h1. Data Acquisition
The Flocculator Residual Turbidity Analyzer (FReTA) allows us to gather data and investigate a number of different factors affecting flocculator performance, including shear (G), residence time (θ), alum dose, and influent turbidity. The shear rate in the flocculator can be controlled in [Process Controller] by either holding constant or varying the plant flow rate as desired. A given flow rate will define a particular shear rate in the flocculator. The shear rates in the tube flocculator can be calculated from flow rates and other characteristics of the setup using the following equations:
_The following equations and methods were developed to describe shear in FReTA by Ian Tse in his thesis:_ _[_Fluid shear influences on hydraulic flocculation systems characterized using a newly developed method for quantitative analysis of flocculation performance_|Tube Floc Data Acquisition^Ian Tse MS Thesis.doc]_
_Based on dimensional analysis, the velocity gradient G can be expressed as a function of the average energy dissipation rate (ε) and kinematic viscosity of the fluid (ν):_
{latex}
\large
$$
G = \sqrt {{\varepsilon \over \nu }}
$$
{latex}
_(1.3)_
_Using conservation of energy, ε can be expressed as kinetic energy loss over a period of time:_
{latex}
\large
$$
\varepsilon = {{gh_L } \over \theta }
$$
{latex}
_(1.4)_
_where: g is gravitational acceleration, hL is head loss and θ is average hydraulic residence time._
_The head loss through a straight tube can, in turn, be defined as (Robertson et al, 1993):_
{latex}
\large
$$
h_L = f_s {L \over d}{{U^2 } \over {2g}}
$$
{latex}
_(1.5)_
_where: L is the length of the flocculator and fs is the friction factor in a straight tube. For laminar flow, the friction factor fs = 64/Red, and Red is the Reynolds number as defined as:_
{latex}
\large
$$
{\mathop{\rm Re}\nolimits} _d = {{Ud} \over \nu }
$$
{latex}
_(1.6)_
_where: U is the average axial velocity and d is the tube inner diameter._
_The formulation for G derived by Gregory (1981) (see Equation 1.2) can also be derived from algebraic rearrangement of Equations 1.3-1.6. A correlation factor (Mishra & Gupta 1979) can be applied to Equation 1.7 to replace fs with fc and correct for the differences in head loss between straight and curved tubes._
{latex}
\large
$$
{{f_c } \over {f_s }} = 1 + 0.033\log \left( {De} \right)^4
$$
{latex}
_(1.7)_
_where: De is the nondimensional Dean Number and characterizes the effect of curvature on fluid flow:_
{latex}
\large
$$
De = \sqrt {{r \over {R_c }}} {\mathop{\rm Re}\nolimits} _d
$$
{latex}
_(1.8)_
_where: r is the inner radius of the tube, Rc is the radius of curvature._
_The average head loss measured as the pressure drop across the tube flocculator was within 2% of the head loss calculated using Equations 1.5 and 1.7 (Figure 1.4). The figure eight coil configuration used in this research was different from the flow regime modeled by Mishra and Gupta. The fact that our data agrees with their model suggests that the change in direction of the coil had only a small effect on total head loss. The following G value obtained from combining Equations 1.3-1.8 was used to design the experimental runs._
{latex}
\large
$$
G_c = G_s \left( {1 + 0.033\log \left( {De} \right)^4 } \right)^{{\raise0.7ex\hbox{$1$} \!\mathord{\left/
{\vphantom {1 2}}\right.\kern-\nulldelimiterspace}
\!\lower0.7ex\hbox{$2$}}}
$$
{latex}
_(1.9)_
We can also study the effect of increasing the residence time in the flocculator and holding shear constant by increasing the length of the flocculator while holding the flow rate constant; this will increase the amount of time water spends in the flocculator without changing the shear rate. Currently, setup can easily be modified to handle three different flocculator lengths, 27.96 m, 55.92 m, and 83.88 m. [Process Controller] can also be used to vary alum dosage, and set the desired influent turbidity for the raw water. This allows us complete control over what enters the flocculator, how long it spends in the flocculator, and how quickly it moves through the flocculator.
When running an experiment on FReTA, we allow 1.5-2 residence times to pass before collecting data. This ensures that the alum has the necessary time to react with the clay particles in order to produce a steady state distribution of flocs at the end of the flocculator.
After this loading time, [Process Controller] begins the actual data collection. The pumps ramp down gradually, and a ball valve is used to seal off the settling column (see [Apparatus Setup|Tube Floc Fall 09 Experimental Apparatus]) from the rest of the flocculator over a period of 6 seconds. The reason for this gradual shut down is to prevent turbulence that could disrupt flocs in the settling column. [Process Controller] then records the residual turbidity every second for half an hour (1800 s) at which point the valves open to begin backwashing for a new run.
The settling velocities corresponding to the time range we are studying are calculated by dividing the distance between the valve and the effluent turbiditmeter in the settling column (16 cm) by the time since settling began. Thus, the residual turbidity after 10 s of settling would correspond to all particles with a settling velocity of greater than 1.6 cm/s. We are not interested in recording data after half an hour because this corresponds to extremely low settling velocities (>0.0889 mm/s) which means that these particles would not have time to settle out in the sedimentation tank and would remain in the effluent. This is defined as the residual turbidity.
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