent experiments.

Figure 10
Fed-batch culture for spiculisporic acid production from different carbon source by T. trachyspermus NBRC32238. a Glucose culture, with feeding of additional sugar, at 6 and 12 d. b Sucrose culture, with feeding of additional sugar, at 4 and 8 d. The cultures were operated in an aeration stirring-type reactor containing 1 L medium controlled at 28°C and 700 rpm with an aeration rate of 0.5 vvm for 19 d in case of glucose culture and for 15 d in case of sucrose culture.