A comparison of submerged and sidestream tubular membrane bioreactor configurations

This paper provides an improved understanding of the effect of sidestream (SS) and submerged (Sub) MBR configurations on hydraulic and biological system performance for a tubular membrane geometry. Effects of key flow parameters, these being aeration rate (U_G) in the Sub MBR and cross flow velocity (CFV) in the SS MBR, on fouling behaviour have been assessed during short-term flux-step experiments. Both synthetic and real sewage feeds have been used. Series of tests carried out with both feeds indicate the similar fouling behaviour observed for Sub and SS MBRs operated at U_G of 0.07-0.11 m s⁻¹ and CFV of 0.25-0.55 m s⁻¹ respectively. Analysis of the TMP-based parameters determined from the flux-step experiments show the effect of U_G in Sub configuration to be greater than those of CFV in SS MBR, and to be more efficient at higher fluxes (up to 97% decrease in fouling rate for U_G increased from 0.02 to 0.2 m s⁻¹, at 291 m⁻² h⁻¹). The influence of MBR configuration on biomass characteristics was also assessed by acclimatising the biomass at three MLSS concentrations for both configurations and revealed the carbohydrate contained in the biomass supernatant to be a possible indicator of fouling for MBR operation.     

Experimental studies of flame stability and emission characteristics of simple LPG jet diffusion flame

In the present study, experiments were carried out to measure the lift-off height, H_L; flame length, L_f and blow-off velocity for a simple LPG (liquefied petroleum gas) jet diffusion flames. It is observed that lift-off height is proportional to the fuel exit velocity, U_f. A semi-empirical correlation between lift-off height and global strain rate, U_f/D_f is proposed. Two regimes identified either as buoyancy or momentum dominated were characterized by Froude number, Fr. For momentum dominated jet diffusion flames, L_f/D_f remains almost constant and therefore is independent of the Froude number. The NO_x emissions, expressed in terms of emission index, EINO_x is found to decrease with U_f. This decreasing trend is consistent with the concept that increasing jet velocity reduces the residence time as reported in the literature. The present data is also compared with the available data of propane gas and found to be in good agreement well particularly in trend wise. Besides these data, EINO_x scaling law is also reported in the present study.     

Microstructure and rheological properties of pH-responsive core-shell particles

The microstructure and rheological properties of core-shell pH-responsive microgels consisting of poly(methyl methacrylate) (PMMA) particles grafted with a soft layer of methacrylic acid-ethyl acrylate (MAA-EA) cross-linked with di-allyl phthalate (DAP) were examined using dynamic light scattering and rheological techniques. The validity and limitation of the semi-empirical approach to model charged soft microgel particles developed by our group were tested on this core-shell system. The viscosity data for three different core-shell particles showed excellent agreement with the modified Krieger-Dougherty (K-D) model. Good agreement was also observed when our semi-empirical approach was compared against a theoretical model, which confirmed the validity of the semi-empirical approach to model charged soft particles. In addition, we confirmed that the new scaling law which relates the swelling ratio Q of microgels as a function of neutralization degree, α, average number of monomers between two cross-links, N_x, molar fraction of acidic units, y and concentration of mobile counter-ions, CK⁺ and C⁺Na, represented as (Nx/c₀)(CK⁺+C⁺Na)Q+Q2/3 is proportional to yN_xα. All the core-shell data at varying ionic strength and mobile counter-ions concentrations fall onto a master curve.     

Estimation of hindered settling velocity of suspensions

Four effective-medium models (EM-I, II, III, IV) are utilized and compared for determining hindered settling velocity of equi-sized particles in a viscous fluid. Among the models, EM-IV model is found to accurately predict the effective viscosity and the hindered settling velocity of monodisperse suspensions. In EM-IV model which was developed for determining the diffusivity of proteins in a biological membrane by Dodd et al. [T.L. Dodd, D. A. Hammer, A.S. Sangani, D.L. Koch, J. Fluid Mech. 293 (1995) 147], the effective-medium region begins at the distance R = a[(1 ? S(0))/?]^1/3 from the origin where the center of the test particle is located, where a is the radius of the particle, ? is the volume fraction of the particles in the suspension, and S(0) is the zero wavenumber limit of the structure factor. The estimations by EM-IV model agree very well with the exact calculations and the experimental observations. The hindered settling velocity U of the particles is given, in Richardson–Zaki form, by U/U₀ = (1 ? ?)^5.5, where U₀ is the settling velocity for an isolated particle.     

Prediction of bubble size in a gas fluidised bed

It is shown that existing data on bubble size (when this is not restricted by the vessel dimensions) can be described by

where (U — U_mf) is the excess gas flow, h is the height above the distributor and h₀, a measure of the initial bubble size, characterises the distributor. h₀ is effectively zero for a porous plate but may be more than a meter for large tuyeres.     

Hydrodynamic and mass transfer characterization of a flat-panel airlift photobioreactor with high light path

This work evaluates the volumetric mass transfer coefficient (k_La), the gas hold-up (?) and the mixing time (t_m) as a function of superficial gas velocity (U_G) in a flat-panel photobioreactor (PBR) with high light path. CO₂ utilization efficiency and volumetric power consumption (P/V) were also evaluated. A 50 L working volume photobioreactor was developed, 0.67 m in length, 0.57 m in height and 0.15 m in width (light path). The height-width ratio was 3.8, which is lower than reported in most PBRs. Initially, experiments were performed with air and tap water (biphasic system) and, subsequently, using a Spirulina sp. culture (triphasic system: air, culture medium, cells). Minimum and maximum superficial gas velocity values were 5 × 10⁻⁵ and 8.4 × 10⁻³ m s⁻¹, respectively. Maximum values for k_La and ? were 20.34 h⁻¹ (0.0057 s⁻¹) and 0.033 in the biphasic system, and 31.27 h⁻¹ (0.0087 s⁻¹) and 0.065 in the triphasic system. CO₂ utilization efficiency was 30.57%. Results indicate that the hydrodynamic and mass transfer characteristics of this photobioreactor are more efficient than those reported elsewhere for tubular and other flat-plate PBRs, which opens the possibility of using PBRs with higher light paths than yet proposed.     

Dependence of particle fluctuation velocity on gas flow, and particle diameter in gas fluidized beds for monodispersed spheres in the Geldart B and A fluidization regimes

In this paper we present new experimental data on the steady-state, mean squared, fluctuation velocity, or granular temperature, of Geldart B polymer, glass, nickel, and stainless steel monodispersed spheres averaged over the wall of a gas fluidized bed, as a function of gas flow and sphere diameter. The granular temperature is obtained by Acoustic Shot Noise technology—namely power spectral analysis of the steady state vibrational energy of the wall excited by random sphere impact, and calibrated by hammer excitation over the wall. The new data extends to polymer and metallic spheres the experimental discovery of a 1996 paper of Cody et al. that the fluctuation velocity of Geldart B glass spheres when scaled to the gas superficial velocity, U_s, is inversely proportional to sphere diameter, directly proportional to a fundamental length scale, D_o^B, and is a universal function of U = (U_s / U_mf). We also demonstrate that the new data is consistent with the diameter dependence of the fluctuation velocity that can be derived from both the 1997 paper of Menon and Durian, who measured random sphere motion near the wall through the spectroscopy of scattered laser light, and the 1992 paper of Rahman and Campbell, who measured the average granular pressure of random sphere impact on a porous steel membrane. While the inverse scaling of the fluctuation velocity with sphere diameter, and the existence of a fundamental length scale for gas fluidization, D_o^B, had not been a feature of any published fundamental model, or computer simulation, of the steady state granular temperature of spheres in gas fluidized beds, we show that it is a feature of two recent dense kinetic fluidization models published in 1999, by Buyevich and Kapbasov, and Koch and Sangani. Both theories implicitly define a fundamental length scale for the fluctuation velocity, D^? = (μ_f² / ρ_p²g)^1 / 3, where ρ_p is the sphere density, μ_f is the gas viscosity, and g is the laboratory gravitational field. The new data for polymer, glass, nickel and stainless steel spheres presented in this paper, defines D_o^B = (56 ± 2)D^?. We use the Anderson-Jackson stability model to show that the length scale D_o^B, also defines a stability length scale, such that for D < D_o^B(D > D_o^B), the uniform dense phase of the fluidized bed is stable (unstable), against one dimensional, first order fluctuations in sphere concentration. The length scale, D_o^B is thus the theoretical equivalent to the empirical scaling length introduced by Geldart, D_B/A, to distinguish spheres (D > D_B/A) that bubble at fluidization, from spheres (D < D_B/A) that fluidize before bubbling. Finally, we present new experimental data, on the remarkable changes in the granular temperature, bed expansion, and bed collapse time, between Geldart B and Geldart A monodispersed glass spheres, and compare that data to granular temperature, and bed expansion, for Geldart A rough, non-spherical, log-normal dispersed diameter catalytic particles.     

Forced translocation of polymer chains through a nanotube: A case of ultrafiltration

Translocation of polymer chains under the application of an external force has been studied through coarse-grained Monte Carlo simulations. The chains are pulled through a nanotube of finite length and diameter and their translocation times measured. The average translocation time, τ follows a scaling relation involving the chain length, N and applied force, F as, τ ∼ N^ν′F^−μ, where ν′ and μ are two different exponents (ν′ = 0.674, and μ = 0.95 ± 0.05). The scaling law is closely similar to the nanopore translocation scaling law reported by Milchev et al. [Ann N Y Acad Sci 2009;1161:95]. Characteristic signatures of the chain escape time have been exhibited by the square of end-to-end distance R², axial radius of gyration R_g−x and other constituent properties. The behavior of the linear polymers under the application of a pulling force has been exploited to gain insights into the ultrafiltration process of unentangled polymers in dilute solution. The generic pulling force-translocation time (F, τ) data obtained through simulation can be matched reasonably well with the hydrodynamic force-critical macroscopic flow time (f_h, Q_c⁻¹) data and also with the hydrodynamic force-reduced critical microscopic flow time (f_h, q_c⁻¹) data obtained in the ultrafiltration experiment on long linear polystyrene chains in cyclohexane, as recently reported by Ge et al. [Macromolecules 2009;42:4400] The simulation technique reported here may be extended to study biomolecular transports occurring in long protein channels, as studied experimentally through current-time or voltage-time traces.     

Effect of System Variables on Heat Transfer to Canned Particulate Non-Newtonian Fluids During End-Over-End Rotation

Apparent heat transfer coefficients h_ap and U_a were evaluated to quantify the heat transfer process with particulates in high viscosity non-Newtonian fluids in end-over-end thermal processing. An orthogonal array L16 experiment was used to examine the significances of system factors on h_ap and U_a values with plastic particles in CMC aqueous solutions. The variance analysis showed that rotation speed, liquid viscosity, retort temperature, particle material and particle concentration were significant factors (P < 0.05) for h_ap and U_a. The effects of can size was also significant for h_ap. A central composite rotatable design (CCRD) experiment and two full factorial experiments were carried out to study the effects of those significant factors on h_ap and U_a values. Results showed that with the decrease of liquid viscosity and the increase of rotation speed, particle density and retort temperature, h_ap and U_a values increased. With the increase of can size h_ap values decreased. With the particle concentration increasing h_ap and U_a values firstly increased and then decreased with further increase in particle concentration.     

Radial gas mixing in a fluidized bed using response surface methodology

Radial gas mixing in a fluidized bed was studied using response surface methodology (RSM), which enables effect examinations of parameters with a moderate number of experiments. All experiments were conducted in a 0.29-m ID fluidized-bed cold model. The gas dispersion process within the bed is described using the dispersed plug flow model. Pure carbon dioxide was used as the tracer gas, continuously injected into the center of the bed by a point source. The downstream radial tracer concentration profile was measured using a gas chromatograph.The radial gas dispersion coefficient, D_r, was well correlated with operating parameters and the particle and gas properties: (U−U_mf)/U_mf, H_s/d_b, φ_d, and Ar, with a determination coefficient R² of 0.966. Effect test indicates that the dimensionless characteristic velocity, (U−U_mf)/U_mf, has the most significant influence on D_r, while the static bed height to bed diameter ratio, H_s/d_b, is less remarkable. The interactions of (U−U_mf)/U_mf with the distributor open-area ratio, φ_d, and with the Archimedes number, Ar, both play important roles. An evolutive response surface model was proposed to describe the radial gas mixing in the bubbling/slugging fluidization regimes.     

The heat transfer coefficient between a particle and a bed (packed or fluidised) of much larger particles

The heat transfer coefficient has been measured for a heated phosphor-bronze sphere (diam. 2.0, 3.0 or 5.56 mm) added to a bed of larger particles, through which air at room temperature was passed. The bronze heat transfer sphere was attached to a very thin, flexible thermocouple and was heated in a flame to before being immersed in the bed. The cooling of the bronze sphere enabled the heat transfer coefficient, h, to be measured for a variety of U/U_mf, as well as diameters of both the particles in the bed and the heat transfer sphere. It was found that before the onset of fluidisation, h rose with U, but h reached a constant value for U?U_mf. These measurements indicate that in this situation (of a relatively small particle in a bed of larger particles) all the heat transfer is between the hot bronze sphere and the gas flowing over it. Consequently, a Nusselt number, based on the thermal conductivity of the gas, is easy to define and for U?U_mf (i.e. a packed bed), Nu is given by

     

Numerical modeling of particle fluidization behavior in a rotating fluidized bed

In this study, numerical modeling of particle fluidization behaviors in a rotating fluidized bed (RFB) was conducted. The proposed numerical model was based on a DEM (Discrete Element Method)-CFD (Computational Fluid Dynamics) coupling model. Fluid motion was calculated two-dimensionally by solving the local averaged basic equations. Particle motion was calculated two-dimensionally by the DEM. Calculation of fluid motion by the CFD and particle motion by the DEM were simultaneously conducted in the present model. Geldart group B particles (diameter and particle density were 0.5 mm and 918 kg/m³, respectively) were used for both calculation and experiment. First of all, visualization of particle fluidization behaviors in a RFB was conducted. The calculated particle fluidization behaviors by our proposed numerical model, such as the formation, growth and eruption of bubble and particle circulation, showed good agreement with the actual fluidization behaviors, which were observed by a high-speed video camera. The estimated results of the minimum fluidization velocity (U_mf) and the bed pressure drop at fluidization condition (ΔP_f) by our proposed model and other available analytical models in literatures were also compared with the experimental results. It was found that our proposed model based on the DEM-CFD coupling model could predict the U_mf and ΔP_f with a high accuracy because our model precisely considered the local downward gravitational effect, while the other analytical models overpredicted the ΔP_f due to ignoring the gravitational effect.     

Process development and modeling of pyruvate recovery from a model solution and fermentation broth

The mono- and bi-polar electrodialysis processes for pyruvate recovery and pyruvic acid generation, respectively, were examined in order to determine their feasibility for application in the pyruvate production process. Under optimum process conditions (constant current mode i = 39.7 A m⁻², pyruvate model solution c_p = 50 g dm⁻³ in the monopolar electrodialysis experiment pyruvate flux reached 367 g m⁻² h⁻¹ and specific energy consumption was 1.4 kWh kg⁻¹. In the bi-polar electrodialysis experiment under optimum process conditions (constant current mode i = 9.6 A m⁻², pyruvate model solution c_p = 48 g dm⁻³, pyruvate flux reached 125 g m⁻² h⁻¹ and specific energy consumption was 1.5 kWh kg^-1. Generally speaking, performances of the bi-polar electrodialysis were equal to the best process conditions observed with mono-polar electrodialysis. On the other hand, current densities investigated in the bi-polar electrodialysis experiments were four-fold lower than those applied in the mono-polar electrodialysis experiments. Additionally, a mathematical model to represent the ion and water transport behavior of an electrodialysis process for concentrating pyruvic acid under the influence of different current density was developed. Estimation of both the model parameters and model validation were demonstrated in the work.     

Kinetics of Sedimentation of a Coagulating Suspension

The coagulation–sedimentation kinetics in a spatially heterogeneous disperse system is theoretically analyzed. The expression for the suspension concentration c as a function of time t and depth h is obtained in the form c ～ t ^?ε h ^εν. The concentration of the dispersed phase formed in coagulant hydrolysis depends on the coagulant concentration c ₀ as c ～ c ₀ ^{? γ} . It is determined how the exponents in the expressions derived are related to the characteristics of the coagulation kinetics and the aggregate size distribution. The results obtained are compared with published experimental data.     

Translocation of compact polymer chains through a nanopore

We perform dynamical Monte Carlo simulation to study the forced translocation of compact polymer chains in three-dimensional lattices. The chains are driven through a nanopore connecting two infinite channels by an external field. The scaling properties of average translocation time τ and translocation time distribution (TTD) are studied. The effects of contact energy (?_C), electric field strength (E), and nanopore width (L) on the scaling exponent (α) of average translocation time τ ∼ N^α and the TTD are investigated. For the scaling behavior of τ ∼ N^α, we have found that there is no crossover behavior with weak field strength when the nanopore width is one lattice spacing, which is less than average bond length, while crossover behaviors are observed for larger nanopore widths. The scaling exponent α also depends on contact energy ?_C and electric field strength E. For the TTD, it shifts from the Gaussian to a right-skew distribution with the electric field E increasing for short chains; while for long chains, multi-peak distributions are observed. As a primary and simple model, compact polymer chains are extensively used to capture the structure and thermodynamic properties of proteins, therefore we can investigate the protein translocation by simulating compact chain translocation, and this study will be useful for exploring the complex translocation behaviors of proteins.     

Influence of the lift force closures on the numerical simulation of bubble plumes in a rectangular bubble column

Numerical Eulerian-Eulerian simulations of the unsteady gas-liquid flow in a centrally aerated two-dimensional bubble column were carried out in order to understand the effect of different formulations of the lift force coefficient (C_L) on the computational results. Three different values of the superficial gas velocity (U_G=2.4, 12.0 and 21.3 mm s⁻¹) that ensure the existence of different flow regimes were experimentally and computationally studied. The validation of the simulated results was based on visual observations and measurements of the global gas hold-up (ε_G) and the plume oscillation period (POP). The results presented reveal that, at U_G=12.0 and 21.3 mm s⁻¹, using C_L<0 results in under- and over-estimation of the ε_G and POP, respectively. On the other hand, taking C_L>0 does not affect the POP while it leads to increasingly higher ε_G values, which are different from those experimentally reported. At U_G=2.4 mm s⁻¹, the effect of the lift force is not so evident, although it slightly improves the prediction of experimental values. Particularly interesting is the case of C_L>0.4 at U_G=21.3 mm s⁻¹, producing a non-symmetric bubble plume oscillation. Since using Tomiyama's lift coefficient correlation does not improve the results, including the lift force into the simulation of bubble plumes is not recommended.     

High capacity immobilization of U3O8 in Gd2Zr2O7 ceramics via appropriate occupation designs

An optimal occupation of U⁴⁺ and U⁶⁺ in Gd₂Zr₂O₇ is necessary for a really high immobilization capacity of U₃O₈ in Gd₂Zr₂O₇ based waste forms. Based on four kinds of occupation methods, a series of U₃O₈-doped Gd₂Zr₂O₇ compositions have been synthesized. The effects of U₃O₈ content on the phase and microstructure evolution of Gd₂Zr₂O₇ pyrochlore waste forms were investigated. Detailed XRD analysis show that the four sets of samples exhibit a single defect fluorite structure within the range of 0<x≤0.4, 0<x≤0.66, 0<x≤0.6 and 0<x≤1, respectively. The highest solubility of U₃O₈ is about 82.29 wt% when the occupation design (U⁴⁺ and U⁶⁺ substitute for Gd and Zr, respectively) was employed. It was found that the cell parameters of compounds in Set A (Gd_2–3x(U⁴⁺_xU⁶⁺_2x)Zr₂O_7+7x/2) decrease with increasing _x, while those of the other compositions increase. Moreover, the uranium are almost homogeneously distributed in all samples.     

A refined methodology for evaluation of heat transfer coefficients in canned particulate fluids under rapid heating conditions

The conventional methodology was refined for calculating the heat transfer coefficients (U and h_fp) under rapid heating conditions. The conventional methodology of h_fp evaluation became unreliable and/or non-reproducible under rapid heating conditions such as those encountered during reciprocation thermal processing. This was due to fluctuations in gathered transient temperatures during rapid reciprocating motion and due to very short equilibration times (EQT) (heat-up time to 1 °C below operating temperature).In this method, U and h_fp were calculated employing temperature profiles predicted by using an average retort temperature (after the come-up period) and heat penetration parameters, instead of real data points from experimental temperature profile as used in conventional methodology. The method was validated for various reciprocation frequencies (0–3 Hz) and amplitudes (0–20 cm). Results revealed that the refined methodology was robust and produced reliable and consistent values of U and h_fp, under both slow and rapid heating conditions. Also, the heat transfer coefficient values, using the developed method, consistently matched the results and trends observed with conventional methods. A parameter sensitivity analysis was also conducted and the effects of perturbations of different parameters employed in the refined methodology were reported.     

The solids flow in the riser of a Circulating Fluidised Bed (CFB) viewed by Positron Emission Particle Tracking (PEPT)

Circulating Fluidised Beds (CFB) are attracting increasing interest for both gas-solid and gas-catalytic reactions, although the operating modes in these two cases are completely different. In modelling CFBs as reactors, the solids residence time is an important parameter. Previous studies mostly assess operations at moderate values of the solids circulation rates (≤ 100 kg/m² s), whereas gas-catalytic reactions and e.g. biomass pyrolysis require completely different operating conditions. In the current work, Positron Emission Particle Tracking (PEPT) is used to study the movement and population density of particles in the CFB-riser.The PEPT results can be used to obtain: (i) the vertical particle movement and population density in a cross sectional area of the riser; (ii) the transport gas velocity (U_tr) required in order to operate in a fully established circulation mode; (iii) the overall particle movement mode (core flow versus core/annulus flow); and (iv) the particle slip velocity (U_s).Only in a core flow mode can the particle slip velocity be estimated from the difference between the superficial gas velocity (U) and the particle terminal velocity (U_t). The slip velocity is lower than U − U_t outside the core flow mode. To operate in core flow, the superficial gas velocity should exceed U_tr by approximately 1 m/s and the solids circulation rate should exceed 200 kg/m² s.     

Application of the DNDC model to the Rodale Institute Farming Systems Trial: challenges for the validation of drainage and nitrate leaching in agroecosystem models

Ecosystem models are increasingly used to guide natural resource management policy decisions. In this study, we build on available agroecosystem policy modeling tools by testing two methodologies for applying the Denitrification-Decomposition (DNDC) model to naturally-drained, temperate grain cropping systems. We used long-term observations from the Rodale Institute Farming Systems Trial (FST) to validate the DNDC model for application to grain cropping systems on silty clay loam soils typical of mid-Atlantic farmlands. Based on modeling efficiency (EF), Theil’s Inequality (U ²), and correlation coefficient (r) metrics, the DNDC model showed moderate fit between observations and simulations at annual time scales for drainage (EF = 0.34, U ² = 0.12, r = 0.74) and nitrate leaching (EF = ?0.05, U ² = 0.4, r = 0.86). Replication of observed seasonal water flux and nitrate leaching trends were difficult to capture in model simulations, resulting in a weak fit between observations and simulations for drainage (EF = ?1.2, U ² = 0.89, r = 0.28) and nitrate leaching (EF = ?2.5, U ² = 2.1, r = 0.3). Our comparison of observations and model outcomes highlights the challenge of scaling up belowground fluxes to farm or watershed scales. Ecosystem model representation of water transport generally assumes highly homogeneous soil conditions. In contrast, data from lysimeter sampling represents a small percentage of the total study area and is unlikely to capture average soil field properties. Additionally, our Rodale work highlights the limitation of biogeochemistry models which use vertical mass movement to describe water drainage and nitrate leaching. The application of the DNDC model to the Rodale FST demonstrates that model studies are not a simple substitute for field observation. The predictive utility of model outcomes can only be broadened through rigorous testing against long-term field observations.