从肉桂酸生物发酵液中提取苯乙酮的研究

开展了从肉桂酸生物转化合成苯乙酮过程中的发酵液提取苯乙酮的研究,通过比较溶剂萃取法和水蒸汽蒸馏法提取的特点,提出了水蒸汽蒸馏-溶剂萃取偶合法从发酵液提取苯乙酮的提取分离方法。结果表明,用溶剂萃取法时,经过乙酸乙酯和调节pH前处理、环己烷萃取、浓缩等步骤,苯乙酮的萃取得率为89.0%,萃取溶剂使用量为1 mL发酵液需要1 mL有机溶剂(乙酸乙酯与环己烷之和);而用水蒸汽蒸馏-溶剂萃取偶合法萃取得率为92.1%,萃取溶剂使用量为1 mL,发酵液仅需0.1 mL乙酸乙酯。     

络合萃取法分离发酵液中丙酸

利用络合萃取法对模拟溶液和发酵液中的丙酸分离进行研究。络合剂、稀释剂筛选结果表明:选用甲基三辛基氯化胺(MTAC)为络合剂、正辛醇为稀释剂时,萃取受pH值和无机阴离子影响较小,对丙酸具有较高的选择性。以1.2mol/L的MTAC为萃取有机相,有机相/水相(体积比)为3的条件下,萃取15min即能达到平衡;该系统适用于较高浓度丙酸发酵液萃取,经4级萃取丙酸萃取率达86.2%。     

2,3-丁二醇分离纯化中反应精馏工艺

乙醛-环己烷反应萃取体系能够有效分离发酵液中的2,3-丁二醇。文章重点研究了2,3-丁二醇-乙醛反应萃取液的连续水解精馏工艺,为工业化生产提供理论基础。水解精馏使用阳离子交换树脂HZ732为水解催化剂,以2,4,5-三甲基-1,3-二氧戊环(2,3-丁二醇-乙醛缩醛)水解率为指标,考察了反应段温度、反应段级数、进料速度、进料油水比(2,4,5-三甲基-1,3-二氧戊环和水摩尔比)和回流比的影响。通过实验得到优化水解精馏工艺条件为:反应段平均温度90℃,反应段理论板数为20,进料油水比为0.6,进料速度0.2 h-1。在该条件下2,4,5-三甲基-1,3-二氧戊环水解率为73%,未水解2,4,5-三甲基-1,3-二氧戊环被回收。水解液经精馏得到2,3-丁二醇产品,纯度(质量分数)>96%,总收率≥93%。开发了连续水解精馏工艺,为整个工艺工业化实践提供了参考。     

发酵液絮凝过程絮凝体微尺度与分离性能

为探索发酵液絮凝分离过程规律以提高分离效率,本文在微观层面上研究发酵液絮凝过程中的剪切力、絮凝体尺度对絮凝体过滤分离效果的影响。以小诺霉素发酵液为研究对象,在絮凝过程中改变絮凝体所受的剪切力,使用激光粒度分析仪在0.02～2000 μm尺度内测定不同剪切力下絮凝体的粒度及粒度分布,并测定絮凝体的过滤速率及沉降速率。实验结果显示：絮凝体的粒度随剪切力的增大而减小,絮凝体的粒度分布宽度随剪切力的增大而增大;絮凝体的沉降分离速率随絮凝体粒度的增大而增大;在适度的剪切力下絮凝体有一适度的粒度及粒度分布宽度和较大的密实度,此时絮凝体的过滤分离速率有一最大值。实验结果表明：絮凝过程中的剪切力显著影响絮凝体的粒度、粒度分布和密实度,从而显著影响絮凝体的过滤速率及沉降速率。     

固定化米根霉发酵生产乳酸的研究进展

根霉属中的米根霉是迄今认为生产L-乳酸较为理想的菌种.利用游离的米根霉发酵乳酸时会产生菌种利用率低、生产效率低等一系列不足,因此展开了菌体固定化发酵的研究.目前米根霉固定化发酵工程的研究主要集中于载体的选择和新型生物反应器的研制.本文对此研究进展作了综合评述与讨论,认为米根霉固定化发酵乳酸可以进一步降低生产成本,提高乳酸产率.     

发酵液中鼠李糖脂的活性炭吸附-酸沉淀分离

采用活性炭吸附-酸沉淀法从铜绿假单胞菌发酵液中提取鼠李糖脂。探讨了活性炭吸附鼠李糖脂的热、动力学规律,研究了p H值对活性炭吸附鼠李糖脂的影响及洗脱剂与洗脱时间的选择。结果表明:p H 7.0、吸附温度40—80℃时果壳活性炭的吸附平衡时间为60—140 min,80℃得到最大吸附量40.2 mg/g;酸沉淀能显著提高吸附量,p H 2.0时,果壳活性炭对鼠李糖脂的平衡吸附量提高至120.6 mg/g,一次吸附回收率达76.1%。适宜的洗脱剂为体积分数95%乙醇,洗脱时间为2 h,鼠李糖脂一次洗脱回收率为30.2%。该方法避免了有毒挥发性有机溶剂的使用,是一种经济环保的鼠李糖脂分离提取工艺。     

Oil and fungal biomass dispersion in a stirred tank containing a simulated fermentation broth

The production of γ‐decalactone by the filamentous fungus Trichoderma harzianum involves four phases (oil–water–air–mycelium) and its dispersion is crucial during fermentation. Oil and biomass (when present) dispersion, as a function of the volumetric power drawn (P/V), was characterized, in two; three‐ and four‐phase systems agitated with Rushton turbines. Trichoderma harzianum mycelium was used as the solid phase in the four‐phase system. Two stages of the fermentation were simulated: the beginning (15% oil and 1.4 kgm^?3 of mycelium) and the end (2% oil and 10.6 kg m^?3 of mycelium). In the two‐phase system, the use of exhausted broth achieved higher oil dispersions at low P/V values as compared with distilled water. Aeration decreased the oil dispersion for the high‐oil system, but enhanced oil dispersion for the low‐oil system. Compared with the P/V used in the actual fermentation (0.2 kW m^?3), a high segregation of the system was observed for the high‐oil/low‐biomass system, due to the difficulty of mixing the thick oil–air emulsion present at the top of the tank. The system simulating the end of the fermentation reached almost complete homogeneity of oil and biomass, a phenomenon due to the high biomass/oil ratio and the biomass acting as an oil carrier. © 2001 Society of Chemical Industry     

Synthesis and characterization of cellulose acetate-polysulfone blend microfiltration membrane for separation of microbial cells from lactic acid fermentation broth

This work is focused on synthesis and characterization of a polymer blend microfiltration membrane for separation of microbial cells from lactic acid fermentation broth in a continuous process. The membranes were prepared by blending hydrophilic cellulose diacetate (CA) polymer with hydrophobic polysulfone (PSF) polymer in wet phase inversion method. Polymers were blended in N-methyl-2-pyrrolidone (NMP) solvent (70 wt.%) where polyethylene glycol was added as a pore former. The membranes were characterized in terms of morphology, porosity, flux and microbial separation capability. The best prepared membrane with PSF/CA weight ratio of 25/75 yielded a pure water flux of 1830 LMH (liter/m² h) and a fermentation broth flux of 1430 LMH at around 1.5 bar TMP (trans-membrane pressure). The membrane was successful in complete retention of microbial cells from the broth in a continuous crossflow membrane module integrated with the fermentor.     

Extraction of whole fermentation broth with karr reciprocating plate extraction column

The conventional equipment employed in the pharmaceutical industry for extracting fermentation broths is the centrifugal extractor. However, a recent case history indicates that the Karr Reciprocating Plate Extraction Column should be considered for such applications. A pharmaceutical company had been using a Podbielniak centrifugal extractor to extract a whole fermentation broth. However, they could not feed the broth to the extractor unless they pretreated the broth by a “hand wash” or a preliminary batch extraction. Subsequently, it required three passes through the centrifugal machine to achieve the desired degree of extraction. On the other hand, with one pass through the Karr Column, essentially complete extraction was achieved. The advantages evident included a 55% reduction in solvent requirements, and substantially less capital cost, utilities cost, maintenance cost, and solvent losses.     

Removal of contaminated organic acids from simulated succinic acid fermentation broth by reactive extraction process: Single- and mixed-solute solution

This work aims to study how to remove the organic acid by-products from simulated fermentation broth containing succinic acid by reactive extraction. Model solutions including single-, binary-, ternary-, and quaternary-solute solutions were used. The broths were reactively extracted using 0.25 mol TOA/kg 1-octanol under pH of 2.45-6.0. The extracted broths were then distillated under vacuum -0.017 MPa with operating temperature between 45 and 65°C. Finally, the distilled broths were crystallized at 4°C and pH of 2.0. The results showed that the purity and yield of succinic acid of 99.10% and 30.25%, respectively, were obtained.     

酯化水解法提取L-乳酸工艺研究

L-乳酸是一种重要的发酵有机酸,又是生产生物可降解材料聚乳酸的原料。采用酯化水解法精制提取L-乳酸,得出成熟的工艺条件：乳酸与甲醇用量比为1∶3.5,乳酸浓度为85%左右,硫酸加入量为总投料量的2.5%左右,酯化时间为2.5 h。在最佳工艺条件下,酯化水解工序总收率由70%提高到85%,且产品质量稳定,经济效益明显提高。     

苯乳酸发酵液脱色工艺及吸附方程的探讨

以脱色率及苯乳酸回收率为指标,研究了4种活性炭对发酵液吸附脱色的影响。通过单因素实验和正交实验对脱色条件进行优化,得到适宜的脱色条件为:活性炭添加质量浓度为0.015 g/L,初始pH值为6.5,温度90℃,脱色时间为30 m in,在此条件下,活性炭AC1脱色苯乳酸发酵液的脱色率为90.5%,苯乳酸回收率为88.6%。对苯乳酸发酵液脱色体系的吸附等温方程进行了研究,其吸附过程以物理吸附为主,遵循Freund lich等温方程。     

用电渗析法从谷氨酰胺模拟发酵液中脱除谷氨酸

为改进微生物发酵法生产谷氨酰胺的流程,提出用电渗析方法来分离谷氨酰胺和谷氨酸。在对混合氨基酸溶液中离子成分进行分析的基础上,预测了此方法的可行性,并通过电渗析方法对模拟发酵液进行实验来验证此预测结果。还考察了在混合物中含有硫酸铵时的情况。通过理论预测和实验验证,可以用电渗析法直接分离谷氨酰胺和谷氨酸,且原料中少量的硫酸铵有利于分离过程的进行。     

D,L-乳酸聚合工艺研究

以D,L-乳酸为原料,采用直接熔融聚合法制备聚乳酸(PDLLA),研究了催化剂种类、用量,聚合时间和温度等工艺条件对PDLLA相对分子质量的影响,并对PDLLA的性能进行了表征。结果表明,以质量分数0．5％(相对D,L-乳酸)氯化亚锡为催化剂,在175℃下反应10 h时,可得到相对分子质量较高的PDLLA。差示扫描量热测试表明,PDLLA无熔点,其玻璃化转变温度为52．72℃,属无定型结构。     

头孢菌素C过滤过程中总过滤时间的优化与控制

针对头孢菌素C(CPC)发酵液在工业生产中难过滤的问题,在收率衡算模型基础上,结合浓差极化机理引入时间参数,针对连续洗滤过程(CFD)建立考虑时间的膜分离过程估算式,并以最短膜处理时间t_min为目标进行了优化求解。结果表明,在优化的膜处理过程中,CPC收率从85%增长到95%所用时间占总处理时间的30%～40%;而前浓缩比a值在0.5～0.8范围内时,总膜过滤时间差别不大。在一个相对较宽的可操作范围内,适当调整前浓缩比或/和调整目标收率,可以对生产过程的时效性及CPC收率、滤液/保留液体积等生产指标进行优化与控制。     

分子蒸馏法分离发酵液中的乳酸

以预处理后乳酸发酵液为对象,用分子蒸馏法来进行乳酸的分离提纯,在pH值为2、温度为80℃、进料速率为150～180 mL/h、真空度在20～80 Pa下得到了纯度为96%、耐热15 min的乳酸,同时分析了乳酸的其它几项指标并做了乳酸产品及标准品的质谱图对比。分析的指标中,完全达到GB 2023—80对乳酸的质量规定,并且乳酸产品与标准品的质谱图吻合很好。     

酸处理后1,3-丙二醇发酵液电渗析脱盐研究

研究了1,3-丙二醇发酵液经酸处理之后电渗析脱盐的情况.经酸处理后发酵液中的盐类由乳酸钠、丁二酸钠、乙酸钠变成硫酸钠,实验证明电渗析脱除酸处理后无机盐较传统工艺中电渗析脱有机盐,速率增大1倍,1,3-丙二醇损失率减小80%,电流效率提高34%,能耗降低38%.     

两性霉素和制霉菌素发酵及添加其发酵液对甘油发酵影响的比较

研究了两性霉素和制霉菌素的发酵过程,比较了添加两性霉素和制霉菌素发酵液对克鲁氏假丝酵母发酵甘油的影响,结果表明两性霉素发酵菌体与制霉菌素发酵菌体的生长过程类似,都存在一个最大值;当两性霉素和制霉菌素发酵至156h和144h时,菌体分别达到最大,但制霉菌素发酵的菌体高于两性霉素发酵的菌体;当两性霉素和制霉菌素发酵至192h时,发酵液中两性霉素和制霉菌素的质量浓度分别达到148μg/mL和181μg/mL。与不添加两性霉素和制霉菌素发酵液的甘油发酵相比,添加两性霉素和制霉菌素发酵液可进一步提高甘油的含量,其甘油质量分数分别增加了0.57%和2.0%;此外,添加制霉菌素发酵液的菌体和甘油含量要高于添加两性霉素发酵液的菌体和甘油含量,而残糖较低,而且添加制霉菌素发酵液的甘油含量比添加两性霉素发酵液的甘油质量分数增加了1.47%。     

Design and manufacture of emulsion liquid membrane based on various amine extractants for separation and extraction of succinic acid from fermentation broth

The aim of this study was to design a new emulsion liquid membrane(ELM) system for the separation of succinic acid from aqueous solutions.The concentration of succinic acid varied from 20 to 60 mmol·L^-1.The prepared ELM system includes tributylamine(TBA) as a carrier,commercial kerosene as a solvent,Span 80 as a surfactant,and Na₂CO₃ as a stripping agent.In order to control the membrane swelling,different values of cyclohexanone were added to the membrane phase.T...