Biobutanol production in a Clostridium acetobutylicum biofilm reactor integrated with simultaneous product recovery by adsorption
- Dong Liu†1,
- Yong Chen†1,
- Feng-Ying Ding1,
- Ting Zhao1,
- Jing-Lan Wu1,
- Ting Guo1,
- Heng-Fei Ren1,
- Bing-Bing Li1,
- Huan-Qing Niu1,
- Zhi Cao1,
- Xiao-Qing Lin1,
- Jing-Jing Xie1,
- Xue-Jun He1 and
- Han-Jie Ying1Email author
© Liu et al.; licensee BioMed Central Ltd. 2014
Received: 6 October 2013
Accepted: 24 December 2013
Published: 8 January 2014
Clostridium acetobutylicum can propagate on fibrous matrices and form biofilms that have improved butanol tolerance and a high fermentation rate and can be repeatedly used. Previously, a novel macroporous resin, KA-I, was synthesized in our laboratory and was demonstrated to be a good adsorbent with high selectivity and capacity for butanol recovery from a model solution. Based on these results, we aimed to develop a process integrating a biofilm reactor with simultaneous product recovery using the KA-I resin to maximize the production efficiency of biobutanol.
KA-I showed great affinity for butanol and butyrate and could selectively enhance acetoin production at the expense of acetone during the fermentation. The biofilm reactor exhibited high productivity with considerably low broth turbidity during repeated batch fermentations. By maintaining the butanol level above 6.5 g/L in the biofilm reactor, butyrate adsorption by the KA-I resin was effectively reduced. Co-adsorption of acetone by the resin improved the fermentation performance. By redox modulation with methyl viologen (MV), the butanol-acetone ratio and the total product yield increased. An equivalent solvent titer of 96.5 to 130.7 g/L was achieved with a productivity of 1.0 to 1.5 g · L-1 · h-1. The solvent concentration and productivity increased by 4 to 6-fold and 3 to 5-fold, respectively, compared to traditional batch fermentation using planktonic culture.
Compared to the conventional process, the integrated process dramatically improved the productivity and reduced the energy consumption as well as water usage in biobutanol production. While genetic engineering focuses on strain improvement to enhance butanol production, process development can fully exploit the productivity of a strain and maximize the production efficiency.
KeywordsBiofilm reactor Clostridium acetobutylicum Simultaneous product recovery Acetoin Adsorption Redox modulation
Butanol fermentation, commonly known as ABE (acetone, butanol, and ethanol) fermentation, once the second largest biotechnological industry in the world , has attracted renewed interest in recent years for several economic and environmental reasons [2, 3]. However, low alcohol yield (<25% w/w), low reactor productivity (approximately 0.3 g · L-1 · h-1), and high energy-consumption and water usage due to low solvent titer (approximately 20 g/L) are major challenges of conventional ABE fermentation, limiting the development of economically viable biobutanol production [2, 3].
The low butanol yield in ABE fermentation is largely attributed to the fact that considerable amounts of glucose are converted to acetone with concomitant release of CO2 and H2. Genetic engineering technologies, for example, disrupting the adc gene  or reinforcing the direct butanol-forming route , have been applied to improve butanol yield. Introducing CO2 fixation pathways into a butanol-producing host may also be a promising approach to improve the product yield . To address the low solvent-productivity, immobilized cell systems have been developed that maintain a high cell-activity and reduce the downtime of a repeated batch fermentation mode or continuous fermentation mode . The highest ABE productivity, 15.8 g · L-1 · h-1 was obtained by continuous fermentation of immobilized Clostridium beijerinckii (C. beijerinckii) cells adsorbed to clay brick; this productivity was approximately 50 times the typical productivity of planktonic cell fermentation . However, the butanol titer in this process was only about 5 g/L. A more elaborate process should be designed to avoid the loss of substrate in the effluent and to increase the solvent titer.
Product toxicity to the producing strain at low solvent-concentrations is another critical limitation of biobutanol production. Due to the susceptibility of Clostridia to butanol, the solvent titer during ABE fermentation is low. Until now, the highest butanol concentration achieved in the fermentation broth without simultaneous product recovery was only 20.9 g/L, which was obtained in a batch fermentation using C. beijerinckii BA101 generated by nitrosoguanidine (NTG) mutagenesis . Solvent recovery using conventional distillation is energy intensive and expensive. Low butanol titers increase recovery costs and water usage. Numerous processes have been developed for simultaneous recovery of solvent from the broth during fermentation. The most common solvent recovery techniques are liquid-liquid extraction, gas stripping, pervaporation, and adsorption. In particular, gas stripping has been extensively explored in recent years, and attractive results have been obtained in terms of solvent concentration and productivity. By fed-batch culture of a genetically engineered strain with gas-stripping recovery, 585.3 g of butanol was produced from 1,861.9 g of glucose, with a productivity of 1.32 g · L-1 · h-1. Similarly, by applying gas stripping intermittently in fed-batch fermentation with a butanol tolerant strain, 172 g/L ABE (containing 113.3 g/L butanol) were produced with an overall ABE productivity of 0.53 g · L-1 · h-1. Although gas stripping is a favorable choice due to its operation simplicity, it usually requires a higher energy-input because of the intensive product-capturing step . Since the energy density of butanol is only 36 kJ/g, it is essential to minimize the energy consumed for butanol recovery in order to recover the highest net energy increase. The energy requirements for butanol recovery by conventional distillation, gas stripping, extraction, pervaporation, and adsorption-desorption have been estimated at 24, 21, 14, 9, and 8 kJ/g butanol, respectively [12, 13], highlighting the superiority of adsorption-desorption with respect to energy return. An assessment conducted by Oudshoorn and his co-workers also demonstrated that adsorption- and pervaporation-based techniques are the most attractive recovery options for the recovery of butanol from aqueous solution . Silicalite, bonopore, polyvinylpyridine, zeolite, activated carbon, and polymeric resins have been exploited for butanol adsorption. Being solid phase, the adsorbents have the advantages of complete immiscibility and ease of regeneration and reuse . However, application of adsorbents in butanol fermentation has been limited by their low adsorption selectivity and capacity .
In our preliminary work, Clostridium acetobutylicum (C. acetobutylicum) cells were immobilized as a biofilm on a fibrous matrix, which increased the butanol tolerance and dramatically improved the ABE productivity of the cells . A novel macroporous resin, KA-I, was also synthesized and used for the recovery of butanol from the model solution, with high selectivity and capacity [15, 16]. Based on these results, we aimed to develop an integrated process to maximize the butanol production efficiency with minimal resource consumption. First, the adsorption behavior of KA-I during fermentation was investigated and controlled. Second, a system integrating a biofilm reactor with fixed-bed adsorption using KA-I was constructed and optimized for the production of ABE and acetoin with simultaneous product recovery.
In situ product removal using the macroporous resin KA-I
Effects of resin amount
Effects of resin quantity on the final product yield
Butyric acid (g/L)
Acetic acid (g/L)
0 to 80
0 to 70
0 to 60
40 to 65
0 to 45
40 to 60
0 to 45
The amounts of residual acids could be reduced by adding the resin at a later time point. An optimal time point for adding the resin was found to be 40 h, when the acids started to be re-assimilated. Addition of 50 g/L of resin at 40 h, rather than at 0 h, led to a 43% reduction in the residual acids, and thus a higher butanol production was achieved. Based on the solvent production and fermentation time, 50 g/L was considered the optimal amount of resin to be added at 40 h.
Inverse relationship between the production of acetoin and acetone
An inverse relationship between acetoin and acetone production was observed in the adsorptive fermentation. Addition of resin significantly increased acetoin production and decreased acetone production (Table 1). An increase in the resin amount or addition at an earlier time led to a higher acetoin production and lower acetone production. When 60 g/L resin was initially added to the culture, acetoin production was as high as 3.8 g/L, whereas acetone production was only 1.9 g/L. Interestingly, an inverse relationship between acetoin and acetone production was also observed in the study by Doremus et al., who investigated the effects of pressure and agitation on ABE fermentation . Thus, it appears that acetoin can be overproduced at the expense of acetone without negatively affecting butanol production. However, acetoin production by C. acetobutylicum, as reported in early studies, was usually not higher than 1.0 g/L . To the best of our knowledge, 3.8 g/L is the highest yield of acetoin produced by C. acetobutylicum.
Batch fermentation in biofilm reactors coupled with fixed-bed adsorption
Performance of the biofilm reactors with butanol maintained at different levels
Productivity(g · L-1 · h-1)
Biofilm reactor, fixed-bed adsorption 2.5 to 3.2 g/L butanol
Biofilm reactor, fixed-bed adsorption 4.0 to 5.5 g/L butanol
Biofilm reactor, fixed-bed adsorption 5.2 to 6.4 g/L butanol
Biofilm reactor, without adsorption
Traditional planktonic cell fermentation, without adsorption
Importance of the butanol level
The online fixed-bed adsorption system was constructed by packing the KA-I resin in glass columns and connecting the glass columns to the biofilm reactor (Figure 2). The butanol titer was maintained at different levels to investigate the effects of the titer on the fermentation. As shown in Table 2, lowered butanol titers in the biofilm reactor did not improve the productivity but increased the cell density of the bulk medium as well as the residual butyric acid level at the end of the fermentation, resulting in a low butanol yield. In addition, low butanol titers also significantly decreased the adsorption capacity of the KA-I resin (data not shown). Hence, the butanol titer was maintained above 6 g/L in the subsequent experiments.
Fed-batch fermentation in biofilm reactors coupled with fixed-bed adsorption
Results of fed-batch fermentation in biofilm reactors coupled with fixed-bed adsorption
Fermentation with selective adsorption of butanol
Fermentation with co-adsorption of acetone
Fermentation with redox modulation
Fermentation time (h)
Glucose fermented (g/L)
Resin used (g)
Adsorbed ethanol (g)
Adsorbed acetone (g)
Adsorbed butanol (g)
Adsorbed acetoin (g)
Adsorbed butyrate (g)
Equivalent ethanol concentration (g/L)
Equivalent acetone concentration (g/L)
Equivalent butanol concentration (g/L)
Equivalent acetoin concentration (g/L)
Equivalent butyrate concentration (g/L)
aSolvent concentration (g/L)
aSolvent productivity (g · L-1 · h-1)
aSolvent yield (g/g)
bTotal product yield (g/g)
Butanol-acetone molar ratio
Kinetics of fixed-bed adsorption
Fermentation with co-adsorption of acetone
Redox modulation for improved product yield
During ABE fermentation by C. acetobutylicum, the release of H2 causes a deficiency in nicotinamide adenine dinucleotide (phosphate) (NAD(P)H) reducing equivalents used for ethanol and butanol production. Therefore, a large quantity of oxidation products (especially acetate and acetone) is commonly produced, resulting in a low alcohol yield . In fact, acetone was produced in greater quantities in the biofilm reactor than in the planktonic cell reactor due to the increased H2 release. Methyl viologen (MV) was used to enhance butanol production because MV can divert the electron flow from H2 to NAD(P)H . The results are summarized in Table 3. With addition of 1 mM MV, butanol production was markedly increased whereas acetone was reduced. Thus, the butanol-acetone molar ratio increased from 1.9 to 3.2. More importantly, when one glucose molecule is converted to the C4 compound butanol instead of the C3 compound acetone, the mass yield is expected to increase. Indeed, the total solvent yield (ABE and acetoin) upon MV addition increased by 9%. Redox modulation by MV addition also stimulated butyrate production, consistent with a previous report . The butyric acid was maintained at approximately 1.5 g/L throughout the fermentation, which was a much higher level than the average of 0.5 to 0.7 g/L observed when no MV was added. Due to the adsorption by the KA-I resin, the final butyrate concentration reached 10.8 g/L. Therefore, the total product yield (ABE, acetoin, and butyric acid) was further increased by 16%. This increased product yield will reduce carbon emission in the ABE fermentation. In addition, MV was not adsorbed by the KA-I resin, suggesting that MV could be reused in the fermentation. However, the use of MV resulted in a slower fermentation rate, likely due to the inhibition of cell growth  or through a toxic effect of butyric acid on metabolism  during the prolonged fermentation.
Comparison with other studies
Performance of different types of resin used as adsorbents during butanol fermentation
Solvent productivity(g · L-1 · h-1)
Batch fermentation, in situ adsorption
Mainly butanol, isopropanol, glucose
Two-stage continuous fermentation, in-line adsorption
Butanol, acetone, acetate, and butyrate; no lactose
0.30 to 0.36
Repeated batch fermentation, batch adsorption
Bonopore, copolymers of divinylbenzene, and styrene
Solvent and acids
Batch fermentation, in situ adsorption
Dowex Optipore SD-2ploy(styrene-co-DVB) derived
Mainly butanol and butyrate
0.27 to 0.40
Repeated fed-batch fermentation, fixed-bed adsorption
Reillex 425, polyvinylpyridine
ABE and acids; no glucose
Fed-batch fermentation, fixed-bed adsorption
KA-I, cross-linked polystyrene framework
Butanol, butyrate, and acetone; no glucose
Fed-batch fermentation, fixed-bed adsorption, MV addition
KA-I, cross-linked polystyrene framework
Butanol, butyrate, and acetone; no glucose or MV
Acetoin: a value-added product
Interestingly, an inverse relationship was observed between the production of acetoin and acetone. Acetoin (3-hydroxybutanone) is a fine chemical widely used for food flavoring and as a fragrance. Acetoin is also used to synthesize novel optically active α-hydroxyketone derivatives and liquid crystal composites . Recently, the ratio of d-acetoin to l-acetoin produced by Clostridium strain ATCC 824 was found to be 12:1 . In contrast, acetoin produced by butanediol-producing strains are often racemic. The inverse relationship suggests that ABE fermentation may be switched to acetoin-butanol-ethanol fermentation, which is a promising approach to improve the product value of ABE fermentation. It was presumed that acetoin is a structural analog of acetoacetate and could not be decarboxylated by acetoacetate decarboxylase, which would impede acetone production . However, exogenous addition of 1, 2, or 4 g/L acetoin to the fermentation broth failed to lower the acetone production (data not shown). Recent insights from molecular studies indicate that acetoin is the product of als SD (encoding an α-acetolactate synthase and an acetolactate decarboxylase), which is regulated by the transcription factor als R in response to acetate accumulation and a pH change in Bacillus subtilis. Study of disruption of als R in C. acetobutylicum is ongoing to better understand the mechanisms underlying the inverse relationship.
High productivity of the biofilm reactor
Our previous study demonstrated that C. acetobutylicum cells exhibited improved butanol tolerance and production rate in biofilm compared with planktonic cells . Thus, the C. acetobutylicum B3 biofilm was used for butanol fermentation in this study. The solvent production rate was increased dramatically, from 0.25 to 0.30 to 0.97 to 1.66 g · L-1 · h-1. Meanwhile, in the biofilm reactor, fermentation can be performed in a repeated batch mode or a continuous mode, which can overcome the drawbacks of batch operation, such as down times and long lag periods. Thus, the reactor productivities were greatly improved, which can significantly reduce capital investment and operational costs . Furthermore, the cells can remain in the biofilm during a prolonged feeding fermentation or repeated batch fermentations, and the already established solvent-producing capacity of the cells would increase the carbon flux to solvent production rather than biomass synthesis.
Conservation of energy and water by simultaneous product removal
Due to product toxicity, C. acetobutylicum fermentation rarely produces >13 g/L butanol . Product recovery from the dilute fermentation broth by conventional distillation is energy intensive because water is the major component, with a boiling point below that of butanol (100 versus 117°C). When the fermentation was coupled to a simultaneous adsorption process using KA-I, the product was removed, and the levels of butanol and acetone were maintained below the inhibitory threshold. Thus, the fermentation could be prolonged with a continuous feed of highly concentrated nutrients, and a high equivalent-solvent titer was achieved. When the resin columns were eluted with methanol, the average concentration of butanol in the eluent could be increased by approximately 6-fold to 50 to 60 g/L. Distillation technology showed that if the butanol concentration could be raised from 12 to 19 g/L, the energy consumption of butanol recovery from the fermentation broth could be cut in half . Together with the low methanol boiling point (64°C), the high butanol titer in methanol would significantly reduce the energy requirement for butanol separation. Moreover, the high equivalent solvent concentration obtained in the integrated process meant that the fermentation was performed with a highly concentrated medium, which reduced the water usage and resulted in significant savings in sterilization and wastewater treatment.
Improvement of yield by redox modulation
Theoretically, butanol can be produced from glucose with 100% molar yield. However, release of H2 causes a deficiency of the reducing equivalents NAD(P)H, thus resulting in a large quantity of oxidation products, especially acetone . Except for acetoin, butanol is the preferred product, attracting the highest price of the solvents. Addition of MV diverted the electron flow from H2 to NAD(P)H , which facilitated acetoacetyl-CoA reduction to butanol rather than decarboxylation to acetone. Thus, the butanol-acetone ratio was improved, and the emission of H2 and CO2 was reduced, leading to increased product yield. Hence, redox modulation of C. acetobutylicum metabolism by small-molecule effectors can be used to improve both the butanol-acetone ratio and the total solvent yield in ABE fermentation, which has been rarely achieved by genetic manipulations [4, 33, 34].
In summary, the process developed in this study could potentially (1) reduce capital investment and operational costs due to high reactor productivity, (2) reduce energy consumption and wastewater treatment due to the highly concentrated medium and high solvent titer, and (3) increase product value and reduce gas emission due to the improved butanol ratio and solvent yield. Genetically engineered strains with modified product spectra (for example, diminished acetone and acid production, or selective butanol production) will make this process more economically favorable.
KA-I resin can be used as a good adsorbent for product recovery in ABE fermentation. Use of KA-I resin enhanced acetoin production at the expense of acetone production during the fermentation. To reduce butyrate adsorption by KA-I, the butanol titer should be maintained at a relatively high level (>6.5 g/L). The biofilm reactor dramatically enhanced the fermentation productivity compared with the planktonic reactor. In fed-batch production with simultaneous product recovery, the equivalent solvent concentration was much higher than in a conventional fermentation. Redox modulation was effective for improving the butanol-acetone ratio and the total product yield. While molecular technologies focusing on strain construction are becoming mainstream in the development of economically viable biobutanol production, process technologies should not be overlooked because they can be an effective means of fully exploiting the productivity of a strain and maximizing the production efficiency.
Organism and culture conditions
C. acetobutylicum B3 (CGMCC number 5234) was used in all of the fermentation experiments. The strain was stored in 30% (v/v) glycerol at −80°C and was grown in solid reinforced clostridia medium (RCM) at 37°C in an anaerobic chamber (Bug Box, Ruskinn Technology, Leeds, UK). Cultures of C. acetobutylicum B3 were grown in modified P2 medium (containing 10 g/L glucose as the sole carbohydrate source) for seed culture. Unless otherwise stated, the fermentation experiments were performed in P2 medium (comprising glucose, 60 g/L; K2HPO4, 0.5 g/L; KH2PO4, 0.5 g/L; CH3COONH4, 2.2 g/L; MgSO4 · 7H2O, 0.2 g/L; MnSO4 · H2O, 0.01 g/L; NaCl, 0.01 g/L; FeSO4 · 7H2O, 0.01 g/L; p-aminobenzoic acid, 1 mg/L; thiamine, 1 mg/L; and biotin, 0.01 mg/L)  at 37°C with 10% inoculum (v/v).
Biofilm formation and repeated batch fermentations
For biofilm formation, a 2-L stainless steel column was packed with a spiral fibrous matrix (90 g). The columns were sterilized at 121°C for 30 minutes before use. Subsequently, 150 mL of 12-h-old seed culture was inoculated into 1.5 L of P2 medium and allowed to grow statically for 20 h at 37°C. Next, the culture was transferred to the stainless steel column and circulated through the fibrous matrix at a pumping rate of 25 mL/minute to allow the cells to immobilize onto the fibrous matrix and form a biofilm. The temperature was controlled via connection of the jacketed column to a warm water bath at 37°C. After 20 h of continuous circulation, the broth was replaced with fresh P2 medium to start the ABE fermentation. The medium circulation rate was maintained at 35 mL/minute via a peristaltic pump during fermentation. When a batch ended, fresh P2 medium was fed to the column to replace the fermentation broth. Subsequently, the medium was circulated again, and the next batch fermentation was started with the biofilm on the fibrous matrix.
Scanning electron microscopy
For SEM, the cells were collected at 48 h. A piece of cotton towel was harvested and rinsed twice with PBS buffer (137 mM NaCl, 2.7 mM KCl, 8 mM Na2HPO4, and 2 mM KH2 PO4, pH 7.40) to remove contaminating planktonic cells before being freeze-dried using the FreeZone Freeze Dry System (Labconco Corporation, Kansas City, MO, USA). The samples were scanned and photographed by SEM (Philips XL-30 ESEM, Eindhoven, Holland).
In situ product adsorption
In situ adsorption experiments were conducted in 500-mL Duran bottles with a 300-mL working volume. The macroporous adsorption resin KA-I, with a cross-linked polystyrene framework, was supplied by the National Engineering Technique Research Center for Biotechnology (Nanjing, China) . The resin was first soaked in methanol for 24 h and then washed with water before being pumped dry and weighed. Subsequently, the resin was sterilized in a small amount of deionized water by autoclaving for 15 minutes at 121°C. The desired mass of resin was added to 300 mL of culture medium at different times according to the experimental design.
A schematic diagram of the process is shown in Figure 2. When the butanol titer reached the predetermined threshold, the fermentation broth was transferred to a microporous filtration unit (Tianjin MOTIMO Membrane Technology Co., Model MOF-1b, Tianjin, China) to separate the cells before being loaded onto the resin bed. The effluent was transferred back to the reactor for further fermentation. In the fed-batch mode, 1 L of P2 medium was initially fed into the reactor. Subsequently, P2 medium containing a high glucose concentration (500 g/L) was fed into the reactor using a peristaltic pump to maintain the glucose concentration within the desired range. When the resin column was saturated, it was replaced with a new resin column.
MV was purchased from Sigma-Aldrich (Saint Louis, Missouri, USA ) as the dichloride hydrate. It was prepared as a sterile stock solution and added to the fermentation broth as necessary to achieve a final concentration of 1 mM. The MV concentration was determined spectrophotometrically as described previously  to determine whether it had adsorbed to the KA-I resin.
Solvent desorption and resin regeneration
The resin in the in situ adsorption experiment was collected at the end of the fermentation and washed gently with 100 mL of deionized water. Subsequently, the resin was soaked in 500 mL of methanol and agitated at 200 rpm for 30 minutes at 25°C. The supernatant liquids were filtered and analyzed by gas chromatography. The solvents adsorbed to the resin packed in the glass columns were desorbed in a fixed-bed mode using one bed volume of 85% (v/v) methanol. The solvent recovery from the KA-I resin was >99%. The resin could be regenerated using two bed volumes of water (for details, see ).
Metabolite analyses and calculations
The cell concentration was determined spectrophotometrically as the OD600nm. The concentrations of glucose, acetate, and other organic acids were determined by HPLC analysis (Agilent 1100 series, Hewlett-Packard, California, USA), using an Aminex HPX-87H ion exclusion column (300 × 7.8 mm; Bio-Rad Laboratories, Hercules, CA, USA) heated to 50°C. The analytes were separated with a mobile phase of 5.0 mM H2SO4 at 0.6 mL/minute and detected using a refractive index detector. Acetone, ethanol, butanol, butyric acid, and acetoin were analyzed using gas chromatography (7890A, Agilent, Wilmington, DE, USA) equipped with a flame ionization detector and an Agilent HP-INNOWAX column (0.25 mm × 60 m).
The equivalent solvent concentration was calculated as the total amount of solvent produced, including the aqueous volume and the adsorbed mass (g) divided by the total volume of medium (L) in the fermentor, cell separator, and samples. The solvent productivity was calculated as the equivalent solvent concentration (g/L) divided by the fermentation time (h). The yield was calculated as the total mass of solvent (ABE and acetoin) produced (g) divided by the total mass of glucose utilized (g).
High performance liquid chromatography
Reduced nicotinamide adenine dinucleotide (phosphate)
Scanning electron microscopy.
This work was supported by the National Outstanding Youth Foundation of China (Grant No. 21025625), the National High-Tech Research and Development Program of China (863) (Grant No. 2012AA021203), the National Basic Research Program of China (973) (Grant No. 2013CB733602), the Major Research Plan of the National Natural Science Foundation of China (Grant No. 21390204), The National Technology Support Program (Grant No. 2012BAI44G01), the National Natural Science Foundation of China, General Program (Grant No. 21376118), the National Natural Science Foundation of China, Youth Program (Grant No. 21106070), the Program for Changjiang Scholars and Innovative Research Team in University (Grant No. IRT1066), Jiangsu Provincial Natural Science Foundation of China (Grant No. SBK 201150207), and the Priority Academic Program Development of Jiangsu Higher Education Institutions (PAPD). Dong Liu was supported by the Research Innovation Program for College Graduates of Jiangsu Province (CXLX12_0451).
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