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The demo plant was designed for a plant flow of 100 mL/min, with a residence time of 650 s. The above test was run for plant flows between 25 mL/min and 175 mL/min, at 25 mL/min intervals.
Results & Discussion
The graph Figure 3 below shows the effluent turbidities for various plant flows, plotted against dimensionless time, which is real time divided by the residence time of the plant at that plant flow. This is done for ease of comparison between different experimental flow rates. The effluent turbidities plotted are the average effluent turbidity values obtained through several experimental trials.
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The graphs show that as plant flow rate decreases, the effluent turbidity also decreases, until we reach 50 mL/min. At 25 mL/min, we found observed that the effluent turbidity is unstable, but not lower than that of 50 mL/min.
Figure 4 below shows the total degree of mixing and the degree of mixing contributed by the 180 bends only, against plant flow. It also shows the maximum shear attained at the 180 bends and the average shear throughout the plant, againt plant flow. All values are calculated using a slightly modified version of the flocculator design program.
The We plotted the actual amount of mixing as a result of shear and the maximum allowable shear in the figure below, as calculated by the MathCAD file versus flow rate. This calculation included losses in both the 180-degree bends as well as the vertical sections. This graph shows an increase in the degree of mixing and shear with increasing flow rate. The large G-theta calculated by the MathCAD file shown on the graph also shows that G-theta of the Demo Plant depends on both the loss in the 180-degree bend sections as well as in the vertical columns. This is due to the fact that the Demo Plant lamellas are very thin, compared to those in the actual plant, so that frictional interactions with the baffle walls are significant and cannot be neglected.
Figure 4. Degree of mixing & peak shear vs. plant flow.
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