应用Coriolus vericolor菌丝球脱色染料及印染废水的研究

对白腐真菌(Coriolus vericolor)产生漆酶进行〖JP2〗了研究。发现该菌产漆酶的最适初始pH值为45。提高微量元素浓度或添加藜芦醇都可使C.versicolor的产酶能力增加,添加Tween80会有一定的抑制作用。采用C.versicolor菌丝球进行重复分批产酶试验,结果表明菌丝球的稳定性很好,同一批菌丝球可连续利用14次,平均每批酶活力可保持在672U/mL,产酶能力优于聚氨酯泡沫固定化菌丝。将粗酶液用于染料的脱色降解试验,在酶活力为3.3IU/mL〖JP〗,酸性橙浓度为500mg/L条件下,经过24h反应,脱色率达到98.5%;对含弱酸大红和卡布龙红的印染废水进行脱色试验,脱色率也达到了93%。     

混合添加乙醇和H2O2对嗜热子囊菌产过氧化氢酶的影响

在以嗜热子囊菌( T. aurantiacus WSH03-01BC)生产过氧化氢酶的7L罐发酵研 究中,发现混合添加适量的乙醇(75%)和H2O2可以促进菌体产酶.在发酵36h和 48h分别添加0.8%(v/v)的乙醇时,酶活比对照提高了34.3%;当添加乙醇的总量超过2.4 %时 ,对菌体的生长及产酶有明显的抑制作用;在发酵36～60h恒速流加1.6%的乙醇,CAT的酶活 达到2519U/mL,单位细胞产酶能力提高了47.3%;在发酵36h～60h恒速流加1.6%的乙醇并在4 8h混合添加0.4%的H2O2时,CAT的酶活达到2786U/mL,比对照提高了50.1% .     

核茎点霉发酵产纤维素酶的培养基优化

利用响应面分析法对核茎点霉(Phoma putaminum)LYYZ90-19的发酵产酶培养基进行优化。在单因素试验基础之上,通过Box-Behnken试验设计原理,以酶活力值为响应值进行响应面分析,借助Minitab软件对回归模型进行分析,得到优化后的培养基条件:麸皮4.27 g/L,蛋白胨0.79 g/L,K2HPO40.59 g/L。在优化条件下发酵液比酶活13.47 U/mL,而优化前该菌比酶活为7.73 U/mL,比酶活提高了约74.1%。     

用快中子法选育细菌脂肪酶高产菌株

研究了从土壤中筛选产脂肪酶的菌株,利用紫外线,快中子,快中子和磁场复合,γ射线,γ射线和磁场复合诱变,以酶活为筛子进行诱变育种,结果,出发菌酶活较低的一株得到了一株酶活为396．22U/mL的诱变株,此酶活比出发菌株高92倍,并发现比菌对紫外线和快中子比较敏感,而出发菌酶活较高的一株得到了酶活为424．60U/mL发酵液的诱变株,此酶活为出发菌株3．0倍,在此基础上,初步探讨了快中子,γ射线及磁场复合处理在产脂肪酶菌种诱变中的作用,并认为,在产脂肪酶菌株的诱变中快中子诱变更为有效。     

壳聚糖固定化真菌漆酶及其用于处理酚类污染物的研究

Trametessp. AH282在液体培养条件下经邻甲苯胺诱导能有效合成漆酶同工酶A。以壳聚糖为载体,戊二醛为交联剂进行了漆酶A的固定化研究,确定酶固定化适宜条件为：0.1g壳聚糖与15 mL 5%戊二醛交联8 h后,加入30.0U酶固定12h。在此条件下获得的固定化漆酶催化能力为176.4U/g载体,酶活回收率58.5%。与游离酶相比,固定化漆酶与作用底物愈创木酚的亲和力降低,但固定化酶的稳定性有明显改善。固定化漆酶的最适温度为55℃,比游离酶提高5℃;70℃条件下保温8 h,固定化酶保留酶活56.5%,而在相同条件下游离酶酶活明显下降。使用固定化漆酶反应装置进行酚类化合物转化实验,连续进行12批次操作,固定化酶酶活仍保持60%以上,漆酶使用效率明显提高。     

pH值对绿色木霉(Trichoderma viride)产纤维素酶的影响

采用微晶纤维素为唯一诱导性碳源,对绿色木霉(Trichoderma viride)在摇瓶发酵过程中控制与不控制pH产纤维素酶进行比较.控制pH时胞外蛋白浓度为0.72 mg/mL比不控制pH时提高43%;FPA、EG、GB和CBH酶活为15.0U/mL,120.0U/mL,1.75U/mL,0.85U/mL分别是不控制pH时的2.1、2.3、11.7和1.7倍.在不同pH下测定纤维素酶液各酶活,表明pH值显著影响纤维素酶各单酶酶活.在pH2.7时,β-葡萄糖苷酶酶活仅为pH4.8时酶活的4%;pH回调试验结果表明β-葡萄糖苷酶对pH敏感,并在催化功能上发生不可逆变化.对纤维素酶液添加分离得到的各单酶,当添加β-葡萄糖苷酶时最多可以提高FPA酶活20%.因此β-葡萄糖苷酶是影响综合酶活的关键酶.通过拉曼光谱检测出β-葡萄糖苷酶在pH5.0有活性状态下,酶蛋白主链结构主要为a-螺旋和无规则卷曲;在pH2.0没有活性状态下,酶蛋白主链结构的无规则卷曲发生较大变化,a-螺旋也受到一定影响.这说明pH对β-葡萄糖苷酶构象的改变是造成其活性变化的主要原因.     

纳豆激酶液态发酵条件的研究

考察纳豆杆菌在7.5 L发酵罐中分批发酵产纳豆激酶的条件,纳豆激酶酶活采用四肽底物测定。结果表明:纳豆杆菌生长和产酶的适宜条件不一致。发酵过程中发酵罐搅拌转速控制为500 r/min不变,0～12 h时控制pH为8.0、温度为37℃;12～36 h调整pH为7.0、温度为30℃;16 h时补加外源C源,连续发酵36 h。该过程中发酵液中比酶活最高达到3 232 U/mL,与摇瓶发酵相比,比酶活提高了58%。     

里氏木霉与黑曲霉混合发酵产纤维素酶及其水解特性

研究了利用里氏木霉和黑曲霉混合培养产纤维素酶,以黑曲霉孢子悬浮液的不同活化浓度及不同的活化时间来寻找2个菌种发挥最大协同作用的结合点以及所产纤维素酶的水解特性。以里氏木霉单一培养和黑曲霉单一培养为参照进行对比研究。底物为农林废弃物之一的玉米秸秆,经过蒸气爆破预处理后,用作产酶C源。结果表明:黑曲霉孢子悬浮液活化浓度为10个/mL,活化时间为12 h时,滤纸酶比酶活最高,达3.32 U/mL,高于里氏木霉单一培养的2.25 U/mL,β-葡萄糖苷酶比酶活达1.32 U/mL,高于里氏木霉单一培养的0.57 U/mL。为进一步验证混合菌产纤维素酶的水解效果,利用混合菌产纤维酶的酶液及里氏木霉产纤维素酶的酶液进行酶水解实验,当酶用量为20 U/g绝干纤维素,底物质量浓度为100 g/L条件下水解48 h,混合菌所产酶液酶解得率达70.00%,高于里氏木霉所产酶液的酶解得率63.05%。实验表明里氏木霉与黑曲霉混合培养产酶是可行的,并优于单一菌种培养。     

酿酒酵母和米曲霉混合发酵生产a-半乳糖苷酶和转化酶

本研究首次利用酿酒酵母Z-06和米曲霉L-09作为混合菌株, 并通过对液态发酵培养基成分的优化, 使α-半乳糖苷酶和转化酶活力分别达到85.22 U/mL和 563.44 U/mL, 比单菌株发酵产酶活分别提高了5.9倍和8.3倍。     

酿酒酵母和米曲霉混合发酵生产α-半乳糖苷酶和转化酶

本研究首次利用酿酒酵母Z-06和米曲霉L-09作为混合菌株,并通过对液态发酵培养基成分的优化,使α-半乳糖苷酶和转化酶活力分别达到85.22 U/mL和563.44 U/mL.比单菌株发酵产酶活分别提高了5.9倍和8.3倍.     

螺旋纤维床固定化生物反应器同时产酶降解壳聚糖的研究

采用多孔聚酯泡沫固定里氏木霉,在鼓泡柱固定化反应器中同时产酶降解壳聚糖。结果表明通过控制降解时间可以得到不同平均聚合度的降解产物。在28℃,pH4.8,通气量3vvm条件下,利用固定化反应器,在30d内连续进行10批同时产酶降解试验,结果发现壳聚糖酶活力和壳聚糖降解率能保持稳定。每批产生的壳聚糖酶活力平均达到0.15u/mL以上,壳聚糖平均降解率为73%。     

三相鼓泡塔生物反应器培养云芝菌合成漆酶

为了提高云芝菌发酵生产漆酶的效率,提出了一种利用自絮凝菌丝球在三相鼓泡塔生物反应器中重复分批发酵产漆酶的新方法。在优化后的产酶条件下,考察维生素C的添加浓度对漆酶活力的影响,并通过在培养基中添加维生素C进行漆酶多批次培养。研究结果表明,维生素C的添加浓度为1.50mmol/L时,可使漆酶活力提高2.6倍。连续进行了10批培养,每批最大漆酶的活力均在1000 U/mL以上,最高酶活出现在第五批为1919.6 U/mL,总培养时间达25 d。此方法所得漆酶对染料靛蓝具有明显的脱色降解作用,在介体1-羟基苯并三唑（HBT）用量0.10%,漆酶用量100 U/L条件下作用40 min时,靛蓝脱色率达到96.7%。该方法采用的三相鼓泡塔生物反应器性能稳定、菌丝球可重复使用,该方法有利于漆酶的高效、规模化生产。     

Extractive fermentation for improved production of endoglucanase by an intergeneric fusant of Trichoderma reesei/Saccharomyces cerevisiae using aqueous two-phase system

Extractive aqueous two-phase fermentation of endoglucanase, a key enzyme for the conversion of cellulosic substances to fermentable sugars, from an intergeneric fusant of Trichoderma reesei/Saccharomyces cerevisiae is a meaningful approach for better production and simple recovery of this enzyme. A phase composition of 6.5% (w/w) dextran and 7.5% (w/w) polyethylene glycol 6000, having a partition coefficient of 2.89 and 1.31 for endoglucanase from an intergeneric fusant of T. reesei/S. cerevisiae and T. reesei (WT) (being a control in this study), respectively, was chosen for extractive fermentation of the enzyme. Endoglucanase production is higher in medium containing polyethylene glycol (PEG) 6000 than in medium without PEG 6000. Comparative analysis of endoglucanase fermentation by fusant and T. reesei was carried out in shake culture and environment-controlled bioreactor conditions. The fusant produced 0.43U of endoglucanase (overall production: 0.34U) in the top phase of an aqueous two-phase system (ATPS), compared to 0.3U in medium without the phase system in shake culture. In a batch reactor, the endoglucanase level for the fusant in the top phase of ATPS was 0.49U (overall production: 0.40U), compared to 0.38U produced in medium without aqueous two-phase components. To corroborate this study, T. reesei produced 8.41U of endoglucanase (overall production: 5.96U) in the top phase of ATPS, compared to 7.18U in the medium without the phase system in shake culture. On the other hand, in a batch bioreactor, T. reesei produced 10.13U of endoglucanase (overall production: 6.90U) in the top phase of ATPS, compared to 8.56U of the enzyme in medium without aqueous two-phase components. The lower overall enzyme production by T. reesei in the two-phase system might be due to limitation in oxygen transfer to the dispersed phase where the enzyme is produced. A higher cell concentration and a reduced lag phase was obtained in ATPS, compared to a similar medium without phase forming polymers for both the intergeneric fusant of T. reesei/S. cerevisiae and T. reesei.     

Application of image analysis in the fungal fermentation of Trichoderma reesei RUT-C30

Trichoderma reesei was grown in a stirred-tank bioreactor (STB) and a reciprocating plate bioreactor (RPB) at four different agitation speeds. A semiautomatic image analysis protocol that was developed to characterize the mycelium morphology during the fermentation process based on four morphological types (unbranched, branched, entangled, and clumped microorganisms) was applied to study the effect of agitation on the morphology of T. reesei. It was shown via statistical validation that broth samples used for image analysis represented the whole population of the fungi in the bioreactor. High shear was found to be damaging to T. reesei grown in the STB. The gentler shear produced in the RPB was not detrimental to the microorganism even at higher agitation speed. Better productivity was obtained for T. reesei grown in the STB and the highest productivity, 0.121 IU/mL h, was obtained at 400 rpm. The morphological parameter, the hyphal growth unit, was found to be correlated to the productivity. Understanding the effect of agitation on the morphology and productivity of T. reesei could lead to the design of better bioreactors and the selection of operating conditions of bioreactors to optimize the production of cellulase.     

Production of dextransucrase by Leuconostoc mesenteroides immobilized in calcium-alginate beads: I. Batch and fed-batch fermentations

In batch fermentation Leuconostoc mesenteroides immobilized in calcium alginate beads produced a total dextransucrase activity equal to about 93% of that by free, suspended bacterial cells under comparable conditions in a bubble column reactor. Continuous sucrose feeding (5 g/L h) to the immobilized-cell culture in the airlift bioreactor increased production of enzymatic activity by about 107% compared with ordinary batch operation of this reactor. About 14% of the enzymatic activity produced by the immobilized cells appears as soluble activity in the cell-free broth compared with about 40% in case of free cells. In an airlift bioreactor, both the soluble and the intact (sorbed and entrapped) enzymatic activity produced by the immobilized bacterial cells was about 34% greater under automatic pH control, compared to that produced in a bubble column reactor with only manual pH control. During formation of dextran by intact enzyme within cells and beads, declines are observed in apparent enzymatic activity.     

Statistical Optimization of Medium and Fermentation Conditions of Recombinant <Emphasis Type="Italic">Pichia pastoris</Emphasis> for the Production of Xylanase

Recombinant xylanase (rPcXynC) from Pichia pastoris was produced on large-scale by optimizing production-medium composition using statistical experimental methods. Production medium was optimized through the use of statistical methods such as one factor at a time (OFAT), Plackett-Burman design, fractional factorial design (FFD), steepest ascent method (SAM), and response surface methodology (RSM). The optimum medium composition was established to be (g/L); wheat bran 11.62, yeast extract 30, Tween 60.5, DL-β-Phenylalanine 0.5, Thiamine 0.5, FeSO₄ 0.01, KH₂PO₄ 0.66, and KHSO₄ 0.09. The optimum medium composition yielded 3,051 mU/mL of xylanase activity which was three times higher than that obtained from the initial medium composition. Finally, fermentation conditions were examined using the optimized production medium in a laboratory bioreactor. The optimal fermentation conditions were found to be 25ºC, pH 6, 170 rpm and 1 vvm with intermittent feeding of methanol (67.5 mL) and the xylanase activity was 3,683 mU/mL. In repeated-batch fermentation using optimized production medium and fermentation condition, the xylanase activity was 3,680 mU/mL at the first cycle of 96 h harvesting time using 90% of the culture solution. The activity was similarly maintained until the last cycle of 264 h.     

Thermostable lipolytic enzymes production in batch and continuous cultures of Thermus thermophilus HB27

Several studies in laboratory-scale bioreactors are undertaken in order to verify the beneficial effect of thermal spring water in the culture medium of Thermus thermophilus HB27. Two bioreactor configurations, stirred tank and airlift, are investigated to determine the most suitable one to develop a continuous process. Water mineral composition affects the lipolytic enzyme secretion and growth of T. thermophilus HB27 in both bioreactor configurations. Furthermore, the lipolytic activity is strongly enhanced when stirred tank bioreactor is used. Moreover, operation in a stirred tank at an agitation rate of 650 rpm leads to the highest total lipolytic activity (intra- and extracellular enzyme) around 280 U/L after 32 h. Continuous cultures operating in the optimised conditions determined in batch cultures are carried out. It is noticeable that the stirred tank bioreactor was able to operate in a continuous flow mode without operational problems. In addition, the lipolytic activity obtained is about 2-fold higher than that attained in batch cultures.     

Xylanase production by Trichoderma reesei Rut C-30 grown on L-arabinose-rich plant hydrolysates

The suitability of L-arabinose-rich plant hydrolysates as carbon sources and inducers of xylanase production in Trichoderma reesei Rut C-30 was tested. Significantly higher xylanase activities were obtained in cultures on oat husk and sugar beet pulp hydrolysates than on lactose. In batch culture with oat husk hydrolysate and lactose, the xylanase activity was about 9 times higher ( approximately 510 IU/ml) than in lactose ( approximately 60 IU/ml). Even higher xylanase activity ( approximately 630 IU/ml) was obtained when the batch cultivations were done on sugar beet pulp hydrolysate and lactose. In a fed-batch culture using oat husk hydrolysate-lactose the xylanase activity was as high as 1350 IU/ml in 4 days. The cellulase production clearly decreased when T. reesei was cultured on both hydrolysates compared to the cultivation on lactose. Moreover, the relative amounts of the xylanases I-III were similar regardless the used carbon source.     

High concentration cultivation of Bifidobacterium bifidum in a submerged membrane bioreactor

In batch cultures, after 25 h, the maximum cell mass of Bifidobacterium bifidum BGN4 was 4.5 g/L, and the maximum cell count was 3.0 x 10(9) cfu/mL at pH 6.0 and 50 g/L sucrose. To increase the viable counts of bifidobacteria, cell retentive culture was applied using a submerged membrane bioreactor with suction and gas sparging. The maximum mass, count, and productivity of the cells after 36 h were 12.0 g/L, 2.2 x 10(10) cfu/mL, and 6.1 x 10(8) cfu/mL x h, respectively, at the feeding (dilution) rate of 120 mL/h (0.06 h-1) in the feeding medium. The accumulated levels of organic acids and ammonium ions at the end of the cultivation were 1.5 and 1.0 g/L, respectively. The viable counts and volumetric productivity of the cells after the cell retentive culture were 7.3- and 5.1-fold higher, respectively, than the values obtained during batch culture. These high viable counts and volumetric productivities were obtained by maintaining lower concentrations of organic acids and ammonium ions so that the growth of B. bifidum BGN4 was not inhibited. The submerged membrane bioreactor produced the highest viable counts of B. bifidum without membrane fouling and cell damage.