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Monroe L. Weber-Shirk S chool of Civil and Environmental Engineering Flocculation.

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1 Monroe L. Weber-Shirk S chool of Civil and Environmental Engineering Flocculation

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3 Overview  Flocculation definition  Types of flocculators  Mechanical Design  Fractal Flocculation Theory applied to hydraulic flocculators  CFD analysis of hydraulic flocculators  Hydraulic Flocculator Design

4 What is Flocculation?  A process that transforms a turbid suspension of tiny particles into a turbid suspension of big particles!  Requires  Sticky particles (splattered with adhesive nanoglobs)  Successful collisions between particles  Flocs are fractals (“the same from near as from far”)  The goal of flocculation is to reduce the number of colloids (that haven’t been flocculated)  One goal is to understand why some colloids are always left behind (turbidity after sedimentation)  Another goal is to learn how to design a flocculator

5 Mechanical Flocculation  Shear provided by turbulence created by gentle stirring  Turbulence also keeps large flocs from settling so they can grow even larger!  Presumed advantage is that energy dissipation rate can be varied independent of flow rate  Disadvantage is the reactors have potential short circuiting (some fluid moves quickly from inlet to outlet)

6 Recommended G and G  values: Turbidity or Color Removal (Mechanical flocculators) Type “Velocity gradient” (G) (1/s) Energy Dissipation Rate (  ) + GG   (minute) Low turbidity, color removal – 4.950, , High turbidity, solids removal , , Sincero and Sincero, 1996 Environmental Engineering: A Design Approach * Calculated based on G and G  guidelines + average value assuming viscosity is 1 mm 2 /s G is the wrong parameter… (Cleasby, 1984)

7 Mechanical Design: mixing with paddles “velocity gradient” Drag coefficient Projected area of paddles Ratio of relative to absolute velocity of paddles Reactor volume extra

8 Mechanical Flocculators?  Waste (a small amount of) electricity  Require unnecessary mechanical components  Have a wide distribution of energy dissipation rates (highest near the paddles) that may break flocs  Have a wide distribution of particle residence times (completely mixed flow reactors) extra

9 Ten State Standards  The detention time for floc formation should be at least 30 minutes with consideration to using tapered (i.e., diminishing velocity gradient) flocculation. The flow ‑ through velocity should be not less than 0.5 nor greater than 1.5 feet per minute.  Agitators shall be driven by variable speed drives with the peripheral speed of paddles ranging from 0.5 to 3.0 feet per second. External, non-submerged motors are preferred.  Flocculation and sedimentation basins shall be as close together as possible. The velocity of flocculated water through pipes or conduits to settling basins shall be not less than 0.5 nor greater than 1.5 feet per second. Allowances must be made to minimize turbulence at bends and changes in direction.  Baffling may be used to provide for flocculation in small plants only after consultation with the reviewing authority. The design should be such that the velocities and flows noted above will be maintained. Hydraulic flocculators allowed only by special permission!

10 Hydraulic Flocculators  Horizontal baffle  Vertical baffle  Pipe flow  Gravel bed Very low flows and pilot plants A bad idea (cleaning would require a lot of work)

11 Flocculator Geometry 2 Channels Upper Baffles Port between channels Entrance Lower Baffles Exit extra

12 Why aren’t hydraulic flocculators used more often?  Simple construction means that there aren’t any items that private companies (venders) can sell as specialized components  Consulting firms want to be able to pass the design responsibility off to a vender  The presumed operation flexibility of mechanical flocculators (variable speed motor driving a slow mixing unit)  Poor documentation of design approach for hydraulic flocculators (special permission required to use in the US!)  Using electricity is cool, design innovation is suspect…  Prior to AguaClara we didn’t have a design algorithm based on the fundamental physics extra

13 Schulz and Okun (on Hydraulic flocculators)  Recommend velocity between 0.1 and 0.3 m/s  Distance between baffles at least 45 cm  Water must be at least 1 m deep  Q must be greater than 10,000 m 3 /day (115 L/s) These aren’t universal constants! We need to understand the real constraints so we can scale the designs correctly What length scale could make a dimensionless parameter? Surface Water Treatment for Communities in Developing Countries, (1984) by Christopher R. Schulz and Daniel A. Okun. Intermediate Technology Publications

14 AguaClara Flocculator Design Evolution  We began using conventional guidelines based on “velocity gradient” but we were aware that this system was fundamentally incorrect (it doesn’t capture the physics of turbulence)  We were concerned that by using a defective model we could potentially produce defective designs  If the model doesn’t capture the physics, then it won’t scale correctly (and we are designing plants for scales that hadn’t been tested) extra

15 Edge of Knowledge Alert  Why would we ever think that the baffled flocculators invented over 100 years ago were the optimal design for flocculation?  We have better coagulants, shouldn’t that influence flocculator design?  We are only now beginning to understand the physics of fractal flocculation  We are improving the design of hydraulic flocculators based on our evolving understanding of the physics of flocculation extra

16 The Challenge of Flocculation  We would like to know  How do particles make contact to aggregate?  What determines the time required for two flocs to collide?  How strong are flocs?  The challenge of the large changes in scale  The Al(OH) 3 nanoglobs begin at a scale of 100 nanometers  Flocs end at a scale of 100 micrometers

17 Hydraulic Flocculation Theory  Turbulence is caused by the expansion that results when the water changes direction as it flows around each baffle  Colloids and flocs are transported to collide with each other by turbulent eddies and over short distances by viscous shear.  Flocs grow in size with each successful collision  Colloids have a hard time attaching to large flocs* (maybe because the surface shear is too high???) Flocculation model and collision potential for reactors with flows characterized by high Peclet numbers Monroe L. Weber-Shirk, a, and Leonard W. Liona a a *hypothesis from 2012!

18 How do the flocs grow?

19 Exponential growth  How many sequential collisions are required to make a 1 mm particle starting from 1  m particles?  How much larger in volume is the 1 mm diameter particle?  ____________ 1,000,000,000 !

20 Doubling Collisions  1 collision 1+1=2  2 collisions 2+2=4  3 collisions 4+4=8  4 collisions 8+8=16  Number of original particles in the floc = 2 n  What is n to obtain 1,000,000,000 = 2 n ?  n=30 This assumes volume is conserved!

21 Fractal Dimensions  What happens to the density of a floc as it grows larger? diameter of primary particle diameter of floc Number of primary particles in the floc Fractal dimension If volume is conserved, what is D Fractal ? ____ 3 Floc density approaches the density of water because the floc includes water

22 Fractal Flocculation  Fractal geometry explains the changes in floc density, floc volume fraction, and, ultimately, sedimentation velocity as a function of floc size  The fractal dimension of flocs is approximately 2.3 (based on floc measurements)

23 Floc Volume Fraction  The fraction of the reactor volume that is occupied by flocs  For fractal dimensions less than 3 the floc volume fraction increases as floc size increases  Use conservation of volume to estimate initial dominates

24 Floc Volume Fraction Primary particle diameter (clay + coagulant) “super fluffy” flocs Dense flocs

25 Buoyant Density of Flocs Will these flocs settle faster than the primary particles?

26 Floc Terminal Velocity 1  m Upflow velocity for floc blankets Capture velocity for AguaClara plate settlers Why flocculation is necessary! The model takes into account the changing density of flocs D Fractal = 2.3 and d 0 = 1  m shape factor for drag on flocs Laminar flow

27 Analytical Model of the Flocculation Process  The floc porosity increases with floc diameter  The velocity between flocs is a function of whether the separation distance is less or greater than the Kolmogorov scale  The time required per collision is a function of the relative velocity between flocs, the average separation distance between flocs, and the floc size  In the next slides we will explore how to characterize collision time for flocs  We will assume that collisions occur between similar sized flocs. That assumption will need to be evaluated, but it is probably a good assumption for the initial growth of flocs. Are the two flocs in different eddies?

28 How much water is cleared (filtered) from a floc’s perspective?  Volume cleared is proportional to a collision area defined by a circle with diameter = sum of the floc diameters  Volume cleared is proportional to time  Volume cleared is proportional to the relative velocity between flocs

29 How much volume must be cleared before a collision occurs?  What is the average volume of water “occupied” by a floc?  Need to know floc diameter (d Floc )  And floc volume fraction (  Floc ) Floc volume Suspension volume

30 Use dimensional analysis to get a relative velocity given a length scale Viscous rangeInertial range Assume linear The origin of the G notation Re=1 laminar turbulent If the flocculator has laminar flow, then this side doesn’t apply and the G, G  approach applies. L is separation distance

31 Summary for Particle Collisions t c is average time per collision Floc separation distance viscous inertia Is t c a function of d? Yes!

32 Successful Collision Models viscous inertia Time for one collision Number of successful collisions  is fractional surface coverage of colloids with adhesive nanoglobs d Floc is perhaps mean floc size of flocs that are capturing colloids For completeness we should probably include a correction for hydrodynamic effects that make it difficult for non porous particles to approach closely. This may increase the time for the first few collisions when flocs aren’t very porous Number of collisions is equal to time over collision time

33 Relationship between laminar and turbulent The ratio of G  to  is the number of clay particles raised to the 2/9 th power! Set the collisions equal to get the relationship Use the target settled water turbidity as the best guess for a relationship between conventional G  and . For a turbidity of 1 NTU the number of clay particles is 150,000,000 per liter. Schulz and Okun suggest 20,000 as a minimum value of G  equivalent to  65 m 2/3. But this isn’t calculated correctly. Should take their G  and energy dissipation rate to make the conversion.

34 Minimum time to grow from colloid to large floc 20 collisions to grow from 1  m to 0.4 mm How much time is required to produce a 0.4 mm floc? D Fractal = 2.3 d 0 = 1  m  = 6 mW/kg Inertial Viscous 400 s 120 s 40 s

35 Initial Floc Growth: Phase 1 (the 50% solution)  Initial growth phase of flocculation can be modeled with the equations on the previous slide (summing the collision times until the maximum floc size is reached)  The end of the initial growth phase is reached when a significant fraction of the flocs reach a size that can be removed by sedimentation.

36 Observations: Collision time model  The previous analysis was tracking the time required to make the first big flocs  For a highly turbid suspension it may only take a few seconds to produce visible flocs  This is why successful flocculation can be observed very early in a flocculator  This doesn’t mean that a flocculator with a residence time of 100 s will perform well  We need to track the colloids that are left behind!  Performance is based on _______________ residual turbidity

37 Remember our Goal?  Introduce pC*  Sloppy parlance… log removal  What is the target effluent turbidity for a water treatment plant?  What is pC* for a water treatment plant treating 300 NTU water?

38 Tracking the residual turbidity: Phase 2 of Flocculation  After the initial production of flocs at their maximum size the interaction of the colloids change  Most of the collisions are ineffective because collisions with flocs that are maximum size apparently are useless and most flocs are their maximum size

39 Flocculation Model: Integrating and tracking residual turbidity The change in colloid concentration with respect to the potential for a successful collision is proportional to the colloid concentration (the fraction of the colloids swept up is constant for a given number of collisions) Integrate from initial colloid concentration to current colloid concentration Separate variables Classic first order reaction with number of successful collisions replacing time

40 Laminar Flow Cases Only colloids can collide effectively (big flocs are useless) Colloids can attach to all flocs Floc volume fraction that matters for successful collisions is the colloid (small floc) fraction Floc volume fraction is a function of floc size (d) (which is a function of the reaction progression and shear conditions in the reactor

41 Comparison of Flocculation Hypotheses If colloids could aggregate with all of the flocs then colloids would aggregate VERY rapidly Ten state standards 30 minute flocculation time. The graph is laminar flow case, full scale flocculators are turbulent flow. 100 NTU clay suspension,  = 0.1 Show that pC* is proportional to time for “everything aggregates” model

42 Coiled Tube Flocculation Residual Turbidity Analyzer Dr. Karen Swetland Dissertation research

43 Two Phase Floc Model: PACl Initial floc growth

44 Two Phase Floc Model: Alum Initial floc growth

45 Solving for pC*: Lambert W or ProductLog Function (Laminar flow) Use Wolframalpha to solve for C* W is the Lambert W function Log is base 10

46 Laminar Flow Floc Model Velocity gradient Flocculation time Fractional surface coverage of colloid by coagulant Floc volume fraction Sedimentation tank capture velocity Sedimentation velocity of ??? Lambert W Function Collisions to make first big flocs = 0.4 Empirical

47 Turbulent Flow Case Only colloids can collide and attach effectively Colloids can attach to all flocs Why are almost all of these collisions in the inertial range?

48 Turbulent Flow Flocculator: “Big Flocs are useless” hypothesis The predicted performance is quite similar given a wide range of influent turbidities The predictions seem reasonable Ten state standards 30 minute flocculation time. After the big flocs become non reactive, then the average separation distance between the remaining flocs is larger and thus the collisions between active particles is dominated by inertia.  = 0.1 for these plots  = 2.6 mW/kg

49 Turbulent Flow Flocculator: Colloids can attach to all flocs hypothesis The predicted performance is quite different from what we observe. High turbidity would be very easy to treat if this hypothesis were true! Flocculators would be tiny! Ten state standards 30 minute flocculation time. Here the separation distance between reactive flocs might be less than the Kolmogorov length scale For these plots  = 0.1  = 2.6 mW/kg pC* proportional to time

50 Solving for pC*: Lambert W or ProductLog (Turbulent Flow) Use Wolframalpha to solve for C* W is the Lambert W function Log is base 10 extra

51 Lambert W Function  Performance varies very little over wide range of inputs.  Diminishing returns on investment extra

52 Proposed Turbulent Flocculation Sedimentation Model (missing phase 1) Energy dissipation rate Flocculation time Fractional surface coverage of colloid by coagulant Initial floc volume fraction Sedimentation tank capture velocity Sedimentation velocity of ??? -log(fraction remaining) Characteristic colloid size Lambert W Function What does the plant operator control? ________ What does the engineer control? __________  What changes with the raw water? __________

53 Turbulent Flocculation Sedimentation Model Questions  Must represent a characteristic sedimentation velocity of the floc suspension. It could be the average terminal velocity of the full size flocs in the flocculator effluent  Is a characteristic size of a colloid.  Is a function of the characteristic size of the coagulant precipitate, geometry of the colloids, and loss of coagulant to reactor walls

54 Fractal Flocculation Conclusions  It is difficult to flocculate to a low residual turbidity because the time between effective collisions increases as the number of colloids and nonsettleable flocs decreases  Colloids don’t attach to full size flocs  Perhaps because the surface shear on the big floc is too high for a colloid to attach (surface shear increases with diameter)  If we could routinely break up full size flocs perhaps we could speed the aggregation process  Perhaps related to deformability?

55 What is the model missing? The model doesn’t include any particle aggregation that occurs in the sedimentation tank. Residence time in the sed tank is long and energy dissipation rate is low. Flocculation in the sed tank (especially if there is a floc blanket) could be very important. Thus real world performance is likely better than model predictions.

56 Flocculator Collision Potential  The majority of the collisions in a turbulent hydraulic flocculator are in the inertial range and the collision potential is determined by flocculator residence time, , and energy dissipation rate, .  The collision potential is given the symbol  and has the dimension of m 2/3 and this length scale will be a property of the reactor geometry  The next set of notes provides guidance for designing the geometry of a flocculator to obtain a target collision potential

57 Required Collision Potential* *The model has not been validated for turbulent hydraulic flocculator. Thus this is only a rough estimate. Agalteca, Alauca, Marcala 2 were designed to have  =100 m  We are currently using  =75 m 

58 Review  Why is it that doubling the residence time in a flocculator doesn’t double pC* for the flocculator?  Why does increasing floc volume fraction decrease the time between collisions?  Which terms in the model are determined by the flocculator design?

59 Surface coverage (  ) of clay by coagulant precipitate In our modeling work we didn’t cover how to calculate what fraction of the clay surfaces are coated with coagulant. The following slides are the equation heavy derivation of that coverage. We assume coagulant precipitate has some characteristic diameter when it sticks to the clay and that the clay can be represented as a cylinder. We also assume that the coagulant sticks to everything including reactor walls. The coagulant approaches the clay surface randomly and thus accumulates in a Poisson distribution. The random bombardment means that some coagulant is wasted in double coverage of previously covered clay. extra

60 Floc Model Equations for  Surface area to volume ratio for clay normalized by surface area to volume ratio for a sphere Surface area of clay divided by total surface area of clay + reactor walls extra

61 Ratio of clay surface area to total surface area (including reactor walls) extra

62 Poisson distribution and coagulant loss to walls combined to get surface coverage The surface coverage is reduced due to stacking (which is handled by the Poisson distribution) and by the loss of coagulant to the reactor walls. loss of coagulant to the reactor walls extra

63 Clay platelet geometry D.Clay is the diameter of a sphere with equal volume as the clay platelet Model clay as cylinder with height and diameter D.ClayPlatelet is the diameter of a cylinder given ratio of height to diameter and equal volume spherical diameter extra

64 Clay platelet geometry extra

65 Surface coverage of clay If you neglect wall loses extra

66 Solving for Coagulant Dose Coagulant dose is inside coagulant volume fraction Solve for dose… Given a target residual turbidity, solve for required , then solve for coagulant dose extra

67 Loss of clay to reactor walls Loss of coagulant to reactor walls can dominate for low turbidities and small reactors. For the LFSRSF in India treating 5 NTU water and injecting coagulant into 7.5 cm pipes the clay only gets 23% of the applied coagulant! There may be a way to design a larger contact chamber for the coagulant to reduce losses to the walls. extra

68 Effect of stacking and wall loss in a 10 cm diameter flocculator with 20 NTU Stacking due to random bombardment of the clay surface with coagulant nanoglobs. Stacking becomes significant for high surface coverage. Wall losses also cause a significant reduction in clay surface coverage. extra


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