Personal Statements Miriam Clift 21 January 2016 Admissions Manager.
Pipeline Flow of Settling Slurries - Engineers Australia...Head Loss , 5mm gravel,Cv=10%, DN400 Pipe...
Transcript of Pipeline Flow of Settling Slurries - Engineers Australia...Head Loss , 5mm gravel,Cv=10%, DN400 Pipe...
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Pipeline Flow of Settling Slurries
Presentation to Institution of Engineers Australia (Mechanical Branch)
Jeff Bremer - 23 rd April 2008
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Overview and Aims
1. Explain physical laws underlying the behaviour of settling solids in slurry pipeline flow.
2. Compare theories associated with pipeline flow. Why are there so many?
3. Show where and how the theories disagree.
4. Present some preliminary results from recent work (J. Bremer, V.Lim & R.Gandhi )
??
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QUESTIONS
1. Where and why are slurry pipelines used?
2. What is a settling slurry?
3. What are the main features in pipeline flow?
4. Engineers are good at using theoretical and empirical “best fit” theories. What’s the problem?
5. What are the underlying equations and physical phenomena?
6. What are the theories of pipeline flow?
7. What do we know that is right, and can we easilly confirm that we have the “right answer”?
8. What’s the latest, and where to in future?
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Slurry Pipelines
Slurry pipelines are used mostly for “short haul” duties, e.g. dredging (~300m ), process plants (~300m) and tailings (~3 km) In some “long haul duties”, minerals are pumped many hundreds of kilometres.
Alumbrera copper concentrate pipeline (316 km), Argentina
ENGINEERED BY PSI
Photo’s with permission of PSI Australia Pty. Ltd., 66 Kings Park Rd.,West Perth, WA 6005,Tel. no. (08) 9463-6606.
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Slurry PipelinesEach type of duty has its own “best operation point”, where
the size of the particles and the tendency to settle has a strong impact on capital and operating cost.
ENGINEERED BY PSIPhoto’s with permission of PSI Australia Pty. Ltd., 66 Kings Park Rd.,West Perth, WA 6005,Tel. no. (08) 9463-6606.
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Settling Slurries
Settling Slurries contain particles that will fall and settle at the bottom of a container
Non Settling Slurries contain particles that remain in suspension for a long time
NON-SETTLING • Particles < 40 µm
• Viscosity modified by particles
• Increasingly non-Newtonian as concentration increases
SETTLING Particles > 40 µm
Wide range of sizes from
Small (suspensions) 40 µm ~ 200 µm Medium (transition) 200 µm ~ 2 mmLarge (heterogeneous) 2 mm ~ 5 mmVery Large (hetero “ “ ) 5 mm ~ >200 mm?
Transport velocity must increase as size increases
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Settling Slurries
SETTLING Particles > 40 µm
Wide range of sizes from
Small (suspensions) 40 µm ~ 200 µm Medium (transition) 200 µm ~ 2 mmLarge (heterogeneous) 2 mm ~ 5 mmVery Large (hetero “ “ ) 5 mm ~ >200 mm?
Transport velocity must increase as size increases
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Settling Slurries
Dead Donkeys?
SETTLING Particles > 40 µm
Wide range of sizes from
Small (suspensions) 40 µm ~ 200 µm Medium (transition) 200 µm ~ 2 mmLarge (heterogeneous) 2 mm ~ 5 mmVery Large (hetero “ “ ) 5 mm ~ >200 mm?
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Pipeline Flow of Newtonian Liquids
HW = gPρΔ
= g
VDLf
2
2
Darcy-Weisbach equation
H1 =g
P1
ρ +
g2
2v + z1
H2 =g
P2
ρ +
g2
2v + z1
Head LossHW
Pipe Flow
HW = head loss due to friction (m)
f = friction factor (dimensionless)
L = length of pipe (m)
D = internal diameter of pipe (m)
g = accelaration due to gravity (m2/s)
V = mean Flow velocity (m/s)
DLf
Moody Diagram
C.Y. O’Connor Pipeline c.a. 1899
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Features of Settling Slurry Pipeline Flow
Mean Velocity , V (m/s)
Hyd
raul
ic g
radi
ent,
i (m
/m)
Settling Slurry
Carrier
Fixed Bed
Fluidised Heterogeneous Homogeneous
V1 V2 V3 =Vdep V4
Water
HeterogeneousFlow
Fluidised Bed
Homogeneous Flow 1. Size does matter.
• Larger particles require increased transport velocity
• Smaller particles (particularly fines <40 µm) can modify viscosity. Helps to suspend larger particles.
2. Flow velocity generates turbulence which keeps particles suspended.
3. The system curve has a minimum that bounds different flow / friction processes
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Newitt’s Classification of Slurry Pipeline Flow
Newitt et al (1955) described a range of flow flow/deposition phenomena after observing sand and coal particles in 25mm Perspex pipes. His classifications are still used today.
Newitt, D. M., J. F. Richardson, M. Abbott, and R. B. Turtle. 1955. Hydraulic Conveying of Solids in Horizontal Pipes. Trans. Institution of Chemical Engineers 33: 94-113.
Solids Concentration
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Frictional Head loss Mechanisms
• Since we understand the behaviour of water (the carrier) we can calculate the frictional head losses caused by wall friction - HW
• The remainder must be friction losses between
(a) particles and fluid
(b) particles and pipe wall
(c) particle-particle collisions.
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0.00 2.00 4.00 6.00 8.00 10.00 12.00 14.00 16.00 18.00 20.00
Head Los (m‐Water)
Flow Velocity (m/s)
Head Loss , 5mm gravel,Cv=10%, DN400 Pipe
Water
Settling Slurry
Deposition Point
Frictional Head Loss due to wall friction of carrier fluid with pipe- HW
Frictional Head Loss due to solids - Hs
SWM HHH +=
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Durand Theory -1952
Durand, R. 1952. The Hydraulic Transportation of Coal and Other Materials in Pipes. Colloq. of National Coal Board, London.
5.1.82 −ψ=φ
5.12
.82.
−
⎥⎦
⎤⎢⎣
⎡ρ−ρ
ρ=
−D
SWV
WM CgDV
iCii
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Durand Theory – (contd)
1. Durand’s Theory is purely correlative.
2. The curve fit was for 305 points, for sand and coal running between 200 µm and 25 mm.
3. The results are in “Head of Carrier Fluid”– usually water.
4. As transport velocity becomes large, the slurry curve converges to water head loss from above.
“Nothing proves that such a formula is rigorously exact. Doubtless exists a more accurate and more complex means of notation, but the one given above groups quite favourably”
5.12
.8 2.
−
⎥⎦
⎤⎢⎣
⎡ρ−ρ
ρ=
−D
SWV
WM Cg DV
iCii
5.1.8 2 −ψ=φ
).82.1( 5.1−ψ+= VWM CHH
0
50
100
150
200
250
300
350
400
450
500
0.00 2.00 4.00 6.00 8.00 10.00 12.00 14.00 16.00 18.00 20.00
Head Los (m‐Water)
Flow Velocity (m/s)
Head Loss , 5mm gravel,Cv=10%, DN400 Pipe
Water
Settling Slurry
Deposition Point
Frictional Head Loss due to wall friction of carrier fluid with pipe- HW
Frictional Head Loss due to solids - Hs
SWM HHH +=
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More Theories (To name a Few)
1. Durand – 1952
2. Homogeneous Mixture Theory
3. Newitt et. Al - 1955
4. Rose and Duckworth – 1969
5. Heyden and Stelson - 1971
6. Volcado and Charles 1972
7. Wasp et al - 1977
8. Lazarus – Neilson 1978
9. Wilson - 1992
10. Wilson Addie & Clift 1997
Correlation
Correlation
Correlation
Correlation
Correlation
In Current Use
Part theory part correlation
Not in Use
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No Problem – “I’ve got a Computer”
Answers Using commonly accepted theories can vary by several hundred percent – AND MORE!
0
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0 2 4 6 8 10
Head Los (m)
Flow Velocity (m/s)
Head Loss at 6.6 m/s , 5mm gravel, Cv=10% DN400 Pipe x 1000m
Lazarus ‐ Neilson
Wilson‐Addie‐Clift
Durand
Water
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Settling and Drag Forces on Particles
Depends on density , particle diameter, shape, Reynolds number and surface effects
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Settling and Drag Forces on Particles
Particles > 150 µm
Drag coefficient as a function of Reynolds number for smooth spheres and cylinders (Munson et al. 2002, 582)
Known correlations to correction CD based on shape effect
Slip Velocity to Produce drag force FD
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Settling and Drag Forces on Particles
Turbulent fluctuation of particle velocity in the direction of flow
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Settling and Drag Forces on Particles
Frictional Head Loss due to wall friction of carrier fluid with pipe- HW
Frictional Head Loss due to solids - Hs
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200
250
300
350
400
450
500
0.00 2.00 4.00 6.00 8.00 10.00 12.00 14.00 16.00 18.00 20.00
Head Los (m‐Water)
Flow Velocity (m/s)
Head Loss , 5mm gravel,Cv=10%, DN400 Pipe
Water
Settling Slurry
Deposition Point
HW
Hs
SWM HHH +=Solids concentration approaches input concentration Hs=constant
).82.1( 5.1−ψ+= VWM CHH
• In the limit the slip velocity is roughly constant as the average velocity of particles in direction of flow equals approaches the velocity of the liquid i.e.Vsolid = Vliquid the “homogeneous limit” . In other words Hs << Hw
• In Durand Theory in the limit Hs zero
HW = gPρΔ
= g
VDLf
2
2
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Comparison of Theories
0
1 0 0
2 0 0
3 0 0
4 0 0
5 0 0
6 0 0
7 0 0
8 0 0
0 2 4 6 8 1 0 1 2 1 4 1 6 1 8 2 0
Head Los (m)
F low Ve locit y (m / s)
Head Loss , 5mm grave l,C v=10% , DN400 P ipe x 1000m
L azaru s Ne ilson
W ilson A dd ie C lift Du rand
Location of The Deposition Velocity and Head Loss at Deposition is the Key to having an accurate Theory. Clearly the “state of the art is not good”
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Comparison of Theories
Agreement is less critical at 100 µm
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Head loss (m)
Velocity m/s
Head Loss, 100µm particle, Cv=10%, DN100 pipe x 1000m
Wilson Addie Clift DurandLazarus NeilsonWater
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Slope M
Wilson Addie and Clift Theory
Determined in tests on 400 µm sand. Pressure gradient = 0.5 x sliding fr friction factor
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Lazarus Nielsen Theory (1978)
Lazarus Neilsen Theory is a correlation theory that claims to bemore accurate than Durand and Newitt’s theories.
They proposed that the mass flow rate ratio (M*), defined as the ratio of mass flow of solids to carrier fluid, should be used instead of the volumetric concentration (Cv)
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Lazarus Nielsen Theory (contd)
They plotted friction factor fM for the mixture against the “base”friction factor fB to develop their final correlation.
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Current Work – Particle Drag & Deposition Head and VelocityCollaborators : J. Bremer (SKM) , Vincent Lim (K.J. Beer), Ramesh Gandhi (PSI – California)
Mean Velocity , V (m/s)
Hyd
raul
ic g
radi
ent,
i (m
/m)
Settling Slurry
Carrier
Fixed Bed
Fluidised Heterogeneous Homogeneous
V1 V2 V3 =Vdep V4
Water
Heterogeneous
Flow
Fluidised Bed
Homogeneous Flow
Began by describing the equations of drag and pressure loss due to solids at the deposition point.
Assumes : All particles fluidised at the minimum in the pressure gradient curve
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Particle Drag and Deposition Velocity and Head Loss(contd)
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Particle Drag and Deposition Velocity and Head Loss(contd)
Pesky mean path length constan
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Particle Drag and Deposition Velocity and Head Loss(contd)
All terms in the final equation are rearranged to solve for theSlip velocity V’
This is Measurable from experiment!
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Particle Drag a Virtual Experiment Based on Durand Points
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Particle Drag a Virtual Experiment Based on Durand Points
System Parameter Value Range Unit
Lower Upper
Carrier density (ρ) 1,000 1,250 kg/m3
Carrier viscosity (μ) 0.0008 0.001 Pa.s
Pipe diameter (D) 0.1 0.9 m
Particle density (ρp) 2,160 4,000 kg/m3
Particle size (d) (40 μm) 0.02 (20 mm) m
Concentration by
volume (Cv)
0.05 0.4
Pipe length (L) 1,000 m
Pipe roughness Smooth
5104 −×
200 Virtual data points (deposition velocity, and pressure at the deposition point) obtained using Durand equation to
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Virtual Experiment – ResultsDeposition Velocity
5104 −×
Deposition Velocity – Average Error 0.05 %-- Maximum Error 0.42 %
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Virtual Experiment – ResultsHead Loss at The Deposition Point
5104 −×
Head Loss – Average Error 0.55 %-- Maximum Error 1.8 %
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Conclusions
5104 −×
1. Not “all is well” with the theory of slurry transport.
2. There is considerable disagreement amongst theories regarding
1. Deposition velocity
2. Head Loss at Deposition
3. There is no clear agreement on the forces and friction associated with various mechanisms, (e.g. fluidised bed, heterogeneous flow, homogeneous flow etc) or the velocities at which they occur.
4. Many of the theories “blow up” when large particles are involved. Say > 2mm. Comparison between calculations at these sizes indicates a need for model studies in future developments.
5. Where possible don’t pump at sizes > 150 µm.