Separation of lactic acid from acetic acid using a four-zone SMB

A simulated moving bed (SMB) process has been developed to separate l-(+)-lactic acid from acetic acid, a major impurity in the fermentation broth of Lactobacillus rhamnosus. Poly(4-vinylpyridine) resin (PVP) was selected as the adsorbent. Adsorption isotherms and mass transfer parameters of the organic acids were estimated from single-column frontal tests. Experimental results show that the Langmuir isotherms obtained from the frontal tests can be used in the design of an SMB process to achieve 99.9% purity and over 93% yield of lactic acid. The column profiles and effluent histories, however, deviate from rate model predictions based on the Langmuir isotherms. They agree more closely with the predictions based on a modified Langmuir isotherm for lactic acid. The standing wave design method for systems with modified Langmuir isotherms is developed in this study. Rate model simulations show that the process based on the modified design method can achieve high purity (>99.9%) and high yield (>99.9%). For this nonlinear system, accurate isotherm model and model parameters are needed in the design, and the zone flow rates must be closely monitored and controlled in order to ensure high purity and high yield in the SMB process.     

Optimal design of a tandem simulated moving bed process for separation of paclitaxel, 13-dehydroxybaccatin III,and 10-deacetylpaclitaxel

Paclitaxel, 13-dehydroxybaccatin III (13-DHBIII), and 10-deacetylpaclitaxel (10-DAP), which came from the plant cell culture, have been regarded as highly valuable because of their efficacy in the anticancer treatments. Due to these values, the necessity for separating the three components in an economical way has been a matter of grave concern in industry. In this study, a tandem simulated moving bed (SMB) process that consisted of two four-zone SMB units in series was applied to such a ternary separation. First, a series of pulse injection experiments were performed for estimation of the adsorption isotherm and mass-transfer parameters. The estimated parameters were utilized in the tandem SMB optimization tool that was prepared based on the standing wave design principle. During the optimization of interest, the throughput of the tandem SMB was maximized while meeting the requirements on product purities and pressure drop. The results proved that the most economical strategy of utilizing the tandem SMB was to recover paclitaxel in the first SMB unit and then separate the remaining two components (13-DHBIII and 10-DAP) in the second SMB unit. Furthermore, such a strategy was also found to result in better tandem SMB performances over the entire region of a pressure drop limit.     

Comparison of Amberchrom-CG161C and Dowex99 as the adsorbent of a four-zone simulated moving bed process for removal of acetic acid from biomass hydrolyzate

One of the important steps in the application of biomass to producing sugars, which can be converted into bio-ethanol and other valuable chemicals by fermentation, is to hydrolyze the biomass components by sulfuric acid. It was reported that such a hydrolysis entailed the generation of acetic acid, which has been recognized as a key impurity to be surely removed from the biomass hydrolyzate for ensuring high fermentability of the hydrolyzed sugars. Regarding such a removal task, there has been a previous application of a simulated moving bed (SMB) process based on the Dowex99 adsorbent, whose performance, however, was limited by low selectivity between acetic acid and sugars. To overcome such a limitation, another adsorbent alternative to Dowex99 was searched in this study. It was found that Amberchrom-CG161C allowed higher selectivity between acetic acid and sugars than Dowex99. To investigate the relative superiority of Amberchrom-CG161C over Dowex99 as the adsorbent of an SMB process for removing acetic acid from the biomass hydrolyzate, the two SMB processes based on Amberchrom-CG161C and Dowex99 were optimized using the SMB optimization tool based on standing wave design (SWD) method. The optimization results revealed that the Amberchrom-CG161C SMB outperformed the Dowex99 SMB by a wide margin.     

Immobilized metal affinity chromatography in open-loop simulated moving bed technology: Purification of a heat stable histidine tagged β-glucosidase

Open-loop simulated moving bed (SMB) has been used for immobilized metal affinity chromatographic (IMAC) purification of his-tagged β-glucosidase expressed in E. coli. A simplified approach based on an optimized single column protocol is used to design the open-loop SMB. A set of columns in the SMB represent one step in the chromatographic cycle i.e. there will be one set each of columns for load, wash, elution etc within the SMB. Only the wash and elution are operated with columns in sequence. The β-glucosidase was purified to almost single band purity with a purification factor of 15 and a recovery of 91%. SMB-performance showed reduced buffer consumption, higher purification fold, a better yield and higher productivity.     

In silico analysis of the two tandem somatomedin B domains of ENPP1 reveals hints on the homodimerization of the protein

The homodimerization of ENPP1 is mediated by the two somatomedin B (SMB) domains of the protein through a mechanism that is yet unknown at the atomistic level. The tandem arrangement of these domains without an intermediate spacer implies their possible packing into a functional assembly, which we explored by rigid docking. To exclude potential bias in the docking search we assessed the absence of flexible protein regions by evaluating the normalized B-factors calculated from the Cα atom displacements derived from molecular dynamics simulations. After filtering the docking results exploiting the criterion that residues located at the inter-domain interfaces are more conserved than non-interface residues, the resulting best model of the tandem SMB domains revealed the presence of two large conserved surface patches not engaged in the inter-domain contact. The largest patch is flat and contains all the invariant positively charged residues characterized by fully solvent-exposed side chains within the tandem SMB domains, suggesting as a possible role its interaction with the negative phospholipids on the cell surface. We envisage that an ENPP1 monomer bound to the cell membrane via the transmembrane segment can also interact with the cell surface through the largest conserved patch favoring a specific geometry of the tandem SMB module on the cell that optimally exposes the second conserved patch for the symmetric interaction with another membrane-bound ENPP1 monomer, finally promoting the homodimerization. Biological implications of this model and insights into the effects of the K173Q variant associated with insulin resistance and related abnormalities are presented.     

Simulated moving bed chromatography with supercritical fluids for the resolution of bi-naphthol enantiomers and phytol isomers

The combination of the simulated moving bed (SMB) technique with supercritical fluid chromatography (SFC) leads to a process with unique features. Besides the known advantages of the SMB process, the use of supercritical carbon dioxide as the mobile phase offers the advantages of reduction in organic solvents and an easy eluent/solute separation. Because of the low viscosity and high diffusion coefficients of supercritical fluids, a high efficiency is possible. The steps of process development for SMB SFC are presented using the separations of the bi-naphthol enantiomers and phytol isomers as examples. The development of a packed column SFC method at an analytical scale is shown for the separation of the bi-naphthol enantiomers on a chiral stationary phase and CO(2) with a modifier as the mobile phase. The influence of the modifier, modifier content, and column configuration on productivity of the SMB SFC process was investigated by simulation. The first set of experiments was performed in the SMB separation of phytol isomers at low concentration to test the feasibility of the SMB SFC high purity separation of the binary mixtures. In the second set of experiments, the productivity of the process was increased by increasing the feed concentration up to 54 grams feed per liter stationary phase (SP) and hour (g(feed)/l(SP) h).     

Box-Behnken响应面法优化司替霉素B产生菌发酵条件

【背景】粗糙链霉菌(Streptomyces scabrisporus) HBERC-53204是本中心自主分离的一株链霉菌,经鉴定,其产生一种活性化合物司替霉素B (steffimycin B,SMB),对多种动植物重要病原菌具有良好生物活性。【目的】提高SMB发酵水平,拓宽放线菌活性天然产物在农牧业领域的研究及应用。【方法】以本实验室筛选出的一株产SMB的粗糙链霉菌HBERC-53204为研究对象,运用单因素试验筛选培养基的主效碳源、氮源、无机盐及各营养成分最适浓度,并基于单因素试验结果,通过Plackett-Burman(PB)试验设计筛选出显著影响因素,再结合最陡爬坡试验、Box-Behnken (BB)响应面法拟合显著因子与产量的非线性方程求解,进一步优化菌株产SMB的最佳发酵培养基配方。【结果】优化后最佳培养基配方为：葡萄糖36.22 g/L,蛋白胨8.00 g/L,酵母粉8.51 g/L,酸水解酪蛋白1.50 g/L,MgSO₄ 0.68 g/L,KNO₃ 1.00 g/L。经摇瓶验证,优化后SMB效价达到477.26 mg/L...     

Downstream processing of human antibodies integrating an extraction capture step and cation exchange chromatography

In this paper we explore an alternative process for the purification of human antibodies from a Chinese hamster ovary (CHO) cell supernatant comprising a ligand-enhanced extraction capture step and cation exchange chromatography (CEX). The extraction of human antibodies was performed in an aqueous two-phase system (ATPS) composed of dextran and polyethylene glycol (PEG), in which the terminal hydroxyl groups of the PEG molecule were modified with an amino acid mimetic ligand in order to enhance the partition of the antibodies to the PEG-rich phase. This capture step was optimized using a design of experiments and a central composite design allowed the determination of the conditions that favor the partition of the antibodies to the phase containing the PEG diglutaric acid (PEG-GA) polymer, in terms of system composition. Accordingly, higher recovery yields were obtained for higher concentrations of PEG-GA and lower concentrations of dextran. The highest yield experimentally obtained was observed for an ATPS composed of 5.17% (w/w) dextran and 8% (w/w) PEG-GA. Higher purities were however predicted for higher concentrations of both polymers. A compromise between yield and purity was achieved using 5% dextran and 10% PEG-GA, which allowed the recovery of 82% of the antibodies with a protein purity of 96% and a total purity of 63%, determined by size-exclusion chromatography. ATPS top phases were further purified by cation exchange chromatography and it was observed that the most adequate cation exchange ligand was carboxymethyl, as the sulfopropyl ligand induced the formation of multi-aggregates or denatured forms. This column allowed the elution of 89% of the antibodies present in the top phase, with a protein purity of 100% and a total purity of 91%. The overall process containing a ligand-enhanced extraction step and a cation exchange chromatography step had an overall yield of 73%.     

铜藻岩藻黄素提取及纯化工艺研究

为了对岩藻黄素的提取、纯化进行系统研究,进而为高纯度岩藻黄素的工业化生产提供研究基础,筛选了适用于提取铜藻（Sargassum horneri）鲜藻中岩藻黄素的有机溶剂,并通过单因素实验和正交实验确定了最佳的提取溶剂浓度、提取温度、提取时间、料液比等工艺参数。随后采用硅胶柱层析法进行纯化,并通过单因素实验确定了最佳的硅胶柱床高度、上样量和洗脱流速。最后采用制备液相法对经层析纯化的岩藻黄素进一步纯化。结果表明,有机溶剂萃取的最佳工艺条件为：甲醇浓度90%,提取温度50 ℃,提取时间1 h,料液比1∶10,此条件下岩藻黄素提取率达到(0.258 9±0.003 6) mg·g-1鲜重（FW）［(1.078 8±0.015 0) mg·g-1干重（DW）］。硅胶柱层析的最佳工艺条件为：硅胶柱床高度10 cm,上样量6 g,洗脱流速10 mL·min-1,此条件下岩藻黄素得率为0.176 5 mg·g-1FW（0.735 3 mg·g-1 DW）,纯度为87.01%±0.88%。经制备液相进一步纯化后,岩藻黄素得率为0.127 1 mg·g-1 FW（0.529 4 mg·g-1 DW）,纯度为99.27%±0.22%。研究所用工艺简单,岩藻黄素得率高,为高纯度岩藻黄素的制备提供了实验基础。     

Simulation and operation performance of simulated moving bed for enatioseparation of mandelic acid

Separation of mandelic acid enantiomer was carried out by using laboratory simulated moving bed (SMB) chromatography. The SMB process consists of four zones, with each zone having 1 column. The triangle theory was used to obtain the operating conditions for SMB. Adsorption isotherms of the D-/L-mandelic acids were obtained by pulse input method, considering linear isotherms of the two components. Flow rates of extract, raffinate, feed, and eluent streams were systematically changed to understand the effects of operation flow rates of SMB. Simulation results and experimental data from the SMB chromatography showed good agreements. Adjusting the flow rate in zone II increased the purity of D-mandelic acid from extract port. The highest purity of D-mandelic acid in the extract was obtained as 94% under the operating flow rates of Q_feed = 0.1 mL/min, Q_extract = 0.2 mL/min, Q_raffinate = 0.8 mL/min, and Q_eluent = 0.9 mL/min.     

Modified reactive SMB for production of high concentrated fructose syrup by isomerization of glucose to fructose

This work presents modifications to the Hashimoto's hybrid simulated moving bed reactor (SMBR) system which was used to produce 55% high fructose syrup (HFS55). The purpose of this study is to develop a new SMBR system to overcome the disadvantages of Hashimoto system (3-zone SMB with seven reactors), i.e., low utility of reactors when feed being a 50/50 blend of glucose and fructose. Two different configurations of modified system were presented in this paper: the first configuration is 4-zone SMB with one reactor, while the other one consists of one additional reactor. Both of these configurations aim at improving the concentration and purity of glucose at the inlet of the reactor, which will lead to both high productivity and high purity of fructose in the product. A state-of-the-art optimization technique, viz., non-dominated sorting genetic algorithm (NSGA) is used in finding the optimal design and operating parameters for the modified reactive SMB and Varicol processes. Compared with the Hashimoto's system, high productivity and purity of fructose can be achieved in these new systems using less number of reactors.     

Separation of amino acids by simulated moving bed using competitive Langmuir isotherm

The separation of two amino acids, phenylalanine and tryptophan, was carried out using laboratory simulated moving bed (SMB) chromatography. The SMB process consisted of four zones, with each zone having 2 columns. The triangle theory was used to obtain the operating conditions for the SMB. The mass transfer coefficients of the two amino acids were obtained from the best-fit values by comparing simulated and experimental pulse data. The competitive adsorption isotherms of the two amino acids were obtained by single and binary frontal analyses, taking into consideration the competition between the two components. A competitive Langmuir isotherm, obtained from single-component frontal chromatography, was used in the first run, and the isotherm from binary frontal chromatography in the second, with the flow rate of zone I modified to improve the purity. Compared to the first and second runs, the competitive Langmuir isotherm from the binary frontal chromatography showed good agreement with the experimental results. Also, adjusting the flow rate in zone I increased the purity of the products. The purities of the phenylalanine in the raffinate and the tryptophan in the extract were 99.84 and 99.99%, respectively.     

脂肪酸酰化修饰胰岛素的纯化

目的：脂肪酸酰化修饰的胰岛素类似物是常见的获得长效胰岛素的手段,但因其反应位点的偏差易产生多种传统纯化工艺较难以分离的杂质。本文探索以聚苯乙烯类有机聚合物填料为固定相纯化脂肪酸酰化修饰的胰岛素方法。方法：经过填料对比,有机溶剂浓度和pH选择后,再经过一系列正交试验优化,HPLC方法检验纯度和含量,质谱分析定性终产品,从而确定最佳条件。结果：经过对不同厂家不同型号的聚苯乙烯类有机聚合物填料的比较,填料选定采用纳微UniPs30．300为最佳,其目的蛋白吸附量比为6．32mg／ml,洗脱率为95．27％。在一系列的梯度实验中证实采用30-50％异丙醇浓度最佳。之后的pH对比得出。pH在4．0以下才能分离得到纯度在95％以上的产品。在以上一系列的单因素实验基础上,最后经过正交实验优化证实最佳的洗脱方案为采用A相为合25mM硫酸铵的0．1M磷酸盐缓冲液,pH3．0;B相为异丙醇流动相,洗脱梯度为30-50％B的10CV洗脱,流速60cm/h。放大验证可以得到纯度大于97．5％,回收率70％以上的结果。结论：此方法具有分离效果好,成本低,易于放大的优点。     

In silico genome-scale reconstruction and validation of the Corynebacterium glutamicum metabolic network

A genome-scale metabolic model of the Gram-positive bacteria Corynebacterium glutamicum ATCC 13032 was constructed comprising 446 reactions and 411 metabolites, based on the annotated genome and available biochemical information. The network was analyzed using constraint based methods. The model was extensively validated against published flux data, and flux distribution values were found to correlate well between simulations and experiments. The split pathway of the lysine synthesis pathway of C. glutamicum was investigated, and it was found that the direct dehydrogenase variant gave a higher lysine yield than the alternative succinyl pathway at high lysine production rates. The NADPH demand of the network was not found to be critical for lysine production until lysine yields exceeded 55% (mmol lysine (mmol glucose)(-1)). The model was validated during growth on the organic acids acetate and lactate. Comparable flux values between in silico model and experimental values were seen, although some differences in the phenotypic behavior between the model and the experimental data were observed.     

Development of a three-zone simulated moving bed process based on partial-discard strategy for continuous separation of valine from isoleucine with high purity,high yield,and high product concentration

The issue of separating valine from isoleucine has been a major concern in the biotechnological process for production of valine. To address this issue, an optimal three-zone simulated moving bed (SMB) process for continuous separation of valine was developed in this study. It was first found that an Amberchrom-CG161C resin was highly suitable for the adsorbent of such SMB process. The adsorption isotherm and mass-transfer parameters of valine and isoleucine on the Amberchrom-CG161C adsorbent were then determined through multiple frontal experiments. The determined parameters were used in the next stage of optimizing the SMB for valine separation, which was performed on the basis of genetic algorithm. For the optimized SMB process, a partial-discard strategy was applied to the raffinate port in order to make a further improvement in the valine product concentration. Finally, the optimized SMB based on the partial-discard strategy was tested experimentally using the self-assembled SMB equipment. The experimental results showed that the developed process in this study was highly effective in continuous separation of valine from isoleucine while ensuring the attainment of high product concentration. The experimental data for the SMB effluent histories and the SMB column profiles were also in close agreement with the model predictions.     

High‐throughput process development of purification alternatives for the protein avidin

With an increased number of applications in the field of the avidin‐biotin technology, the resulting demand for highly‐purified protein avidin has drawn our attention to the purification process of avidin that naturally occurs in chicken egg white. The high‐throughput process development (HTPD) methodology was exploited, in order to evaluate purification process alternatives to commonly used ion‐exchange chromatography. In a high‐throughput format, process parameters for aqueous two‐phase extraction, selective precipitation with salts and polyethylene glycol, and hydrophobic interaction and mixed‐mode column chromatography experiments were performed. The HTPD strategy was complemented by a high‐throughput tandem high‐performance liquid chromatography assay for protein quantification. Suitable conditions for the separation of avidin from the major impurities ovalbumin, ovomucoid, ovotransferrin, and lysozyme were identified in the screening experiments. By combination of polyethylene glycol precipitation with subsequent resolubilization and separation in a polyethylene glycol/sulfate/sodium chloride two‐phase system an avidin purity of 77% was obtained with a yield >90% while at the same time achieving a significant reduction of the process volume. The two‐phase extraction and precipitation results were largely confirmed in larger scale with scale‐up factors of 230 and 133, respectively. Seamless processing of the avidin enriched bottom phase was found feasible by using mixed‐mode chromatography. By gradient elution a final avidin purity of at least 97% and yield >90% was obtained in the elution pool. The presented identification of a new and beneficial alternative for the purification of the high value protein thus represents a successful implementation of HTPD for an industrially relevant purification task. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:957–973, 2015     

A predictive aggregate transport model for microfiltration of combined macromolecular solutions and poly-disperse suspensions: testing model with transgenic goat milk

To meet the technical challenge of recovering human IgG fusion protein from transgenic whole goat milk at reasonable cost with high purity and yield, a predictive aggregate transport model for microfiltration has been developed (Baruah and Belfort, 2003). Here, to test the model's predictability of permeate flux and mass transport, a comprehensive series of experiments with varying wall shear rate, feed temperature, feed concentration, and module design are presented. A very good fit was obtained between the model predictions and measurements for a wide variety of experimental conditions. For microfiltration module design comparison, a linear hollow fiber module (representing current commercial technologies) gave lower permeation flux and higher yield than a helical hollow fiber module (representing the latest self-cleaning methodology). These results are easily explained with the model that is now being used to define operating conditions for maximizing performance. The procedure described by the model is generalizable and can be used to obtain optimal filtration performance for applications other than milk.     

Optimization of the Ethanol Recycling Reflux Extraction Process for Saponins Using a Design Space Approach

A solvent recycling reflux extraction process for Panax notoginseng was optimized using a design space approach to improve the batch-to-batch consistency of the extract. Saponin yields, total saponin purity, and pigment yield were defined as the process critical quality attributes (CQAs). Ethanol content, extraction time, and the ratio of the recycling ethanol flow rate and initial solvent volume in the extraction tank (RES) were identified as the critical process parameters (CPPs) via quantitative risk assessment. Box-Behnken design experiments were performed. Quadratic models between CPPs and process CQAs were developed, with determination coefficients higher than 0.88. As the ethanol concentration decreases, saponin yields first increase and then decrease. A longer extraction time leads to higher yields of the ginsenosides Rb₁ and Rd. The total saponin purity increases as the ethanol concentration increases. The pigment yield increases as the ethanol concentration decreases or extraction time increases. The design space was calculated using a Monte-Carlo simulation method with an acceptable probability of 0.90. Normal operation ranges to attain process CQA criteria with a probability of more than 0.914 are recommended as follows: ethanol content of 79–82%, extraction time of 6.1–7.1 h, and RES of 0.039–0.040 min⁻¹. Most of the results of the verification experiments agreed well with the predictions. The verification experiment results showed that the selection of proper operating ethanol content, extraction time, and RES within the design space can ensure that the CQA criteria are met.     

A nonchromatographic process for purification of secretory immunoglobulins from caprine whey

Secretory immunoglobulins are an important antibody class being primarily responsible for immunoprotection of mucosal surfaces. A simple, non‐chromatographic purification process for secretory immunoglobulins from caprine whey was developed. In the first process step whey was concentrated 30–40‐fold on a 500 kDa membrane, thereby increasing the purity from 3% to 15%. The second step consisted of a fractionated PEG precipitation, in which high molecular weight impurities were removed first and in the second stage the secretory immunoglobulins were precipitated, leaving a majority of the low molecular weight proteins in solution. The re‐dissolved secretory immunoglobulin fraction had a purity of 43% which could then be increased to 72% by diafiltration at a volume exchange factor of 10. Further increase of purity was only possible at the expense of very high buffer consumption. If diafiltration was performed directly after ultrafiltration, followed by precipitation, the yield was higher but purity was only 54%. Overall, filtration performance was characterized by high concentration polarization, therefore process conditions were set to low trans‐membrane pressure and moderate protein concentration. As such purity and to a lesser extent throughput were the major objectives rather than yield, since whey, as a by‐product of the dairy industry, is a cheap raw material of almost unlimited supply. Ultra‐/diafiltration performance was described well by correlations using dimensionless numbers. Compared with a theoretical model (Graetz/Leveque solution) the flux was slightly overestimated. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:642–653, 2017     

Comparing the performance of one-column process and four-zone simulated moving bed by computer simulation

A new one-column chromatography process, analogous to a four-zone simulated moving bed (SMB), was presented. The basic principle of the process was identical to that of a four-zone SMB. The process consisted of one chromatographic column and four tanks, instead of the four columns in the four-zone SMB (1-1-1-1), and has been used for the separation of two amino acids, phenylalanine and tryptophan, using an ion exchange resin. The operating parameters for the one-column process and four-zone SMB were obtained from equilibrium theory. Computer simulations were used to compare the performances of the new one column process to that of the general four-zone SMB, using Aspen Chromatography^™ v 11.1. The differences between the one-column and SMB processes in terms of the purities and yields of phenylalanine and tryptophan were less than 4 and about 6%, respectively. The lower purities of the one-column process were due to the loss of the developed concentration profiles in the column when the liquid was stored in tanks. The one-column process gave great flexibility, and would be useful for reconstructing an existing conventional chromatography process to one of a SMB.