离子强度和溶质浓度对蛋白质在Q Sepharose FF中吸附动力学的影响

采用孔扩散模型, 模拟不同盐浓度和不同蛋白质初始浓度条件下,吸附牛血清白蛋白(BSA)的动态吸附曲线并获得孔扩散系数;考察了离子强度和溶质浓度对蛋白质在阴离子交换剂Q Sepharose FF中吸附动力学的影响.结果表明,蛋白质的孔扩散系数随初始浓度的增大而下降;在氯化钠浓度小于0.10 mol•L^-1的范围内,蛋白质的孔扩散系数随着盐浓度的增加而增大,但当盐浓度增大到0.15 mol•L^-1时又有所降低,表明存在着一个最佳的离子强度,使蛋白质的孔扩散系数最大.     

盐种类和浓度对蛋白质疏水性吸附过程有效孔扩散系数的影响

研究了牛血清白蛋白在配基密度不同的两种疏水性吸附剂Phenyl Sepharose FF low sub和Phenyl Sepharose FF high sub上的吸附平衡和孔内传质动力学,重点考察了盐种类和浓度的影响.结果表明,Na2SO4溶液中盐浓度的增加导致蛋白质吸附容量的增大和解离常数的降低比(NH4)2SO4溶液更显著.利用孔扩散模型得到的有效扩散系数随盐浓度及配基密度的增大而提高,表明表面扩散作用对孔内传质的贡献随吸附容量提高而增大.     

蛋白质在离子交换吸附剂颗粒中的扩散系数

采用以化学势梯度作为扩散推动力的Maxwell-Stephan扩散方程（MS方程）,结合平行扩散模型,对阴离子吸附剂Q-SepharoseFF吸附牛血清白蛋白（BSA）的动态试验数据进行了模拟,拟舍得到了BSA的表面扩散和孔扩散系数。研究表明表面扩散系数随pH降低、盐浓度增加而增大;孔扩散系数随pH增加、盐浓度降低而增加,随蛋白质初始浓度增加而减小。在表面扩散不容忽视且为非线性吸附的条件下采用Fick定律时得到的表面扩散系数是蛋白质浓度的函数,且大于根据MS方程得到的表面扩散系数。     

琼脂糖-DEAE离子交换介质的配基密度和孔径对BSA吸附的影响

离子交换色谱是蛋白质分离纯化的有效方法之一,配基密度和介质孔径是影响蛋白质吸附的关键因素。采用3种不同琼脂糖浓度的凝胶为基质,具有不同的平均孔径,分别偶联上阴离子交换配基DEAE,通过调控反应条件,包括反应温度、反应时间、碱浓度和DEAE浓度,得到了不同配基密度和介质孔径的系列DEAE离子交换介质。考察了牛血清白蛋白（BSA）的静态和动态吸附性能,发现随配基密度增加或介质孔径减小,BSA饱和吸附容量有所增大;对于吸附动力学,介质孔径显著影响有效扩散系数。结果表明,配基密度和介质孔径共同决定了蛋白质的吸附性能,介质孔径主导蛋白质的孔内扩散,而配基密度则影响配基-蛋白质间的相互作用。     

固定床吸附废水中Cr（Ⅵ）离子的数学模型

研究了２种煤质活性炭对不同浓度６价铬离子溶液的吸附，应用固定床吸附动力学模型，Ｍａｒｑｕａｄ方法非线性回归固定床吸附流出曲线数据，获得了铬离子在活性炭上的扩散传质系数。结果发现，孔扩散系数ＤＰ强烈地依赖于铬离子入口的浓度，随着入口浓度升高，孔扩散系数变小。     

红霉素在大孔树脂上的吸附动力学研究

采用液膜及孔内扩散模型,模拟不同温度和不同红霉素(EM)初始浓度条件下,大孔吸附树脂HZ816及XAD16吸附红霉素的动态吸附曲线,并获得液膜传质及孔内扩散系数;考察了温度及溶质浓度对红霉素在两种树脂中吸附动力学的影响.结果表明,在实验范围内,红霉素在HZ816和XAD16两种树脂上的吸附平衡数据满足Langmuir吸附等温线方程,液膜及孔内扩散模型能较好地描述红霉素在两种树脂上的吸附动力学,同时,模型拟合得到的液膜传质系数随着温度的升高而增大,随着初始浓度的增大而增大,孔内扩散系数随着温度的升高而增大,随着初始浓度的增大而减小.     

大孔吸附树脂HZ816对红霉素的固定床吸附过程研究

在上柱质量浓度为2.31—6.56 mg/mL、流量为14.33—42.80 mL/h的范围内研究了固定床吸附柱中大孔吸附树脂HZ816对红霉素的动态吸附过程,考察了原料液质量浓度和进口流量等操作参数对穿透曲线的影响。并采用基于液膜及孔内扩散模型的动力学模型,同时考虑吸附树脂颗粒内外扩散阻力及轴向扩散的影响,研究了固定床上红霉素在大孔吸附树脂中的吸附动力学,并从穿透曲线回归得到液膜传质系数孔内扩散系数。结果表明,在实验范围内,该模型能较好地描述红霉素在HZ816树脂上的吸附过程,由模型拟合得到的液膜传质系数随着原料液质量浓度减小而增大,随着流量升高而增大;孔内扩散系数随着原料液质量浓度增大而减小,随着流量升高而减小。为采用大孔吸附树脂HZ816吸附技术分离纯化红霉素工艺提供了实验和理论基础。     

双级孔材料内组分有效扩散系数的理论计算

双级孔材料中扩散与吸附现象广泛存在于化工过程中,准确预测其传递性质对指导过程设计具有重要意义。从最小尺度的孔隙开始采用体积平均方法推导出一个扩散型方程,并且得到该孔隙尺度下有效扩散系数的表达式。然后以此扩散方程为基础逐级扩大孔隙尺度,直至获得最大尺度孔隙中对应的扩散型方程及其对应的有效扩散系数的理论表达式。基于此,推导出一个扩散型方程描述双级孔材料内的组分扩散与吸附过程。孔隙结构、扩散速率、吸附强度的影响由有效扩散系数衡量。将上述理论模型与孔尺度模拟方法结合,对多孔圆柱阵列内的扩散吸附过程进行预测,预测结果与文献报道的直接数值模拟的结果吻合。结果表明:体积平均理论以及推导得到的封闭方程可用于预测双级孔材料内组分的有效扩散系数,为理解孔隙结构对有效扩散系数的影响以及调控相关过程性能提供了新的方法。     

固定床吸附烷烃中芳烃的模拟

本文在实验研究烷烃中少量芳烃的固定床吸附动态过程的基础上,进行模型化计算,分别用线性推动力和孔扩散两种固定床吸附模型,拟合得出总传质系数,液膜传质系数和孔扩散系数,两种模型的拟合计算结果表明：在本文的实验条件范围内,传质推动力可用线性推动力表示。总传质阻力由液膜传质阻力和颗粒相传质阻力的共同作用而形成,它随着温度,浓度和流量的降低而增加,孔扩散系数与流量无关。     

干燥条件下水泥基材料中氧气扩散预测模型

将氧气在水泥基材料中的扩散分为Knudsen型扩散、过渡型扩散及Fick型扩散3类,并将水泥基材料孔结构简化为平行管束模型。根据孔尺寸分布密度函数,将3种扩散方式进行定量化表征,结合孔隙率和孔曲折度,建立了干燥条件下水泥基材料的氧气扩散系数预测模型。利用自主研制的氧气扩散系数测定装置对干燥条件下砂浆试件的氧气扩散系数进行测定,结果表明试验值与预测模型计算值吻合度较好,且3种扩散方式中以过渡型扩散和Fick型扩散为主。     

间歇吸附器内活性炭吸附水中微量三氯甲烷——孔扩散模型和表面扩散模型

<正> 近10多年来,各国对饮水氯化处理中的副作用研究甚多．现已发现氯化饮水中含有不同 性质的有机物约300种“’,其中三卤甲烷含量突出,而活性炭吸附是脱除其中不同性质有机物 的有效方法’‘－‘’．一般情况下,溶质在吸附剂内的扩散过程是整个吸附过程的控制步骤．但目 前文献仅限干研究活性炭吸附三卤甲烷的能力,很少涉及与吸附速率有关的有效扩散系数．     

A SIMPLE METHOD OF DETERMINING PORE AND SURFACE DIFFUSIVITIES IN ADSORPTION STUDIES

In this paper, a new graphical method of determining pore and surface diffusivities in adsorption systems is presented. The method involves only a simple linear plot of the inverse of half time of adsorption versus a concentration factor. The pore diffusivity and the surface diffusivity are determined directly from the intercept and the slope of the straight line, respectively. Experimental data of n-butane on Ajax activated carbon are used to illustrate the potential application of this new technique in the diffusivity parameter determination.     

Batch adsorption of trichlorotrifluoroethane (freon-113) onto activated carbon — surface diffusivity and pore diffusivity

Activated carbon was found more active than molécular sieve 13X and silica gel in adsorbing 1,1,2 trichloro-1,2,2 trifluoroethane (CFE). Batch adsorption experiments were carried out with activated carbon to adsorb CFE at 15, 25 and 30°C. The adsorption isotherms of CFE on activated carbon were of the Langmuir type: q(C) = q_m KC / (1 + KC) where q^m and K were evaluated for the three temperatures. The measured bulk concentration-time data were interpreted equally well with the surface diffusion model and the pore diffusion model; for the former model the surface diffusivity increased with increasing initial CFE concentration, and for the latter the pore diffusivity was independent upon the initial CFE concentration.     

Adsorption of methyl iodide on reduced silver-functionalized silica aerogel: Kinetics and modeling

The low concentration methyl iodide (CH₃I) adsorption process on reduced silver-functionalized silica aerogel (Ag⁰-Aerogel) was studied. The kinetic data were acquired using a continuous flow adsorption system. Because the corresponding physical process was observed, the shrinking core model (SCM) was modified and applied. An average CH₃I pore diffusivity was calculated, the CH₃I-Ag⁰-Aerogel reaction was identified as a 1.40 order reaction instead of first order reaction, and the n^th order reaction rate constant was determined. This modified SCM significantly increases the accuracy of adsorption behavior prediction at low adsorbate concentration. Modeling results indicate that the overall adsorption process is controlled by the pore diffusion. However, at low adsorbate concentration (ppbv level), the CH₃I adsorption is limited to the surface reaction due to the low uptake rate in a predictable time period.     

Evaluation of effective diffusivity of adsorbate in the absence of adsorption and surface diffusion

A method is suggested for the evaluation of effective diffusivity of adsorbate in the absence of adsorption and surface diffusion, the precise value of which is required for estimating the effective surface diffusivity and the extent of influence of adsorption on the overall mass flux in a porous solid. The method does not require the knowledge of tortuosity factor, the accurate values of average pore radius for micro, transitional and macro pores, or the porosities corresponding to micro and macro pores, which are required in case of diffusion in the transitional region and in the solids containing bimodal pore size distribution.     

Protein adsorption kinetics in charged agarose gels: Effect of agarose content and modeling

The adsorption kinetics of myoglobin in charged gels of varying agarose content have been measured macroscopically, through batch uptake experiments, and microscopically, using light microscopy with gels supported in microfluidics chips. The apparent effective pore diffusivities, determined by fitting either set of rate data to the shrinking core model, were greater than the free solution diffusivity and concentration‐dependent. Moreover, the microscopically derived concentration profiles were qualitatively different from the predicted ones. Therefore, a new model taking into account an assumed favorable partitioning of the protein in the pore liquid is proposed to describe the adsorption kinetics. The new model yields effective pore diffusivities that are in approximate agreement with the values determined chromatographically under nonbinding conditions and with hindered diffusion theory. In addition, it predicts concentration profiles in the gel that are consistent with those observed microscopically. The overall increase in mass transfer is attributed to the favorable partitioning of the protein in the pores at low ionic strength, which results in a greater diffusional driving force. © 2008 American Institute of Chemical Engineers AIChE J, 2009     

Adsorption on activated carbon in countercurrent flow: An experimental study

The work describes adsorption experiments from aqueous solutions on activated carbon using a counter-current adsorber. Phenol and paranitrophenol were used for single component adsorption and molasses colour for multicomponent adsorption experiments. Isotherms were determined using simple equilibrium experiments. Three different techniques were used for determination of the kinetics. These were finite bath, infinite bath and fixed bed experiments. A mathematical model for countercurrent adsorption was tested. The model includes the effect of film diffusion and pore diffusion as well as surface diffusion, and can handle systems with a nonlinear isotherms. Kinetic data in the form of an average diffusivity in the carbon determined from the finite bath experiments and isotherm data did not predict the operation of the countercurrent column well. Data from the fixed bed experiments predicted countercurrent column operation much better. This is deemed to be due to inhomogeneities in the carbon used, resulting in a fairly quick initial uptake of the main part of the solute and a slower uptake of a minor amount.