离子交换层析纯化透明质酸

考察6种离子交换树脂的静态吸附解析效果,选出201＊7阴离子交换树脂填柱,确定洗脱流速为0.6mL/min,40mL0.3mol/LNaCl和50mL0.5mol/L NaCl双浓度洗脱,实现透明质酸和杂蛋白的分离。制得透明质酸产品蛋白含量为0.057%,葡萄糖醛酸含量为43%,平均相对分子质量大于1.1×10^6,收率为54%,符合医用级透明质酸行业标准的要求。     

Bovine plasma protein fractionation by ion exchange chromatography

An ion exchange chromatography process was developed to separate the main protein fractions of bovine blood plasma using a composite material, Q-HyperD resin, and a gel material, DEAE-Sepharose. The experiments were carried out at semipreparative scale. It was necessary to establish analytical methods of electrophoresis and HPLC to identify the fractionated proteins. Results show that these materials are able to adequately fractionate different protein groups from the raw blood plasma. This method may be used to avoid chemical fractionation using agents such as ethanol or PEG and, thus, decrease protein denaturation of the different fractions to be used for research or pharmaceutical purposes. The Q-HyperD resin presents a better retention capacity for plasma protein than DEAE-Sepharose under the experimental conditions employed.     

Purification of hormone-sensitive lipase by high-performance ion exchange chromatography

We have developed an improved method for purification of hormone-sensitive lipase from adipose tissue. The method employs two preparative high-performance ion-exchange chromatography steps on Mono Q and Mono S after detergent solubilization and partial fractionation of the enzyme by gradient sievorptive chromatography on QAE-Sephadex. About 0.2 mg of greater than 70% pure enzyme is prepared at 10% yield within 6-7 days from adipose tissue of 500 rats. This protocol is a major improvement over the previously established procedure in terms of accessibility, rapidity, enzyme purity, and yield.     

Matrix assisted refolding of proteins by ion exchange chromatography

Two different approaches of matrix assisted refolding have been evaluated and compared to conventional refolding by dilution. Bovine alpha-lactalbumin was used for the studies as model protein. It was adsorbed under denaturing conditions on an ion exchange matrix and refolding was completed on the column prior to elution or, depending on the buffer system, in the eluate. Agarose based chromatography matrices showed high capacities for the denatured alpha-lactalbumin. A positive effect on the yield of refolded protein by the matrix could be observed for Fractogel EMD DEAE and a negative for Toyopearl DEAE 650M, DEAE Sepharose FF and Q Sepharose FF. In the case of Fractogel EMD DEAE the ion exchange surface might act as a folding helper. This property may be caused by the grafted polymers. For Source 30Q only a marginal negative influence on the refolding kinetics was observed, thus the ion exchanger is only a mean for removal of chaotropic agents. Refolding on the column is characterized by a low yield but high productivity due to significant reduction of refolding time.     

The role of lactic acid adsorption by ion exchange chromatography

Background

The polyacrylic resin Amberlite IRA-67 is a promising adsorbent for lactic acid extraction from aqueous solution, but little systematic research has been devoted to the separation efficiency of lactic acid under different operating conditions.

Methodology/Principal Findings

In this paper, we investigated the effects of temperature, resin dose and lactic acid loading concentration on the adsorption of lactic acid by Amberlite IRA-67 in batch kinetic experiments. The obtained kinetic data followed the pseudo-second order model well and both the equilibrium and ultimate adsorption slightly decreased with the increase of the temperature at 293–323K and 42.5 g/liter lactic acid loading concentration. The adsorption was a chemically heterogeneous process with a mean free energy value of 12.18 kJ/mol. According to the Boyd^_plot, the lactic acid uptake process was primarily found to be an intraparticle diffusion at a lower concentration (<50 g/liter) but a film diffusion at a higher concentration (>70 g/liter). The values of effective diffusion coefficient D_i increased with temperature. By using our Equation (21), the negative values of ΔG° and ΔH° revealed that the adsorption process was spontaneous and exothermic. Moreover, the negative value of ΔS° reflected the decrease of solid-liquid interface randomness at the solid-liquid interface when adsorbing lactic acid on IRA-67.

Conclusions/Significance

With the weakly basic resin IRA-67, in situ product removal of lactic acid can be accomplished especially from an open and thermophilic fermentation system without sterilization.     

Kinetic studies of clavulanic acid recovery by ion exchange chromatography

Clavulanic acid (CA) is a beta-lactamase inhibitor produced by strains of Streptomyces clavuligerus. Nowadays, the combination of CA with amoxycillin is the most successful example of the use of a beta-lactam antibiotic sensitive to beta-lactamases together with an inhibitor of these enzymes. Clavulanic acid is purified from fermentation broth by a series of steps consisting mainly of two-phase separation processes such as liquid–liquid extraction, adsorption or ion-exchange chromatography, among others. Amberlite IRA 400, a strong anion-exchange resin, has a very high adsorption capacity for CA (Mayer et al. 1997). This resin can be pre-treated with NaCl (chloride cycle), to remove selectively only those anions, which are able to displace chloride from the resin or with NaOH (hydroxyl cycle), to remove all species of anions. In order to decide the best operating conditions for CA recovery by ion-exchange resins and then to construct a model of this separation process, batch experiments were conducted using Amberlite IRA 400 in the chloride cycle. These runs were carried out in a 200 ml stirred tank, at two different initial solution pH, 6.2 and 4.0; the temperature was maintained at 10 °C and 20 °C during adsorption and 30 °C during the desorption step. It was possible, on the basis of these batch results, to model the separation process, including the adsorption kinetics, equilibrium data and mass transfer limitations. This revised version was published online in July 2006 with corrections to the Cover Date.     

Single-step protein purification by back flush in ion exchange chromatography

Ion exchange chromatography, one of the major procedures for protein purification, seldom provides single-step purification due to a lack of specific affinity. In this work, a novel and simple method called “back flush” (i.e., reversing the flow direction of elution relative to that of sample loading) was developed to achieve single-step purification on an ion exchanger. Tips for the conditions and operation by back flush are presented. Our study demonstrates, for the first time, the feasibility and dramatic improvement for protein purification by the back-flush method.     

Purification of RanGDP, RanGTP, and RanGMPPNP by ion exchange chromatography

Ran is a small GTPase that cycles between a guanosine diphosphate (GDP)-bound form (RanGDP) and a guanosine triphosphate (GTP)-bound form (RanGTP) and plays important roles in nuclear transport and mitosis. For studies of Ran function and its interactions with partner proteins, pure RanGDP and RanGTP complexes are critical. Ran complexed with the nonhydrolyzable GTP analog, GMPPNP (RanGMPPNP), is used instead of RanGTP when inhibition of hydrolysis is required. In this study, we demonstrate that the binding of Ran to a UNO Q ion exchange column is remarkably sensitive to small shifts in MgCl(2) concentration, and we use this property to purify recombinant RanGTP, RanGMPPNP, and RanGDP complexes. At 10 mM MgCl(2), Ran was found predominantly in the flow-through and, thus, was separated from the vast majority of bacterial proteins. After reducing the concentration of MgCl(2) to 5 mM, further purification of RanGTP, RanGMPPNP, and RanGDP was achieved by loading onto ion exchange columns and elution with an NaCl gradient. Purity of the resulting preparations was confirmed by releasing the bound nucleotide and checking it against a known nucleotide by high-performance liquid chromatography (HPLC). To further confirm the purity and function of the Ran preparations, appropriate protein-binding, enzymatic, and nuclear import assays were carried out. These methods should facilitate studies of cellular processes involving Ran by providing pure functional Ran-nucleotide complexes.     

Fractionation of Aspergillus niger cellulases by combined ion exchange affinity chromatography

Eight chemically modified cellulose supports were tested for their ability to absorb components of the Aspergillus niger cellulase system. At least two of the most effective adsorbents, aminoethyl cellulose and carboxymethyl cellulose, were shown to be useful for the fractionation of cellulases. These supports apparently owe their resolving capacity to both ion exchange and biospecific binding effects; however, the relative importance of each effect is unknown. These observations form the basis for a new cellulase fractionation technique, combined ion exchange-affinity chromatography.     

Purification of type E botulinum neurotoxin by high-performance ion exchange chromatography

A purification procedure for type E botulinum neurotoxin has been developed, based solely on high-performance ion exchange chromatography. The method exploits the differential chromatographic behavior of the free neurotoxin versus the neurotoxin-protein 12S complex. The high purity of the product was demonstrated with sodium dodecyl sulfate-gel electrophoresis and amino acid sequencing. Beginning with dialyzed crude extract, at least 4 mg of pure neurotoxin could be obtained in two working days. The method has been adapted to user-prepared columns for processing large volumes of crude neurotoxin in one batch.     

An exclusion mechanism in ion exchange chromatography

Protein dynamic binding capacities on ion exchange resins are typically expected to decrease with increasing conductivity and decreasing protein charge. There are, however, conditions where capacity increases with increasing conductivity and decreasing protein charge. Capacity measurements on two different commercial ion exchange resins with three different monoclonal antibodies at various pH and conductivities exhibited two domains. In the first domain, the capacity unexpectedly increased with increasing conductivity and decreasing protein charge. The second domain exhibited traditional behavior. A mechanism to explain the first domain is postulated; proteins initially bind to the outer pore regions and electrostatically hinder subsequent protein transport. Such a mechanism is supported by protein capacity and confocal microscopy studies whose results suggest how knowledge of the two types of IEX behavior can be leveraged in optimizing resins and processes.