色谱反应分离器中青霉素G的水解特性

6-氨基青霉烷酸(6-APA)是半合成青霉素的关键中间体,通常采用固定床反应器在青霉素酰化酶作用下水解青霉素来制备^[1]。由于该反应是典型的产物抑制可逆反应,工业生产中需不断加碱中和苯乙酸,以维持反应在最适pH条件下进行。为进一步提高青霉素的水解速率,除了维持最适反应条件外．消除产物抑制具有重要作用。近年来一些研究者提出采用伴有分离作用的反应分离组合系统水解青霉素 制取6-APA。Ishimura等^[2]采用电渗析膜耦合式生物反应器连续移除苯乙酸．将反应速率提高了近1倍;陈坚等^[3]研究了固定化酶-离子交换组合系统移除苯乙酸过程。本文报道青霉素在生化反应与液相谱分离过程相耦合而形成的色谱反应分离器中的水解特性。     

酶法合成头孢环己二烯

以环己二烯甘氨酸甲酯盐酸盐为酰基供体,7-氨基脱乙酰氧基头孢烷酸为酰基受体,γ－氧化铝为载体的固定化巨大芽孢杆菌胞外青霉素G酰化酶为酰化剂,合成了头孢环己二烯。5％酰基供体,2％酰基受体,每毫升反应物加44IU固定化酶,pH7．5,25℃振荡反应5h,头孢环己二烯产率为81％。苯乙酸、苯氧乙酸和头孢霉素G对酶法合成有不同程度的抑制作用。     

固定化细胞膜反应器生产6－APA的研究

将青霉素酰化酶基因工程菌大肠杆菌A56(pPA22)通过交联截留固定化在由中空纤维膜或平板膜构成的膜反应器内,提高了单位体积反应器的酶活,实现了高浓度青霉素的裂解。采用反冲模式操作的中空纤维膜反应器裂解7．8％医用青霉素钠盐50批,产品6－APA的平均重量收率达到90．1％,纯度达98．6％,50批反应操作后,膜反应器内剩余酶活力仍在80％以上。     

固定化青霉素酰化酶在光-pH敏感可回用两水相中裂解青霉素G为6-APA

两水相体系在发展中存在的关键问题是相体系回收困难.由于生产成本及降低污染的原因, 用过的相体系需要回收和重复使用.用环境敏感型溶解可逆聚合物形成可回用两水相体系是当前是为可行的回收方法。本文在光敏感可回用高聚物PNBC与pH敏感型可回用高聚物PADB形成的两水相体系中进行固定化青霉素酰化酶的相转移催化青霉素G产生6-APA的反应。在这个两水相体系中,通过优化,在1% NaCl 存在下,６－ＡＰＡ的分配系数可达5.78。催化动力学显示,达平衡的时间近7h,反应最高得率约85.3%（pH 7.8, 20℃）。较相近条件下的单水相反应得率提高近20%。在反应过程中,通过底物及产物的分配系数检测,发现底物分配系数变化不大,而产物6-APA及苯乙酸的分配系数发生很大变化,从而引起产物的得率变化。在两水相中,底物及产物主要分配在上相,固定化酶分配在下相,底物青霉素G进入下相经酶催化产生的6-APA及苯乙酸又转入上相,从而解除了青霉素酰化酶催化反应的底物及产物抑制作用,达到提高产物得率的效果。此外,采用固定化酶较固定化细胞效率高,占用下相体积小,较游离酶稳定性高,且完全单侧分配在下相。因此,在两水相中进行固定化酶的催化反应具有明显的优越性。形成两水相的高聚物PNBC通过488 nm 的激光照射或经滤光的450nm 光源照射得到回收;pH敏感型成相聚合物PADB可通等电点 4.1沉淀可实现循环利用,高聚物的回收率在95%-98%之间,按此回收率计算,聚合物可使用60次以上。     

以聚丙烯腈纤维为载体制备固定化青霉素G酰化酶的研究

以酸部分水解聚丙烯腈纤维为载体 ,以戊二醛为交联剂 ,共价键结合制备了固定化胞外青霉素G酰化酶。当水解后的载体中 NH2 基含量为 690 μmol g和含水量为 64%时 ,对酶蛋白的固定量达 1 0 0mg g以上 ,固定化酶的活力达 2 30 0IU g ,酶活力总产率为 30 % ,固定化效率为 56%。酶活力的总产率和固定化率随加酶量的增加而降低。该酶可以将浓度为 2 5%～1 2 5%的青霉素G钾盐水解 98%以上。批投青霉素G钾盐为 1 0g,酶负荷为 1 50IU g(PGK) ,经2 0批水解反应后 ,剩余酶活力为 80 %。用二硫基苏醣醇处理固定化酶 ,对水解青霉素G钾盐的操作稳定性有促进作用。固定化酶的室温保存半衰期为 1 30d。用戊二醛和硼氢化钠溶液处理固定化酶后 ,酶活力的室温保存稳定性有所降低。     

巨大芽孢杆菌青霉素G酰化酶在新型环氧载体ZH-HA上的固定化

巨大芽孢杆菌青霉素G酰化酶共价结合在新型环氧-氨基型载体ZH-HA 上,通过对酶浓度、固定化时间、pH以及缓冲液浓度等条件的考察,确定了最优固定化条件:50 mg比活力6000 U/g的巨大芽孢杆菌青霉素G酰化酶蛋白和1g ZH-HA悬浮于pH 9.01 mol/L磷酸缓冲液,室温搅拌6 h,制得固定化巨大芽孢杆菌青霉素G酰化酶,活力2126 U/g湿载体,活力回收率7.67%.比较研究了固定化酶与原酶性质,原酶最适温度45℃,最适pH为8.0.固定化酶则分别是50℃和9.0,分别比溶液酶偏移5℃、1.0个pH单位.经过40批连续水解青霉素G钾盐,固定化巨大芽孢杆菌青霉素酰化酶仍保持80%的活力,显示出良好的工作稳定性.     

不同反应器裂解青霉素制备6-APA的条件

利用固定化酶或固定化细胞裂解青霉素制备6-APA(6-氨基青霉烷酸),在半合成青霉素工业上有重要意义。但上述反应过程中,反应液的pH逐渐下降,常使反应不能正常进行,因此研究适合的反应器和反应条件非常重     

壳聚糖固定化脲酶研究Ⅱ

从废弃的蟹虾壳中提取壳聚糖,探讨了壳聚糖(载体),戌二醛(交联剂)、脲(保护剂)及给酶量四者之间的最适固定化脲酶条件,并对固定化脲酶的理化性质进行了初步探讨。同时还探讨了引入铜离子保护部分氨基制备的固定化脲酶制成柱式反应器,让底物逆流通过反应柱,考察了相同浓度底物溶液在不同温度下过柱后的转化率。     

固定化大肠杆菌AS1.76青霉素酰化酶的研究

用固定化青霉素酰化酶连续生产6-氨基青霉烷酸(简称6-APA)已有许多报道。近年来关于固定化微生物细胞的研究不断发展。Sato等曾用固定化的产青霉素酰化酶的细胞连续生产6-APA。我们用双功能试剂戊二醛固定化大肠杆菌AS 1.76的青霉素酰化酶,用来水解青霉素G生产6-APA。现将结果报告如下。     

微水——有机溶剂两相体系中消旋萘普生的酶法拆分

研究了微水－有机溶剂两相体系中固定化脂肪酶催化的萘甲酯的立体选择性水解反应,固定化酶活性受载体极性、水含量、有机溶剂的ｌｏｇＰ值,产物抑制的影响,据此构建了一种可以连续拆分产生（Ｓ）－（＋）－萘普生的微水－有机溶剂两相体系。反应在一个具有回路的连续流搅拌反应器中进行,反应器中添加有采用吸附法固定化的脂肪酶,截体为一种弱极性的合成载体,水相连同固定化酶颗粒一起永久保持在反应器中,有机流动相带入底物,     

Performance of a cyclic operated multicolumns recirculated packed bed batch reactor for 6-APA production

The methodology for designing a multicolumns recirculated packed bed batch reactor (MRPBR) system is developed. The performance of the system employing immobilized penicillin-G amidase (IPGA) for the production of 6-APA is studied. The total IPGA activity in the cyclic operated MRPBR system is maintained within a constant range by periodically replacing the oldest column in the system. The reaction time for each cycle of batch reaction is, therefore, maintained within a constant range by employing a sufficient number of columns and independent on the cycle number. The variations of 6-APA production rate is held to a desired level. The production yield of IPGA increases and 6-APA production rate decreases with the number of column installed in the MRPBR system. Both the production yield and production rate increase with the IPGA lifetime in the system. The production yield can be enhanced significantly by extending the batch reaction time. For a system designed to allow the batch reaction to be completed within 240 min, the production yield of IPGA can be 80% higher than that in the stirred tank reactor (STR) system. However, the 6-APA production rate decreases to 55% of that in STR system.     

Immobilization of permeabilized Escherichia coli cells with penicillin acylase activity.

Escherichia coli cells with penicillin acylase activity were sequentially treated at pH 7.8 with aqueous solutions of N-cetyl-N,N,N-trimethylammonium bromide and glutaraldehyde and then immobilized within porous polyacrylamide beads. The immobilized whole cells showed enhanced hydrolysis rates in the conversion of benzylpenicillin to 6-aminopenicillanic acid (6-APA) compared to untreated cells immobilized and used under identical conditions. The immobilized system showed no apparent loss in enzyme activity when used repeatedly over 90 cycles for 6-APA production from 4% benzylpenicillin.     

Mathematical modeling of diffusion and reaction in the hydrolysis of vegetable protein in an immobilized enzyme recycle reactor

Experimental investigation is by far the most effective approach for studying the behavior of physical systems. However, an enzymatic solubilization of vegetable protein is a complex combination of intrinsic problems, of which many are not easily adaptable to experimental investigation. Experimental designs to study enzyme vegetable protein reactions yield data which describe the extramembraneous activity of the immobilized enzyme. In a continuous recycle immobilized enzyme reactor, the microenvironment concentration of the substrate or product in the membrane phase, or the concentrations along the reactor axial length in the bulk phase are not discernible to the experimenter. However, the knowledge of such concentration profiles is important in weighing the significance of such factors as intermembrane diffusion, enzyme loading, wet membrane size, and the mode of operation of the reactor. The simulation of mathematical models, which describe the physical system within the constraints imposed, yields information which is vital to the understanding of the process occurring in the reactor. The kinetics and diffusion of an immobilized thermophilic Penicillium duponti enzyme at pH 3.4-3.7 and 50 degrees C was modeled mathematically. The kinetic parameters were evaluated by fitting a model to experimental data using nonlinear regression analysis. Simulation profiles of the effects of reactor geometry, substrate concentration, membrane thickness, and enzyme leading on the hydrolysis rate are presented. From the profiles generated by the mathematical model, the best operational reactor strategy is recommended.     

Comparative study of controlled pore glass, silica gel and poraver for the immobilization of urease to determine urea in a flow injection conductimetric biosensor system

This study compared the responses of three enzyme reactors containing urease immobilized on three types of solid support, controlled pore glass (CPG), silica gel and Poraver. The evaluation of each enzyme reactor column was done in a flow injection conductimetric system. When urea in the sample solution passed though the enzyme reactor, urease catalysed the hydrolysis of urea into charged products. A lab-built conductivity meter was used to measure the increase in conductivity of the solution. The responses of the enzyme reactor column with urease immobilized on CPG and silica gel were similar and were much higher than that of Poraver. Both CPG and silica gel reactor columns gave the same limit of detection, 0.5 mM, and the response was still linear up to 150mM. The analysis time was 4-5 min per sample. The enzyme reactor column with urease immobilized on CPG gave a slightly better sensitivity, 4% higher than the reactor with silica gel. The life time of the immobilized urease on CPG and silica gel were more than 310h operation time (used intermittently over 7 months). Good agreement was obtained when urea concentrations of human serum samples determined by the flow injection conductimetric biosensor system was compared to the conventional methods (Fearon and Berthelot reactions). These were statistically shown using the regression line and Wilcoxon signed rank tests. The results showed that the reactor with urease immobilized on silica gel had the same efficiency as the reactor with urease immobilized on CPG.     

Agro industrial by-products as flavinogenic stimulators for riboflavin production

Plate and frame filter used as a recirculated batch reactor for the production of 6-APA was studied. Penicillin-G solution was recirculated between the immobilized penicillin-G amidase (IPGA) loaded filter and the pH controlled neutralization tank. As penicillin-G solution flowed convectively through the frames loaded with IPGA particles, penicillin-G was hydrolyzed by IPGA and 6-APA was produced. Because of the large filtration area and short filtration depth of plate and frame filter, the batch hydrolysis reaction was operated at high recirculation flow rate without causing high pressure drop. The effect of recirculation flow rate on 2% penicillin-G hydrolysis was stronger than that on 8% penicillin-G hydrolysis. The amount of IPGA loaded in filter had no significant effect on the production yield of IPGA. The operational stability of IPGA in the filter was very satisfactory. There was no appreciable activity decrease after 25 batches of reaction.     

颗粒状固定化青霉素酰化酶的研究

将巨大芽孢杆菌 (Bacillusmegaterium)胞外青霉素酰化酶通过共价键结合到聚合物载体EupergitC颗粒环氧基团上 ,制成的颗粒状固定化青霉素酰化酶表现活力达 1 40 0 μ/g左右。固定化酶水解青霉素的最适 pH8 0 ,最适温度为 55℃。在pH6 0～ 8 5、温度低于 40℃时固定化酶活力稳定。在 pH8 0、温度 37℃时 ,固定化酶对青霉素的表现米氏常数Ka为 2×1 0 - 2 mol/L ;苯乙酸为竞争性抑制剂 ,抑制常数Kip为 2 8× 1 0 - 2 mol/L ;6 APA为非竞争性抑制剂 ,抑制常数Kia为 0 1 2 5mol/L。固定化酶水解青霉素 ,投料浓度为 8% ,在使用 2 0 0批后 ,保留活力 80 %左右 ,6 APA收率平均达 89 48%。     

Fiber entrapment of naringinase from Penicillium sp. and application to fruit juice debittering

Naringinase from Penicillium sp. was immobilized on cellulose triacetate by the fiber entrapment method. Although the optimum pH (3.7) and optimum temperature (55°C) of the fiber-entrapped enzyme were similar to those of the native form, the immobilized enzyme had better heat stability. Kinetic studies showed that the immobilized enzyme had higher K_m values than its native form. When this immobilized naringinase was successively used in a column reactor for the hydrolysis of ρ-nitrophenyl-α-l-rhamnoside or naringin in a simulated fruit juice system or grapefruit juice, the enzyme column could be operated with satisfactory stability. In addition, when the natural grapefruit juice was recycled through the column reactor, no column blocking or filtering action of the catalyst bed was observed.     

The kinetics of penicillin-V deacylation on an immobilized enzyme

An immobilized Penicillin-V-acylase (commercial name, Novozym 217) with high specificity for the phenoxyacetyl-(V)- side chain was investigated in a recycle reactor and in a batch reactor to find the enzymatic reaction rate as a function of conversion, x, substrate concentration, c(A) (0) and pH. The reaction rate depends strongly on pH, and both products, phenoxy-acetic acid and 6-APA, inhibit the reaction. Nonspecific side reactions amount to only a few per cent when c(A) (0) <150mM and pH& gt; 6.5. The effectiveness factor for commercial-size particles is found to be about 0.65, and a value of 1.3mM is obtained for the equilibrium constant, K(eq), of the deacylation reaction. A kinetic model for the deacylation process which includes the effect of pH and of the reverse (acylation) reaction is proposed. Rate data for particles of different size are fitted to the nonlinear model. Five kinetic parameters and an effective diffusivity for the immobilized enzyme particles are determined.     

An evaluation of different enzymatic cleavage methods for recombinant fusion proteins, applied on des(1–3)insulin-like growth factor I

Different enzymatic methods for cleavage of recombinant fusion proteins were compared. To find an efficient cleavage method, five different fusion proteins were produced. The fusion proteins differed only in the linker region between the fusion partner and the desired product, human des(1–3)insulin-like growth factor I. A cleavage study was performed with enterokinase, plasmin, thrombin, urokinase, and recombinant H64A subtilisin. Significant cleavage was obtained using thrombin, H64A subtilisin, and enterokinase. Thrombin cleavage was studied on a larger scale and des(1–3)IGF-I was recovered at a final yield of 3 mg/L growth medium. Thrombin and enterokinase were also studied as immobilized proteases and they cleaved the fusion proteins with retained activity. To further improve thrombin cleavage, a continuous reactor was constructed, consisting of a closed system with a thrombin column and an ion exchange column in series. Here, the fusion protein circulated while free des(1–3)IGF-I was bound to the ion exchange column after release from the fusion protein. In the reactor, thrombin was as efficient as the free enzyme but gave a diminished rate of product degradation.     

Effect of biocatalyst swelling on the operation of packed-bed immobilized enzyme bioreactor

A general mathematical model was developed for predicting the performance and simulation of a packed-bed immobilized enzyme reactor performing a reaction that follows Michaelis–Menten kinetics with competitive product inhibition. The performance of a packed-bed immobilized enzyme reactor was analyzed taking into account the effect of bed swelling on various diffusional phenomena such as axial dispersion, internal and external mass transfer limitations. The numerical solutions were compared with experimental data obtained for a packed-bed reactor operating with β-galactosidase entrapped in Ca-alginate-K-κ-carrageenan gels for lactose hydrolysis.