Sunday, September 4, 2011

Design Calculations for Slurry Agitators in Alumina Refinery

Hi Friends,

Today I am presenting the gist of my technical paper on "Motor rating calculations for slurry mixing agitators in Alumina refinery" which has been published recently in aluminium issue of the magazine "Minerals & Metals Review" (page 30 and 31 in MMR, August 2011 issue).

In various technical forums, process experts as well as equipment manufacturers have opined that the design of agitators for mixing bauxite, residue and hydrate in Alumina refinery is complicated and tricky issue. In this paper, we will discuss the subject with brief description of involved terminology, associated design parameters and methodology with sample motor rating calculations for the slurry mixing agitator of a Pre-desilication tank of Alumina refinery. 

Method to arrive at motor rating: 

Impeller power for slurry mixing agitator is calculated using following mathematical relations-
Impeller Power, P = Np * ρ *N3 * Di5/(16*104) h.p.
Where Di = Diameter of impeller in meters,
N  = Revolution per minute for impeller,
Np = Power number for impeller and
ρ   = Specific gravity of slurry.

Sample calculations:

Simplified calculations to arrive at the motor rating for the agitator of Pre-desilication tank of around 3000 m3 gross capacity with realistic assumptions have been presented below-

Fluid Height in Tank , H = 16 m and Diameter of tank, Dt = 14 m
Slurry volume in tank   = π *Dt2*H/4 =  π * (14)2*16 /4 = 2463 m3   
Solid consistency in Slurry = 50 % (w/w),   Specific gravity of slurry, ρ = 1.602,
Viscosity of slurry, μ  = 550 cp
Agitator Impeller Diameter, Di= 33 % of tank diameter = 14 * 33% m = 4.62 m
Tip speed of Impeller = 290 m/minute,      Drive motor RPM = 1500 rpm.
Gear Box Reduction Ratio = 75
Agitator RPM, N = Drive Motor RPM/Gear Box Reduction Ratio = 1500/75 = 20 rpm
Flow Number Nq   = 0.56 and Power Number,     Np  = 0.51 (assumed figures)
Pumping Capacity  =  Nq * N * Di3  m3/minute
= 0.56 * 20 * (4.62)3 = 1104.44 m3/min.  = 18.41 m3/sec.
Area of Tank               = π  * Dt2   = π  *(14)2 / 4 = 153.94 m2
Bulk fluid Velocity      = pumping capacity/area of tank
= 1104.44 / 153.94= 7.18 m/min.= 23.55 ft./min.
Degree of Agitation   = bulk fluid velocity / 6     
(For 6 ft/min., degree of agitation =1 and Degree of agitation varies from 0 to 10)
= 23.55 / 6  = 3.93 ~ 4
Annular Area  = π  * (Dt2- Di2 ) /4  
Where Dt = Diameter of tank      and        D= Diameter of impeller in meters.
= 3.14 * (142 – (4.622) / 4 = 137.18 m2
Rising velocity of particles = pumping capacity / annular area
= 1104.44 / 137.18 = 8.051 m/min.  = 0.1342 m/sec. 
Tank Turnover rate   = Pumping capacity / tank capacity
= 1104.44 / 2463 = 0.45 times / min.
Power Number Np    = 0.51
Shaft Power,      P      = Np* ρ *(Di)5 * N3 /(16 *104)
Where Np = Impeller power no.,               Di = Diameter of impeller in meters,
Shaft RPM,             N = revolutions per minute
Shaft Power, P   = 0.51 * 1.602 * (4.402)5 * 203 / (16 *104) = 85.98 h.p.
Taking Gear Box Efficiency   = 80% and Drive Motor Efficiency = 95%,
Design margin           = 1.15
Drive Motor Rating = 1.15 * 85.98/(0.80 * 0.95) =130 h.p. = 97.0 kW.

Thus the drive motor of about 100 kW shall be adequate for successful operation of agitator of 3000 m3 Pre-desilication tank in Alumina refinery. 


The developed methodology clearly reveals that motor rating calculations for any slurry mixing agitator can be carried out easily by simply replacing the associated input process conditions, operating parameters, dimensions of tanks / vessel and appropriate power number for impeller in above simplified derivation.

Please put your views / suggestion / remarks / comments, if any.

If you like this article, then please press your rating as  +1  .
Thanks and regards.

Kunwar Rajendra


  1. Hi, I would like ask is it the method you proposed above can be use for design the precipitation tank as well?

  2. Dear Mr. Roger Soon,

    Yes, you are absolutely correct. This is the method to carry out the basic design depending on the characteristics of material to be handled and operating conditions suiting the process requirement more particularly the RPM of agitator blades. Based on the basic design, Mechanical design of agitator is done.

    Kunwar Rajendra

  3. Dear Mr. Rajendra ,
    I have a open top slurry tank which holds 5 m3 of Ca(OH)2 ,in other words it is called milk of lime .
    The tank height & internal diameter both are about 2.0 m and i intend to design and install a top mounted agitator on top of the tank.
    Much appreciated if you could post a typical calculation methodology for sizing agitator based on the below data.
    Slurry density =1080 kg/m3
    Viscocity = 10 cP
    % Solids (w/w)=12.5
    Fluid temp = 50 deg max

  4. Dear Mr. Kiran Kumar,
    It appears from your e.mail that you do not want to learn new things. May be that you are either very old or lethargic in nature.Do you want that some body else should develop calculations for you? It is just too much.Request you to take a piece of paper and a simple calculator to carry out calculations systematically as explained above. It will not take more than 10 minutes for you. Take this small challenge and let me know the outcome of your design calculations.
    Hope, you will follow my advice and keep me posted.

    Kunwar Rajendra

  5. Hi,
    Can you suggest me how would we assume the impeller power number and flow number?

    1. Hi Manas,
      Thanks for the very interesting question. Flow number and Power number are purely based on the design of impeller carried out by manufacturers. Thus, based on the experience of Designer with various types of impellers used in operating plants, these numbers are assumed and taken into consideration while designing such complicated system.
      Hope, the above clarifies your doubts.

      Kunwar Rajendra

    2. Hi,
      Kindly clarify me whether the slurry viscosity plays any role for selection of agitator or not?

  6. Dear Manas,

    Viscosity, Specific gravity and Particle size in slurry play vital role in selection of agitator including its drive components.
    Thanks and regards.

    Kunwar Rajendra

  7. Dear Mr. Rajendra, thanks for this important contribution. I have two questions.
    1. How can we integrate the fact if having 2 impellers on the same shaft.
    2. What are the main differences with calculating a thickener

  8. Dear Roger,
    Thank you very much for appreciating the articles published on my blog. The number of stages of impellers are decided on the basis of degree of agitation required for particular service conditions to prevent settling of solids. However, agitator (rake) for settling tanks are designed on the basis of torque developed for movement of settled mud.
    Trust, the above clarifies your doubts.

    Kunwar Rajendra

  9. This comment has been removed by the author.

  10. From: chinmoy panda
    Sent: ‎11-‎01-‎2015 00:48
    Subject: regarding your article in alumina technology( AG DRIVE MOTOR POWER CALCULATION)


    i saw the article of yours.
    thanks for the info. I'm a mechanical guy.i m little bit puzzled by seeing the terms.i googled the term term but not able to undersatnd.

    my question regarding

    What is

    1.Bulk fluid Velocity = pumping capacity/area of tank

    2.Degree of Agitation = bulk fluid velocity / 6
    (For 6 ft/min., degree of agitation =1 and Degree of agitation varies from 0 to 10)

    3.Rising velocity of particles = pumping capacity / annular area

    4.Tank Turnover rate = Pumping capacity / tank capacity

    we have EKATO AGITATORS having 5 stages blades.
    the designed you mentioned by taking into considearion only one blade or what?

    Chinmoy Panda

    1. Dear Mr. Chinmoy Panda,

      I am delighted to have your e.mail.
      Thank you for your interest in going through the articles published on my blog. These articles have been developed for enthusiastic and progressive guys like you who have interest to learn. You must have also realized the quantum of efforts taken in originating and writing such valuable technical articles. It's my hobby to learn and share the knowledge of public domain nature with my younger generation in particular. I have observed personally that people of bauxite-alumina-aluminium fraternity in general are hesitant in sharing their knowledge with the fear that others will climb to higher position compared to them. It's nothing but the wrong fear psychosis as per my perception. Now, coming to your interesting questions, the outcome published are gist of studies assimilated from the renowned books related to Agitators only. Any way, let me give clarify your doubts in subsequent paragraphs.

      There are two types of agitation required in process vessels of chemical / pharmaceutical and mineral processing industries-
      (a) Off- Bottom solid suspension and
      (b) Full tank solid suspension.

      Off-bottom suspension, agitator has the duty for keeping the solids present in the slurry (mixture of solid particles and liquid) just in suspension to prevent settling of solids in tanks. Where as full tank suspension means keeping the slurry homogeneous so as to have same solid content in vessel and discharge overflow slurry as well.

      Thus Degree of agitation is the guide line for optimizing the rate of suspension of solids which ranges from 1 to 10. The degree of agitation can not be worked out without calculating the bulk fluid velocity as elaborated under point-1 of your e.mail. For vigorous agitation in any vessel the calculated degree of agitation may work out to more than 10 but it is considered as equal to 10 only. It is similar to scoring marks in any examination.

      Tank turn over rate is the guideline figure to optimize the revolution rate of impeller. The settling velocity of particles of solids can not be kept more than the upward velocity in order to avoid settlement and accumulation of solids in tanks.

      Hope, above will clarify your doubts.

      Request you to put your question, if any, under "Comment" space provided below each article on my blog so that others will also learn from your comments / remarks. Avoid sending separate e.mails to me.

      Remember to share your knowledge with others to increase your own knowledge. Never feel that you know every thing and remain hungry for learning new concepts and techniques.
      Best wishes.

      Kunwar Rajendra