Radial equilibrium adsorption dynamics for the rectangular isotherm

Conclusions The problem of radial equilibrium adsorption dynamics, taking into account longitudinal diffusion, was discussed for highly convex (rectangular) isotherms. A rule was obtained for movement of the adsorption wave front in a cylindrical adsorber. The time of the adsorber protective action was estimated.Translated from Izvestiya Akademii Nauk SSSR, Seriya Khimicheskaya, No. 6, pp. 1455–1458, June, 1975.     

Mixed-matrix membrane adsorbers for protein separation

The separation of two similarly sized proteins, bovine serum albumin (BSA) and bovine hemoglobin (Hb) was carried out using a new type of ion-exchange mixed-matrix adsorber membranes. The adsorber membranes were prepared by incorporation of various types of Lewatit ion-exchange resins into an ethylene-vinyl alcohol copolymer porous structure. The obtained heterogeneous matrices, composed of solid particles surrounded by the polymeric film, display high static and dynamic protein adsorption capacities. The effect of operational parameters such as filtration flow-rate, pH, and ionic strength on the protein separation performances was investigated for cation- as well as anion-exchange adsorber membranes. An average separation factor was calculated by numerical integration of the protein concentration in the permeate curve during the filtration run. High average separation factor values were obtained for BSA-Hb separation at physiological ionic strength with a filtration flow-rate up to 20 1/h per m2, until the protein breakthrough point at 10% of the feed concentration.     

Diffusional study of the reaction of sulfur dioxide with reactive porous matrices

A single-pellet high-temperature diffusion cell reactor is used to study the sulfation of calcined Greer limestone pellets. The effective diffusivities of gases through the reactive pellets, during the calcination and sulfation are determined. The experimentally determined effective diffusivity of sulfur dioxide through the pores of the product shell is used in the modified expanding grain model to obtain the diffusivity of sulfur dioxide through the product shell of the grains as a function of the conversion and the reaction temperature. The activation energy for the initial diffusivity of sulfur dioxide through the product shell of grains, is found to be 34.13 kcal mol^?1; the diffusivity values decreased with increasing conversion. Additionally it is found that the ratio of the tortuosity of reacting shell of pellet to the initial pellet tortuosity before any sulfation was increased with increasing conversion.     

Stability of the Front of Filtration Combustion of Bidisperse Fuel Mixture in an Inclined Rotating Gas Generator

To characterize the stability of the filtration combustion (FC) front, a dimensionless coefficient that describes the spatial distortions of the combustion front and is equal to the ratio between the maximum and minimum front width is suggested. It was shown for the example of bidisperse fuel mixtures of hard coal that, with an inclined rotating reactor, the gasification process can be stabilized as compared with the vertical reactor. A stable combustion front was observed at any content of the fine fraction in experiments of gasification of a fuel composed of 5–7- and 3–5-mm fractions. A stable combustion front was observed in experiments with a fine (1–2 mm) fraction up to its content of 60%.     

Structural and Electrokinetic Characteristics of High-Silica Porous Glasses in Nickel Chloride Solutions

Colloid Journal - The structural (structural resistance coefficient, volume porosity, tortuosity coefficient, filtration coefficient, and specific surface area) and electrokinetic (specific...     

Hollow-fiber membrane adsorber: Mathematical model

Two opposite design strategies for ultrafiltration/microfiltration filters: (1) reduction of concentration polarization and particle deposition to increase permeate velocity and (2) utilization of particle deposition on membrane surface to produce an additional (to permeate) volume of clarified water, are analyzed. It is shown that the first strategy is always associated with additional expenditures in power or other material resources, making it not enough cost-effective to be competitive with non-membrane filtration processes in some water treatment applications. At the same time, the second strategy does not require additional power expenditures and provides high water recovery and cost-effectiveness. The mathematical model describing the performance of hollow-fiber membrane adsorber, which represents a second-strategy filter, is studied. A general form of the particle-deposition equation is introduced, and its terms are analyzed. As a result, its linearized form, looking like a linear equation of reversible adsorption, is chosen. A numerical solution to the system of governing equations is obtained and used to assess the accuracy of approximate solutions. A new approximate solution allowing one to evaluate the adsorber particle retentions with an acceptable accuracy is suggested.     

Characteristics of the Porous Structure of Cement Stone

The complex study of filtration and electric properties of the samples of cement stone with different water-cement ratios is performed. It is established that filtration coefficient decreases by 4–6 times with an increase in a pressure drop and becomes constant at pressure drops above 3–3.5 MPa. The observed effect is interpreted as a reversible change in the internal structure of cement stone upon the filtration of a liquid through the stone. It is revealed that the filtration coefficient and porosity of samples decrease with time. Total open porosity and the most probable pore radius are determined by mercury porosity technique. Coefficients of structural resistance and pore tortuosity of the samples are determined from the comparison of through and total porosity. The values of streaming potential are measured and values of surface charge and potential of the samples of cement stone are calculated.     

Elimination of non-uniform, extra-device flow effects in membrane adsorbers

Commercial use of membrane adsorbers in the biotechnology industry is increasing. Here the system time lag created by membrane adsorber peripherals and the membrane adsorber flow distribution headers has been modeled using an anion exchange membrane and bovine serum albumin (BSA). The system time lag was modeled as a zero order and first order time lag. The zero and first order time lags have been removed from the breakthrough curve. The method used does not involve fitting a mathematical expression to the breakthrough curve. Further no assumptions are made regarding the shape of the breakthrough curve in the absence of the time lag. The method has been used to calculate the Langmuir isotherm parameters.The membrane capacity was found to be twice as large as the capacity determined after removal of the time lag. The Langmuir constant was five times as large for the system without accounting for the time lag. Errors in fitting isotherm parameters can significantly impact frontal analysis and membrane adsorber scale-up. The Langmuir isotherm calculated under dynamic conditions with the system time lag removed, was in agreement with the static adsorption isotherm.     

Diffusion macroscopique dans un tuffeau et un alginate,mesure IRM

Although Pulsed Field Gradient experiments allow measuring a diffusion coefficient at different time and length scales, it may be of some interest to use macroscopic methods. The result of a macroscopic diffusion is viewed here by proton MRI. For water in a limestone, analysing a concentration profile following a superficial coating gives a precise measure. For a divalent ion diffusing in an alginate gel or in the initial alginate solution, the reaction front position allows a tortuosity comparison. The originality of the last part is to visualize the syneresis phenomenon. Moreover, it makes it possible to estimate the maximum reaction time for the chelation (1 ms).     

Modelling of solid-liquid adsorption: effects of adsorbent heterogeneity

Effects of adsorbent heterogeneity on the adsorption of cobalt phthalocyanine dye on activated carbon have been studied. Adsorption experiments were carried out by varying the temperature and adsorbent mass in batch adsorbers and, in addition, the adsorbent particle size and fluid flow rate in a continuous stirred tank reactor (CSTR)-type adsorber in order to investigate the equilibrium and the kinetics of adsorption.The Brunauer-Emmett-Teller (BET), Langmuir with uniform distribution (LUD) and Langmuir-Freundlich equations are able to represent the equilibrium data with similar accuracy within the range of measurements. Reasonably large values of the heterogeneity parameter (2.69–2.86) show that the carbon surface is energetically heterogeneous.A mathematical model that describes the adsorption dynamics, including film-, pore- and concentration-dependent surface diffusion on an energetically and structurally heterogeneous adsorbent, is presented here and fitted to the experimental concentration vs. time curves obtained in the continuously stirred tank adsorber.Structural heterogeneity of the carbon, if not accounted for in the kinetic model, can be responsible for the very strong concentration dependence of the surface diffusion coefficient and for the variation in the parameter D_o with particle size and adsorber porosity as shown in this work.     

Modeling of submicrometer aerosol penetration through sintered granular membrane filters

We present a deep-bed aerosol filtration model that can be used to estimate the efficiency of sintered granular membrane filters in the region of the most penetrating particle size. In this region the capture of submicrometer aerosols, much smaller than the filter pore size, takes place mainly via Brownian diffusion and direct interception acting in synergy. By modeling the disordered sintered grain packing of such filters as a simple cubic lattice, and mapping the corresponding 3D connected pore volume onto a discrete cylindrical pore network, the efficiency of a granular filter can be estimated, using new analytical results for the efficiency of cylindrical pores. This model for aerosol penetration in sintered granular filters includes flow slip and the kinetics of particle capture by the pore surface. With a unique choice for two parameters, namely the structural tortuosity and effective kinetic coefficient of particle adsorption, this semiempirical model can account for the experimental efficiency of a new class of "high-efficiency particulate air" ceramic membrane filters as a function of particle size over a wide range of filter thickness and texture (pore size and porosity) and operating conditions (face velocity).     

Hydrogen PSA process product purity control method and controller

It is well known in the industry that a primary means for controlling the pressure swing adsorption (PSA) process product gas purity is the adjustment of PSA feed time or adsorption time. If the product impurity is too high, the feed time is shortened and if the impurity level is below the target the feed time is increased. Conventionally, the plant operator monitors the product purity and manually adjusts the feed time. Several control methodologies such as classical feedback and feedforward systems were suggested to automate this task with limited success. A novel control methodology based on the measurement of impurity fronts within the adsorber bed was developed by the Praxair Adsorption R&D team. The response of the concentration measurements inside the adsorber vessel to the process upsets and changes in feed time is more rapid than in the product stream. Consequently, closed loop control performance can be made much more effective and the operating impurity set points for product gas can be more aggressive resulting in longer PSA feed times, higher bed utilization and thus higher hydrogen recovery. The control methodology will be discussed in greater detail along with the advantages it has to offer such as improved process performance, disturbance rejection capability and improved process robustness. The control methodology will be illustrated using the hydrogen PSA process as an example.     

The role of salts derived from benzilic acid and quinolines in the adsorption of some actinides Part I: Characterization of the adsorbers

The salt of the 8-hydroxyquinoline and benzilic (diphenylglycolic) acid was prepared and incorporated into active charcoal in order to have an adsorber able to concentrate actinides dispersed in natural waters before quantitative or radiochemical analysis. The formation and the characterization of this adsorber, (adsorber B), was compared with another system containing benzilic salt of the substituted quinoline, 2-methyl, 8-hydroxyquinoline, (adsorber R). The adsorption ability of the adsorbers B and R was compared with a third product (adsorber G), prepared by incorporating benzilic acid with d-glucosamine into the charcoal. In this case, d-glucosamine gives a better stability to the system, as otherwise the benzilic acid could partially be dissolved into the water system at equilibrium, during the adsorption experiments. The dissociation acid constants of all the considered components were measured, in order to have some information on the adsorption mechanism. The compound formed during the adsorption on the prepared adsorbers with uranium, thorium, and samarium were separately analyzed and identified by means of IR and NMR. The role of the components in the adsorption was evidenced. This revised version was published online in July 2006 with corrections to the Cover Date.     

Combustion Rate of Solid Fuels in the Superadiabatic Mode

Theoretical and experimental dependences of the combustion front propagation velocity in a layer of a solid carbon fuel on various external factors and conditions were examined in the case of filtration of the gaseous oxidizing agent. Particular attention was given to the superadiabatic modes with heat accumulation. It was shown that, in the case of a superadiabatic filtration combustion mode, the combustion velocity is primarily determined by the supply rate of the oxidizing agent and by the stoichiometric process ratio for particular conditions.     

Capillary rise of liquids over a microstructured solid surface

The location of the triple line as a function of time has been recorded for a series of organic liquids, with various surface tension to viscosity ratios, wicking upward a rough Cu(6)Sn(5)/Cu intermetallic (IMC) substrate. The complex topographical features of such an IMC rough surface are characterized by surface porosity and surface roughness. A theoretical model for wicking upward a rough surface has been established by treating the rough IMC surface as a two-dimensional porous medium featuring a network of open microtriangular grooves. The model is verified against experimental data. The study confirms that the kinetics of capillary rise of organic liquids in a nonreactive flow regime over a porous surface having arbitrary but uniformly distributed topographical features involves (i) surface topography metrics (i.e., permeability, tortuosity/porosity, and geometry of the microchannel cross section); (ii) wicking features (i.e., contact angle and filling factor); and (iii) physical properties of liquids (i.e., surface tension and viscosity). An excellent agreement between theoretical predictions and experimentally obtained data proves, for a selected filling factor η, validity of the analytically established model. Scaled data sets show that, for a given rough surface topography, (i) wicking kinetics of considered liquids depend on properties of liquids, that is, surface tension to viscosity ratios and contact angles; (ii) the filling factor for all tested liquids is an invariant, offering good prediction within the range of ~0.9-1.0. The distance of the wicking front versus square root of time relationship was well established throughout the whole considered wicking evolution time.     

Surface structural characterization of highly porous activated carbon prepared from corn grain

A novel corn grain precursor was used for the preparation of activated carbon by chemical activation. The detailed investigation of the porosity development in the prepared activated carbon was done by altering the various activation conditions such as the activation temperature, activation time and ratio between the powdered form of carbonized corn grain char and KOH. The surface characteristics including the surface roughness of all the activated carbon samples were evaluated from the analysis of nitrogen (N₂) adsorption isotherm data. At the maximum of 2978 m²/g, a super surface area having the corn grain‐based activated carbon (CG‐AC) was synthesized by using the following conditions: 1/4 ratio of powdered form of carbonized corn grain char/KOH; 800 °C; and 4 h. The possibility of preparing highly porous activated carbons with controlled porosity by varying different activation conditions was found from the pore size distribution results. In particular, the domination of the ratio between the powdered form of carbonized corn grain char and KOH on the porosity development was high compared to the activation temperature and activation time. In addition, the surface roughness calculated from the surface fractal dimension indicates the decrease of surface roughness with increasing activation conditions. Copyright © 2009 John Wiley & Sons, Ltd.     

Influence of microstructure and crystalline phases on impedance spectra of sodium conducting glass ceramics produced from glass powder

Crystallization of highly ionic conductive N5 (Na₅YSi₄O₁₂) phase from melted Na_3+3x-1Y_1-xP_ySi_3-yO₉ parent glass provides an attractive pathway for cost-effective manufacturing of Na-ion conducting thin electrolyte substrates. The temperature-dependent crystallization of parent glass results in several crystalline phases in the microstructure (N3 (Na₃YSi₂O₇), N5 and N8 (Na8.1Y Si6O18) phases) as well as in rest glass phase with temperature dependent viscosity. The electrical properties of dense parent glass and of compositions densified and crystallized at 700 °C, 800 °C, 900 °C, 1000 °C, and 1100 °C are investigated by impedance spectroscopy and linked to their microstructure and crystalline phase content determined by Rietveld refinement. The parent glass has high isolation resistance and predominantly electrons as charge carriers. For sintering at ≥ 900 °C, sufficient N5 phase content is formed to exceed the percolation limit and form ion-conducting pathways. At the same time, the highest content of crystalline phase and the lowest grain boundary resistance are observed. Further increase of the sintering temperature leads to a decrease of the grain resistance and an increase of grain boundary resistance. The grain boundary resistance increases remarkably for samples sintered at 1100 °C due to softening of the residual glass phase and wetting of the grain boundaries. The conductivity of fully crystallized N5 phase (grain conductivity) is calculated from thorough impedance spectra analysis using its volume content estimated from Rietveld analysis, density measurements and assuming reasonable tortuosity to 2.8 10⁻³ S cm⁻¹ at room temperature. The excellent conductivity and easy processing demonstrate the great potential for the use of this phase in the preparation of solid-state sodium electrolytes.

     

Accurate evaluations of both porosity and tortuosity of anodic films grown on rolled AA 1050 and on rolled or machined AA 2024 T3

The porosity of the anodic films grown on aluminium substrates depends on various operating conditions related to the anodization electrolyte and to the applied electrical parameters, as well as to the substrate itself. In the present study, three different aluminium substrates were studied and anodized: AA 1050 (rolled; thickness = 1 mm), AA 2024 T3 (rolled; 1 mm), and AA 2024 T3 (machined; 3 mm). For each type of anodic film, the porosity, as well as its changes during anodization, was accurately characterized using both field-emission gun scanning electron microscopy (FEG-SEM) and a reanodization technique. Moreover, for the first time, the corresponding tortuosity was quantified for all studied substrates. Results for rolled AA 2024 T3 and for machined AA 2024 T3 especially showed significant differences in tortuosity values, contributing towards clarifying, in part, their different wettability characteristics or anticorrosion behaviour, so far not clearly explained.     

Experimental Results and Analysis for Adsorption Ice-Making System with Consolidated Adsorbent

An adsorption ice-making machine has been built with a single consolidated adsorber and activated carbon-methanol pair. A consolidated adsorbent block made of activated carbon mixed with a binder with good heat transfer properties has been developed and implemented in the adsorber. The design is focused on the adsorber consisting of copper finned tubes and carbon blocks. Experimental tests have been performed suitable for ice making. This paper describes the experimental results of such an ice-maker operating with an intermittent cycle and a cycle time of 35 minutes. The thermal conditions used to test the cycle are: 115°C heat source, 22°C heat sink, the evaporator temperature corresponding to the chilled ethylene glycol temperature is –7°C. At this evaporating pressure, the mass transfer resistance controls the adsorption process. Test results show that the COP reaches 0.07 whereas the SCP (specific cooling power) is 11 W kg^–1 activated carbon. A two-bed adsorptive prototype ice-making machine operating with a heat and mass recovery cycle has also been made for onboard adsorption refrigeration in fishing boats. Good performances have been achieved due to improved mass transfer and the new ice maker can produce 18–20 kg h^–1 of flake ice at mean temperature of –7°C.     

Mass transfer in composite polymer-zeolite catalytic membranes

The incorporation of zeolite-encaged iron-phthalocyanine partial oxidation catalysts into a dense hydrophobic polymer membrane results in a substantial improvement in catalyst performance. The diffusion through these zeolite-filled membranes is described using a two-dimensional model, and it is demonstrated that for a permeability ratio (polymer over catalyst) higher than 10⁴, the diffusion through composite polymer-zeolite membranes can be described by a one-dimensional model. Such a one-dimensional mathematical model was developed and validated with the experimental data, obtained from the time lag measurements on zeolite-filled poly(dimethylsiloxane) polymer membranes. Consequently diffusion through composite catalytic membranes can be predicted using the mass transfer coefficients of pure catalyst and polymer material, and a single tortuosity factor, only dependent on the catalyst loading.