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Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
Particle Technology Two Phase Flow Rheology and Powders
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Particle Technology Two Phase Flow Rheology and Powders

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The eighth lecture in the module Particle Technology, delivered to second year students who have already studied basic fluid mechanics. Two phase flow, rheology and Powders covers flow of dispersions …

The eighth lecture in the module Particle Technology, delivered to second year students who have already studied basic fluid mechanics. Two phase flow, rheology and Powders covers flow of dispersions of powders in liquids and gases, as well as the storage of powders and why they sometimes do not flow. Equations to predict the pressure drop in pumped systems are provided, for both streamline and turbulent flows.

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  • 1. Two Phase Flow, Rheology and Powder Flow
    Chapters 6, 9 & 10 in Fundamentals
    Watch this lecture at www.vimeo.com
    Also visit; http://www.midlandit.co.uk/particletechnology.htm for further resources.
    Course details:
    Particle Technology, module code: CGB019 and CGB919, 2nd year of study.
    Professor Richard Holdich
    R.G.Holdich@Lboro.ac.uk
  • 2. Two Phase Flow, Rheology and Powder Flow
    • Rheology – Section 6.7
    • 3. Homogeneous systems; Newtonian and non-Newtonian, laminar/turbulent
    • 4. Homogeneous but with slip
    • 5. pneumatic conveying - dilute phase
    • 6. Heterogeneous systems
    • 7. pneumatic conveying - dense phase
    • 8. hydraulic conveying
    • 9. Powder flow
  • Flow of dispersions
  • 10. Rheograms
    Non-time dependent
    Newtonian:
    Power law:
  • 11. Rheograms
    Time dependent
  • 12. Apparent viscosity
    Is the viscosity of a Newtonian fluid that flows under the same conditions of shear rate and stress as the non-Newtonian fluid.
    R (Pa)
    Apparentviscosity
    dv/dr (s-1)
  • 13. Apparent viscosity
    In order to use Newtonian flow equations we really need “apparent viscosity for pipe flow” - from the “flow characteristic”, etc.
    In order to predict flow rate and pressure drop use simpler approach - appropriate to power law fluids.
    Force balance on a wall gives:
  • 14. Wilkinson’s equation
    Combine the power law viscosity equation with the shear stress on the wall - much like the derivation of Hagen’s equation and integrate to give:
    Laminar flow of non-Newtonian power law fluids and suspensions.
  • 15. Turbulent flow
    Generalised expression based on a friction factor:
    • For Newtonian fluids:
  • Turbulent flow
    Dodge and Metzner - turbulent flow power law fluid:
  • 16. Turbulent flow
    Need a Reynolds number that reduces to Newtonian equation when n=1, and the turbulent friction expression should reduce to Wilkinson’s equation given f=16/Re* - i.e. for laminar flow.
  • 17. Turbulent flow
    The Generalised Reynolds number - threshold value of 2000 for laminar to turbulent flow.
  • 18. Turbulent flow - Q from known pressure drop
    Solution to turbulent equation - note that f occurs on both sides of equation:
    estimate Q from laminar equation,
    calculate v and Re,
    calculate f from wall shear and friction factor equations, then square root of f,
    calculate RHS of D&M correlation, and
    check agreement, if doesn’t then …………. the flow rate - iterate until it agrees.
  • 19. Turbulent flow - Q from known pressure drop
    • Wall shear equation:
    Friction factor equation:
  • 20. Summary for suspensions
    For Newtonian:
    Use Krieger for viscosity f(C) and use mean suspension density, then
    Treat as homogeneous fluid (i.e. CGA001)
    For non-Newtonian
    Wilkinson’s equation for LAMINAR
    Dodge & Metzner for TURBULENT
  • 21. Pneumatic conveying
    • Distinction between homogeneous (+slip) and heterogeneous:
  • Pneumatic conveying
  • 22. Pneumatic conveying
    • Positive pressure:
  • Pneumatic conveying
    • Negative pressure:
  • Pneumatic conveying
    • Mixed:
  • Pressure drops in pneumatic conveying
    acceleration of the gas - Bernoulli
    acceleration of the solids - Bernoulli
    friction of gas on pipe wall - friction factor
    friction of solids on pipe wall - friction factor
    static head of gas - Bernoulli
    static head of solids - Bernoulli
    additional drop due to bends
    See Fundamentals – Problem 9.6
  • 23. Saltation velocity
    Comes from Rizk correlation:
    Dimensional constants in SI units
    Ms is mass flow rate (kg/s) and D is pipe diameter (m).
  • 24. Slip velocity (solid-gas)
    Solids will slip in the gas flow:
    Dimensional constants in SI units, empirical equation relating solid velocity to superficial gas velocity.
  • 25. Dense phase design
    Difficult!
    Dense phase design:
    http://www.cheresources.com/pnuconvey.shtml
  • 26. Hydraulic transport
    Firstly, identify occurrence of boundary between homogeneous and heterogeneous transport.
    Empirical correlation due to Kim et al, 1986, Int. Chem. Eng., p 731.
  • 27. Hydraulic transport
    Secondly, use homogeneous non-Newtonian (or Newtonian) transport equations - if appropriate.
    If heterogeneous, correlation due to Durand (1953) but much better to empirically investigate own materials.
  • 28. Powder Flow
    Powder flow issues
    Hopper failure
    Explosion
    Powder flood
    Hopper discharge
    Mass flow
    Core flow
    Wall and powder pressure - FRICTION
    Testing
  • 29. Powder Flow & Storage
    Definitions:
    Hopper:
    Conical section, bottom
    Bin
    Cylindrical section, top
    Silo
    Used for both
    Interchangeable in use
  • 30. Powder Flow Disasters
    Powder flood
    Silo failure
    Images removed from copyright reasons.
    For a suitable example please see
    http://www.jenike.com/Solutions/silofail.html
    Image created by R J Leask found at http://picasaweb.google.com/rjleask
    http://creativecommons.org/licenses/by/3.0/
  • 31. Explosion
    Powder Flow Disasters
    Image removed from copyright reasons.
    For a suitable example please see
    http://www.teachersdomain.org/asset/lsps07_int_expldust/
  • 32. Flow Patterns
    MASS FLOW: first in – first out
    CORE FLOW: first in – last out
  • 33. Comparison of flow patterns
    Mass flow Core flow
    Flow is uniform and Erratic flow whichcan well controlled cause powderto aerate and flood (avalanche)
    No dead (static) regions Static zones at sides - no perishable spoilage - may empty at the end
    Channelling and bridging Piping may occurshould be absent
    Less segregation Particles roll in discharge
    Tall and thin May have higher capacity for capital cost
    High stress where Arrangement maydirection changes relieve wall stresses
  • 34. Angle of Repose
    For a FREE FLOWING powder the hopper angle needs to be greater than the angle of repose for flow to occur. This is typically 30o BUT a different approach is required for COHESIVE powders. Angle of repose is difficult to measure - best to pour powder into an upside down glass funnel and carefully remove to leave heap in place.
  • 35. Bulk Density
    Is the combined density of the powder and the void space. Remembering the definition of porosity:
    Porosity =  = void volume/total volume
    Hence the bulk density will be:
    the above densities are, in order: bulk, solid & fluid. If the fluid is air the furthest right term can be ignored.
  • 36. Pressure transmission and powder discharge
    Unlike fluids there isn't a linear increase in pressure with height - for all heights. In fact, the pressure stabilises after a few metres and the rate of discharge from a hopper will, therefore, be remarkably constant. For free flowing powders the empirical equation:
    where D is the opening diameter. Note that this equation does not include powder height.
  • 37. Pressure transmission Janssen’s analysis
    where Pvo is the pressure at z=0, called the 'surcharge' or uniform stress applied at the top of the powder. For Pvo=0 and at small values of z:
    as exp(-Az)  1 - Az for low z
    Thus, - a similar result to that of liquids BUT only for small values of z. At large values of z:
    as the exponential term disappears.
    i.e. pressure asymptotes to the above uniform value.
  • 38. Importance of Janssen’s work
    Stress is not transmitted in a similar way to hydraulic head, and
    Wall friction has a very significant influence on the internal powder stresses.
  • 39. Hopper design
    Mass flow discharge is based upon two factors: the hopper angle steep enough and the discharge opening wide enough to provide the flow.
    The Powder Flow Function (PFF or sometimes called the Material Flow Function), characterises the ease, or otherwise, of powder transport and storage.
  • 40. Stable Arch Formation
    Thus the minimum hopper opening diameter needs to be
    The main stage is to identify the unconfined yield stress for a powder inside a hopper, and to know more about the functional relation H().
  • 41. Mohr’s circle and principal planes
    The maximum principal plane stress for the circle formed by conditions of a and a is given by the Mohr's circle drawn through those points and is read off at the =0 axis.
    The unconfined yield stress is the stress (Pa) given by the Mohr's circle that goes through the origin AND is a tangent to the yield locus. It is the maximum principal plane stress for this circle.
  • 42. Material or Powder Flow Function
    Obtained from a series of yield locii giving the maximum principal stress and unconfined yield stress; one data point from each yield locus.
    PFF
    Unconfined yield stress
    Maximum principal stress
  • 43. Jenike shear cell
    Two rings are used. The powder in the rings has a consolidating (normal) load applied. This load is removed and a lower load used, together with a shear stress applied via the bracket on the side of the top ring.
    When the shear stress is sufficient the top ring will slide over the bottom, and the powder has sheared. This gives one value for shear and consolidating stress, that may be plotted on a Mohr circle.
  • 44. Useful sites
    Description of Jenike and other techniques for yield locus determination – then how to use the data for hopper design.
    http://members.aol.com/SchulzeDie/grdle1.html
    Also, try the freeware program ‘spannung.exe’
    A well known name and company with many useful resources:
    http://www.jenike.com
    On-line magazine for powder and bulk handling:
    http://www.powderandbulk.com/
    Highly recommended article on different flow types:
    http://www.erpt.org/992Q/bate-00.htm
    and more generally on this subject:
    http://www.erpt.org/technoar/powdmech.htm
    http://www.erpt.org/technoar/powddyna.htm
  • 45. This resource was created by Loughborough University and released as an open educational resource through the Open Engineering Resources project of the HE Academy Engineering Subject Centre. The Open Engineering Resources project was funded by HEFCE and part of the JISC/HE Academy UKOER programme.
    © 2009 Loughborough University
    This work is licensed under a Creative Commons Attribution 2.0 License.
    The name of Loughborough University, and the Loughborough University logo are the name and registered marks of Loughborough University. To the fullest extent permitted by law Loughborough University reserves all its rights in its name and marks which may not be used except with its written permission.
    The JISC logo is licensed under the terms of the Creative Commons Attribution-Non-Commercial-No Derivative Works 2.0 UK: England & Wales Licence.  All reproductions must comply with the terms of that licence.
    The HEA logo is owned by the Higher Education Academy Limited may be freely distributed and copied for educational purposes only, provided that appropriate acknowledgement is given to the Higher Education Academy as the copyright holder and original publisher.

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