Separation of D‐psicose and D‐fructose using simulated moving bed chromatography

Simulated moving bed (SMB) processes have been widely used in the sugar industries with ion‐exchange resin as a stationary phase. D ‐Psicose, a rare monosaccharide known as a valuable pharmaceutical substrate, was synthesized by the enzymatic conversion from D ‐fructose. The SMB process was adopted to separate D ‐psicose from D ‐fructose. Before the SMB experiment, the reaction mixture including D ‐psicose and D ‐fructose was treated by a deashing process to remove contaminants, such as buffers, proteins, and other organic materials. Four columns packed with Dowex 50WX4‐Ca²⁺ (200–400 mesh) ion‐exchange resins were used in the four‐zone SMB. Single‐step frontal analysis was performed to estimate the isotherm parameters of each monosaccharide. The operating conditions of the SMB process were determined based on the Equilibrium Theory. According to the simulation of the SMB process, the purity and yield of extract product (D ‐psicose) achieved were 99.04 and 97.46%, respectively and those of raffinate product (D ‐fructose) were 99.06 and 99.53%, respectively. Under the optimized operating condition, complete separation (extract purity = 99.36%, raffinate purity = 99.67%) was achieved experimentally.     

Experimental evaluation of the effect of a modified port‐location mode on the performance of a three‐zone simulated moving‐bed process for the separation of valine and isoleucine

The removal of isoleucine from valine has been a key issue in the stage of valine crystallization, which is the final step in the valine production process in industry. To address this issue, a three‐zone simulated moving‐bed (SMB) process for the separation of valine and isoleucine has been developed previously. However, the previous process, which was based on a classical port‐location mode, had some limitations in throughput and valine product concentration. In this study, a three‐zone SMB process based on a modified port‐location mode was applied to the separation of valine and isoleucine for the purpose of making a marked improvement in throughput and valine product concentration. Computer simulations and a lab‐scale process experiment showed that the modified three‐zone SMB for valine separation led to >65% higher throughput and >160% higher valine concentration compared to the previous three‐zone SMB for the same separation.     

Effect of the homogeneity of the column set on the performance of a simulated moving bed unit. I. Theory

Although it is impossible to manufacture identical columns for use in a simulated moving bed (SMB) process, theoretical studies assume that all the columns in an SMB unit have identical characteristics. In practice, calculations in modeling and optimization studies are made with the average values of each column parameter set. In this report, the effects on SMB process performance caused by column-to-column fluctuations of the parameters are discussed. As a first step, we show how the differences in porosity of the columns may be taken into account with a revised set of separation conditions. Reductions in the purity of the extract and the raffinate streams are quantitatively related to the column-to-column fluctuations of the retention times of the two components arising from these porosity differences. For the sake of simplicity, the discussion first addresses the case of a four-column SMB operating under linear conditions. Then, the scope is extended to the cases of SMB units incorporating several columns in each section and to SMB units operating under nonlinear conditions.     

Optimization of a hybrid chromatography-crystallization process for the separation of Tröger's base enantiomers

This paper presents an analysis of a hybrid process consisting of simulated moving bed (SMB) chromatography and crystallization and studies its performance for the separation of the Tr?ger's base enantiomers. The SMB is simulated using a detailed model including column efficiency, thus, implying a proper evaluation of the effect of column size on column efficiency and separation performance. The crystallization operations are accounted for through material balances, assuming equilibrium between enantiopure crystals and mother liquor. A genetic algorithm is used to optimize the combined process, using proper definitions of objective functions. Multi-objective optimization of this hybrid process for productivity and evaporation cost in terms of operating parameters, column length, and SMB feed concentration shows an optimum SMB purity value as a trade off between increased SMB performance and recycle of the mother liquor.     

Enantioseparation of 1-phenyl-1-propanol by supercritical fluid-simulated moving bed chromatography

The enantioseparation of 1-phenyl-1-propanol through the supercritical fluid-simulated moving bed (SF-SMB) process is studied. Non-linear isotherms were measured on an analytical column, and used together with the triangle theory for SMB design to select operating conditions for the SF-SMB. Experiments were carried out on a pilot-scale SF-SMB plant at conditions that corresponded to the non-linear range of the isotherm. Under conditions of low feed concentration, complete separation (extract purity = 99.5%; raffinate purity = 98.4%) was achieved. Under conditions of larger feed concentration, the best separation corresponded to an extract purity of 98.0% and a raffinate purity of 94.0%, and yielded a productivity of 110 g of racemate per kg stationary phase per day.     

Optimization of simulated moving bed and column chromatography for a plasmid DNA purification step and for a chiral separation

This work analyzes the performance of the SMB and the column chromatography processes for two different case studies: the first stage of the plasmid DNA (pDNA) polishing, and the Tr?ger's base enantiomer separation, in which the adsorption isotherms are linear and non-linear, respectively. Simulation tools are used together with an optimization routine (Non-Sorting Genetic Algorithm (NSGA)) in order to find the optimum operating conditions leading to maximum productivity and minimum solvent consumption; the optimum solution for each of the processes is a curve on the productivity-solvent consumption plane, the so-called Pareto set. The comparison between the column and the SMB processes is based on the relative position of the two Pareto sets calculated at equal conditions and for the same final purity and recovery of the target species. The results show that SMB is superior to column chromatography in the two case studies investigated, i.e. in the case of the linear isotherm (pDNA), the productivity gain is up to a factor two for a given value of the solvent consumption. Furthermore, the flexibility of the SMB operation is larger, since the Pareto sets are flatter and they prolong into regions of the productivity-solvent consumption plane that are not accessible with the column chromatography process.     

Partial-discard strategy for obtaining high purity products using simulated moving bed chromatography

A new "partial-discard" operation strategy was developed to improve the performance, especially purity, achievable in simulated moving bed (SMB) chromatography. This strategy was applied to the four-zone SMB process with two columns per zone for binary separation within the linear range. The "partial-discard" strategy significantly enhanced the purity or enrichment when the discard time and discard length were controlled. In addition, the "partial-feed with partial-discard" strategy improved remarkably the extract and raffinate purities at an intermediate feed time compared with the "partial-feed" operation. Adjustments of the discard length and discard time played key roles in achieving the desired product purity in SMB chromatographic performance.     

Bi-level optimizing control of a simulated moving bed process with nonlinear adsorption isotherms

A bi-level optimizing control scheme originally proposed for a simulated moving bed (SMB) with linear isotherms has been extended to an SMB with nonlinear isotherms. Cyclic steady state optimization is performed in the upper level to determine the optimum switching period and time-varying feed/desorbent flow rates, and repetitive model predictive control is run in the lower level for purity regulation, taking the decision variables from the upper level as feed-forward information. Experimental as well as numerical study for an SMB process separating a high-concentration mixture of aqueous L-ribose and L-arabinose solutions showed that the proposed scheme performs satisfactorily against various disturbances. In contrast, an alternative scheme based on an SMB model with linear isotherms showed a limitation in the control performance; this scheme was apt to fail in purity regulation.     

Model-based design of a pilot-scale simulated moving bed for purification of citric acid from fermentation broth

One of the conventional processes used for the recovery of citric acid from its fermentation broth is environmentally harmful and cost intensive. In this work an innovative benign process, which comprises simulated moving bed (SMB) technology and use of a tailor-made tertiary poly(4-vinylpyridine) (PVP) resin as a stationary phase is proposed. This paper focuses on a model-based design of the operation conditions for an existing pilot-scale SMB plant. The SMB unit is modeled on the basis of experimentally determined hydrodynamics, thermodynamics and mass transfer characteristics in a single chromatographic column. Three mathematical models are applied and validated for the prediction of the experimentally attained breakthrough and elution profiles of citric acid and the main impurity component (glucose). The transport dispersive model was selected for the SMB simulation and design studies, since it gives a satisfactory prediction of the elution profiles within acceptable computational time. The equivalent true moving bed (TMB) and SMB models give a good prediction of the experimentally attained SMB separation performances, obtained with a real clarified and concentrated fermentation broth as a feed mixture. The SMB separation requirements are set to at least 99.8% citric acid purity and 90% citric acid recovery in the extract stream. The complete regeneration in sections 1 and 4 is unnecessary. Therefore the net flow rates in all four SMB sections have been considered in the unit design. The influences of the operating conditions (the flow rate in each section, switching time and unit configuration) on the SMB performances were investigated systematically. The resulting SMB design provides 99.8% citric acid purity and 97.2% citric acid recovery in the extract. In addition the citric acid concentration in the extract is a half of its concentration in the pretreated fermentation broth (feed).     

On-line enantiomeric analysis using high-performance liquid chromatography in chiral separation by simulated moving bed

An automated on-line enantiomeric analysis system comprising an analytical HPLC set-up with two UV detectors sharing the same light source has been employed to monitor the internal composition profile in chiral simulated moving bed chromatography. This monitoring scheme does not use a polarimeter. Using a sampling interface placed between two SMB columns, effluent samples are directed onto a high-efficiency analytical column at a sampling rate faster than the overall dynamics of the preparative unit to achieve on-line enantiomeric analysis of the composition profile. The other UV detector is placed in the SMB loop before the fraction collector to provide instantaneous measurement of the total enantiomeric concentration. The feasibility and effectiveness of the on-line enantiomeric monitoring scheme were assessed experimentally on the separation of Tr?ger's base racemate, using Chiralpak AD as stationary phase and methanol as eluent. It was found that robust monitoring of the concentration profiles of the individual enantiomers is best achieved when the enantiomeric purity obtained from the peak areas of the on-line enantiomer analysis chromatograms is combined with the on-line UV measurement of total enantiomeric concentration. The accuracy and robustness of the proposed on-line enantiomeric monitoring system open up promising perspectives for process control and dynamic optimization of the SMB.     

Recombinant protein purification using gradient assisted simulated moving bed hydrophobic interaction chromatography. Part II: process design and experimental validation

In the first part of this work adsorption isotherm parameters were acquired to describe the migration of recombinant streptokinase in Butyl Sepharose columns at different salt concentrations. Based on these results, a simulated moving bed (SMB) chromatographic process was designed and realised, which exploits a two-step salt gradient and allows the continuous separation of streptokinase from contaminants present in a clarified Escherichia coli cell lysate solution. This second part describes the design of the three-zone open-loop gradient SMB process applying both equilibrium theory and an equilibrium stage model and presents results of a series of experiments aiming to obtain pure streptokinase. Moreover, the potential of the SMB process and the design approach are evaluated.     

Purification of erucic acid by preparative high-performance liquid chromatography and crystallization.

Erucic acid (C22:l fatty acid) has been found to be useful in the treatment of adrenoleukodystrophy (ALD). It appears to work by reducing the blood levels of very-long-chain fatty acids (VLCFAs) which destroy the myelin sheaths of the nerves. Erucic acid was purified by reversed-phase high-performance liquid chromatography (HPLC) on columns packed with YMC C18 (10-20 microns, 120 A). Using ethanol-water as the mobile phase, the recovery of erucic acid was 69% and the purity was more than 97% as measured by gas chromatography. The amount of saturated VLCFAs was found to be within the limits specified for ALD treatment. The production rate (yield per 8 h shift) was low, however. Using methanol-water instead of ethanol-water as the mobile phase, a ninefold increase in the production rate was achieved. The recovery of erucic acid was 65% and the purity of erucic acid was 98%. All other purity specifications were met. By performing a low-temperature crystallization after the preparative HPLC step, the production rate was increased a further 142%. This represents a 22-fold increase in production rate over the ethanol-water method. The crystalline erucic acid was found to be 99% pure. All other purity requirements were met. The yield for the combined process (HPLC plus crystallization) decreased to 55%, however.     

Model-based optimization of a preparative ion-exchange step for antibody purification

A method using a model-based approach to design and optimize an ion-exchange step in a protein purification process is proposed for the separation of IgG from a mixture containing IgG, BSA and myoglobin. The method consists of three steps. In the first step, the model is calibrated against carefully designed experiments. The chromatographic model describes the convective and dispersive flow in the column, the diffusion in the adsorbent particles, and the protein adsorption using Langmuir kinetics with mobile phase modulators (MPM). In the second step, the model is validated against a validation experiment and analyzed. In the third and final step, the operating conditions are optimized. In the optimization step, the loading volume and the elution gradient are optimized with regard to the most important costs: the fixed costs and the feed cost. The optimization is achieved by maximizing the objective functions productivity (i.e. the production rate for a given amount of stationary phase) and product yield (i.e. the fraction of IgG recovered in the product stream). All optimization is conducted under the constraint of 99% purity of the IgG. The model calibration and the analysis show that this purification step is determined mainly by the kinetics, although as large a protein as IgG is used in the study. The two different optima resulting from this study are a productivity of 2.7 g IgG/(s m3) stationary phase and a yield of 90%. This model-based approach also gives information of the robustness of the chosen operating conditions. It is shown that the bead diameter could only be increased from 15 microm to 35 microm with maximum productivity and a 99% purity constraint due to increased diffusion hindrance in larger beads.     

Rational design of core–shell molecularly imprinted polymer based on computational simulation and Doehlert experimental optimization: application to the separation of tanshinone IIA from Salvia miltiorrhiza Bunge

Computational simulation and Doehlert experimental optimization were done for the rational design of a core-shell molecularly imprinted polymer (CS-MIP) for use in the highly selective separation of Tanshinone IIA (TSIIA) from the crude extracts of Salvia miltiorrhiza Bunge (SMB). The functional monomer layer of the polymer shells directed the selective occurrence of imprinting polymerization at the surface of silica through the copolymerization of vinyl end groups with functional monomers and also drove TSIIA templates into the formed polymer shells through the charge-transfer complex interactions between TSIIA and the functional monomer layer. As a result, the maximum rebinding capacity was achieved with the use of optimal grafting ratio by the Doehlert design. The CS-MIP exhibited high recognition selectivity and binding affinity to TSIIA. When the imprinted particles were used as dispersive solid phase extraction sorbents, the recovery yield of TSIIA reached 93% by a one-step extraction from the crude extracts of SMB, and the purity of TSIIA was larger than 98% by HPLC analysis. These results show the possibility of a highly selective separation and enrichment of TSIIA from the SMB using the TSIIA-imprinted core-shell molecularly imprinted polymers.     

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.     

分子动力学方法研究单链聚乙烯的结晶过程

用分子动力学方法（ＭＤ）研究了单链聚乙烯在不同温度（１００Ｋ、２００Ｋ、３００Ｋ、４００Ｋ、５００Ｋ）下的结晶过程,并用能量和结构参数进行了描述．结果表明伸直分子链的结晶过程都经历了三个阶段,首先是伸直链的卷曲与聚集,然后通过链段的排列形成规整的片晶结构,最后是结晶形成的片晶在结构与能量上的涨落变化。研究表明,结晶温度越高,分子链的内聚速度越快．研究发现,分子链在内聚阶段经历一个局部凝聚的中间状态,在结晶温度很低（１００Ｋ）时,局部凝聚的结构是有序的．而在５００Ｋ时,该结构为无规线团．结晶温度的差异,一般来说,将导致得到的片晶厚度的不同．对于模拟的单链,随着结晶温度的降低而形成了较厚的片晶．该行为与聚乙烯本体结晶中片晶厚度对结晶温度的依赖性相反．在有序化阶段和之后的片晶调整运动阶段,分子链线团的回转半径基本保持不变．这与宏观多链体系的结果相同．另外,在模拟中发现,尺寸微小的单链聚乙烯晶片的扭转运动     

Crystallization from the micellar phase of imidazolium-based cationic surfactants

The self-assembly and phase behavior of the aqueous dispersions consisting of the cationic surfactant, 1-hexadecyl-3-methylimidazolium chloride (C(16)mimCl), were studied by differential scanning calorimetry, synchrotron small- and wide-angle X-ray scattering, freeze-fracture electron microscopy, polarizing optical microscopy, and Fourier transform infrared spectroscopy. We found that the crystallization of C(16)mimCl upon cooling is strongly concentration-dependent. At low concentrations (10-25 wt%), the samples change directly from a spherical micellar solution to a lamellar crystalline phase. While at high concentrations (50-67 wt%), the initial cylindrical micelles first convert to the lamellar gel phase and then to the lamellar crystalline phase. Particular efforts have been devoted to unveiling the submolecular mechanisms of the phase transition processes. The transformation from the initial micellar phase to the final crystalline phase upon cooling involves both an ordering rearrangement in the alkyl tails and a dehydrating process in the head region. At high concentrations, the transformation is divided into two steps, i.e., the gelation and subsequent crystallization processes, both involving evident rearrangements of the surfactant tails. Moreover, a significant dehydration of the surfactant head part takes place in the gelation step and a partial rehydration occurs in the crystallization step.     

From the dilute solution to the pure compound: Extraction strategy based on a multi-stage process of phase separation

It is very rare that a one-step process of extraction leads to the pure compound with a high degree of purity specified by an industrial application. The various stages of a synthesis process and possible secondary reactions may lead to the synthesis of more or less complex and highly diluted solutions. In this work, the rationale and strategy for extraction and purification of a high added value compound are discussed. All the thinking is based on the knowledge and the exploitation of phase diagrams and then developed for different unit operations of the process. The most significant research tools are the experimental data and the modelling of phase equilibrium to estimate the yield of each step of extraction. The significant example chosen involves all the basic methods of phase separation, starting with liquid-vapour equilibrium: stripping of high volatility components and then more or less complex distillation are classically employed. The theoretical plateau number can be deduced from the equilibrium equation curves. The second step is based on the study of the liquid-liquid equilibrium and is an intermediate step for enrichment of the solution when distillation is not possible. A final step based on solid-liquid equilibrium consists of the selective crystallization of the pure product at low temperature, in order to satisfy the requirements of purity and safety imposed by industrial use. The conclusion includes all isolation operations in the form of a general extraction and purification scheme.

     

A practical and step-economic route to Favipiravir

A practical and step-economic route to Favipiravir, an antiviral drug, was developed. Favipiravir was synthesized in only six steps from 3-aminopyrazine-2-carboxylic acid with an overall yield of about 22.3%. Key intermediates 3 and 6 were obtained in excellent purity via recrystallization from optimized solvents, which was beneficial to large-scale production. In the key synthetic reaction, 3,6-dichloropyrazine-2-carbonitrile (6) was reacted sequentially, in one pot, with KF and 30% H₂O₂ to give (after crystallization from 95% EtOH) favipiravir as colorless crystals, with a 60% yield for this final step of the synthesis.     

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.