反胶团萃取蛋白质技术的反萃过程研究进展

反胶团萃取分离技术是一种新型的生物产品分离技术,本文简要介绍了反胶团萃取蛋白质技术的反萃过程的动力学,重点综述了在提高蛋白质反萃效率方面的研究进展,并对目前存在的问题、发展方向等进行了评述。     

反胶束萃取技术分离胰激肽原酶

研究了用十六烷基三甲基溴化铵（CTAB）/正己醇/正辛烷反胶束溶液萃取和反萃取商业用胰激肽原酶时,水相pH值、离子强度和种类、CTAB浓度和助表面活性剂浓度等因素对分离效率的影响,并从反胶束微观结构给予解释。结果表明：［CTAB］＝0.02 mol•L-1,正己醇／正辛烷(V/V)＝1：5,萃取pH＝9.0,反萃pH＝7.0,萃取［KBr］＝0.1 mol•L-1,反萃［KBr］＝1.5 mol•L-1,反萃取加15％乙醇(V/V)时,萃取率接近100%,反萃取活性回收得率在80%以上。商业用酶的纯化倍数最高为1.97倍,粗酶为7.15倍,且粗酶纯化后比活在200U／mg以上,电泳分析证实了纯化效果,显示了很好的工业前景。     

反胶束萃取血红蛋白的研究

研究了ＣＴＡＢ－正辛醇－正庚烷交束溶液萃取牛血红蛋白（ｐＨｂ）时、ｐＨ值、表面活性剂浓度、助表面活性剂浓度、离子种类和离子强度、溶剂比以及蛋白质浓度等因素对萃取效果的影响,并以蛋白质分子与表面活性剂分子间的相互作用以及反胶束大空间阻碍作用上进行了解释。研究表明,水相ＰＨ值在１０．５￣１２．５之间,ＫＣ１浓度为０．１ｍｏｌ／ｌ,反胶束溶液中表面活性剂浓度为０．０２ｍｏｌ／ｌ,正辛醇与正庚烷之比为０．     

用乙醇消除AOT/异辛烷反胶束体系萃取过程中蛋白质的变性失活

用反胶束技术分离纯化蛋白质,具有高选择性、易于大规模操作等优点,具有良好的工业应用前景。但是离子型表面活性剂形成的反胶束体系萃取蛋白质容易引起蛋白质的变性,这是由于离子型表面活性剂的强电荷作用会导致蛋白质发生变性,从而在两相界面上产生沉淀。这也是离子型反胶束体系用于蛋白质萃取所存在的最大的困难。本文对用AOT/异辛烷反胶束体系从胰酶粗提物中萃取胰蛋白酶进行了研究,通过在反胶束相加入乙醇,解决了反胶束萃取蛋白质时使蛋白质变性失活的问题,并且大大减少了分相的时间。前萃取和反萃取之后的分相时间只需要10分钟左右,简化了实验步骤,优化了实验方法,在工业上的大规模应用成为可能。在本研究中,胰蛋白酶的前萃取率达到90%,反萃取率接近100%。最终得率为88%。纯化后的比活提高了5倍多,从300U/mg左右提高到了1800U/mg。     

AOT/异辛烷反胶束萃取纯化胰蛋白酶及酶变性失活问题的解决

用反胶束技术分离纯化蛋白质,具有高选择性、易于大规模操作等优点,具有良好的工业应用前景。但是离子型表面活性剂形成的反胶束体系萃取蛋白质容易引起蛋白质的变性,这是由于离子型表面活性剂的强电荷作用所导致的。对用AOT/异辛烷反胶束体系从胰酶粗提物中萃取胰蛋白酶进行了研究,通过在反胶束相加入乙醇,解决了反胶束萃取蛋白质时蛋白质变性失活的问题。并且由于乙醇的加入大大减少了分相的时间,简化了实验步骤,优化了实验方法,使此技术在工业上的大规模应用成为可能。通过优化各种实验条件,胰蛋白酶的前萃取率达到90%,反萃取率接近100%。最终得率为88%。纯化后的比活提高了5倍多,从300U/mg左右提高到了1800U/mg。     

苦参碱的反胶束萃取研究

本文探索AOT-异辛烷反胶束萃取苦参碱的最佳工艺和条件,以AOT-异辛烷反胶束对粗苦参碱中的苦参碱进行萃取,利用毛细管电泳对苦参碱进行定量分析,通过正交试验优化萃取工艺和条件,确定影响萃取率的主要因素为萃取水相的酸度,次要因素为水相的温度,反胶束的W0和离子强度对萃取率的影响较小,得出最优萃取条件为:pH=12,W0=30,T=35℃。     

微生物转谷氨酰胺酶(MTGase)的AOT反胶束纯化研究

研究微生物转谷氨酰胺酶(MTGase)反胶束纯化的工艺和条件,调节MTGase离心上清液等电点,除去部分杂蛋白,MTGase活力升高7.5倍;用截留分子量为10000的超滤膜除去小分子杂蛋白,MTGase活力升高1.33倍;用0.05mol/L的AOT/异辛烷反胶束进一步纯化MTGase,其最适萃取条件是粗MTGase蛋白质浓度20mg/mL,[Na ]0.12mol/L,水相pH4.80～5.20,相比1:1(v/v);荷载MTGase的AOT反胶束用2.0mol/LKCl进行反萃取,MTGase活力为14.2U/g,纯化8.875倍;冷冻干燥脱盐反萃取液,获得MTGase冻干粉,其活力为110.3U/g,与粗酶液相比较,纯化689.4倍。经过AOT/异辛烷反胶束萃取纯化的MTGase,其SDS-聚丙烯酰胺凝胶电泳为一条带。Ca2 与表面活性剂非极性尾上丁二酰羰基氧、极性头磺酸基硫氧基氧及MTGase分子表面具有孤电子对的基团的配位结合放大了AOT反胶束的另一种萃取作用——配位萃取,致使其对MTGase的萃取率高于K 而接近Na 。     

反胶束萃取胰蛋白酶的研究

本文以含有反胶束的有机溶剂作为萃取剂,进行了将胰蛋白酶从水相传入有机相,再从有机相传入另一水相的研究。结果表明：影响萃取率的主要因素为水相ｐＨ值、离子强度和种类,以及反胶束溶液中表面活性剂浓度等;在适宜的条件下,酶的单级萃取和反萃取率都很高,显示了良好的工业应用前景。     

乳酸脱氨酶DAB－环己烷反胶束溶液中的活性

研究了兔肌乳酸脱氢酶Ｍ４（ＬＤＨ）在十二胺丁酸盐（ＤＡＢ）－环己反烷胶束溶液中的催化活性。发现ＬＤＨ在ＤＡＢ反胶束中的催化转换数（Ｋｃａｔ）同水溶液中的相近,ＬＤＨ在ＤＡＢ反胶束中的活性随增溶水量的增加而增加,随ＤＡＢ浓度的增加而降低,文中还提出了ＬＤＨ在ＤＡＢ反胶束中的增溶方式。     

生姜蛋白酶提取及反胶束纯化工艺初步研究

本文研究了生姜中生姜蛋白酶的分布及贮藏中的活力变化 ,研究了从新鲜生姜中提取生姜粗蛋白酶及用AOT 异辛烷和CTAB庚烷 /辛醇反胶束萃取该酶的工艺和方法。实验结果指出 :在贮藏茎中生姜蛋白酶的活力为 2 .7μg/mL·min-1,在膨大茎中该酶活力为 0 .6 8μg/mL·min-1,而在幼嫩茎中活力最低 ,仅为0 .4 8μg/mL·min-1。新鲜生姜在 0℃下贮藏 2 4h即完全丧失活力 ,在室温下贮藏 3d后其活力损失达38 2 5 %。用 10倍 0 .2mol/L、pH =6 .0的磷酸缓冲液 (4℃ )三次提取生姜蛋白酶 ,其提取率分别为 6 4 .75 %、14 .2 8%和 5 .2 %。用 6 5 %饱和度的 (NH4) 2 SO4沉淀提取液中的生姜蛋白酶 ,再以 pH 6 .2、0 .1mol/L的柠檬酸缓冲液溶解 ,其比活力达到 4 .2 1(μgPro/ μgPro·min-1)。生姜蛋白酶的 pI =5 .4～ 5 .5 ,在pH 5 .4以上 ,用AOT 异辛烷反胶束不能萃取出生姜蛋白酶 ,但却可以萃取出 71.86 %的杂蛋白。用CTAB庚烷 /辛醇反胶束二次萃取AOT 异辛烷萃余液 ,其蛋白质萃取率为 6 0 .2 5 % ,萃取液中生姜蛋白酶理论比活力达到 4 9.77(μgPro/ μgPro·min-1)。     

Affinity extraction of BSA with reversed micellar system composed of unbound Cibacron Blue

Affinity Cibacron Blue 3GA (CB) dye in aqueous phase was directly transferred to the reversed micelles due to electrostatic interaction between anionic CB and cationic cetyltrimethylammonium bromide (CTAB). The bovine serum albumin (BSA) transfer to the reverse micelles increases significantly in a wide range of pH by the addition of a small amount of CB ( approximately 1.0-7.0% of the total surfactant concentration) to the aqueous phase. For pH < pI, the selectivity can be significantly improved with the presence of affinity CB because no BSA was extracted in the absence of CB. For backward extraction of BSA from the micellar phase with stripping aqueous solution, the addition of 2-propanol to the aqueous phase can recover almost all BSA (98.5%) extracted into the reverse micelles.     

Affinity extraction of proteins with a reversed micellar system composed of Cibacron Blue-modified lecithin

Crude soybean lecithin was used as a novel surfactant to form reversed micelles in n-hexane. Cibacron Blue F-3GA (CB) was directly immobilized to the reversed micelles by a two-phase reaction. The reversed micellar system without CB showed low solubilizing capacity for low molecular weight proteins, lysozyme, and cytochrome c due to the weak electrostatic interactions. The introduction of CB significantly increased the solubilization of lysozyme because of its affinity binding to CB but showed no effect on the solubilization of cytochrome c since it did not bind to CB. Although bovine serum albumin had an affinity for CB, it was not extracted to the reversed micelles containing CB because its high molecular weight resulted in a significant steric hindrance effect. Thus the reversed micellar system had a high selectivity resulting from both biospecific and steric hindrance effects. The extraction yield of lysozyme decreased significantly with increasing ionic strength. Therefore, the back extraction of lysozyme was carried out using a stripping solution with an ionic strength of 0.865 mol/L. The overall recovery yield of lysozyme after back extraction could be increased to 87% by stripping for 2 h. The recovered lysozyme exhibited an activity equivalent to native lysozyme, and its secondary structure was also unchanged.     

Purification of industrial alphaamylase by reversed micellar extraction

The purification of industrial alpha-amylase by liquid-liquid extraction with Aliquat 336 reversed micellar solution as the extractant was studied. Seven kinds of Aliquat 336 reversed micellar solution, formed by using seven kinds of straight chain alkyl alcohols as cosolvent, have been utilized to extract industrial a-amylase. It was found that these seven kinds of reversed micellar solution can all achieve a high protein transfer efficiency in the forward extraction process. After a full forward and backward extraction cycle, however, only the reversed micelles with n-butanol as the cosolvent was found to be able to maintain the activity of alpha-amylase in the stripping solution. By using the reversed micelles of Aliquat 336/isooctane/1% (v/v) n-butanol to perform a full extraction cycle, it was found that 85% of the total activity of alpha-amylase in the industrial a-amylase could be recovered at the end of an extraction cycle and the specific activity of alpha-amylase could be concentrated about 1.5-fold; meanwhile, most of the neutral protease in the industrial a-amylase could be removed. The separation factor of alpha-amylase to neutral protease at the end of an extraction cycle can reach about 10. (c) 1995 John Wiley & Sons, Inc.     

Solubilizing water involved in protein extraction using reversed micelles

The extraction of protein using reversed micelles was investigated in relation to the amount of solubilizing water in the reversed micellar organic phase. The minimal concentration of amphiphilic molecule di-2-ethylhexyl sodium sulfosuccinate (C(20)H(37)O(7)Na) (AOT) required for 100% cytochrome c extraction was recognized. This critical AOT concentration increased with protein concentration in the aqueous phase. On this minimal AOT condition, the molar ratio of solubilizing water to extracted protein was found to be a constant of 3500 under C(KCI) = 1.0 x 10(2) mol . m(-3) in this system. This ratio means the hydrophillic surroundings required for extracting one protein molecule into the micellar organic phase under the suitable pH and salt concentration for the forward extraction. In this regard, AOT molecules seemed to take the part of water solubilizing agent in the reversed micellar extraction. This role of AOT is important to extract protein under the suitable pH and salt concentration. The amount of solubilizing water in the protein-containing system was larger than in the protein-free system. This difference shows that the water molecules accompany the extracted protein into the reversed micellar organic phase at constant ratio 2200 under C(KCI) = 1.0 x 10(2) mol . m(-3), i.e., accompanying water molecules per one extracted protein. The minimal AOT concentration increased with ionic strength. On this minimal AOT condition, the molar ratio of solubilizing water to extracted protein also increased with ionic strength, so that in higher ionic strength, more solubilizing water was required. Then more AOT was required to provide the hydrophillic surroundings for protein. The pH affected the minimal AOT concentration required for 100% protein extraction.     

Important parameters affecting efficiency of protein refolding by reversed micelles

Refolding of denatured RNase A as a model of inclusion bodies was performed by reversed micelles formulated with sodium di-2-ethylhexyl sulfosuccinate (AOT) in isooctane. In the novel refolding process, a solid-liquid extraction was utilized as an alternative to the ordinary protein extraction by reversed micelles based on a liquid-liquid extraction. First, the effects of operational parameters such as concentration of AOT, W(o) (= [H(2)O]/[AOT]), and pH were examined on the solubilization of solid denatured proteins into a reversed micellar solution. The solubilization was facilitated by a high AOT concentration, a high W(o) value, and a high pH in water pools. These conditions are favorable for the dispersion of the solid protein aggregates in an organic solvent. Second, the renaturation of the denatured RNase A solubilized into the reversed micellar solution was conducted by addition of glutathione as a redox reagent. A complete renaturation of RNase A was accomplished by adjusting the composition of the redox reagent even at a high protein concentration in which protein aggregation would usually occur in aqueous media. In addition, the renaturation rates were improved by optimizing water content (W(o)) and the pH of water pools in reversed micelles. Finally, the recovery of renatured RNase A from the reversed micellar solution was performed by adding a polar organic solvent such as acetone into the reversed micellar solution. This precipitation method was effective for recovering proteins from reversed micellar media without any significant reduction in enzymatic activity.     

Reverse micellar extraction of papain with cationic detergent based system: An optimization approach

In this study, reverse micellar extraction of papain model system was performed using cetyltrimethylammonium bromide (CTAB)/iso-octane/hexanol/butanol system to optimize the forward and back extraction efficiency (BEE). A maximum forward extraction efficiency of 55.0, 61.0, and 54% was achieved with an aqueous phase pH of 11.0, 150?mM CTAB/iso-octane and 0.1?M NaCl, respectively. Taguchi’s orthogonal array was applied to optimize the pH of stripping phase, concentration of isopropyl alcohol (IPA) and potassium chloride (KCl) for maximizing BEE. The optimal levels of stripping phase pH, concentration of IPA and KCl were found to be 6, 20% (v/v), and 0.8?M, respectively. Under these optimal levels, the BEE was found to be 88% after which enzyme activity was recovered with 2.5-fold purification. Further optimization was performed using artificial neural network-linked genetic algorithm, where the BEE was improved to 90.52% with pH 6, IPA (%)?=?19.938, and KCl (M)?=?0.729.     

Effect of chaotropes in reverse micellar extraction of kallikrein

Reverse micellar extraction is a promising technique in large-scale bioseparation. However, low recovery and high salt concentration in back extraction limit its application. In CTAB/n-octane/n-hexanol reverse micellar system, the enzyme, pancreatic kallikrein could be effectively enwrapped into reverse micelles in forward extraction, but was difficult to be released during back extraction. In this study, dilute chaotropes (urea and GuHCl) were introduced to enhance the release of enzyme instead of high salts in back extraction. Kallikrein enwrapped in reverse micelles was released effectively in the presence of dilute urea and GuHCl during back extraction. Nearly 100% activity recovery of kallikrein from commercial product was obtained by adding 0.60 M urea, and for kallikrein from crude material, the recovery increased greatly by adding 0.80 M urea and 0.08 M GuHCl in the stripping solution. The mechanism of chaotrope for enhancing the release of enzyme from micelles was explored and dynamic light scatter analysis showed that the chaotrope would influence the sizes of micelles during reverse micellar extraction.     

Studies on the extraction and back-extraction of a recombinant cutinase in a reversed micellar extraction process

This work deals with the extraction and back-extraction of a recombinant cutinase using AOT reversed micelles in isooctane. The effect of pH, ionic strength, AOT concentration and temperature on the extraction and back-extraction of the cutinase was investigated. High extraction (97%) of the cutinase was achieved at pH 7.0 with a 50 mM Tris-HCl buffer solution containing 100 mM KCl, but a low activity was detected in the reversed micellar phase. At pH 9.0, cutinase was extracted (75%) to the reversed micelles with higher activity. Cutinase was recovered (50%) from a reversed micellar phase (100 mM AOT/isooctane) into a 50 mM Tris-HCl buffered solution at pH 9.0 with 100 mM KCl, and 20°C. Protein and cutinase activity global yields of 38 and 45%, respectively, were obtained for the global process, extraction and back-extraction steps, using low ionic strength, pH 9.0, 100 mM AOT and 20°C.Maria das Graças Carneiro da Cunha acknowledges a Ph.D. fellowship from Conselho Nacional de Desenvolvimento Científico e Tecnológico (CNPq) and Centro de Pesquisas Aggeu Magalhães, Brasil. This work was partly financed by the BRIDGE Programme (Contract BIOT-CT91-0274(DTEE)).     

Process optimization for reverse micellar extraction of stem bromelain with a focus on back extraction

In the current study, reverse micellar extraction (RME) for the purification of stem bromelain was successfully achieved using the sodium bis(2‐ethylhexyl) sulfosuccinate (AOT)/isooctane system. A maximum forward extraction efficiency of 58.0% was obtained at 100 mM AOT concentration, aqueous phase pH of 8.0 and 0.2 M NaCl. Back extraction studies on altering stripping phase pH and KCl concentration, addition of counter‐ion and iso‐propyl alcohol (IPA) and mechanical agitation with glass beads indicated that IPA addition and agitation with glass beads have significant effects on extraction efficiency. The protein extraction was higher (51.9%) in case of the IPA (10% v/v) added system during back extraction as compared to a cetyltrimethylammonium bromide (100 mM) added system (9.42%). The central composite design technique was used to optimize the back extraction conditions further. Concentration of IPA, amount of glass beads, mixing time, and agitation speed (in rpm) were the variables selected. IPA concentration of 8.5% (v/v), glass bead concentration of 0.6 (w/v), and mixing time of 45 min at 400 rpm resulted in higher back extraction efficiency of 45.6% and activity recovery of 88.8% with purification of 3.04‐fold. The study indicated that mechanical agitation using glass beads could be used for destabilizing the reverse micelles and release of bromelain back into the fresh aqueous phase. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:845–855, 2014     

Adsorption of BSA on QAE-dextran: equilibria

Equilibrium isotherms for adsorption of bovine serum albumin (BSA) on a strong-base (QAE) dextran-type ion exchanger have been determined experimentally. They were not affected by the initial concentration of BSA but were affected by pH considerably. They were correlated by the Langmuir equation when pH >/= 5.05 and by the Freundlich equation of pH 4.8, which is close to pl approximately 4.8 of BSA. The contribution of ion exchange to adsorption of BSA on the ion exchanger was determined experimentally. The maximum amounts of inorganic anion exchanged for BSA were 1% and 0.4% of the exchange capacity of the ion exchanger at pH 6.9, respectively. Since the effect of the ion exchange on the adsorption appeared small, BSA may be adsorbed mainly by electrostatic attraction when pH >/= 5.05 and by hydrophobic interaction or hydrogen bonding at pH 4.8. When NaCl coexisted in the solution, the shape of the isotherm was similar to the Langmuir isotherm, but it is shifted to the right. When the concentration of NaCl was 0.2 mol/dm(3), BsA was not adsorbed on the resin. When BSA was dissolved in pure water, the saturation capacity of BSA on HPO(4) (2-),-orm resin was about 2 times larger than that for adsorption from the solution with buffer (pH 6.9 and 8.79). The saturation capacity for adsorption of BSA in pure water on HPO(4) (2-) + H(2)O(4) (-)-from resin was much smaller than that from the solution with buffer. The isotherms for univalent Cl(-)-and H(2)PO(4) (-)-form resin was peculiar; that is, the amount of BSA adsorbed decreased with increasing the liquid-phase equilibrium concentration of BSA. (c) 1993 John Wiley & Sons, Inc.