Estimation Of Agitator Flow Shear Rate

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Mixing and Blending liquids, solids and gases into water and

Understanding the fluid flow in these tanks is critical for equipment design, scale-up, process control and economic factors. CFM models allow you to see what is taking place in the mixing vessel. The results enable an engineer to select the best agitator design to bt i th d i d f 20 obtain the desired process performance.


An analysis of the flow curves of the solutions under study showed that the maximum differences in shear stress between part of the hysteresis deter-mined at an increasing shear rate and the part of the hysteresis determined at a decreasing shear rate occurred at shear rate exceeding 121.5 s 1. This means

Hydrodynamic characteristics and mixing behaviour of

flow rate 1.4 vvm, pH 4.5±0.2. Biomass concentration was measured by dry weight estimation using GF/C filters (Whatman, Maidstone, UK). Extracellular polysaccharide was measured by precipitating scleroglucan from cell-free broth samples by addition of 2 vol of absolute alcohol. The precipitated biopolymer was then filtered, washed, dried and

stock preparation Total Stock Chest Mixing

impeller produces primary flow that induces a secondary flow within the vessel. In shear thinning fluids, the primary flow weakens severely within a relatively short distance from the impeller. Therefore, induced flow may not be adequate to produce the necessary shear stress to overcome yield stress. Fig. 3.

Introduction to mass transfer in single-use bioreactors

factors, including reactor geometry, agitator selection, power input, mixing, agitator shear, critical control parameter sensing, sparging, and bubble shear. Virtually all of these factors also play a role in the efficiency of the reactor, including oxygen mass transfer. The essential nature of oxygen mass transfer as a potential growth-

Aug us t 12-17, '1979 Sunday, August 12, 1979 3: 00 p.m. - 9

IIA Correlation - Tracking Technique for Shear Rate t<1easurement ll A cross beam laser technique, developed to measure particle fluid velocities in an agitated vessel, was extended to obtain shear rates. The estimation of the shear rates are useful in characterization of mixing operations. H H

Effect of aeration and agitation on volumetric oxygen

a value of 441.36 was obtained when the agitator speed 300 RPM and aeration 1.5 vvm was maintained. This shows that the volumetric oxygen transfer rate varies in variation with aeration and agitation and not based on organism used. The optimum conditions of agitation and aeration to achieve maximum K L a for a given microorganism

Aromatic nitrations by mixed acid. Fast liquid-liquid

where We is the Weber number of the main flow, defined as We = ~0: CT (4) This expression cannot be used when the dispersed phase hold-up is larger than 0.05 or when the dispersed phase is viscous, because the deformation rate is ne- glected. To take into account these restrictions, various

Estimation of Agitator Flow Shear Rate - Wiley

Apr 07, 2006 Estimation of Agitator Flow Shear Rate Jie Wu, Lachlan J. Graham, and Nabil Noui Mehidi Fluids Engineering Research Laboratory, Commonwealth Scientific and Industrial Research Organization (CSIRO), Highett 3190, Victoria, Australia DOI 10.1002/aic.10857 Published online April 7, 2006 in Wiley InterScience (

Coagulation and Flocculation - KFUPM

A cross-flow, horizontal shaft, paddle wheel flocculation basin is to be designed for a flow of 25,000m3/d, a mean velocity gradient of 26.7/sec (at 10°C), and a detention time of 45 minutes. The GT value should be from 50,000 to 100,000. Tapered flocculation is to be provided, and the three compartments of equal depth in series are to be used.

University of Groningen Circulation time prediction in the

and total viscous shear mixing in the helix. Integration of eqn. 5b with respect y yields the following expression for the velocity along the channel, u,: v, = v COSB - (7) where gg has been replaced by p where AP, is the total pressure drop across the helix. The flow rate, Q, through the helix (2 channels) is then


It Includes : Cost Estimation as per CPWD & General Specs. Generation of Monthly Cash Flow, Value, Cost, Over Head, Taxes, Profit & Labour. 55 Nos. of Forms / Data Sheets Including Fan /Blower /Pump/ Agitator/ Mixer Data Sheets. Measurement / Daily Progress Report. Includes 42 Nos of Design Programs.

Improving the process performance of gold cyanide leaching

A typical agitator configuration is two downward-pumping hydrofoil impellers, which requires a low mixing power input and results in low shear rates inside the reactor. This results in an economically efficient process with low levels of carbon attrition, to thus minimizing carbon and gold losses in CIL applications.


Agitator Retention: Permanent GROUT HOPPER MODELING STUDY JULY 2011 Savannah River National Laboratory Savannah River Nuclear Solutions Aiken, SC 29808 Prepared for the U.S. Department of Energy Under Contract Number DE-AC09-08SR22470

PHU6ROXWLRQ Tomohiro Nimura, Takuya Kawata and

cells in wall-bounded shear flow Tomohiro Nimura, Takuya Kawata and Takahiro Tsukahara-Vortical Structures in Wall-Bounded Turbulent Flow with Recirculation Syed Imran Shah-This content was downloaded from IP address on 03/07/2020 at 00:31


by dividing the liquid volume (in gallons) of a basin by the plant flow rate (gallons per minute). Actual detention time in a basin will be less than the calculated detention time because of dead areas and short circuiting, which could be due to inadequate baffling.

Flow Enhancement of Water-Soluble Polymers Through Porous

where Q is the flow rate, R 0 is the outlet radius and 𝜀ℎ is the Hencky strain found from the following equation: 𝜀ℎ= ( 𝑖 2/ 0) (S10) where R i is the inlet radius of the capillary. 4. Molecular weight estimation of polymer To determine the average molecular weight, the polymer needs to be extracted from the polymer solution.

Tackling Difficult Mixing Problems - AIChE

Shear-thickening fluids are sometimes called dilatant fluids, because many are high-concentration slurries that must expand (dilate) at the particle level in order to flow. Time-dependent non-Newtonian fluids change appar-ent viscosity not only with shear rate, but also during and following the applied shear. Time-dependent, shear-thinning

Application of the Ultrasound Velocity Profiling + Pressure

The UVP determines the volumetric flow rate by integration of the velocity profile. The LOGAC flow meter is capable of continuously measuring the volumetric flow rate. However, the measured flow rate is the average over a certain period of time; hence the true fluctuation of the flow rate remains unknown.

In the Name of God - Ferdowsi University of Mashhad

give constant shear. o Constant Reynolds number( ) implies geometrically similar flow pattern. Scale-up 27 Scale-up Important depended variables used in scale-up. 1. Energy input 2. Energy input/volume P/V N3 D i 2 3. Pump rate of impeller Q N D i 3 4. Pump rate of impeller/volume Q/V N 5. Impeller Tip Velocity V

Recognizing the Potential Impact of Agitation Directionality

CW direction result in Downward Axial Flow. Figure 2. Demonstration of potential for improved oxygen mass transfer with Upward Directional Flow Axial Agitation within the BIOne SUB. As ag-itation rate was increased over 250 rpm, improved mass transfer of oxygen was observed for upward axial flow agitation. Data are mean values of n = 2 trials.

Rheology and local study of a transparent model cohesive sediment

for a 300µm gap. Before flow curve measurements and to ensure a reproducible proceeding a pre-shear is applied with a shear rate of 10s-1 during 120s following by a 600s rest period. Then shear rate steps ranging from 10-3 3to 10 s-1 are applied in a logarithmic repartition to obtain up and down curves.

Mixing and Reaction Technology - flow control and applicators

Sulzer mixers create plug flow and greatly enhance heat transfer both within the fluid, and with contacting surfaces for temperature control. Turbulent mixing in an SMV mixer with 3 mixing elements. Mixing is one of the most important unit operations. The quality of mixing and dispersion and the rate it is achieved often have a major

Pellet Morphology, Broth Rheology and Statin Production in

viscosity (1.4 to 1.3 cP), pellet number (490-102) and size (3-5 to 0.5 to 3mm), also in yield stress and flow index while there was an increase in the consistency index under maximal conditions. The non-Newtonian (viscous)

Bioreactor Design - Weebly

with an internal loop cycle of fluid flow. 6.3.3 Loop Bioreactor A modified type of airlift system with gas and liquid flow patterns in which a pump trans-ports the air and liquid through the vessel. Here, an external loop is used, with a mechanical pump to remove the liquid. Gas and circulated liquid are injected into the tower through a noz-zle.


The dimensions of the larger agitator and tank are: D A2 = RD A1 = 1.587 × 0.203 = 0.322 m D T2 = RD T1 = 1.587 × 0.61 = 0.968 m For equal mass transfer rate n = 2/3. NN 21R 2 = 1 3 (8-38) = 458 1 1 587 2. 3. = 3.37 rev/sec The Reynolds number N Re is N ND A Re = ρ µ 22 2 = ( )( )( ) 909 3 37 0 322 002 2 3 2. sec kg sec m

Hydrodynamic extensional stress during the bubble bursting

between cells and droplets in a flow was also discussed by Garcia-Briones and Chalmers (1994). Primary reasons for reduced damage in shear flow are the presence of the vor-ticity and the linear nature of stretch, in comparison with the exponential stretch. In a shear dominant flow with the shear rate , cells experience time-periodic extension and

Non-Newtonian shear-thinning flows past a flat plate

shear rate (l/sec) Fig. 2. Rheology of Carbopol 940 water solution over a range of concentration. 3. Theory and numerical method 3.1. Newtonmn creeping flow: a linear model In order to understand the flow at low Reynolds numbers, it is illuminating to examine the extreme case, i.e. creeping flow.


shear rate, s-1 boundary shear rate, s-1 pump efficiency when pumping slurry, - pump efficiency when pumping water, - slurry kinematic viscosity, cSt slurry density, kg/m3 yield stress parameter in Herschel-Bulkley flow model, Pa 1. INTRODUCTION The process of derating the performance of a centrifugal pump at a fixed impeller

Chapter 10: Sterilization and Bioreactor Operation

Oxygen Transfer Rate: OTR = k L a (C*-C) k L a = k P g V R 0.4 (v S)0.5 (N)0.5 see equation 10.2a k = empirical constant (fluid and reactor -specific) P g = power requirement for an aerated bioreactor V R = bioreactor volume v S = superficial gas exit speed = (F a /A) F a = volumetric flow rate of air A = bioreactor cross -sectional area

Structural Behaviour Analysis of Vertical V Shaped Soil

agitator body. The agitator is subjected to vibration due to multi-pointed forces resulting from bending and pushing force imported by the Agitation operation. The approach followed in this work involves in step wise (1) Stress analysis of agitator shaft for unit displacement using FE method (2) Estimation of stress outcomes

Grout pump characteristics evaluated with the Ultrasound

Current flow meters used in the field are not accu-rate enough to determine the fluctuation of the flow rate when it is less than 1 l/min. In addition, currently available flow meters measure the average of the flow over a cer-tain period of time, hence the true fluctuation of the flow rate due to the pulsation of the piston remains unknown.

Statistical Investigation on Coherent Vortex Structure in

decomposition, swirling strength and linear stochastic estimation of the PIV data obtained by the PIV measurement in x y plane. Reynolds number based on bulk velocity and channel height was set to 40000. As a result, the angle of shear layer that cleared up by using Galilean decomposition becomes small in the drag-reducing ow.

Properties Research of Ceramic Layer

One of the basic parameters is the amount and rate of gas from the polystyrene model during its thermal decomposition. Specific properties of ceramic layer used for lost foam castings are required. To ensure optimal process flow of metal in the form proper permeability of the ceramic layer is needed.

E1-MNL032A - Design and Rating of Shell and Tube Heat

Shellside Film Coefficient Methods for Single Component Condensation in Laminar Flow The Nusselt Method is used for horizontal condensation under stratifying conditions where the liquid film is draining under gravity with minimum influence due to vapour shear. This is the CC-THERM default method.


Denoting the average shear rate in the mixing vessel by (Yav), the following equation is given in the laminar region. Tgc = kd3r*vP (10) where k is an installation constant. From Eqs. (9) and '(10), Eq. (ll) is obtained. flN = 2k(uJn) = a(nJn) (ll) As mentioned above, the flow characteristic of the fluid of a Bingham model is shown as follows: