Kinetics and mass transfer for lactic acid recovered with anion exchange method in fermentation solution

An anion exchange method for lactic acid recovered from lactic acid-glucose solution in an ion-exchange membrane-based extractive fermentation system was examined. The exchange isotherms of anion exchange resins for lactic acid recovered were measured batchwise, and the exchange-desorption kinetics of lactic acid passing through the exchange column was investigated. The determined typical breakthrough and elution curves were measured and simulated by conventional mode. The mass transfer coefficients were identified by numberical method. The effects of the velocity of the fluid on the dynamics were studied. Aqueous NaOH solution was found to be the best solvent for elution. An experiment on anioun exchange from clarified lactic acid fermentation broth was carried out to obtain knowledge of the performance of the ion exchange system from a borth. The ion-exchange mass-transfer coefficient and efficiency from the fermentation broth is found to be lower when compared with aqueous solutions of pure lactic acid. The results show that the separation method with anion exchange resins may be used in the production of lactic acid by fermentation.(c) 1995 John Wiley & Sons, Inc.     

The effects of arginine on protein binding and elution in hydrophobic interaction and ion-exchange chromatography

Arginine is effective in suppressing aggregation of proteins and may be beneficial to be included during purification processes. We have shown that arginine reduces non-specific protein binding in gel permeation chromatography and facilitates elution of antibodies from Protein-A columns. Here we have examined the effects of arginine on binding and elution of the proteins during hydrophobic interaction (HIC) and ion- exchange chromatographies (IEC) using recombinant monoclonal antibodies (mAbs) and human interleukin-6. In the case of HIC, the proteins were bound to a phenyl-Sepharose column in the presence of ammonium sulfate (AS) with or without arginine and eluted with a descending concentration of AS. While use of 1 M AS in the loading buffer resulted in complete binding of the mAb, inclusion of 1 M arginine in loading and equilibration buffer, only when using low-substituted phenyl-Sepharose, resulted in weaker binding of the proteins. While decreasing AS concentration to 0.75 M resulted in partial elution of the mAB, elution was facilitated with inclusion of 0.5-1 M arginine. In the case of IEC, arginine was included in the loading samples. Inclusion of arginine during binding to the IEC columns resulted in a greater recovery and less aggregation even when elution was done in the absence of arginine. These results indicate that arginine enhances elution of proteins bound to the resin, suggesting its effectiveness as a solvent for elution in HIC and IEC.     

谷氨酰胺提取分离研究

谷氨酰胺是一种十分有用的氨基酸,它既可作为治疗药物,又可作为其它合成药物的前体。目前国内以谷氨酸为原料,采用化学合成法生产谷氨酰胺,供作试剂用,产量十分有限。日本用发酵法生产谷氨酰胺,年产1000吨,还有增加趋势。谷氨酰胺的销售价格比较高,经济效益可观。近年来国内有好几个研究小组都在进行谷氨酰胺发酵研究。我们是国内第一个谷氨酰胺研究组,已在5m~3发酵罐上取得中试成功。谷氨酰胺发酵液中混有谷氨酸,而这些少量的谷氨酸采用等电点沉淀法并不能将它们去除,影响谷氨酰胺的纯度。我们采用离子交换树脂法,成功地将谷氨酸从谷氨酰胺和谷氨酸的混合物中分离掉,得到单一的谷氨酰胺。在将发酵液上柱交换之前,必须对发酵液进行预处理,我们试验了4种不同方法,结果表明第4种方法更适合工厂使用。从我们使用过的几种树脂的分离效果及树脂的价格看,考虑到工     

Innovative modular membrane adsorber system for high-throughput downstream screening for protein purification

To develop the most efficient strategy for the purification of proteins, two types of adsorber membrane devices with different functionalities were designed and tested: 8-strips and single spin columns. The most suitable type of membrane adsorber and the optimal chromatographic loading/elution conditions for several target proteins from different biological matrices could be determined simultaneously in microliter scale. Ion exchange (IEX), metal chelate (MC), and Concanavalin A (Con A) modified membrane types were tested in the devices. Bovine serum albumin (BSA) and lysozyme were used as model proteins for investigations of the binding capacity and protein recovery percentage of the 8-strip anion exchange and the cation exchange membrane. The isolation of His(6)-tagged proteins, Bgl-His and GFP-His from fermentation broth and lysate, respectively, was performed using an 8-strip metal chelate affinity membrane loaded with different metal ions. Separation behavior of a ternary protein mixture (BSA, lysozyme, and Bgl-His) was studied in 8-strips IEX and metal chelate membrane chromatography. The Con A affinity devices were developed on the basis of metal chelate membrane spin columns loaded with Cu(2+) ions and investigated using glucose oxidase (GOD) as model protein. In summary, the advantages of the membrane adsorber technology, such as fast processing and easy scale-up, were utilized. The devices made it possible to load the membrane directly with preclarified fermentation broth or cell lysate and separate the protein of interest often in a single step.     

Application of reverse micelle extraction process for amylase recovery using response surface methodology

The effect of different process variables of reverse micelle extraction process like pH, addition of surfactant (AOT) concentration and potassium chloride (KCl) concentration on amylase recovery has been studied and analysed. Solid-state fermentation was used for the production of amylase enzyme. Response surface methodology (RSM) using central composite rotatable design (CCRD) was employed to analyse and optimize the enzyme extraction process. The regression analysis indicates that the effect of AOT concentration, and KCl concentration were significant, whereas the effect of pH was non-significant on enzyme recovery. For the maximum recovery of enzyme, the optimum operating condition for pH, AOT concentration (M) and KCl concentration were 10.43, 0.05 and 1.00, respectively. Under these optimal conditions, the enzyme recovery was 83.16%.     

Recovery of ammonium lactate and removal of hardness from fermentation broth by nanofiltration

Nanofiltration (NF) was investigated as an alternative to desalting electrodialysis (ED) and ion exchange for the recovery of ammonium lactate from fermentation broth. Three commercial NF membranes, NF45, NF70, and NTR-729HF, were characterized with 50 mM NaCl, MgSO(4), and glucose solutions. NF45 membrane was selected because it showed the lowest rejection of monovalent ion, the highest rejection of divalent ion, and the highest rejection of nonpolar molecule. Effects of the operating pressure were investigated in a range of 100-400 psig, on the flux, lactate recovery, and glucose and magnesium removal from a real fermentation broth containing about 1.0 M of ammonium lactate. The flux and recovery rate increased linearly with the pressure. However, lactate rejection also increased with the pressure, lowering the recovery yield. More magnesium ions and glucose were rejected as the pressure was increased, and at 400 psig, for example, magnesium ion was almost completely rejected, highlighting the chance of obviating the necessity of ion exchange to remove hardness, by using NF instead of desalting ED. Membrane fouling was not so severe as expected, considering the complex nature and a rather high concentration of the fermentation broth treated.     

Extraction of penicillin-G by aqueous two-phase partition

Summary Pure potassium penicillin-G solution and penicillin-G fermentation broth were extracted using the aqueous two-phase systems of poly-ethylene glycol and salts. The partition coefficients of penicillin-G were above 10 in both pure solution and broth systems. The partition coefficients of phenyl acetic acid were about 0.25. Cell mass and solid residue in the broth system were partly concentrated around the interfacial region and partly settled to the bottom when under 1000 × g centrifugal force. Accordingly, this technique is a promising alternative for the recovery of penicillins.     

Removal of potassium chloride by nanofiltration from ion-exchanged solution containing potassium clavulanate

In this study, nanofiltration with NF200 membrane was employed to remove KCl from ion-exchanged solutions containing potassium clavulanate. The pore radius of NF200 membrane was estimated to be around 0.39 nm. The effects of operating pressure on separation performance were investigated in a range of 100–400 psig. The influences of cross-flow velocity (0.14–0.70 cm/s), temperature (4–25 °C), and feed composition were also investigated. In all experiments, clavulanate rejection showed high levels from 0.91 to 0.99, while chloride rejection ranged from 0.06 to 0.54. In a case at an operating pressure of 50 psig and 25 °C, as much as 94% of clavulanate was retained while 94% of chloride was removed, indicating that NF200 membrane was a suitable choice for selectively removing KCl. NF200 membrane also showed a stable performance in the operational stability test with an ion-exchanged solution obtained by treating actual fermentation broth.     

Recovery of Nuclease Produced by Lactococcus Lactis Using Expanded Bed Ion Exchange Chromatography

Expanded bed-ionic exchange chromatography (EB-IEC) was used for the recovery and purification of recombinant staphylococcal nuclease secreted by Lactococcus lactis. At the end of the fermentation process, the nuclease activity reached 39 U ml⁻¹. The EB-IEC performances were firstly evaluated with clarified culture broth. The isocratic elution with 0.5 M NaCl led to approximately 80% of nuclease recovery. Proceeding with 3-fold bed expansion resulted in a reduction of the resin capacity by a factor of 32% compared to the process in a packed bed configuration. Simplification of the early purification steps was reached by loading immediately the unclarified culture broth previously diluted to reduce conductivity. Presence of Cells did not affect the chromatography performances resulting in 55-fold purification with the same yield.     

两步串联层析法纯化鼠抗人CD80单克隆抗体4E5

采用阴离子交换与凝胶过滤两步串联层析法,纯化了小鼠腹水来源的CD80阻断型单克隆抗体4E5。腹水样品经离心、过滤预处理后,在Tris-HCl缓冲溶液(pH8.0, 50mmol/L)条件下上阴离子交换柱对目的单抗进行捕集,采用0-0.5 mol/L NaCl浓度分步洗脱;含目的单抗的洗脱馏分再上凝胶过滤柱纯化,用PB缓冲溶液（pH7.2, 20mmol/L）洗脱,获得目的单抗4E5,其生物学活性高、纯度大于95%,抗体总回收率达61%。     

Application of ion exchange to purify acarbose from fermentation broths

Acarbose is conventionally used to reduce the insuline consumption of the diabetic patients. This compound is an oligosaccharide with the general formulae C25H43NO18 and obtained from fermentation processes by certain strains of Actinoplanes Utahensis. After the fermentation process, the acarbose has to be isolated from the fermentation broth where is accompanied of a large amount of substances, such as substrates, intermediate metabolites, proteins and different salts.

Four strong acid resins considering geliform and macroporous matrix types in aqueous and organic media have been tested in order to reach an easy and selective separation process. According to the experimental data, the Finex CS10GC (a gel strong cationic ion exchanger) presented the maximum acarbosa uptake and also the highest rate of ion exchange in water. The best behavior in non-aqueous media was observed with the Purolite CT151 (macroporous ion exchanger) but its maximum capacity of ion exchange was really lower than that exhibited by the Finex CS10GC resin in aqueous media. These results suggest that the acarbose removal from fermentation broths must be carried out in aqueous media to ensure the maximum usage of the resin uptake capacity. The results obtained provide a significant insight into the main equilibrium phenomena that takes place depending on the characteristics of the liquid phase. Finally, the elution of acarbose from the resin can be accomplished of a selectivity way by using a solution of 2.25N of HCl. The proposed separation method seems to be technically and economically feasible.     

Expanded bed adsorption as a unique unit operation for the isolation of bacteriocins from fermentation media

Expanded bed adsorption using a strong cation exchanger allowed the direct isolation of amylovorin L471, a bacteriocin from Lactobacillus amylovorusDCE 471, from the fermentation medium. The pH of the loading and elution buffer were optimised in a packed bed with cell-free culture supernatant. Bound bacteriocin was eluted with 1.0 M NaCl. The highest recovery (30%) was obtained at the lowest pH (3.6). At higher pH values the recovery was lower, namely 12%, 15% and 7% at pH 4.5, 6.5 and 8.0, respectively. In expanded bed mode, direct isolation of the bacteriocin from the fermentation medium at pH 3.6 (loading and elution) initially resulted in a recovery of 12%. After optimisation of the pH (loading and elution at pH 3.6 and 6.5, respectively), the recovery for amylovorin L471 increased up to 30% and higher. Recovery of enterocin A from Enterococcus faeciumCTC 492 fermentation medium averaged 15% (loading and elution at pH 3.6 and 6.0, respectively). With pediocin, produced by Pediococcus acidilactici ATCC 8042, 26% recovery was obtained at a pH of 6.5 during loading and elution. Low recoveries can be ascribed to non-optimal operation conditions (pH of loading and elution buffer), inactivation of the bacteriocin on a cationic resin, and the formation of more insoluble and less active, strongly hydrophobic bacteriocin aggregates upon further purification.     

Evaluation of a solution isoelectric focusing protocol as an alternative to ion exchange chromatography for charge-based proteome prefractionation

Solution isoelectric focusing (sIEF) is evaluated relative to ion exchange chromatography (IEC) as a preferred charge-based prefractionation tool for proteome mixtures. While IEC is extensively employed for proteome prefractionation prior to MS analysis, we demonstrate here that conventional salt gradient IEC has significant shortcomings compared to sIEF. Here, we critically evaluated a custom eight-channel sIEF device for intact protein separation, relative to strong cation exchange (SCX) and strong anion exchange (SAX) chromatography. The resolution, recovery, and uniformity of separation obtained with our sIEF device were comparable or superior to that of optimized IEC separations. Most importantly for intact proteins, sIEF separations strongly correlate with the proteins’ isoelectric point, which contrasts with IEC where no correlation was observed. To validate the sIEF platform for proteome analysis, prefractionation through sIEF resulted in the confident identification of a greater number of proteins from yeast (211) following LC–MS/MS, relative to those obtained through SAX (173) or SCX (148).     

Selective separation and purification of two lipases from chromobacterium viscosum using AOT reversed micelles

Selective separation and purification of two lipases form Chromobacterium viscosum were carried out by liquid-liquid extraction using a reversed micellar system. Optimum parameters for extraction were determined using a 250 mM AOT micellar solution in isooctane. Complete separation of the two lipases was achieved at pH 6.0 with a 50mM potassium phosphate buffer solution containing 50 mM KCI. By adding 2.5% by volume of ethanol to the lipase-loaded micellar solution, 85% of the extracted lipase could be recovered in a new aqueous phase, 50 mM K(2)HPO(4) with 50 mM KCl, at pH 9.0. Lipase A was purified 2.6-fold with a recovery of 86%, and lipase B by 1.5-fold with a recovery of 76%.     

Separation of gamma-aminobutyric acid from fermented broth

Gamma-aminobutyric acid (GABA) is a non-proteinaceous amino acid that is widely distributed in nature and acts as the major inhibitory neurotransmitter in the mammalian brain. This study aimed to find a separation method for getting high-purity GABA from a fermented broth. Firstly, a fermented broth with a high content of GABA (reaching 997 ± 51 mM) was prepared by fermentation with Lactobacillus brevis NCL912. GABA purification was conducted by successive centrifugation, filtration, decoloration, desalination, ion-exchange chromatography (IEC), and crystallization. Inorganic salt (Na₂SO₄) was removed from the both by desalination with 70% ethanol solution. A ninhydrin test strip was designed for the real-time detection of GABA during IEC. The recovery rate for the whole purification process was about 50%. The purified product was characterized by thin-layer chromatography and HPLC, and its purity reached 98.66 ± 2.36%.     

一种同时纯化钙谓神经磷酸酶和钙调素的有效方法

本文报导了一种能同时纯化钙调神经磷酸酶和钙调素的有效方法。牛脑粗提液经DE-52纤维素层析分段洗脱:0.5mol/L NaCl缓冲液洗脱峰经phenyl-sepharose亲和柱和G75 sephadex制得电泳纯钙调素。0.18mol/L KCl缓冲液洗脱峰经Affigel-Blue层析,硫酸铵盐析,钙调素亲和层析,G-200 Sephadex凝胶过滤制得电泳纯钙调神经磷酸酶。     

Recovery of yeast invertase from ethanol fermentation broth

Summary Ethanol fermentation broth produced by an aggregated form ofSaccharomyces uvarum strain contained invertase when sucrose-based raw materials were used. The amount of invertase in the borth was in the range of 1.4 to 4.8 units/ml, which was affected by the dilution rate, the concentration of corn steep liquor, and the type of sugar used. The activity of invertase in the broth could be maintained at 0.8 units/ml over two months. When the broth was passed through DEAE-cellulose beads and eluted with a NaCl-Tris-HCl buffer solution, a 75% recovery yield of invertase with 9-fold purification and 30-fold concentration could be achieved.     

Renal palmitate transport: possible sites for interaction with a plasma membrane fatty acid-binding protein

Summary In previous studies from this laboratory [14], a mediated transport system for long chain fatty acids was observed in rat renal basolateral membrane vesicles. Transport was measured in the absence of albumin and indicated the presence of a Na⁺ independent anion exchange mechanism. The present experiments were done to characterize renal transport of fatty acids derived from fatty acid-albumin complexes. ³H-palmitate uptake by brush border (BBMV) and basolateral membrane vesicles (BLMV) isolated from rat renal cortex was determined using a rapid filtration technique. All incubation media contained 100 µM ³H-palmitate complexed to 100 µM bovine serum albumin. Up to 65% of initially bound fatty acid-albumin complexes were displaceable by washing with solution containing 0.1% albumin. Total palmitate uptake was measured as the remaining non-displaceable radioactivity. In BBMV in low ionic strength (300 mM mannitol) or ionic buffers (100 mM mannitol + 100 mM NaCl or KCl), total palmitate uptake at 15 sec did not differ from equilibrium (60 min) values of 10–11 nmoles/mg protein. Uptake was primarily due to binding. A similar pattern was seen with BLMV in 300 mM mannitol buffer: In BLMV in 100 mM NaCl or KCl buffers, equilibrium uptake was 10-fold lower than at 15 sec. This suggests binding followed by cation-dependent translocation. If a putative FABP_PM is involved in transport only, its presence should be confined to BLMV.     

Ion channels in human endothelial cells.

Ion channels were studied in human endothelial cells from umbilical cord by the patch clamp technique in the cell attached mode. Four different types of ion channels were recorded: i) potassium channel current that rectifies at positive potentials in symmetrical potassium solutions (inward rectifier); ii) low-conductance non-selective cation channel with a permeability ratio K:Na:Ca = 1:0.9:0.2; iii) high-conductance cation-selective channel that is about 100 times more permeable for calcium than for sodium or potassium; iv) high-conductance potassium channel with a permeability ratio K:Na = 1:0.05. The extrapolated reversal potential of the inwardly rectifying current was near to the potassium equilibrium potential. The slope conductance decreased from 27 pS in isotonic KCl solution to 7 pS with 5.4 mmol/l KCl and 140 mmol/l NaCl in the pipette but 140 mmol/l KCl in the bath. The low-conductance non-selective cation channel showed a single-channel conductance of 26 pS with 140 mmol/l Na outside, 28 pS with 140 mmol/l K outside, and rectified in inward direction in the presence of Ca (60 mmol/l Ca, 70 mmol/l Na, 2.7 mmol/l K in the pipette) at negative potentials. The current could be observed with either chloride or aspartate as anion. The high-conductance non-selective channel did not discriminate between Na and K. The single-channel conductance was about 50 pS. The extrapolated reversal potential was more positive than +40 mV (140 K or 140 Na with 5 Ca outside). Both the 26 and 50 pS channel showed a run-down, and they rapidly disappeared in excised patches. The high-conductance potassium channel with a single-channel conductance of 170 pS was observed only rarely. It reversed near the expected potassium equilibrium potential. The 26 pS channel could be stimulated with histamine and thrombin from outside in the cell-attached mode. Both the 26 pS as well as the 50 pS channel can mediate calcium flux into the endothelial cell.     

Some aspects of the cation status of soil moisture

Summary The effect of potassium ions on a River Estate soil-water system was investigated by equilibrating the soil with 0.0001 to 0.02M KCl solutions. Soil solutions were obtained from soil samples prepared over a wide range of solution/soil ratios, both within and outside the field range. The soil-soil solution equilibrium remained undisturbed over the field range of solution/soil ratios, 0.25 to 1.0, for the 0.0001M 0.0002M, and 0.0005M KCl systems. Values of pK–1/2p(Ca+Mg) for these systems tended to decrease at ratios greater than 1.0 and with increasing strength of the KCl-equilibrating solutions. This is suggested to be due to the increasing potassium release from the soil with increasing solution/soil ratio for the 0.0001M KCl system and the increasing amounts of potassium present in the 0.0002M, 0.0005M, and 0.02M KCl systems.Both release and uptake of potassium were shown to be functions of the potassium concentration of the equilibrium soil solution. A value K₀, was defined as the concentration of potassium in the soil solution when potassium was neither released nor taken up by the soil. It is suggested that if this value is known, measurement of the soil solution potassiujm concentration under any particular conditions would indicate whether potassium was being released or taken up by the soil.It was deduced that the exchange complex of this soil had to be 62 per cent saturated with potassium before fixation occurred.