Production of poly(3-hydroxybutyrate) by high cell density fed-batch culture of Alcaligenes eutrophus with phospate limitation

High cell density fed-batch fermentation of Alcaligenes eutrophus was carried out for the production of poly(3-hydroxybutyrate) (PHB) in a 60-L fermentor. During the fermentation, pH was controlled with NH(4)OH solution and PHB accumulation was induced by phosphate limitation instead of nitrogen limitation. The glucose feeding was controlled by monitoring dissolved oxygen (DO) concentration and glucose concentration in the culture broth. The glucose concentration fluctuated within the range of 0-20 g/L. We have investigated the effect of initial phosphate concentration on the PHB production when the initial volume was fixed. Using an initial phosphate concentration of 5.5 g/L, the fed-batch fermentation resulted in a final cell concentration of 281 g/L, a PHB concentration of 232 g/L, and a PHB productivity of 3.14 g/L . h, which are the highest values ever reported to date. In this case, PHB content, cell yield from glucose, and PHB yield from glucose were 80, 0.46, and 0.38% (w/w), respectively. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 28-32, 1997.     

Multi-stage high cell continuous fermentation for high productivity and titer

We carried out the first simulation on multi-stage continuous high cell density culture (MSC-HCDC) to show that the MSC-HCDC can achieve batch/fed-batch product titer with much higher productivity to the fed-batch productivity using published fermentation kinetics of lactic acid, penicillin and ethanol. The system under consideration consists of n-serially connected continuous stirred-tank reactors (CSTRs) with either hollow fiber cell recycling or cell immobilization for high cell-density culture. In each CSTR substrate supply and product removal are possible. Penicillin production is severely limited by glucose metabolite repression that requires multi-CSTR glucose feeding. An 8-stage C-HCDC lactic acid fermentation resulted in 212.9 g/L of titer and 10.6 g/L/h of productivity, corresponding to 101 and 429% of the comparable lactic acid fed-batch, respectively. The penicillin production model predicted 149% (0.085 g/L/h) of productivity in 8-stage C-HCDC with 40 g/L of cell density and 289% of productivity (0.165 g/L/h) in 7-stage C-HCDC with 60 g/L of cell density compared with referring batch cultivations. A 2-stage C-HCDC ethanol experimental run showed 107% titer and 257% productivity of the batch system having 88.8 g/L of titer and 3.7 g/L/h of productivity. MSC-HCDC can give much higher productivity than batch/fed-batch system, and yield a several percentage higher titer as well. The productivity ratio of MSC-HCDC over batch/fed-batch system is given as a multiplication of system dilution rate of MSC-HCDC and cycle time of batch/fed-batch system. We suggest MSC-HCDC as a new production platform for various fermentation products including monoclonal antibody.     

固定化米根霉发酵制L-乳酸

采用海藻酸钙包埋法固定化米根霉（Ｒｈｉｚｏｐｕｓｏｒｙｚａｅ）,菌体在颗粒表面形成一层菌丝膜,有利于氧气和其它营养物质的传递;三相流化床生物反应器结构简单、动力消耗低、反应器内物质混合均匀、氧传递量大于固定化米根霉的需氧量,非常适合好氧的固定化米根霉发酵。利用它进行重复使用固定化米根霉的间歇发酵或连续发酵制备Ｌ 乳酸,整个过程一般可持续两周以上。固定化米根霉的产酸速率达１６～１８ｇ／Ｌ ｂｅａｄ．ｈｒ,得率为７０～８０％,反应器生产能力约为传统搅拌罐的３倍。采用海藻酸钙包埋法固定化米根霉在三相流化床生物反应器中进行发酵可以有效地提高Ｌ 乳酸的生产效率,具有良好的工业应用前景。     

Citric acid production by Candida lipolytica Y 1095 in cell recycle and fed-batch fermentors

The effect of dissolved oxygen on citric acid production and oxygen uptake by Candida lipolytica Y 1095 was evaluated in cell recycle and fed-batch fermentation systems. The maximum observed volumetric productivity, which occurred at a dilution rate of 0.06 h(-1), a dissolved oxygen concentration of 80%, and a biomass concentration of 5% w/v, in the cell recycle system, was 1.32 g citric acid/L . h. At these same conditions, the citric acid yield was 0.65 g/g and the specific citric acid productivity was 24.9 mg citric acid/g cell . h. In the cell recycle system, citric acid yields ranged from 0.45 to 0.72 g/g. Both the volumetric and specific citric acid productivities were dependent on the dilution rate and the concentration of dissolved oxygen in the fermentor. Similar productivities (1.29 g citric acid/L . h) were obtained in the fed-batch system operated at a cycle time of 36 h, a dissolved oxygen concentration of 80%, and 60 g total biomass. Citric acid yields in the fed-batch fermentor were consistently lower than those obtained in the cell recycle system and ranged from 0.40 to 0.59 g/g. Although citric acid yields in the fed-batch fermentor were lower than those obtained in the cell recycle system, higher citric:isocitric acid ratios were obtained in the fed-batch fermentor. As in the cell recycle system, both the volumetric and specific citric acid productivities in the fed-batch fermentor were dependent on the cycle time and dissolved oxygen concentration. (c) 1995 John Wiley & Sons, Inc.     

Conversion of acid hydrolysate of oil palm empty fruit bunch to L-lactic acid by newly isolated Bacillus coagulans JI12

Cost-effective conversion of lignocellulose hydrolysate to optically pure lactic acid is commercially attractive but very challenging. Bacillus coagulans JI12 was isolated from natural environment and used to produce L-lactic acid (optical purity?>?99.5 %) from lignocellulose sugars and acid hydrolysate of oil palm empty fruit bunch (EFB) at 50 °C and pH 6.0 without sterilization of the medium. In fed-batch fermentation with 85 g/L initial xylose and 55 g/L xylose added after 7.5 h, 137.5 g/L lactic acid was produced with a yield of 98 % and a productivity of 4.4 g/L?h. In batch fermentation of a sugar mixture containing 8.5 % xylose, 1 % glucose, and 1 % L-arabinose, the lactic acid yield and productivity reached 98 % and 4.8 g/L?h, respectively. When EFB hydrolysate was used, 59.2 g/L of lactic acid was produced within 9.5 h at a yield of 97 % and a productivity of 6.2 g/L?h, which are the highest among those ever reported from lignocellulose hydrolysates. These results indicate that B. coagulans JI12 is a promising strain for industrial production of L-lactic acid from lignocellulose hydrolysate.     

Fed-batch sorbose fermentation using pulse and multiple feeding strategies for productivity improvement

Microbial oxidation of D-sorbitol tol-sorbose byAcetobacter suboxydans is of commercial importance since it is the only biochemical process in vitamin C synthesis. The main bottleneck in the batch oxidation of sorbitol to sorbose is that the process is severely inhibited by sorbitol. Suitable fed-batch fermentation designs can eliminate the inherent substrate inhibition and improve sorbose productivity. Fed-batch sorbose fermentations were conducted by using two nutrient feeding strategies. For fed-batch fermentation with pulse feeding highly concentrated sorbitol (600 g/L) along with other nutrients were fed intermittently in four pulses of 0.5 liter in response to the increased DO signal. The fed-batch fermentation was over in 24 h with a sorbose productivity of 13.40 g/L/h and a final sorbose concentration of 320.48 g/L. On the other hand, in fed-batch fermentation with multiple feeds, two pulse feeds of 0.5 liter nutrient medium containing 600 g/L sorbitol was followed by the addition of 1.5 liter nutrient medium containing 600 g/L sorbitol at a constant feed rate of 0.36 L/h till the full working capacity of the reactor. The fermentation was completed in 24 h with an enhanced sorbose productivity of 15.09 g/L/h and a sorbose concentration of 332.60 g/L. The sorbose concentration and productivity obtained by multiple feeding of nutrients was found to be higher than that obtained by pulse feeding and was therefore a better strategy for fed-batch sorbose fermentation.     

Production of mannitol by Lactobacillus intermedius NRRL B-3693 in fed-batch and continuous cell-recycle fermentations

Improved fermentation processes were developed for the production of mannitol by a heterofermentative lactic acid bacterium (Lactobacillus intermedius NRRL B-3693). A fed-batch fermentation protocol overcame limitations caused by high substrate concentrations. The process was developed using corn steep liquor and glucose as inexpensive industrial nutrient sources, supplemented with a small amount of soy peptone and manganese. The fed-batch process resulted in a concentration of 176 ± 0.5 g mannitol from 184 ± 0 g fructose and 92 ± 0.1 g glucose per L of final fermentation broth in 30 h with a volumetric productivity of 5.9 g/(L h). Further increases in volumetric productivity of mannitol were obtained in a continuous cell-recycle fermentation process that reached more than 40 g/(L h), despite reduced mannitol levels of 78–98 g/L and residual substrate of 10–20 g/L. This is the first report of such a high volumetric productivity of mannitol by a heterofermentative lactic acid bacterium.     

Biotransformation of R-2-hydroxy-4-phenylbutyric acid by D-lactate dehydrogenase and Candida boidinii cells containing formate dehydrogenase coimmobilized in a fibrous bed bioreactor

R-2-hydroxy-4-phenylbutyric acid (R-HPBA) is an important intermediate in the manufacture of angiotensin converting enzyme inhibitors. In this work, a recombinant D-lactate dehydrogenase (LDH) was used to transform 2-oxo-4-phenylbutyric acid (OPBA) to R-HPBA, with concomitant oxidation of beta-nicotinamide adenine dinucleotide (NADH) to NAD(+). The cofactor NADH was regenerated by formate dehydrogenase (FDH) present in whole cells of Candida boidinii, which were pre-treated with toluene to make them permeable. The whole cells used in the process were more stable and easier to prepare as compared with the isolated FDH from the cells. Kinetic study showed that the reaction rate was dependent on the concentration of cofactor, NAD(+), and that both R-HPBA and OPBA inhibited the reaction. A novel method for co-immobilization of whole cells and LDH enzyme on cotton cloth was developed using polyethyleneimine (PEI), which induced the formation of PEI-enzyme-cell aggregates and their adsorption onto cotton cloth, leading to multilayer co-immobilization of cells and enzyme with high loading (0.5 g cell and 8 mg LDH per gram of cotton cloth) and activity yield ( > 95%). A fibrous bed bioreactor with co-immobilized cells and enzyme on the cotton cloth was then evaluated for R-HPBA production in fed-batch and repeated batch modes, which gave relatively stable reactor productivity of 9 g/L . h and product yield of 0.95 mol/mol OPBA when the concentrations of OPBA and R-HPBA were less than 10 g/L.     

Optimization of L-phenylalanine production of Corynebacterium glutamicum under product feedback inhibition by elevated oxygen transfer rate.

Production feedback inhibition both on cell growth and on product formation of phenylalanine fermentation might be alleviated by elevated oxygen supply. Batch fermentations by a high phenylalanine producing strain Corynebacterium glutamicum CCRC 18335 at various initial phenylalanine concentrations (P(0)) ranging from 0 to 20 g/L and different oxygen transfer rate coefficients (K(L)a) ranging from 23 to 76 h(-1) were studied. The fermentation parameters with respect to P(0) were strongly dependent on K(L)a. Cell yield favored higher K(L)a and lower P(0). Product yield with respect to varying phenylalanine concentration was evaluated by the relative oxygen availability (ROA). The optimal ROA for phenylalanine formation was strongly dependent on the product concentration. While P(0) was low, the product inhibition was less significant and the maximum product yield occurred while ROA was at 0.5-0.6. While P(0) was high, the product inhibition was significant and the maximum product yield occurred while ROA was at 0.8-0.9. These results suggest that the product feedback inhibition of phenylalanine fermentation processes can be alleviated by a gradual increase in oxygen supply rate while the increasing product concentration is taken into account. The strategy is demonstrated in a fed-batch culture with elevated oxygen supply. The final phenylalanine concentration was 23.2 g/L, which was 45% better than that of the fed-batch fermentation without elevated oxygen supply. Likewise, the maximum productivity was improved by 42% at 0.37 g/(L x h).     

Low-cost propionate salt as road deicer: evaluation of cheese whey and other media constituents

Propionate and acetate salts are environmentally friendly, effective road deicer substitutes for widely used sodium chloride. A low-cost medium, using raw cheese whey and hydrolyzed whey permeate/whey permeate powder as substrates, and corn-steep liquor as a nutrient supplement, was studied for lactic acid production, replacing synthetic lactose and other high-cost nutrients. A non-sterile stage-I fermentation process for improved lactate productivity using an inexpensive commercial medium was performed at a 20-L fermenter level. A lactate yield of 0.98 g/g lactose and a productivity of 1.1 g/L/h was obtained with complete lactose utilization. When synthetic lactate and glucose were used as substrates in propionate and acetate fermentation, a total acid yield of 0.55 g/g glucose and lactate consumed and a batch productivity of 0.22 g/L/h was obtained. A stage-II fermentation process to produce propionate and acetate salts from cheese whey-derived lactate (stage-I fermentation broth) resulted in 1.6%( w/v) propionate after a total of 161 h (stages I and II).     

SSF production of lactic acid from cellulosic biosludges

The use of cellulosic biosludges generated in a Kraft pulp mill was investigated as substrate for lactic acid production by simultaneous saccharification and fermentation (SSF). The effect of the operation mode (batch or fedbatch), the initial liquid to solid ratio (12 or 30 g/g) and the nutrient supplementation (MRS components or none) on several parameters including lactic acid concentration, volumetric productivity and product yields, were evaluated. When the operation was carried out in fedbatch mode with nutrient supplementation and using a LSR(0)=12 g/g, a broth containing 42 g/L was obtained after 48 h with a volumetric productivity of 0.87 g/L h and a product yield of 37.8 g lactic acid/100 g biosludges. In a similar experiment carried out without nutrient supplementation, a lactic acid concentration of 39.4 g/L was obtained after 48 h with a volumetric productivity of 0.82 g/L h and a product yield of 35.5 g L-lactic acid/100 g biosludges.     

L-lactic acid production by Lactobacillus casei fermentation with corn steep liquor-supplemented acid-hydrolysate of soybean meal

Batch and fed-batch fermentation studies were performed to evaluate the potential of corn steep liquor (CSL)-supplemented acid-hydrolysate of soybean meal (AHSM) as an alternative to yeast extract (YE) for the production of L-lactic acid by Lactobacillus casei LA-04-1. The CSL-supplemented AHSM gave an outstanding result in supporting L-lactic acid production from glucose. In the exponential fed-batch fermentation, the concentration, yield and productivity of L-lactic acid were 162.5 g/L, 89.7% and 1.69 g/L per h, respectively, which were lower than those with 20 g/L YE (180 g/L, 90.3%, 2.14 g/L per h) after 96 h of fermentation. However, the raw material cost of the nitrogen resource was estimated as only 25% of that using the YE.     

溶氧对Candida glycerinogenes产甘油发酵过程的影响

研究了溶氧浓度对产甘油假丝酵母分批发酵生产甘油过程的影响。实验结果表明：当溶氧浓度控制在30%时,C. glycerinogenes的甘油产量、得率和产率达到最高,分别为120.7 g/L、0.575 g/g和1.69 g/(L•h),而糖酵解代谢副产物形成最少。当溶氧浓度为10%时,发酵过程呈现出“巴斯德效应”的特征,生成的酵解代谢副产物维持在较高水平。在快速生长阶段,随着溶氧从10%增加到60%,细胞呼吸类型表现为从厌氧呼吸向好氧呼吸转变,酵解代谢副产物依次减少。在生长稳定期,控制的溶氧浓度越高,酵解代谢副产物乙醇、乙酸等的生成减少。分别选用Logistic方程、Luedeking-Piret方程和Luedeking-Piret-like方程,能较好地模拟细胞生长、甘油合成和葡萄糖消耗的动力学过程。     

Enhanced propionic acid production from Jerusalem artichoke hydrolysate by immobilized Propionibacterium acidipropionici in a fibrous-bed bioreactor

Propionic acid is an important chemical that is widely used in the food and chemical industries. To enhance propionic acid production, a fibrous-bed bioreactor (FBB) was constructed and Jerusalem artichoke hydrolysate was used as a low-cost renewable feedstock for immobilized fermentation. Comparison of the kinetics of immobilized-cell fermentation using the FBB with those of fed-batch free-cell fermentation showed that immobilized-cell fermentation gave a much higher propionic acid concentration (68.5 vs. 40.6 g/L), propionic acid yield (0.434 vs. 0.379 g/g) and propionic acid productivity (1.55 vs. 0.190 g/L/h) at pH 6.5. Furthermore, repeated batch fermentation, carried out to evaluate the stability of the FBB system, showed that long-term operation with a high average propionic acid yield of 0.483 g/g, high productivity of 3.69 g/L/h and propionic acid concentration of 26.2 g/L were achieved in all eight repeated batches during fermentation for more than 200 h. It is thus concluded that the FBB culture system can be utilized to realize the economical production of propionic acid from Jerusalem artichoke hydrolysate during long-term operation.     

Dissolved-oxygen-stat fed-batch fermentation of 1,3-dihydroxyacetone from glycerol by Gluconobacter oxydans ZJB09112

This study investigated the effects of DO concentration on DHA fermentation and of DO-stat fed-batch fermentation using a pH control strategy, on 1,3-dihydroxyacetone (DHA) production. The results showed that DO-stat fed-batch fermentation with pH-shift control was the optimal bioprocess for DHA production. DO-stat fed-batch fermentation was carried out at 30% air saturation, and the culture pH was automatically maintained at pH 6.0 during the first 20 h and then shifted to pH 5.0 until the end of the fermentation. An optimal DHA concentration of 175.9 ± 6.7 g/L, with a production yield to glycerol of 0.87 ± 0.04 g/g, was obtained at 72 h of DO-stat fed-batch fermentation at 30°C in a 15 L fermenter.     

Lactic acid production directly from starch in a starch-controlled fed-batch operation using Lactobacillus amylophilus

Based on the batch results, we constructed a simplified simultaneous saccharification and fermentation (SSF) model for the simulation of lactic acid production directly from unhydrolyzed potato starch using Lactobacillus amylophilus. The results of batch operation at different initial starch concentrations (20, 40 and 60 g/l) indicated that a higher initial starch concentration would lead to a slightly lower productivity, but would largely decrease the yield. Among that, the batch with 20 g/l of initial starch had the maximum productivity and the maximum yield, which would be 0.31 g/(l h) and 98% (g/g), respectively. In view of increasing the productivity and the final lactic acid concentration, a starch-controlled fed-batch operation with 20 g/l of initial starch was performed. It showed the fed-batch operation with starch controlled at 8 ± 1 g/l by adjusting the starch-feeding rate led to the maximum productivity of 0.75 g/(l h) and the yield of 69%.     

Co-culturing of Lactobacillus paracasei subsp. paracasei with a Lactobacillus delbrueckii subsp. delbrueckii Mutant to Make High Cell Density for Increased Lactate Productivity from Cassava Bagasse Hydrolysate

To increase the productivity of lactic acid, a co-culture of lactobacilli was made by mixing 1:1 ratio of Lactobacillus paracasei subsp. paracasei and a fast growing L. delbrueckii subsp. delbrueckii mutant. The culture was embedded on to polyurethane foam (PUF) cubes as a biofilm and used for fermentation. In order to prevent the cell leakage, the PUF cubes were further entrapped in calcium cross-linked alginate. The maximum lactic acid production using a high cell density free culture was >38 g l(-1) from ~40 g l(-1) of reducing sugar within 12 h of fermentation. Using PUF biofilms, the same yield of lactic acid attained after 24 h. When the cubes were further coated with alginate it took 36 h for the maximum yield. Even though, the productivity is slightly lesser with the alginate coating, cell leakage was decreased and cubes were reused without much decrease in production in repeated batches. Using a conventional control inoculum (3%, w/v), it took 120 h to yield same amount of lactic acid.     

Bioethanol from fermentation of cassava pulp in a fibrous-bed bioreactor using immobilized Δldh, a genetically engineered Thermoanaerobacterium aotearoense

There is an increasing worldwide interest in bioethanol production from agricultural, industrial, and urban residues for both ecological and economic reasons. The acid hydrolysis of cassava pulp to reducing sugars and their fermentation to ethanol were evaluated in a fibrousbed bioreactor with immobilized Δldh, a genetically engineered Thermoanaerobacterium aotearoense. A maximum yield of total reducing sugars of 53.5% was obtained after 8 h of hydrolysis at 85oC in 0.4 mol/L hydrochloric acid with a solid-to-liquid ratio of 1:20, which was optimized by using an orthogonal design based on preliminary experiments. In the FBB, the fed-batch fermentation, using glucose as the sole carbon source, gave a maximum ethanol production of 38.3 g/L with a yield of 0.364 g/g in 100 h; whereas the fed-batch fermentation, using xylose as the sole carbon source, gave 34.1 g/L ethanol with a yield of 0.342 g/g in 135 h. When cassava pulp hydrolysate was used as a carbon source, 39.1 g/L ethanol with a yield of 0.123 g/g cassava pulp in185 h was observed, using the fed-batch fermentation model. In addition, for repeated batch fermentation of cassava pulp hydrolysate carried out in the fibrous-bed bioreactor, long-term operation with high ethanol yield and volumetric productivity were achieved. The above results show that the acid hydrolysate of cassava pulp can be used for ethanol production in a fibrous-bed bioreactor, although some inhibition phenomena were observed during the process of fermentation.     

重组巴氏毕赤酵母高密度发酵表达rHSA

对基因工程菌Pichiapastoris的摇瓶发酵条件进行了试验 ,并根据摇瓶发酵的优化结果进行了补料分批高密度发酵。在摇瓶发酵时 ,甲醇诱导基因工程菌P .pastoris表达重组人血清白蛋白的发酵周期为 96h ;甲醇的最佳诱导浓度为 1 0g L ;发酵pH范围为 5 72～ 6 5 9;在摇瓶培养时 ,随着接种量的增加 ,虽然目的蛋白表达量缓慢增加 ,但单位细胞光密度的蛋白产率却明显下降 ,符合y =1 2 941x- 0 50 59方程 (线性相关系数r=0 9789) ,其限制性因子很可能为溶氧。在分批发酵 ,接种量为 1 0 %且种子细胞光密度 (OD60 0 )为 2 0左右时 ,细胞生长的延迟期为 2 1 1h左右 ,细胞生长光密度与培养时间的关系模型为 :y =0 7841e0 .2 3 19t(线性相关系数r=0 .993 6 ) ;在补料发酵时细胞干重浓度可达到 1 1 5g L— 1 6 0g L ,在 1 2 0h重组人血清白蛋白表达量最大达到 3 6g L。     

Improved oxygen transfer and increased l-lactic acid production by morphology control of Rhizopus oryzae in a static bed bioreactor

Rhizopus oryzae was immobilized on a cotton matrix in a static bed bioreactor. Compared with free cells in a stirred tank bioreactor, immobilized R. oryzae in this bioreactor gave higher lactic acid production but lower ethanol production. The highest lactic acid production rate (2.09 g/L h) with the final concentration of 37.83 g/L from 70 g/L glucose was achieved when operating the bioreactor at 700 rpm and 0.5 vvm air. To better understand the relationship between shear effects (agitation and aeration) and R. oryzae morphology and metabolism, oxygen transfer rate, fermentation kinetics, and lactate dehydrogenase activity were determined. In immobilized cell culture, higher oxygen transfer rate and lactic acid production were achieved but lower lactate dehydrogenase activity was found as compared with those in free cell culture operated at the same conditions. These results clearly imply that mass transport was the rate controlling step in lactic acid fermentation by R. oryzae.