光度显色剂8-羟基喹啉-5-磺酸的纯化方法

报道了8-羟基喹啉-5-磺酸硅胶干柱层析纯化方法，探讨了固定相、淋洗剂、洗脱剂对产品纯化的影响，确定了以层析硅胶为固定相，以V(正(异)丙醇)：V(氨水)＝2：1为淋洗剂，以蒸馏水为洗脱剂的纯化条件。经过红外光谱和高效液相色谱分析证明，使用本方法可获得纯度大于99％的产品，结果满意。     

Numerical simulation of rapid pressurization and depressurization of a zeolite column using nitrogen

The required durations of pressurization and depressurization steps of a rapid pressure swing adsorption process are primarily governed by adsorbent particle size, adsorption kinetics, column pressure drop, column length to diameter ratio, and the valve constant of the gas inlet and outlet control valve attached to the adsorbent column. A numerical model study of the influence of these variables for an adiabatic LiX zeolite column is presented using pure N₂ as an adsorbate gas. An adsorbent particle size range of 200–350 μm was found to minimize (<1 s) the times required for the pressurization and depressurization steps.     

Novel simulated moving-bed method for reduced solvent consumption

Simulated moving-bed (SMB) chromatography is attractive for reducing sorbent and solvent consumption relative to fixed-bed systems. In this contribution, we describe a novel and versatile method for further reducing solvent consumption in the case of reversed-phase chromatography. The method is based on the variation of the distribution coefficients of solutes to be separated upon varying the composition of a multi-component mobile phase. If the solvent strength of the desorbent is set higher than the solvent strength of the feed, the components will have smaller distribution coefficients in the extraction section of the SMB and hence will be more easily eluted. This will result in a lower desorbent flow and possibly also in a shorter desorbent zone, and, ultimately, in more concentrated products. The so-called "Triangle-method" by Storti et al. [AIChE J., 39 (1993) 471] to obtain the region of complete separation, is extended for this novel SMB method. Theoretical evaluation of the proposed methodology supports the anticipated solvent reduction relative to fixed-bed RP-HPLC for the cases of the purification of the polyketide antibiotic nystatin and the separation of bovine insulin from porcine insulin.     

Optimization of azeotropic protein separations in gradient and isocratic ion-exchange simulated moving bed chromatography

The separation of dilute binary mixtures of proteins by salt aided ion-exchange simulated moving bed (SMB) chromatography is optimized with respect to throughput, desorbent consumption and salt consumption. The optimal flow-rate ratios are analytically determined via an adopted "triangle theory". Azeotropic phenomena are included in this procedure. The salt concentrations in the feed and recycled liquid are subsequently determined by numerical optimization. The azeotropic separation of bovine serum albumin and a yeast protein is used to illustrate the procedure. Gradient operation of the SMB is generally preferred over isocratic operation. A feed of azeotropic salt concentration can only be separated in a gradient SMB. Desorbent and salt consumption are always lower in gradient than in isocratic SMB chromatography.     

Streamlined,two-column,simulated countercurrent chromatography for binary separation

We report on a numerical and experimental study of two-column versions of streamlined, multicolumn, semi-continuous chromatography for binary separation. The systems combine a flexible node design, cyclic flow-rate modulation, and relayed operation of the inlet/outlet ports to extend the mass-transfer zone over the largest possible length, while keeping it inside the system at all times. One advantage of these streamlined designs is the simplicity of their physical realization: regardless of the number of columns, they only require two pumps to supply feed and desorbent into the system, while the flow rates of liquid withdrawn from the system are controlled by material balance using simple two-way valves. In one case, an extra pump is needed to recirculate the fluid in closed-loop. A rigorous model-based optimization approach is employed in the optimal design of the cycles to generate solutions that are physically realizable in the experimental set-ups. The optimized schemes for two-column operation supply fresh feed into the middle of the system where the composition of the circulating fluid is closest to that of the feedstock fluid, and recover the purified products, extract and raffinate, alternately at the downstream end of the unit, while desorbent is continuously supplied into the upstream end of the system. By internally recycling part of the non-pure cut fraction, the scheme with a step of closed-loop recycling significantly reduces its solvent consumption. The feasibility and effectiveness of the reported two-column processes have been verified experimentally on the linear separation of nucleosides by reversed phase subject to 99% purity constraints on both products. It is shown that our processes compare favorably against single-column batch chromatography, steady-state recycling, and four-column, open-loop SMB, for the same amount of adsorbent; they are also better than the four-column, closed-loop SMB at high feed throughputs.     

Optimization of throughput in preparative column luquid chromatography by column overloading and partial fractionation of the effluent

Summary The criteria for the optimization of preparative chromatography are sample throughput and product purity. It is shown for column liquid chromatography that the throughput has been maximized for a given purity by column overloading and appropriate fractionation. The size and position of the fraction must be determined by chemical analysis, since overlapping peaks under overloading conditions are usually distorted compared to the peaks of the same amounts of pure compounds. With overloading of the column larger particles can be used as column packings without reduction of the separation effect.     

Improved performance of protein separation by continuous annular chromatography in the size-exclusion mode.

In size-exclusion chromatography (SEC), proteins and peptides are separated according to their molecular size in solution. SEC is especially useful as an effective fractionation step to separate a vast amount of impurities from the components of interest and/or as final step for the separation of purified proteins from their aggregates, in a so-called polishing step. However, the throughput in SEC is low compared to other chromatographic processes as good resolution can be achieved only with a limited feed volume (i.e., maximal approximately 5% of the column volume can be loaded). This limitation opposed widespread application of conventional SEC in industry despite its excellent separation potential. Therefore a continuous separation process (namely preparative continuous annular chromatography) was developed and compared to a conventional SEC system both using Superdex 200 prep grade as sorbent. An immunoglobulin G sample with a high content of aggregates was chosen as a model protein solution. The influence of the feed flow-rate, eluent flow-rate and rotation rate on the separation efficiency was investigated. The height equivalent to a theoretical plate was lower for preparative continuous annular chromatography which could be explained by reduced extra column band broadening. The packing quality was proved to be identical for both systems. The productivity of conventional batch SEC was lower compared to continuous SEC, consequently buffer consumption was higher in batch mode.     

Displacement chromatography of biomolecules

Displacement chromatography was used for the preparative-scale separation of peptides, antibiotics, and proteins. The feed components were both purified and concentrated during the separation processes. The components of a peptide mixture were separated on a reverse-phase analytical column using 2-(2-butoxyethoxy) ethanol as the displacer. The use of organic modifiers in the carrier along with an elevated column temperature of 45 degrees C enabled the efficient separation of relatively hydrophobic peptides by displacement chromatography. In addition, the throughput of the process was significantly increased by carrying out the separation at an elevated flow-rate with no adverse effect on product purity. The antibiotic cephalosporin C was isolated from impurities in a fermentation broth using 2-(2-butoxyethoxy)ethanol as the displacer along with a step change in column temperature. The proteins cytochrome c and lysozyme were purified on a weak cation-exchanger column using cationic polymers as the displacers. While polymers of 60 and 20 kilodaltons were both found to be good displacers for these proteins, only the lower molecular weight polymer was readily removed from the column by standard regeneration techniques.     

Optimizing the separation of gaseous enantiomers by simulated moving bed and pressure swing adsorption

The resolution of racemic gas mixtures by simulated moving bed (SMB) and pressure swing adsorption (PSA) is investigated by dynamic simulation and optimization. Enantiomer separation of inhalation anesthetics is important because there is evidence that the purified enantiomers may have different pharmacological properties than the racemate. The model parameters reported in an experimental investigation performed elsewhere are used to study the feasibility of this separation using SMB and PSA configurations. Both processes were modeled in gPROMS^® as systems of differential algebraic equations. Operating conditions are optimized such that the feed throughput and product recovery for each process were maximized subject to equal constraints on the pressures and superficial gas velocities. SMB was found to be capable of resolving racemic feed mixtures with purity and recovery exceeding 99%. On the other hand, PSA was also able to provide a single purified enantiomer with low recovery of about 30% which may limit its application to enantiomer separation. Nevertheless, PSA consumes less desorbent, and achieves higher throughput at the sacrifice of lower recovery.     

化学改性琼脂糖凝胶的物化性能及其对重组人血白蛋白的纯化应用研究

考察了几种经过化学改性后带有离子交换配基的琼脂糖凝胶介质的理化性能.通过外形观察、元素及金属含量分析、柱效测定、耐压及流速测定、离子交换容量和蛋白吸附容量测定,从多方面对性能进行验证比较,并对其在分离纯化重组人血白蛋白的应用性能进行了初步研究.结果表明国产产品与进口产品理化性能相当.     

Preparative anion-exchange chromatography of soybean trypsin inhibitor: the alternative of column-overload methods.

The objective of preparative separation is to purify the largest amount of material in the shortest time and at a minimum cost, i.e. to maximize throughout. One of the techniques for increasing throughput is to overload the column while maintaining purity and cycle time at the same level. This principle is applied in sample displacement mode chromatography, in which the column is overloaded with sample mixture until it is completely saturated. Soybean trypsin inhibitor was purified from a crude protein extract by this technique using an analytical anion-exchange column with small particle size (20 microns). The comparison of these results, using the criterion of throughput, with those derived from a conventional scale-up, using a 40-microns preparative column, led to the conclusion that the overloaded 20 microns column gave a higher throughput than the 40-microns column.     

Separation and purification of fructooligosaccharides on a zeolite fixed‐bed column

Fructooligosaccharides (FOS), a well‐known prebiotic product, are obtained by enzymatic synthesis and consist of a mixture of mono‐ and disaccharides. In this work, a methodology for their separation and purification was developed using a zeolite fixed‐bed column. The effects of column temperature (40–60°C), eluent flow rate (0.10–0.14 mL/min), injected to bed volume percent ratio (2.6–5.1%), and ethanol concentration in the eluent (40–60%, v/v) were investigated using a fractionary factorial design (2^4–1), having the separation efficiency and purity as target responses. Additional experiments were performed as well, where the temperature and ethanol concentration were studied in a central composite design (2²). In this work, the zeolite fixed‐bed column was shown to be a good alternative for FOS purification, allowing a FOS purity of 90% and separation efficiency of 6.86 between FOS and glucose, using an eluent at 45°C with 60% ethanol concentration.     

Effect of phenyl sepharose ligand density on protein monomer/aggregate purification and separation using hydrophobic interaction chromatography

In the large-scale manufacturing and purification of protein therapeutics, multiple chromatography adsorbent lots are often required due to limited absorbent batch sizes or during replacement at the end of the useful column lifetime. Variability in the adsorbent performance from lot to lot should be minimal in order to ensure that consistent product purity and product quality attributes are achieved when a different lot or lot mixture is implemented in the process. Vendors of chromatographic adsorbents will often provide release specifications, which may possess a narrow range of acceptable values. Despite relatively narrow release specifications, the performance of the adsorbent in a given purification process could still vary from lot to lot. In this case, an alternative use test (one that properly captures the lot to lot variability) may be required to determine an acceptable range of variability for a specific process. In this work, we describe the separation of therapeutic protein monomer and aggregate species using hydrophobic interaction chromatography, which is potentially sensitive to adsorbent lot variability. An alternative use test is formulated, which can be used to rapidly screen different adsorbent lots prior to implementation in a large-scale manufacturing process. In addition, the underlying mechanism responsible for the adsorbent lot variability, which was based upon differences in protein adsorption characteristics, was also investigated using both experimental and modeling approaches.     

Numerical study of nitrogen desorption by rapid oxygen purge for a medical oxygen concentrator

Efficient desorption of selectively adsorbed N₂ from air in a packed column of LiX zeolite by rapidly purging the adsorbent with an O₂ enriched gas is an important element of a rapid cyclic pressure swing adsorption (RPSA) process used in the design of many medical oxygen concentrators (MOC). The amount of O₂ purge gas used in the desorption process is a sensitive variable in determining the overall separation performance of a MOC unit. Various resistances like (a) adsorption kinetics, (b) column pressure drop, (c) non-isothermal column operation, (d) gas phase mass and thermal axial dispersions, and (e) gas-solid heat transfer kinetics determine the amount of purge gas required for efficient desorption of N₂. The impacts of these variables on the purge efficiency were numerically simulated using a detailed mathematical model of non-isothermal, non-isobaric, and non-equilibrium desorption process in an adiabatic column. The purge gas quantity required for a specific desorption duty (fraction of total N₂ removed from a column) is minimum when the process is carried out under ideal, hypothetical conditions (isothermal, isobaric, and governed by local thermodynamic equilibrium). All above-listed non-idealities (a?Ce) can increase the purge gas quantity, thereby, lowering the efficiency of the desorption process compared to the ideal case. Items (a?Cc) are primarily responsible for inefficient desorption by purge, while gas phase mass and thermal axial dispersions do not affect the purge efficiency under the conditions of operation used in this study. Smaller adsorbent particles can be used to reduce the negative effects of adsorption kinetics, especially for a fast desorption process, but increased column pressure drop adds to purge inefficiency. A?particle size range of ??300?C500???m is found to require a?minimum purge gas amount for a given desorption duty. The purge gas requirement can be further reduced by employing a pancake column design (length to diameter ratio, L/D<0.2) which lowers the column pressure drop, but hydrodynamic inefficiencies (gas mal-distribution, particle agglomeration) may be introduced. Lower L/D also leads to a smaller fraction of the column volume that is free of N₂ at the purge inlet end, which is required for maintaining product gas purity. The simulated gas and solid temperature profiles inside the column at the end of the rapid desorption process show that a finite gas-solid heat transfer coefficient affects these profiles only in the purge gas entrance region of the column. The profiles in the balance of the column are nearly invariant to the values of that coefficient. Consequently, the gas-solid heat transfer resistance has a minimum influence on the overall integrated N₂ desorption efficiency by O₂ purge for the present application.     

Comparaison de la purification par fusion de zone et par cristallisation en colonne dans le cas d'amines aromatiques liquides a temperature ordinaire

Purification by zone melting of seven aromatic amines was studied; 400 g of substance could be purified at one time between +15° and -35°. Criteria of purity and some physical constants of puritied amines are given. A related method—column crystallisation-was also studied for the same starting materials and the results are compared. The two methods of purilication give comparable results. Column crystallisation does not give such good purification as zone melting, but has the advantages that it can be operated with continuous throughput, much less time is needed, and rather impure starting materials can be employed     

Optimal operation of simulated moving bed chromatographic processes by means of simple feedback control

In this contribution, simple methods are presented for controlling a simulated moving bed (SMB) chromatographic process with standard PI (proportional integral) controllers. The first method represents a simple and model-free inferential control scheme which was motivated from common distillation column control. The SMB unit is equipped with UV detectors. The UV signals in the four separation zones of the unit are fixed by four corresponding PI controllers calculating the ratio of liquid and solid flow in the respective separation zone. In order to be able to adjust the product purity a second, model-based control scheme is proposed. It makes use of the nonlinear wave propagation phenomena in the apparatus. The controlled chromatographic unit is automatically working with minimum solvent consumption and maximum feed throughput--without any numerical optimization calculations. This control algorithm can therefore also be applied for fast optimization of SMB processes.     

Optimization of the fractional precipitation of paclitaxel from a Taxus chinensis cell culture using response surface methodology and its isolation by consecutive high‐speed countercurrent chromatography

A consecutive preparation method for the isolation and purification of paclitaxel from the Taxus Chinensis cell culture was developed in this study. The process involved alkaline Al₂O₃ chromatography, fractional precipitation, and high‐speed countercurrent chromatography. The original cell culture materials were first extracted with methanol using ultrasound‐assisted extraction, and then the extract (the content of paclitaxel is 1.5%) was separated by alkaline Al₂O₃ column chromatography. Subsequently, fractional precipitation was used to obtain paclitaxel. In particular, response surface methodology was used to optimize the factors of fractional precipitation (methanol concentration, material‐to‐solvent ratio, and precipitating time were optimized as 48.14%, 8.85 mg/mL, and 48.71 h, respectively) and the yield of fractional precipitation product was 30.64 ± 0.60 mg (the content of paclitaxel is 89.3%, 27.37 ± 0.54 mg) from a 100 mg fraction by Al₂O₃ column separation (the content of paclitaxel is 32.4%). Then, the product was used for further isolation by high‐speed countercurrent chromatography. About 1.00 g paclitaxel (200 ± 2 mg in each loading) with a purity up to 99.61% was isolated from 1.25 g of fractional precipitation product with a solvent system of n‐hexane/ethyl acetate/methanol/water (1.2:1.8:1.5:1.5, v/v/v/v) in one run of five consecutive sample loadings without exchanging a new solvent system.     

加芯毛细管填充柱的理论研究

 从速率方程和柱压降两个方面对加芯毛细管填充柱的柱效和渗透性进行了探讨，并详细讨论了柱直径、芯直径、芯根数和柱压降的关系。综合考虑柱压降、板高和拉制柱子时颗粒在柱内的镶嵌状况可知最佳柱型是３芯的毛细管填充柱。     

Efficient purification of paclitaxel from yews using high-performance displacement chromatography technique

Paclitaxel was purified using high-performance displacement chromatography (HPDC) technique, but not by the mechanism of HPDC. On small scale, paclitaxel was extracted with methanol from dry needles of Taxus canadensis and was enriched by extracting with chloroform after removing water-soluble hydrophilic components and hexane-soluble hydrophobic components. Then, 93-99% purity of paclitaxel was obtained using the HPDC technique. On large scale, taxanes were enriched by solvent partitioning between acetic acid/MeOH/H(2)O and hexane and extracted with CH(2)Cl(2). Taxanes except paclitaxel were further removed by extracting with methanol-water-trifluoroacetic acid (1.0:98.9:0.1, v/v/v). Applying HPDC technique to water-insoluble substances is problematic as this method requires a highly aqueous solvent system. In order to overcome this incompatibility, a system was set up where paclitaxel, although in low concentration, was extracted by methanol-water-trifluoroacetic acid (10.0:89.9:0.1, v/v/v). Recycling the extracting solvent to ensure minimal volume, the extracted paclitaxel was adsorbed on a C(18) trap column. A C(18) column of 4.6mm internal diameter was then connected to the trap column. The HPDC technique was thus carried out using an isocratic acetonitrile-water-trifluoroacetic acid (30.0:69.9:0.1, v/v/v) mobile phase consisting of a displacer cetylpyridinium trifluoroacetate (3mg/mL). Paclitaxel was co-eluted with the displacer and spontaneously crystallized. The crystal (114mg) showed 99.4% purity and only 10% of paclitaxel in the starting crude extract was lost during the enrichment/purification processes. This large scale purification method was successfully applied to purify paclitaxel from Chinese yew in small scale, suggesting general applicability of the method. This is the first report of purifying a water-insoluble natural product using HPDC technique.     

Adsorption Strategy of Plasmid DNA Nanoparticulate: Preparative Purification by a Simple Custom Expanded Bed Column

This paper summarizes the critical examination of the hydrodynamic performance of the NBG expanded bed contactor operated with streamline-DEAE adsorbent under various operating conditions for expanded bed adsorption of plasmid DNA nanoparticles from alkaline lysate. The purification process is not RNase-free. In this study, a rapid and efficient scaleable purification protocol obtaining, plasmid DNA nanoparticles (average size of 40 nm) with a high purity level for use as therapeutic agent in customized NBG expanded bed columns was developed. This technique allows efficient levels of binding to the column media and vector purification without centrifugation or filtration steps. Residence time distribution (RTD) studies were exploited to achieve the optimal condition of plasmid DNA nanoparticle (pDNA) recovery upon anion exchange adsorbent in this contactor. In addition, the purification experiments were carried out in the expanded bed columns with settle bed height of 6.0 ± 0.2 cm. NaCl gradient elution enabled the isolation of supercoiled plasmid from low-Mr RNA, cDNA and plasmid variants. Subsequently dynamic binding capacity of the adsorbent was calculated while these values decreased with increase in flow velocity. Moreover, the effect of pH upon the performance of this recovery process and the feedstock volume upon the expanded bed anion exchange purification was investigated. The results demonstrated that separation of low-Mr RNA from plasmid DNA isoforms in the range of pH between 5.5 and 7.5 is achievable in this column. The yield of recovery of pDNA in optimal condition was higher than 88.51% which was a superior result in one-pass frontal chromatography. The generic application of simple customized NBG expanded bed column and its potential for the purification and recovery of plasmid DNA as a nanoparticulate bioproduct is strongly discussed.