基于途径分析的L-异亮氨酸发酵溶氧控制研究

利用途径分析方法对黄色短杆菌（Brevibacterium flavum）TC-21 生产L-异亮氨酸的途径进行了分析,确定了黄色短杆菌TC-21生产L-异亮氨酸的最佳途径的通量分布,根据途径分析的结果,TCA循环的代谢流量对L-异亮氨酸产量有明显影响,而TCA循环与发酵过程中的溶氧密切相关,因此可以通过控制溶氧来提高L-异亮氨酸产量。在发酵过程的不同阶段,根据菌体生长和产酸的需求,改变TCA代谢流量,可以有效提高产酸率。实验证明,通过溶氧分阶段控制发酵生产L-异亮氨酸,比溶氧恒定控制方式发酵产率提高了15.77％。实验结果说明,用途径分析的结果指导发酵过程中的溶氧可以大幅度提高L-异亮氨酸的产量。     

溶氧对L-苏氨酸发酵的影响

探索溶氧对L-苏氨酸发酵过程的影响及其控制方法。通过摇瓶装液量试验、不同溶氧控制方式考察发酵过程中溶氧对L-苏氨酸合成的影响。采用补料分批发酵工艺发酵L-苏氨酸,利用氨基酸分析仪测定发酵液中L-苏氨酸的产量,通过10L罐补料分批发酵36h,产酸可达118.9g/L,糖酸转化率为47.6%。可以得出溶氧对L-苏氨酸生物合成有重要影响,并建立了最佳溶氧控制条件。     

L-异亮氨酸分批发酵动力学模型的研究

对黄色短杆菌L－异亮氨酸高产菌XQ－4（AHV^rAEC^rSuc^gSG^rEth^rα－AB^rIleHx^r）分批发酵动力学模型进行了研究。建立了比较合理的L－异亮氨酸分批发酵动力学模型,为L－异亮氨酸补料分批发酵最优化的研究奠定基础。     

赤霉素发酵溶氧优化调控研究

为了解溶氧对赤霉素发酵过程影响以及相应工艺优化,采用不同溶氧条件下藤仓赤霉菌Gibberella fujikuroi分批发酵生产赤霉素的过程进行菌丝浓度、残糖浓度和GA3产物浓度检测,并微分运算得出比生长速率与比产物合成速率随发酵时间变化,分析了溶氧对比生长速率与比产物合成速率以及得率的影响,进而提出Gibberella fujikuroi发酵高产的溶氧控制策略:在发酵初始阶段(0–50h)控制溶氧30%左右,以维持较高的菌体生长速率;发酵中后期(50–184h),溶氧控制在15%,以获取菌丝持续较高的GA3合成速率能力。采用这一优化溶氧控制策略,发酵过程中最大菌丝浓度19.24g/L、最终赤霉素浓度2 180mg/L和平均比产物合成速率0.616mg/(g·h),比未优化前发酵分别提高了8.33%、13.25%和4.58%,表明所采取的分阶段溶氧控制策略对促进GA3生产有效。     

L-异亮氨酸发酵代谢分析

通过在5L自控发酵罐上对L-异亮氨酸的发酵过程进行研究,分析了发酵基本特征,并结合菌体形态及发酵控制参数的变化,指出发酵过程中代谢流流向及代谢平衡和可能存在的代谢流迁移,为进一步发酵条件优化和分阶段控制发酵研究奠定基础。     

产生L-异亮氨酸的黄色短杆菌的代谢途径分析

目的:代谢工程要解决的主要问题是改变某些途径中的碳架物质流量或改变碳架物质流在不同途径中的流量分布,其目标就是修饰初级代谢,将碳架物质流导入目的产物的载流途径,以获得产物的最大转化率。方法:利用途径分析方法对黄色短杆菌生产L-异亮氨酸的途径进行了分析。结果:建立了9种基础模型,确定L-异亮氨酸理论最高摩尔产率是1;确定了黄色短杆菌生产L-异亮氨酸的最佳途径的通量分布,并以此为依据进行发酵溶氧控制优化,溶氧分阶段控制发酵生产L-异亮氨酸比溶氧恒定控制方式发酵的产率提高了8.2%。结论:根据途径分析结果,通过改变发酵过程有关参数,可使目的产物产率得到提高。     

L—异亮氨酸发酵对氧需求的研究

L—异亮氨酸主要用于医药和食品行业,是人体八种必需氨基酸之一.合理地供氧L—异亮氨酸产酸多,杂氨基酸量低.以钝齿棒杆菌(Corynebacterium Crenatum)为菌株,在71自动控制发酵罐中分批培养,在1.0—1.5vvm通气量范围内,测得了L—异亮氨酸发酵的多项参数,并对它们之间的关系及控制手段进行综合分析,提出了工业发酵过程中继续提高发酵水平的依据.     

溶氧对L-缬氨酸发酵过程的影响

目的:以黄色短杆菌XV0505为供试菌,探索溶氧对L-缬氨酸发酵过程的影响及其控制策略。方法:利用5L发酵罐,考察了不同溶氧浓度对L-缬氨酸发酵的影响,并采用代谢流分析对其结果进行阐述,提出分阶段溶氧控制策略。结果:采用分阶段溶氧控制策略,即在0～24h溶氧浓度为20%,24～60h溶氧浓度为5%,发酵60h,L-缬氨酸可达到58.36g/L,比5%和20%溶氧浓度下分别提高了18.95%和13.56%。结论:溶氧浓度对L-缬氨酸发酵有重要影响。     

溶氧对Blakeslea trispora分批发酵生产β-胡萝卜素的影响

在摇瓶和5 L发酵罐中研究了溶氧 (DO) 对Blakeslea trispora分批发酵生产β-胡萝卜素的影响,总结了5 L发酵罐中β-胡萝卜素发酵过程中溶氧的变化规律.结果表明,当500 mL摇瓶装液量为50 mL,转速为240 r/min条件下发酵生产β-胡萝卜素产量最大,达到3.416 g/L; 5 L发酵罐中,在搅拌转速为1 000 r/min,通气量为1.5 vvm的条件下,β-胡萝卜素的产量可达到3.712 g/L,略高于摇瓶,这可能是由于5 L发酵罐中的气液传递和混合状况好于摇瓶,促进了产物的合成.     

不同溶氧条件下L-苏氨酸生物合成菌株的代谢流量分析

[目的]探索L-苏氨酸生物合成机理及影响因素.[方法]建立了大肠杆菌L-苏氨酸的代谢流平衡模型,应用MATLAB软件计算出不同溶氧条件下发酵中后期代谢网络的代谢流分布及理想代谢流分布.[结果]5%溶氧条件下,25.5%碳架进入HMP途径,74.5%碳架进入糖酵解途径,获得33.9%质量转化率;20%溶氧条件下,58.08%碳架进入HMP途径,41.92%碳架进入糖酵解途径,获得46.5%质量转化率;[结论]与理想代谢流(88.23%质量转化率)相比,应从菌种改造和发酵控制方面通过改变6-磷酸葡萄糖异构酶借以增加HMP途径代谢流量,通过增加磷酸烯醇式丙酮酸羧化反应代谢流提高天冬氨酸族合成代谢流,减少TCA循环代谢流量,从而达到减少副产物生成,增加L-苏氨酸生物合成的目的.     

Combined dissolved oxygen and pH control strategy to improve the fermentative production of l-isoleucine by Brevibacterium lactofermentum

The effect of both dissolved oxygen (DO) and pH on l-isoleucine production by batch culture of Brevibacterium lactofermentum was investigated. A two-stage agitation speed control strategy was developed, and the isoleucine production reached 23.3 g L⁻¹ in a relative short time (52 h), increased by 11.6% compared to the results obtained in the single agitation speed control process. In order to make sure whether the combination of DO and pH control can boost the production by a mutual effect, different control modes were conducted, based on the data obtained from the two-stage agitation speed control strategy and the analysis of kinetics parameters at different pH values. The results showed that the mode of combining two-stage DO with two-stage pH control strategy was the optimal for isoleucine production. The isoleucine production can reach 26.6 g L⁻¹ at 56 h, increased by 14.3% comparing to that obtained by the single two-stage DO control strategy.     

An energy cost minimizing strategy for fermentation dissolved oxygen control

A cost-minimizing mathematical model for on-line control of dissolved oxygen using agitation speed and aeration rate was developed. In pilot scale monensin fermentation using Streptomyces cinnamonensis, this algortihm provided stable control of dissolved oxygen at 40%, reducing energy usage 27.8%. The agitation and aeration profiles provided by the algorithm respresent the pathway of least energy cost for control at the desired dissolved oxygen level. Other observed advantages of bivariable control were reduction of foaming, evaporation, and gas holdup. Reduced maintenance of compressors and agitator motors could also be expected due to decreased load. Monensin productivity equivalent to fermentation with constant agitation and aeration was not obtained, however, with potency reduced 14.8% with the dissolved oxygen control strategy.List of Symbols A m² cross sectional area of fermentor - A ₁, A ₂, A ₃, A ₄ constants of polynomial fit to Calderbank's equations - BP N/m² gauge back pressure - C _ag $/W/s cost of electrical power - C _Q $/m³ cost of compressed air - CE mol/m³/s carbon dioxide evolution rate - D m impeller diameter - DO, DO _meas, DO _sp % dissolved oxyen saturation at any time, measured, and setpoint respectively - h m height of liquid in fermentor - H N/m²/mmol Henry's constant for oxygen in water - H _av average gas holdup in fermentor - k _L a, k _L a _meas, k _L k _sp s^–1 oxygen mass transfer coefficient at any time, measured, and setpoint respectively - N, N _sp s^–1 agitation speed at any time and setpoint respectively - N _a, N _{a, sp} aeration number at any time and setpoint respectively - N _i total number of impellers - N _p impeller power number - N _s number of impellers into which air is directly sparged - OU, OU _meas mol/m³/s Oxygen uptake rate at any time and measured respectively - P W ungassed agitation power - P _g, P _g,meas, P _g,sp W gassed agitation power at any time, measured, and set point respectively - Q, Q _meas, Q _sp m³/s aeration rate at any time, measured, and setpoint respectively - T K fermentation temperature - u _g m/s linear gas velocity - V m³ fermentation liquid volume - mole fraction of oxygen in fermentation off-gas - calculation constant - motor efficiency - $/s sum of agitation and aeration costs - kg/m³ liquid density     

谷氨酸棒杆菌NAD激酶的过表达对L-异亮氨酸合成的促进作用

NAD激酶催化辅酶Ⅰ[NAD(H)]发生磷酸化,转变成辅酶Ⅱ[NADP(H)],而还原态辅酶Ⅱ(NADPH)是L-异亮氨酸合成的必要辅因子。为了提高NADPH的供应,首先克隆了谷氨酸棒杆菌NAD激酶基因ppnK,并利用大肠杆菌-棒状杆菌诱导型穿梭表达载体pDXW-8和组成型穿梭表达载体pDXW-9在L-异亮氨酸合成菌——乳糖发酵短杆菌JHI3-156中进行表达。摇瓶发酵后,ppnK诱导表达菌JHI3-156/pDXW-8-ppnK的NAD激酶酶活(4.33±0.74 U/g)比pDXW-8空载菌提高了83.5%,辅酶Ⅱ与辅酶Ⅰ的比例提高了63.8%,L-异亮氨酸产量(3.86±0.12 g/L)提高了82.9%;ppnK组成表达菌JHI3-156/pDXW-9-ppnK的NAD激酶酶活(7.67±0.65 U/g)比pDXW-9空载菌提高了2.20倍,辅酶Ⅱ与辅酶Ⅰ的比例提高了1.34倍,NADPH含量提高了21.7%,L-异亮氨酸产量(2.99±0.18 g/L)提高了41.7%。这说明NAD激酶有助于辅酶Ⅱ的供应和L-异亮氨酸的生物合成,这对于其他氨基酸的生产也有一定的参考依据。     

L-异亮氨酸产生菌XQ-4在连续培养中的动力学特性

以黄色短杆菌（Brevibacterium flavum)ATCC14067诱变选育获得的L-异亮氨酸高产菌XQ－4（AHV^rSuc^gSG^rEth^rα-AB^rIleHx^r）在连续培养中进行动力学特性研究,以葡萄糖为限制性底物时,XQ－4菌株的生长符合Monod方程,其最大比生长速率μmax=0.265h^-1,饱和常数Ka=0.789g/L.XQ-4菌株L-异亮氨酸发酵时菌体最大实际转化率Yx=0.499g/g,产物最大实际转化率Yp=0.379g/g。     

Bi-stage control of dissolved oxygen to enhance cyclic adenosine monophosphate production by Arthrobacter A302

Experiments confirmed dissolved oxygen (DO) definitely affects cyclic adenosine monophosphate (cAMP) production by Arthrobacter A302. Production of cAMP by batch fermentation was investigated under various DO conditions. A two-stage DO control strategy was proposed to achieve optimal production of cAMP based on the kinetic analysis: the DO level was controlled at 40% during the first 18?h and then switched to 30%. Relatively high cAMP production (9.9?g?L(-1)) was achieved by applying this strategy. The cAMP productivity (0.14?g?L(-1)?h(-1)) was also successfully improved by 85.1, 59.3, 15.1 and 28.0%, compared to cases in which DO was uncontrolled or DO levels were held at 20, 30 and 40%, respectively. This is the first report of the use of a two-stage DO control strategy in cAMP production, and it was verified to be an effective method for enhancing the cAMP yield via this strain.     

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。     

Enhancement of pyruvate production by Torulopsis glabrata using a two-stage oxygen supply control strategy

The effect of agitation speeds on the performance of producing pyruvate by a multi-vitamin auxotrophic yeast, Torulopsis glabrata, was investigated in batch fermentation. High pyruvate yield on glucose (0.797 g g(-1)) was achieved under high agitation speed (700 rpm), but the glucose consumption rate was rather low (1.14 g l(-1) h(-1)). Glucose consumption was enhanced under low agitation speed (500 rpm), but the pyruvate yield on glucose decreased to 0.483 g g(-1). Glycerol production was observed under low agitation speed and decreased with increasing agitation speed. Based on process analysis and carbon flux distribution calculation, a two-stage oxygen supply control strategy was proposed, in which the agitation speed was controlled at 700 rpm in the first 16 h and then switched to 500 rpm. This was experimentally proven to be successful. Relatively high concentration of pyruvate (69.4 g l(-1)), high pyruvate yield on glucose (0.636 g g(-1)), and high glucose consumption rate (1.95 g l(-1)h(-1)) were achieved by applying this strategy. The productivity (1.24 g l(-1) h(-1)) was improved by 36%, 23% and 31%, respectively, compared with fermentations in which agitation speeds were kept constant at 700 rpm, 600 rpm, and 500 rpm. Experimental results indicate that the difference between the performances for producing pyruvate under a favorable state of oxygen supply (dissolved oxygen concentration >50%) was caused by the different regeneration pathways of NADH generated from glycolysis.     

Effects of dissolved oxygen concentration on lipase production by Rhizopus delemar

Summary The influence of the concentration of oxygen on lipase production by the fungus Rhizopus delemar was studied in different fermenters. The effect of oxygen limitation ( 47 mol/l) on lipase production by R. delemar is large as could be demonstrated in pellet and filamentous cultures. A model is proposed to describe the extent of oxygen limitation in pellet cultures. Model estimates indicate that oxygen is the limiting substrate in shake flask cultures and that an optimal inoculum size for oxygen-dependent processes can occur.Low oxygen concentrations greatly negatively affect the metabolism of R. delemar, which could be shown by cultivation in continuous cultures in filamentous growth form (D_optimal=0.086 h^-1). Continuous cultivations of R. delemar at constant, low-oxygen concentrations are a useful tool to scale down fermentation processes in cases where a transient or local oxygen limitation occurs.Symbols and Abbreviations CO Oxygen concentration in the gas phase at time = 0 (kg·m^-3) - C_{O 2i} Oxygen concentration at the pellet liquid interface (kg·m^-3) - C_{O 2i} Oxygen concentration in the bulk (kg·m^-3) - D Dilution rate (h^-1) - ID_{O 2} Diffusion coefficient for oxygen (m²·s^-1) - dw Dry weight of biomass (kg) - f Conversion factor (rs _{O 2} to oxygen consumption rate per m³) (-) - k Radial growth rate (m·s^-1) - K Constant - kla Volumetric mass transfer coefficient (s^-1) - klA Oxygen transfer rate (m^-3·s^-1) - kl Mass transfer coefficient (m·s^-1) - K _{O 2} Affinity constant for oxygen (mol·m^-3) - K _w Cotton plug resistance (m^-3·s^-1) - M Henry coefficient (-) - NV Number of pellets per volume (m^-3) - R Radius (m) - RO Radius of oxygen-deficient core (m) - RQ Respiration quotient (mol CO₂/mol O₂) - rs _{O 2} Specific oxygen consumption rate per dry weight biomass (kg O₂·s^-1[kg dw]^-1) - rX Biomass production rate (kg·m^-3·s^-1) - SG Soytone glucose medium (for shake flask experiments) - SG ₄ Soytone glucose medium (for tower fermenter and continuous culture experiments) - V Volume of medium (m^-3) - X Biomass (dry weight) concentration (kg·m^-3) - XR _o Biomass concentration within RO for a given X (kg·m^-3) - Y _{O 2} Biomass yield calculated on oxygen (kg dw/kg O₂) - Thiele modulus - Efficiency factor =1-(RO/R)³ (-) - Growth rate (m^-1·s^-1·kg^1/3) - Dry weight per volume of pellet (kg·m^-3)