过程优化提高解脂亚洛酵母积累α-酮戊二酸

目前,应用解脂亚洛酵母发酵生产α-酮戊二酸由于产量和底物转化率低、生产周期长等问题,仍未大规模工业化生产。为了解决这些问题,以研究室诱变选育获得的1株高产α-酮戊二酸的解脂亚洛酵母Yarrowia lipolytica WSH-Z06 C3为出发菌株,考察了该菌株在50 L发酵罐中转速、碳酸钙浓度、溶氧以及补料方式(多节点补料、恒速补料)等因素对α-酮戊二酸积累的影响。结果表明,当转速为300 r/min时,α-酮戊二酸和丙酮酸的产量分别为32.4 g/L和19.66 g/L;碳酸钙质量浓度为20 g/L时,α-酮戊二酸的产量提高至38.55 g/L,丙酮酸降低至8.28 g/L;控制溶氧水平在50%时,α-酮戊二酸产量为42.39 g/L,此时丙酮酸为6.22 g/L。比较高初始甘油浓度和不同的补料发酵策略,发现恒速补料效果最好,发酵144 hα-酮戊二酸产量达到66.27 g/L,丙酮酸产量为20.82 g/L。通过上述发酵过程参数的优化,α-酮戊二酸的产量和底物的转化率比未优化前分别提高了67.3%和4.56%,为解脂亚洛酵母工业化生产α-酮戊二酸提供一定参考。     

毕赤酵母高密度发酵工艺的研究

高密度发酵是毕赤酵母提高蛋白表达量的一种重要策略,发酵工艺是高密度发酵的一个重要因素。采用下列措施均可以有效地提高表达水平：调节基础培养基,采用变pH和变温发酵,提高DO,选择最适的诱导前菌体密度和比生长速率并降低甘油初始浓度和采用分段式指数流加进行调控。选择合适的甲醇补料策略：甲醇限制补料（MLFB）、氧气限制补料（OLFB）、甲醇不限制补料（MNLFB）和温度限制补料（TLFB）。采用两种方式调控补料：诱导阶段菌体生长时,甲醇比消耗速率(qMeOH)为0.02-0.03gg-1h-1,而菌体不生长时,qMeOH采用较高值。     

补料发酵工艺的应用及其研究进展

综述了补料工艺在发酵工业中应用和研究。介绍了补料发酵工艺及其优点,着重讨论了补料发酵动力学和控制理论研究,以期为补料发酵的应用提供充分的参考依据。     

带His-tag的解脂耶氏酵母脂肪酶Lip2在毕赤酵母中的表达及纯化

将去自身信号肽并且N-端带6×His标签的YlLip2基因克隆至表达载体pPIC9K中,电转化GS115获得高效表达脂肪酶His₆-YlLip2的基因工程菌。筛选到的阳性克隆子摇瓶发酵脂肪酶活力最高为400U/ml。对重组毕赤酵母在10 L发酵罐中表达His₆-YlLip2的分批补料发酵工艺进行了初步优化,探讨了培养基、pH、温度对生物量和重组蛋白表达量的影响。结果表明:采用FM22培养基,诱导温度为25℃,pH 5.0,甲醇诱导114 h后His₆-YlLip2的最高酶活力达到3160U/ml。SDS-PAGE分析表明,蛋白的分子量大约为38kDa。重组的His₆-YlLip2经镍柱一步纯化后的纯度达到95.43%,比酶活达到4250U/mg。     

补料工艺对两株法夫酵母菌株产虾青素的影响

【目的】考察不同补料工艺对法夫酵母菌株生长和虾青素合成的影响。【方法】对法夫酵母JMU-VDL668和JMU-MVP14菌株在7 L罐中进行分批及分批补料培养; 同时, 测定发酵过程中生物量、虾青素和葡萄糖含量的变化。【结果】采用恒DO补料, 法夫酵母JMU-VDL668菌株获得的生物量最大(64.6 g/L), 是分批培养的2.2倍; 采用恒pH补料发酵, 虾青素的产量最高(20.6 mg/L), 是分批培养的1.5倍。与JMU-VDL668菌株不同, 虾青素高产菌株JMU-MVP14菌株采用恒pH补料, 获得生物量最大(48.5 g/L), 但虾青素产量大大降低(仅17.5 mg/L); 采用脉冲补料, 虾青素产量最高, 达到414.1 mg/L, 与分批发酵相比提高了200.2%; 采用恒DO补料, 生物量(38.5 g/L)和虾青素产量(403.2?mg/L)增加显著, 与分批发酵相比分别提高了133.1%和192.3%。【结论】不同补料工艺对法夫酵母菌株生产虾青素影响很大。其中, 采用恒pH补料工艺, 法夫酵母JMU-VDL668菌株可以获得最高的虾青素产量, 而采用脉冲补料工艺, 最适于法夫酵母JMU-MVP14菌株发酵生产虾青素。     

重组巴斯德毕赤酵母高密度发酵表达植酸酶

对巴斯德毕赤酵母的高密度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方式的研究。在摇瓶发酵时,最佳种龄为16h,接种量为3％,甲醇的诱导浓度为15g／L,生长阶段最适pH为5．0,诱导阶段最适pH为5．5。在间歇补料、恒速补料、变速补料三种补料方式中以变速流加最优。     

裂殖壶菌发酵产DHA过程呼吸参数的在线检测分析

利用尾气分析仪对发酵过程的尾气中的O2、CO2含量进行实时检测,建立了裂殖弧菌发酵生产DHA过程中的呼吸参数在线检测方法,实现了裂殖壶菌补料分批发酵过程及双阶段供氧控制发酵过程中的呼吸参数在线检测分析。通过呼吸参数在线检测分析,从氧消耗机制方面解释了双阶段氧传递控制工艺能获得较高生物量、油脂和DHA含量的原因,从而为该工艺过程提供了理论指导。根据发酵过程中菌体生长不同时期的呼吸参数的变化情况,建立了基于呼吸商变化的在线补料控制方法,设计了一种基于RQ-Stat的补料工艺。RQ-Stat补料方式最终获得的油脂含量、DHA产量和产率比间歇式补料工艺分别提高了11.58%、12.19%和11.40%。     

植物乳杆菌Lp-2的高密度发酵

高密度培养植物乳杆菌是制作其发酵剂的重要环节。首先,研究了不同的溶氧和pH对植物乳杆菌的分批发酵的影响。在分批发酵的基础上,为进一步提高发酵液中的菌体浓度,进行了补料分批发酵实验。最终通过对蔗糖反馈补料发酵试验对比改造获得了pH反馈补料发酵工艺。此发酵补料工艺可以控制蔗糖残糖量始终处于较低的水平,因此获得了最高的菌体产量。菌体干重达到13.56g/L,较分批培养提高90.05%。     

基于pH的反馈补料方法在谷氨酸发酵中的应用

为简化谷氨酸发酵补料工艺,提出了一种新型的基于pH的补料方式。考察谷氨酸发酵过程中氨消耗量 (x) 和糖消耗量 (y) 发现,两者之间存在较好的线性关系 (y=7.4744x,R2=0.9989),以此为pH反馈补料工艺中补料液中葡萄糖与氨的混合比例,能较好地将谷氨酸发酵过程中葡萄糖浓度稳定在12~21 g/L。比较恒定葡萄糖浓度补料工艺与pH反馈补料工艺发现,采用pH反馈补料工艺进行发酵,葡萄糖转化率、谷氨酸产酸速率分别提高了9.06％和17.5％左右,同时发酵周期缩短2 h以上。     

固态间歇补料乙醇生料发酵新工艺

浓醪发酵是酒精生产的发展方向。与现行酒精厂普遍采用的热蒸煮工艺相比, 生料发酵技术的发展使得浓醪发酵更容易进行。本研究首次在生料发酵中直接采用固态原料间歇补料, 比较了STARGENTM生淀粉水解酶间歇补料工艺和传统无补料工艺, 并对不同补料方式进行了研究。结果表明: 与传统无补料生料发酵工艺相比, 在相同的干基配料浓度30%、相同的生料酶添加量0.22%(W/W)的条件下, 采用15%的起始配料浓度、发酵15~25 h进行间歇补料的新工艺, 酒精产量从17.06%提高到18.50%。该间歇补料优化工艺的建立, 丰富了生料发酵技术的应用。     

Biosensor online control of citric acid production from glucose by Yarrowia lipolytica using semicontinuous fermentation

Our study aimed at the development of an effective method for citric acid production from glucose by use of the yeast Yarrowia lipolytica. The new method included an automated bioprocess control using a glucose biosensor. Several fermentation methodologies including batch, fed‐batch, repeated batch and repeated fed‐batch cultivation were tested. The best results were achieved during repeated fed‐batch cultivation: Within 3 days of cycle duration, approximately 100 g/L citric acid were produced. The yields reached values between 0.51 and 0.65 g/g and the selectivity of the bioprocess for citric acid was as high as 94%. Due to the elongation of the production phase of the bioprocess with growth‐decoupled citric acid production, and by operating the fermentation in cycles, an increase in citric acid production of 32% was achieved compared with simple batch fermentation.     

Citric acid production from sucrose by recombinant Yarrowia lipolytica using semicontinuous fermentation

The genetically modified yeast strain Yarrowia lipolytica H222‐S4(p67ICL1)T5 is able to utilize sucrose as a carbon source and to produce citric and isocitric acids in a more advantageous ratio as compared to its wild‐type equivalent. In this study, the effect of pH of the fermentation broth (pH 6.0 and 7.0) and proteose‐peptone addition on citric acid production by the recombinant yeast strain were investigated. It was found that the highest citric acid production occurred at pH 7.0 without any addition of proteose‐peptone. Furthermore, two process strategies (fed‐batch and repeated fed‐batch) were tested for their applicability for use in citric acid production from sucrose by Y. lipolytica. Repeated fed‐batch cultivation was found to be the most effective process strategy: in 3 days of cycle duration, approximately 80 g/L citric acid was produced, the yield was at least 0.57 g/g and the productivity was as much as 1.1 g/Lh. The selectivity of the bioprocess for citric acid was always higher than 90% from the very beginning of the fermentation due to the genetic modification, reaching values of up to 96.4% after 5 days of cycle duration.     

Repeated fed-batch fermentation using biosensor online control for citric acid production by Yarrowia lipolytica

Biosensor-controlled substrate feeding was used in a citric acid production process with the yeast strain Yarrowia lipolytica H222 with glucose as the carbon source. The application of an online glucose biosensor measurement facilitated the performance of long-time repeated fed-batch process with automated bioprocess control. Ten cycles of repeated fed-batch fermentation were carried out in order to validate both the stability of the microorganism for citric acid production and the robustness of the glucose biosensor in a long-time experiment. In the course of this fermentation with a duration of 553 h, a slight loss of productivity from 1.4 g/(L×h) to 1.1 g/(L×h) and of selectivity for citric acid from 91% to 88% was observed. The glucose biosensor provided 6,227 measurements without any loss of activity.     

Continuous production of citric acid from sugarcane molasses using a combination of submerged immobilized and surface stabilized cultures of Aspergillus niger KCU 520

Summary A high performance fermentation process for the continuous production of citric acid from sugarcane molasses by using the combination of submerged calcium alginate-immobilized and surface-stabilized cultures of Aspergillus niger KCU 520 in a continuous flow horizontal bioreactor is described. The citric acid productivity was dependent on the dilution rate with an optimum value of 0.015/h. Presaturation of fermentation medium with sterile air, in addition to surface aeration, before feeding into the bioreactor enhanced the citric acid productivity. The highest productivity, citric acid product concentration and yield obtained were 1.7 kg M^–3h^–1, 110kg M^–3 and 91% respectively. The cultures were continuously used for 30 days without any apparent loss in citric acid productivity.     

Mathematical modeling of citric acid production by repeated batch culture

A mathematical model has been created for the process of citric acid biosynthesis by yeast (mutant strain Yarrowia lipolytica) cultivated by the repeated batch (RB) method on ethanol under conditions of nitrogen limitation. The model accounts for cell growth as a function of nitrogen concentration in the culture liquid; nitrogen uptake by growing cells; citric acid production; pH control in the fermentor by means of NaOH addition; and changes in system volume. The model represents a system of five nonlinear differential equations. Experimental measurements of cell concentration, citric acid concentration, and cultivation broth volume were used with the least squares method to determine the values of eight model parameters. The parameter values obtained were consistent with literature data and general concepts of cell growth and citric acid biosynthesis. The model has been used to predict optimum RB culture conditions.     

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.     

A novel recycling process using the treated citric acid wastewater as ingredients water for citric acid production

In this study, an integrated process coupling citric acid and methane fermentations was proposed to solve severe wastewater pollution problem in cassava-based citric acid production. The accumulation patterns of the potential and major inhibitors in this process, including organic compounds, volatile fatty acids (VFAs), total ions and pigments were investigated. Both simulation and experimental results indicated that these inhibitors could reach their equilibrium levels after 3–7 fermentation runs when reutilizing the treated citric acid wastewater. As a result, the proposed citric acid fermentation process by recycling the wastewater treated in methane fermentation could be stably operated for more than 15 runs, which could save a large amount of fresh water and relieve the severe wastewater pollution in citric acid production potentially.     

Repeated batch production of citric acid from sugarcane molasses using recycled solid-state surface culture ofAspergillus niger

Summary The recycled solid-state surface fermentation (SSF) culture ofAspergillus niger KCU520 was used for repeated batch production of citric acid from sugarcane molasses. The rate of citric acid production was doubled, reducing the fermentation time to half, compared to the normal single cycle batch submerged or surface fermentation process. About 80% sugar was converted to citric acid in five-day batch fermentation and three batches were carried out with the same fungal mat without any significant loss of productivity.     

Effect of propionic acid on citric acid fermentation in an integrated citric acid–methane fermentation process

In this study, an integrated citric acid-methane fermentation process was established to solve the problem of wastewater treatment in citric acid production. Citric acid wastewater was treated through anaerobic digestion and then the anaerobic digestion effluent (ADE) was further treated and recycled for the next batch citric acid fermentation. This process could eliminate wastewater discharge and reduce water resource consumption. Propionic acid was found in the ADE and its concentration continually increased in recycling. Effect of propionic acid on citric acid fermentation was investigated, and results indicated that influence of propionic acid on citric acid fermentation was contributed to the undissociated form. Citric acid fermentation was inhibited when the concentration of propionic acid was above 2, 4, and 6 mM in initial pH 4.0, 4.5 and, 5.0, respectively. However, low concentration of propionic acid could promote isomaltase activity which converted more isomaltose to available sugar, thereby increasing citric acid production. High concentration of propionic acid could influence the vitality of cell and prolong the lag phase, causing large amount of glucose still remaining in medium at the end of fermentation and decreasing citric acid production.     

Fate and role of ammonium ions during fermentation of citric acid by Aspergillus niger

Stoichiometric modeling of the early stages of the citric acid fermentation process by Aspergillus niger revealed that ammonium ions combine with a carbon-containing metabolite inside the cell, in a ratio 1:1, to form a nitrogen compound which is then excreted by the mycelium. High-performance liquid chromatography analysis identified glucosamine as the product of the relationship between glucose and ammonium during the early stages of the citric acid fermentation process. Slightly acidic internal pHs, extremely low ammonium ion concentrations inside the cell, and glucosamine synthesis come into direct contradiction with the earlier theory of the ammonium pool inside the cell, regarded as responsible for inhibition of the enzyme phosphofructokinase. At later fermentation stages, when the mycelium is involved in a process of fragmentation and regrowth, the addition of ammonium sulfate leads to a series of events: the formation and secretion of glucosamine in elevated amounts, the short inhibition of citrate synthesis, growth enhancement, the utilization of glucosamine, and finally, the enhancement of citric acid production rates. Obviously, the enzymatic processes underlining the phenomena need to be reexamined. As a by-product of the citric acid fermentation, glucosamine is reported for the first time here. Suitable process manipulations of the system described in this work could lead to successful glucosamine recovery at the point of its highest yield before degradation by the fungus occurs.