青霉素G亚砜的合成

以青霉素G钾盐为原料,采用15%左右低浓度过氧乙酸为氧化剂合成青霉素G亚砜,反应时间2～2.5h,n(过氧乙酸):n(青霉素G钾盐)=(1.1～1.2):1.0,反应温度和结晶温度在0～5℃,总收率可达96%以上。所得青霉素G亚砜可直接从溶液中结晶析出,解决了产物与反应体系的分离。产品纯度较高。     

青霉素G亚砜二苯甲酯的合成研究

以青霉素G钾为原料制备青霉素G亚砜二苯甲酯。氧化反应优化条件为:n(过氧乙酸)∶n(青霉素G钾)=1.2∶1.0,氧化温度0～5℃,反应时间2h,青霉素G亚砜酸收率为97.3%;酯化反应优化条件为:二氯甲烷的用量为17mL/g青霉素G亚砜,投料比n(二苯甲醇)∶n(青霉素G亚砜)=1.8∶1.0,反应温度为-15℃,反应时间为60min,酯化收率为79.5%,反应总收率为77.4%。此工艺成本低廉,操作安全简便,对工业化生产具有积极意义。     

青霉素G亚砜对甲氧基苄基酯的合成

以青霉素G钾盐为原料,用过氧乙酸进行氧化,得到青霉素G亚砜;再以对甲氧基苄氯对青霉素G亚砜进行酯化,得到青霉素G亚砜对甲氧基苄酯,两步总收率为86%。     

青霉素G亚砜对-硝基苄酯的制备研究

对青霉素G钾制备青霉素G亚砜对-硝基苄酯工艺进行了研究。在青霉素G钾:过氧乙酸(mol)为1∶1.15,氧化温度<5℃,反应时间2 h的条件下,青霉素G亚砜收率为89.0%。酯化反应最佳反应条件为:DMF的用量为4.28 mL/1 g青霉素亚砜,反应温度为室温,青霉素亚砜与对-硝基氯苄的投料比(mol)为1∶1.15,反应时间为24 h,在此条件下酯化收率为80.23%。此方法对于控制产品品质和确保操作安全简便,对工业化生产具有参考意义。     

青霉素G亚砜对-硝基苄酯的合成工艺研究

以青霉素G钾为原料制备青霉素G亚砜对-硝基苄酯.氧化反应的条件为:青霉素G钾与过氧乙酸的投料比(mol)为1:1.15,氧化温度＜5℃,反应时间2h,青霉素G亚砜收率为93.5%;酯化反应最佳反应条件为:DMF的用量为4.28ml/1g青霉素亚砜,青霉素亚砜与对一硝基溴苄的投料比(mol)为1:1.15,反应温度为室温,反应时间为24小时,酯化收率为83.36%,反应总收率为77.92%.此方法可控制产品质量,确保操作安全简便,对工业化生产具有参考意义.     

青霉素G亚砜对甲氧基苄酯的合成研究

以青霉素G钾盐为原料,用对甲氧基苄氯酯化得青霉素G对甲氧基苄酯,不经分离,直接用用过氧乙酸和过氧化氢的混合物进行氧化,酯化氧化两步收率为84.1%;用浓度为17%的过氧乙酸氧化,酯化氧化两步收率为94.0%.本工艺安全、经济、收率高,具有工业应用价值.     

青霉素制备青霉素亚砜的研究

以青霉素G钾盐与低质量分数过氧乙酸为原料氧化制备青霉素亚砜 ,其最佳工艺条件为 :n(C16 H18N2 O4 SK)∶n(CH3CO3H) =1 .0∶( 1 1～ 1 2 ) ,反应温度 0～ 5℃ ,反应时间 2 .0～ 2 5h ,w(CH3CO3H) =8 5% ,w(CH3CO2 H) =1 0 %。青霉素亚砜收率达 96 8%。同时建立了青霉素亚砜的半定量分析方法 ,以硅胶G为固定相 ,以V(CH3CO2 C4 H9 n)∶V(CH3CO2 H)∶V(NaH2 PO4 -H2 O)∶V(C4 H9OH n) =6.0∶2 .0∶1 .0∶0 5为流动相 ,用TLC法对产品进行半定量分析检测 ,并经IR、MS谱图验证了产品结构。     

GCLE中间体青霉素G亚砜对甲氧基苄酯的合成工艺改进

本文研究了目的对合成GCLE中间体青霉素G亚砜对甲氧基苄酯的合成工艺进行改进,提高了反应收率和产物纯度。通过以青霉素G钾盐为原料,四丁基溴化铵为催化剂与对甲氧基苄基氯酯化,再与低浓度过氧乙酸氧化,采用丙酮与正己烷(体积比2:1)重结晶得到目标产物,总收率为85.5%,结果目标产物青霉素G亚砜对甲氧基苄酯通过熔点测定、1H-NMR、IR、元素分析确证其结构特征,发现酯化时加入相转移催化剂四丁基溴化     

青霉素G亚砜酯合成工艺的改进

头孢菌素是一类重要的抗生素 ,它抗菌作用强、疗效高、毒性低 ,有广谱和抗青霉素酶的双重特性 [1]。它们最初由 7-氨基头孢烷酸 ( 7-ACA)为原料来制备 ,成本很高[2 ] 。因此许多人纷纷试探以来源较广、价格相对便宜的青霉素为原料来制备头孢菌素。青霉素亚砜酯 ( 3)是青霉素向头孢菌素转化过程中的一种重要中间体。有关它的合成有很多报道 ,例如青霉素经溴化苄 ( Ph CH2 Br)酯化 ,再将酯化产物用Na IO4 氧化[3 ] 或先将青霉素氧化 ,然后酯化[4 ] 。也有报道用 30 %～ 32 %的过氧乙酸[5]或 35%的过氧化氢 [6]作为制备青霉素亚砜酯的氧化…     

青霉素G亚砜对-硝基苄酯的合成

青霉素G亚砜对—硝基苄酯是合成GCLE的重要中间体 ,可通过以青霉素G为原料 ,用低浓度过氧乙酸氧化 ,再以对—硝基苄氯进行羧基保护获得。本方法既能确保产品质量 ,又有利于安全生产 ,适合于工业化生产     

浊点系统中青霉素水解物系的分配及固定化青霉素酰化酶的稳定性

引言 青霉素是生产β-内酰胺抗生素关键中间体6-氨基青霉烷酸(6-APA)的重要原材料.常规酶法水解工艺的底物为结晶青霉素,水解工艺和青霉素发酵工艺不协调;水解反应在控制pH 7～8的环境中进行,不但消耗中和剂氨而且产生工业废物[1].     

3-环外亚甲基头孢烷酸对硝基苄酯合成工艺的改进

以青霉素G钾盐Ⅰ为原料,与对硝基溴化苄反应生成青霉素G的对硝基苄酯Ⅱ。化合物Ⅱ不需纯化,即行氧化,以过氧化氢代替过氧乙酸,得到4-氧化青霉素G对硝基苄酯(Ⅲ)。在开环反应中,实验了多种酸清除剂,发现用分子筛作催化剂最为简便,可使4-氧化青霉素G对硝基苄酯(Ⅲ)顺利开环生成2-(2-氯亚硫酰基-4-氧-3-苯乙酰氨基氮杂环丁-1-基)-3-甲基-丁-3-烯酸对硝基苄酯(Ⅳ)。化合物Ⅳ不需分离,即与SnCl4反应,闭环生成3-环外亚甲基-7-苯乙酰氨基-5-氧-头孢-2-羧酸-4-硝基苄酯(Ⅴ)。再经还原,得到目标化合物3-环外亚甲基头孢烷酸对硝基苄酯(Ⅵ),总产率34·5%。     

青霉素菌丝中蛋白质酶法水解工艺

采用碱热法溶解青霉素菌丝,研究酶法催化水解菌丝溶解液中蛋白质转化为氨基酸的过程.考察酶种类、溶解液pH值、酶与蛋白质质量比、反应温度和时间等因素对蛋白质水解度的影响,建立最佳水解工艺.结果 表明,酶种类、酶与蛋白质之比、pH、温度和时间均对蛋白质水解过程产生影响.以单酶为催化剂,碱性蛋白酶催化水解效果最好,蛋白质水解度...     

Improved extraction of penicillin G using hydrocarbon sulfoxides

Extraction of penicillin G with sulfoxide extractants, petroleum sulfoxide (PSO) and di‐isooctyl sulfoxide (DISO) was researched systematically. Based on research of the extraction equilibrium of penicillin G, the suitable extraction and re‐extraction conditions were determined, and then extraction cascade and bench‐scale experiments were carried out. The performance of extraction systems composed of PSO and DISO, with sulfonated kerosene as the diluent, is superior to that of n‐butyl acetate owing to the low solubility of these new extractants in water. Their consumption during the extraction process was lower, and the recovery step of extractants from aqueous raffinate was eliminated. Copyright © 2004 Society of Chemical Industry     

GCLE生产中的酯化废水预处理

GCLE生产中的酯化废水由于含有抗菌活性很强的青霉素G钾,严重影响着污水处理站的正常运行。通过酸、碱、氨、醇、氧化剂、加热等处理手段来破坏酯化废水中的青霉素G钾,最后选定氧化废水与酯化废水混合反应的方案,取得了良好效果。该预处理工艺简单易行,并且降低了产品生产成本,挽救了因废水问题即将关闭的GCLE项目。     

Extraction of penicillin G from simulated media by an emulsion liquid membrane process

The extraction of penicillin G from simulated media was performed by water/oil/water (w/o/w) emulsion liquid membranes (ELMs) and studied under various operational conditions in a batch system. The degree of extraction achieved was between 80% and 95% under specific conditions. A concentration of greater than nine times the initial concentration of penicillin G in the external phase was obtained in the internal phase. The pH of the internal aqueous solution, containing a basic salt, was theoretically calculated on the basis of the amount of penicillin G transported into the internal phase. The calculated results agreed with the experimental data well and were used to select a suitable type and concentration of a basic salt in the internal phase to give a pH within the range 5 to 8 where penicillin G was stable after the termination of extraction. The extraction of penicillin G was successfully performed by the ELM process with sodium carbonate in the internal phase.     

Direct extraction of phenylacetic acid from immobilised enzymatic hydrolysis of penicillin G with cloud point extraction

The enzymatic hydrolysis of potassium salt of penicillin G (Pen G) into phenylacetic acid (PAA) and potassium salt of 6‐aminopenicillanic acid (APA) is inhibited not only by the substrate and the product APA but also by the by‐product PAA. The partitioning behaviour of PAA in a cloud point system, a novel two‐phase partitioning system, was determined. Direct extraction of PAA in the process of immobilised penicillin acylase hydrolysis of Pen G without pH control was achieved. Pen G was hydrolysed almost completely and the product APA concentration in the cloud point system was much higher than in the control, suggesting that the cloud point system may be applied as a novel extractive bioreactor for the enzymatic hydrolysis of Pen G. Copyright © 2006 Society of Chemical Industry