Design and Implementation of Differential Agitators to Maximize Agitating Performance

This research is to design and implement a new kind of agitators called d ifferential agitator. The Differential Agitator is an electromechanic set consists of two shafts. The first shaft is the bearing axis while the second shaft is the axis of the quartet upper bearing impellers group and the triple lower group which are called as agitating group. The agitating group is located inside a cy lindrical container equipped especially to contain square directors for the liqu id entrance and square directors called fixing group for the liquid exit. The fixing group is installed containing the agitating group inside any tank whether from upper or lower position. The agitating process occurs through the agitating group bearing causing a lower pressure over the upper group leading to withdrawing the liquid from the square directors of the liquid entering and consequently the liquid moves to the denser place under the quartet upper group. Then, the liquid moves to the so high pressure area under the agitating group causing the liquid to exit from the square directors in the bottom of the container. For improving efficiency, parametric study and shape optimization has been carried out. A numerical analysis, manufacturing and laboratory experiments were conducted to design and implement the differential agitator. Knowing the material prosperities and the loading conditions, the FEM using ANSYS11 was used to get the optimum design of the geometrical parameters of the differential agitator elements while the experimental test was performed to validate the advantages of the differential agitators to give a h igh agitation performance of lime in the water as an example. In addit ion, the experimental work has been done to express the internal container shape in the agitation efficiency. The study ended up with conclusions to maximize ag itator perfo rmance and optimize the geometrical parameters to be used for manufacturing the differential agitator.


Introduction
Agitation is the process of induce mot ion of material in a sp ecified way . In th e ch emical and o th er p ro cess ing industries, many operations are dependent to a great extent on effect ive ag itat ion and mi xing o f flu ids. Generally, agitation refers to forcing a fluid by agitator means to flow in a circulatory or other pattern inside a vessel (see Figure 1.1). In spite that agitator is very effective in industry today but still has many problems which affect the agitation process. Most agitator cause vortex in the center of the liquid which enforces the manufacturers to put Baffles inside the agitating tanks. In add ition, the classical agitator generate bubbles inside the gas causing dribble which is prohibited in liquids of low flash points. These agitators cause bubbles in the liquid of the liquid vapor called Cav itations. Cavitations lead to lowering the agitating efficiency due to storing a great amount of energy in the form of pressure. Ag itation has various purposes such suspending solid particles, blending miscible liquids, d ispersing a gas through a liquid in the form of sma ll bubbles, dispersing a second liquid immiscib le with the first, to form an emulsion or suspension of fine drops, and promoting heat transfer between the liquid and a coil or jacket. There are so me factors affecting the efficiency of agitating; some are related to the liquid characteristics such as viscosity and density, and some are related to the geometry such as the container diameter (D), impeller length (Y), rotating speed (N), height of impellers fro m bottom of the container (h) as shown in Figure 1.2, the later affects the gathered materials in the bottom of the container because this amount can't be min imized to a great value as it demands a high capacity of the motor due to surface tension of the liquid [1].
Other characteristics of mixing include the necessity of performing the process to make the liquid experience all kinds of movement inside the container (fro m down wards to upwards a vice versa -cyclic -diagonal), When agitating two liquids that have a thicker one or agitating a solid material in order to solute in the liquid, various techniques are used; bearing shaft in wh ich different designs are fixed of agitator impellers such as : 1. A xial Impellers 2. Centrifugal Impellers 3. Mu lti Stage Impellers 4. Inclined Impelle rs 5. Helical/Screw Impellers    [2] The first four kinds depend on mixing through withdrawing the denser liquid upwards but they have some defects or problems as follow [1]: 1. Most agitator cause vortex in the center of the liquid the matter that enforces the manufacturers to put Baffles inside the agitating tanks.
2. Most agitator lead to bubbles inside the gas causing dribble which is prohibited in liquids of low flash points.
3. These agitators cause bubbles in the liquid of the liquid vapor which causes cavitations. These cavitations leads to lowering the agitating efficiency due to storing a great amount of energy in the form of p ressure. 4. To design the agitators, there is a need to calculate the electric power of the motor according to the tank size and liquid type. 5. When calculating the electric power of a motor, we are urged suppose that the tank is cylindrical. 6. There is no a universal system till now that is valid for all liquids and all tanks except the differential ag itator.

Background
Weber [3] , develops a new type of agitator for continuous flow reactor for h igh viscosity materials. A reactor of one or more stages for the continuous processing of high viscosity material wherein each stage is provided with a stage barrier for d irecting and controlling. The flow of process material within each stage of the reactor and for controlling the egress of material fro m each stage of the reactor. A rotor shaft is rotatable mounted at opposite end walls o f the reactor and extends through the reactor coaxially with its longitudinal a xis. Fix ably attached to the rotor shaft for rotation within each stage is a mixing assembly including a cylindrical draft tube positioned coaxially with respect to the reactor side wall. A helical screw mounted within the draft tube with a ribbon agitator mounted within the annular space between the draft tube. The reactor wall wh ich having a pitch opposite to the helical screw. The ag itator and the helical screw have pre selected relative pitches and dimensions so that when rotated they cooperate with the stage barrier. The vessels wall and the draft tube to re-circulate a predetermined portion of process material in a fixed flow pattern within each stage while advancing a remaining predetermined portion of the process material out of the stage in one direction. Weetman and Howk [4] ; developed a new type of mixe r to provides axial flo w in a non uniformal flow field. Such as may be established by gas and provides a large axial flo w volu me without flooding and withstands variable loads on the blades. Thereby providing for a reliab le operation. The mixer impeller is made up of paddle shaped blades, which near their tips (e.g., at 90% of the radius of the impeller fro m its a xis of rotation) and which are of a width at least 40% of the impeller's diameter. The blades also have camber and twist. They are formed by establishing bending mo ments which form the blades into sections which are curved and flat, with the flat section being at least in the central area of the base of the blades. The hub for attaching the blades to the shaft of the mixer has radically extending arms with flat surfaces. The bases of the blades are spaced fro m the shaft to define areas there between. These areas are reduced in size, thereby limit ing the passage of sparging gas between the blades and the shaft. The strength of the coupling between the blades and the shaft are enhanced by backing plates of the width greater than the width of arms. These backing plates are fastened between arms and the flat sections of blades. Bolts extending through aligned holes in the arms, backing plates and blades provides stronger and secure attachment of impeller b lades to the shaft. The impeller will operate reliably in the environment which provides variable loads on the blades. In 1999, Inoue and Saito [5] , imp rove mixing device and method. The mixing material around inner agitating means in a mixing vessel is urged upward and outward by rotating the inner agitating in one direction. In simu ltaneously the mixing material around outer agitating is urged downward and inward by rotating the outer agitating in the opposite direction. Consequently the cause of mixing materials urged upward and downward to be circulated by convection in the mixing vessels. The mixing materials urged outward and inward to collide between the inner and outer agitating to forming a high pressure region between the inner and outer agitating. The mixing materials are mashed in high pressure region and well mixed in short time with high efficiency without being agglutinated to the inner agitating. Hockmeyer and He rman [6], Apparatus for processing high viscosity dispersions. The Apparatus for dispersing solid constituent into a liquid immersion mill operating in combination with a low shear mixer blade assembly. Where it sweeps the walls of the tank containing a batch of solid constituents in a liquid circu late the batch through the immersion mill to carry out a milling operation. To establish a relatively high viscosity mixture having a high degree of uniformity. The immersion mill includes an improvement wherein a helical screw impeller is placed within a tubular inlet passage for moving the batch longitudinally through the tubular inlet passage into the imme rsion mill. The helical screw impeller including a helical flight extending along the length of the tubular inlet passage and having a diameter co mplementary to the diameter of the tubular inlet passage. The pitch will be less than the length of the tubular inlet passage such that the helical flight spans the diameter of the tubular inlet passage along plural turns of the helical flight . Agitators can be classified based on how a fluid flo ws through the impeller. The flow of the fluid through the impeller is determined by the design of the agitator casing and the impeller. The three types of flow through the agitator are radial flow, axial flow, and mixed flow. In a radial flo w agitator, the liquid enters at the center of the impeller and is d irected out along the impeller b lades at right angles to the agitator shaft . In an axial flow ag itator, the impeller pushes the liquid in a direction parallel to the agitator shaft. Axial flow ag itator are sometimes called propeller agitators because they operate essentially the same as the propeller of a boat [7]. M ixed flow agitators borrow characteristics fro m both radial flo w and axial flow agitators. As liquid flows through the impeller of a mixed flow agitator, the impeller blades push the liquid out away fro m the agitator shaft and to the agitator suction at an angle greater than 90 o [8]. A centrifugal agitator with a single impeller that can develop a differential pressure of more than 150 psi between the suction and the discharge is difficu lt and costly to design and construct. A mo re economical approach to developing high pressures with a single centrifugal agitator is to include mu ltiple impellers on a common shaft within the same ag itator casing [9]. Internal channels in the agitator casing route the discharge of one impeller to the suction of another impeller. The water enters the agitator fro m the top left and passes through each of the stage impellers in series, going fro m left to right. The water flows fro m the volute surrounding the discharge of one impeller to the suction of the ne xt impeller. An agitator stage is defined as that portion of a centrifugal agitator consisting of one impeller and its associated components. Most centrifugal agitators are single-stage agitators, containing only one impeller. An agitator containing seven impellers within a single casing would be referred to as a seven-stage agitator or, generally, as a mu lt i-stage agitator [9]. Agitators Impellers can be open, semi-open, or enclosed. The open impeller consists only of blades attached to a hub. The semi-open impeller is constructed with a circular p late (the web) attached to one side of the blades. The enclosed impeller has circular p lates attached to both sides of the blades. Enclosed impellers are also referred to as shrouded impellers. Impellers of agitators are either Single-Suction or Double-Suction Impelle rs based on the number of points that the liquid can enter the impeller and also on the amount of webbing between the impeller b lades. Impelle rs can be either single-suction or double-suction. A single-suction impeller allo ws liquid to enter the center of the blades fro m only one direction. A double-suction impeller allows liquid to enter the center of the impeller blades fro m both sides simu ltaneously [9]. The impeller somet imes contains balancing holes that connect the space around the hub to the suction side of the impeller. The balancing holes have a total cross-sectional area that is considerably greater than the cross-sectional area of the annular space between the wearing ring and the hub. The result is suction pressure on both sides of the impeller hub, wh ich maintains a hydraulic balance. There are some parts that affect the efficiency of the agitator and some internal parts are effect ive in the agitators efficiency and agitation process, like d iffuser wearing rings and they also maintain the operation conditions of an agitator to avoid some defects like cavitation [10]. So me centrifugal agitators contain diffusers. A diffuser is a set of stationary vanes that surround the impeller. The purpose of the diffuser is to increase the efficiency of the centrifugal agitator by allo wing a more gradual expansion and less turbulent area for the liquid to reduce in velocity. The diffuser vanes are designed in such a way that the liquid exit ing the impeller will encounter an ever-increasing flow area as it passes through the diffuser. This increase in flow area causes a reduction in flo w velocity, converting kinetic energy into flow pressure. Centrifugal agitators can also be constructed in a manner that results in two d istinct volutes, each receiving the liquid that is discharged fro m a 180o reg ion of the impeller at any g iven time. Agitators of this type are called double volute agitators (they may also be referred to split volute agitators). In some applications the double volute minimizes radial forces imparted to the shaft and bearings due to imbalances in the pressure around the impeller [11]. Centrifugal agitators contain rotating impellers within stationary agitator casings. To allow the impeller to rotate freely within the ag itator casing, a s mall clearance is designed to be maintained between the impeller and the agitator casing. To maximize the efficiency of a centrifugal agitator, it is necessary to minimize the amount of liquid leaking through this clearance fro m the high pressure or discharge side of the agitator back to the low p ressure or suction side. Some wear or erosion will occur at the point where the impeller and the agitator casing nearly come into contact This wear is due to the erosion caused by liquid leaking through this tight clearance and other causes. As wear occurs, the clearances become larger and the rate of leakage increases. Eventually, the leakage could beco me unacceptably large and maintenance would be required on the agitators. To min imize the cost of agitator maintenance, many centrifugal agitators are designed with wearing rings [12]. Wearing rings are replaceable rings that are attached to the impeller and/or the agitator casing to allow a small running clearance between the impeller and the agitator casing without causing wear of the actual impeller or agitator casing material. These wearing rings are designed to be replaced periodically during the life of an agitator and prevent the more costly replacement of the impeller or the casing. The flow area at the eye of the agitator impeller is usually sma ller than either the flow area of the pump suction piping or the flow area through the impeller vanes. When the liquid being pu mped enters the eye of a centrifugal ag itator, the decrease in the flo w area results in an increase in flow velocity accompanied by a decrease in pressure. The greater the agitator flow rate, the greater the pressure drop between the agitator suction and the eye of the impeller. If the pressure drop is large enough, or if the temperature is high enough, the pressure drop may be sufficient to cause the liquid to flash to vapor when the local pressure falls below the saturation pressure for the fluid being pumped. Any vapor bubbles formed by the pressure drop at the eye of the impeller are swept along the impeller vanes by the flow of the fluid. When the bubbles enter a region where local pressure is greater than saturation pressure farther out the impeller vane, the vapor bubbles abruptly collapse. This process of the formation and subsequent collapse of vapor bubbles in an agitator is called cav itation. Cavitation in a centrifugal ag itator has a significant effect on agitator performance. It degrades the performance of an ag itator, resulting in a fluctuating flow rate and discharge pressure. It can also be destructive to agitators internal co mponents. When an agitator cavitates, vapor bubbles form in the low pressure region directly behind the rotating impeller vanes. These vapor bubbles then move toward the oncoming impeller vane, where they collapse and cause a physical shock to the leading edge of the impeller vane. Th is physical shock creates small pits on the leading edge of the impeller vane. Each individual p it is microscopic in size, but the cumulat ive effect of millions of these pits formed over a period of hours or days can literally destroy an agitator impeller. Cav itation can also cause excessive agitator vibration, which could damage agitator bearings, wearing rings, and seals. A s mall number of centrifugal agitators are designed to operate under conditions where cavitation is unavoidable. These agitators must be specially designed and maintained to withstand the small amount of cavitation that occurs during their operation. Most centrifugal agitators are not designed to withstand sustained cavitation. Noise is one of the indications that a centrifugal agitator is cavitating. A cavitating agitator can sound like a can of ma rbles being shaken. Other indications that can be observed fro m a re mote operating station are fluctuating discharge pressure, flo w rate, and agitator motor current [12]. Agitators also have many types and designations. The other classification depends on the impeller type, and the following are some d ifferent types of impeller [13]. The three bladed ma rine type propeller is good for homogenizing and it was the first axial flow impeller used in vessels for agitation. It is often supplied with fixed and variable speed portable agitators up to 5HP with impeller diameters up to 150 mm. Marine propellers are too heavy and too expensive compared with hydrofoil impellers. They are usually applied up to 1750 rp m in vessels up to 2000 liters. Viscosity limit is about 5000 cP, Lower Reynold's Nu mber limit is 200 [14]. The marine propellers are used in applications requiring moderate pump ing action. These propellers are axial flo w impellers. The propeller blades are designed so that the liquid is quickly carried away fro m the blade without occurrence of cav itations. As such, ma rine propellers are used for products with lo wer to med iu m viscosities. The impeller is the hydrofoil high efficiency impeller, but all vendors have competitive impeller such as heat transfer, b lending, and solids suspension at all speeds in all vessels. The economical optimu m D/T (0,4 > D/T optimu m > 0.6) is greater for hydrofoils than for h igher shear impellers lower NRe limit 200 [14]. The 6 blade disk (historically known as the Rushton turbine) impeller is very old. Nevertheless, it still has no peer. For so me application, it invests the highest proportion of its power as shear of all the turbine impellers, except those (e.g. the cowls impeller) specially designed to create stable emu lsions. It is still the preferred impeller fo r gas liquid dispersion for small vessels at low gas rates, and it is still used extensively for liquid-liquid dispersions, and it is the only logical choice for use with fast competitive chemical reactions, lower NRe limit5 [15]. The blade (45 ºC) p itched blade impeller is the preferred choice where axial flow is desired and where there is a need for proper balance between flow and share. It is the preferred impeller fo r liquid-liquid dispersions and for gas dispersion from the vessel headspace (located about D/3 to D/2 below the free liquid surface) in conjunction with a low 6 Bladed Impeller or a concave blade disk impeller, low NRe limit ≈ 20 The pitched blade Turbine produces less axia l flow than hydrofoils but higher shear forces than hydrofoils. It is best suited when both flow velocity and fluid shear are required. The 4-blade flat blade impeller is universally used to provide agitation as a vessel is emptied. It is installed, normally fitted with stabilizers as low in the vessel as is practical. Four Bladed Impeller is often installed at about C/T to provide effect ive agitation at high batch levels . Lower NRelimit 5 Flat Blade Turbine is a radial flow impeller that is used for lo w volu me stirring [15]. The saw tooth (or cowls type) impeller is the ultimate at investing its power as shear rather than flow. It is used extensively for producing stable liquid-liquid (emu lsions) and dense gas-liquid (foa ms) dispersions. It is often used in conjunction with a larger d iameter axial-flo w impeller h igher on the shaft Lower NRe limit 10 Derya Kro m suggests, that it is difficult to disperse chemicals or for mixing powder into the product to form a smooth mixture. The flow pattern of the saw tooth impellers produces very high shear [15]. The 6 blade disk style concave blade impellers which uses half pipes as blades are used extensively and economically for gas dispersion in large vessels (in fermenters up to 350 tons.) at high gas flow rates . This type will handle up to %200 more gas without flooding than will the 6 Blade, and the gassed power draw at flooding drops only about 30%, where as with a 6 BD, the drop in power draw exceeds 50 %. The Gas Turbine is an impeller that provides excellent gas handling. The gas turbine breaks the gas mo lecules into smaller bubbles, thus increasing the surface area. The gas turbine is designed with special blades that handle higher gas rates for imp roved process efficiency.

Overview
The differential ag itator is an electro-mechanic set consists of two shafts. The first shaft is the bearing axis wh ile the second shaft is the axis of the quartet upper bearing impellers group and the triple lower group which are called as agitating group. The agitating group is located inside a cylindrical container equipped especially to contain square directors for the liquid entrance and square directors called fixing group for the liquid exit.  1. It does not cause vortex in the center of the liquid so that there is no need to put baffles inside the agitating tanks.
2. It does not lead to bubbles inside the gas causing dribble so it is considered suitable for liquids of low flash points.
3. It does not cause bubbles or cavitations which leads to increasing the agitating efficiency.
4. To design the differential agitator, there is no need to calculate the electric power o f the motor according to the tank size and liquid type. 5. It is universal and suitable for all liquids and all liquids and tanks. In the differential agitator we will use the Four Bladed (45℃) Pitched Impeller is used to give the axial flow and it's suitable for the operation condition (power , pressure and flow rate). The prototype is in the minimu m value of operation condition as shown in Figure 3.2.

Experi mental work
This investigation of experimental work was carried out to maximize the performance of d ifferential agitator by shape optimization of internal container and impeller shape. There were so many possibilit ies or alternatives to design the internal container of agitator to find out the best values of design parameters. Experimentation with different possibilit ies name ly five alternatives were carried out. First, combination of external tank with one impeller was tried. Secondly, an internal container with fully opened suction and discharge ports, 100 mm X 100 mm , was introduced and experimented along with two impellers mounted axially on the shaft. In third attempt, the mutual d istance between the impellers was changed from 100 mm to 240 mm and observed the result of ag itation. Fourthly, keeping the mutual distance between impellers same (i.e. 100 mm), the suction and discharge ports of internal container were half closed (i.e. 100 mm X 50 mm ) and observed the result of agitation. In fifth experiment, the suction and discharge ports of the internal container were kept half closed and mutual distance between the impellers was varied fro m 100 mm to 240 mm and observed the result of agitation.
The experimental work for impeller shape optimizat ion was started, in which it was discovered that the small impellers caused the high radial movement of water inside the internal container and did not force the liquid to circulate through the suction and discharge ports of the internal container to outer container and deflection of impeller blades at 45 deg gave little better water circu lation. Therefore, large size impeller with blades deflected at 45 deg was used to enhance the agitation process by increasing the flow rate of water fo r circulat ion in the outer tank. As a result of this experimental work, it was determined that larger impeller in all the alternatives/experiments for enhancement of agitation process be used. In these five alternatives, lime water solution has been used by adding 0.2 kg of lime quick , lu mp (849 kg per cubic meter density) to 62.8 kg of portable as shown in Figure 3.9. Water (1000 kg per cubic meter density) and agitate together one minutes of time. Lime water is the common na me for saturated calcium hydro xide solution. It is sparsely soluble. Its chemical formu la is Ca(OH) 2 . Since calciu m hydro xide is only sparsely soluble, i.e. ca. 1.5 g per liter at 25℃, there is no visible distinction to clear water. Attentive observers will notice a slightly earthy smell. It is clearly distinguishable by the alkaline taste of the calciu m hydro xide. The term lime refers to the mineral, rather than the fruit. When exposed with carbon dioxide, lime water turns into a milky solution [17]. While lime water is a clear solution, milk of lime on the other hand is a suspension of calciu m hydro xide particles in water. These particles give it the milky aspect. It is common ly produced by reacting quicklime (calciu m o xide) with an excess of water -usually 4 to 8 t imes the amount of water to the amount of quicklime. Reacting water with quicklime is sometimes referred to as "slaking" the lime. The calciu m oxide will convert to the hydroxide according to the following reaction scheme : CaO + H 2 O → Ca(OH) 2 (1) pH Adjustment/Coagulation -Hydrated lime is widely used to adjust the pH of water to prepare it fo r further treatment. Lime is also used to combat "red water" by neutralizing the acid water, thereby reducing corrosion of pipes and mains fro m acid waters. The corrosive waters contain excessive amounts of carbon dioxide. Lime precipitates the CO 2 to form calciu m carbonate, which provides a protective coating on the inside of water mains. Lime is used in conjunction with alu m or iron salts for coagulating suspended solids incident to the removal of turbidity fro m "raw" water. It serves to maintain the proper pH for most satisfactory coagulation conditions. In some water t reatment plants, alu m sludge is treated with lime to facilitate sludge thickening on pressure filters.
In the experimental work after fin ishing the agitation of lime water, a stop watch was used to read the time which was one minute, and then sample of solution was taken to read the pH by pH meter. The result gave high reading of pH, which was indicative of ho mogenous agitation and good mixing in this alternative. For the all alternatives, the pH reading of lime water solution was taken at three speeds 100, 200 and 300 rp m.
The power for experimental work was 0.5 hp coming fro m 0.5 hp 1800 rp m three phase induction motor, and the variation of speed was controlled by electrical inverter.

Numerical Analysis
Fin ite element modeling using ANSYS11 has been used to optimize the impeller blade dimension to give the experimental result. Both experimental and theoretical analyses done to maximize performance of the differential agitator by parametric and shape optimization. The FEM using ANSYS11 was used to get the optimu m design of the geometrical pap meters of the differential ag itator elements while the experimental test was performed to validate the advantages of the differential agitators to give a high agitation performance of lime in the water as an examp le. In addition, the experimental wo rk has been done to express the internal container shape in the agitation efficiency.

Agitator Geo metry
Where a is Impe ller diameter , is tank diameter , W

Power Calcu lations
Now the power can be consumed in mixing and ag itation the power is a function of power nu mber and Reynolds number which are they depending on dimensions selected: 5 3 . . . In agitation process Power number is Depending on Reynolds number: Reynolds number: = Fluid v iscosity N.s/m 2 Reynolds number was calcu lated for middle density 3120 kg/m 3 , v iscosity 9.50E-04 N.s/m 2 it give 1.64E+05 Renold number.
There is chart shows Relation between Reynolds number and they power number as shown in Figure 3.5. Relat ion between Reynolds number and power number [18] Fro m chart shown in Figure 3.5, Reynolds Nu mber can be observed in relation to power number, like Reynolds number 1.64E+05 normally constant for the same power number increases in the range of power number fro m 1.3 to 1.4 In case of the Power Nu mber is 1.4, the Power required is equal to 0.44 hp, therefore, the motor selected is 0.5 hp and Speed is 0 to 1800 rp m

Impelle r Design
Fro m the power of motor and speed of impeller, the external force wh ich effect in impeller blade as tip force in the end has been calculated. Blade thickness was an obvious mechanical design consideration. The blades must be thick enough to handle fluctuating loads without bending or breaking. The fo llo wing calcu lation takes into account the blade strength.
The min imu m Blade thickness can be calculated as follows: Where, is the location fraction fo r PBT equal to 0.8 , W is the width of the blade (assumed 20mm)[m], is Nu mber of blades , is the blade allo wable stress which is equal to 83.4x106 N/ m 2 and is the blade angle (assumed 45) deg .
The result of blade thickness: Impeller with 3 blades: t= 3.54 mm Impeller with 4 blades: t= 4.09 mm The problem has been solved as static problem using fin ite element method using ANSYS11 with this idealizat ion, modeling was carried out with SOLIDW ORK2011 and was exported to ANSYS11, wh ich made this idealization: element type 3D Solid brick 8 node 45, nu mber of element 4463, boundary condition fix all degree of freedo m at internal surface of impeller, force is 316 N at the tip of impeller and use structural, linear, Elastic, isotropic material with 8027 kg/ m 3 density, 197 GPa modulus of elasticity and 0.3 poisson's ration, impeller after meshing showing in Figure 2.6. After ma king sure the impeller was safe for the static analysis, the optimization analysis of impeller has been done using finite element modeling using ANSYS 11 to perform the minimu m weight design of impeller blade of differential agitator as shown in Figure 3.6 wh ich the H is the thickness of impeller and W is the width of impeller.
The allowable stress in the impeller is assumed to be 0.75 of yield stresses of material and the tip displacement is constrained to be no greater the 1/3000 of the blade length.
FEM using ANSYS11 was made to study this case we start to model the case with following problem description: Impeller length 40 mm and tip force is 130 N, design variable are the impeller thickness (H = 4 mm) and impeller width (W = 20 mm). Objective Variab les is the volu me of impeller b lade to be minimizing to the optimu m volu me. State variable are the stresses to be less than 0.75 of yield stresses of the selected Material is SS304 with y ield stress equal 345 MPa wh ich give the maximu m stress to attend 258MPa. The tip displacement of blade is not greater than 1/3000 of length of impeller which is 40mm wh ich g ive the maximu m d isplacement 1.33e -5m  The analysis time used is structural, linear, Elastic, isotropic material with 8027 kg/m 3 density, 197 GPa modulus of elasticity and 0.3 poissons ration. After making sure that the shaft is safe for the static analysis the optimization analysis of shaft will be started, fin ite element modelling has been performed using ANSYS11 to get the minimu m weight design of shaft of differential agitator as shown in Figure 3.7 where the D is the diameter of the shaft. The allo wable stress in the impeller is assumed to be 0.75 of yield stresses of material and the maximu m d isplacement is constrained to be no greater the 1/3000 of the blade length. Shaft length 500 mm and force is 316 N in impeller location and power take, design variable is the shaft d iameter (D=20 mm). The object ive function is the volu me of shaft to be minimized to the optimu m volu me. The state variable is the stresses to be less than 0.75 of yield stresses for the selected material wh ich is SS304 , with yield stress equal of 345 M Pa which give the maximu m stress to attain 258MPa. The maximu m displacement of shaft is not greater than 1/3000 of length of shaft.

Experi mental Result
The experimental test was performed to validate the advantages of the differential agitators to give a high agitation performance of lime in the water as an examp le. In addition, the experimental wo rk has been done to express the internal container shape in the agitation efficiency. Fo r the first alternative, the experimental wo rk was carried out at impeller speed 100, 200 and 300 rp m and take the reading of pH reading. Figure 3.1 shows the result of pH related to impeller speed in RPM. For this experiment work, it was not available to run the experiment to take measurements at 300 rpm because of high vortex inside of tank. For the second alternative the experimental work was carried out at impeller speed 100,200 and 300 rp m and take the reading of pH reading, Figure 4.2 showing the result of p H related with impeller speed (rp m) , for this experiment work the result is better than the first because of internal container was installed and avoid the high vortex causes. For the third alternative the experimental work was carried out at impeller speed 100,200 and 300 rp m and take the reading of pH reading, Figure 4.3 shows the result of pH related with impeller speed (rpm) , for this experiment work the result was homogeneous and high pH reading and gives the best result for all experimental work.       For the fourth and fifth alternatives, the experimental work was also carried out at impeller speed 100, 200 and 300 rpm and the reading of pH reading is taken. Fro m the above graphs the third alternative is the best alternative to g ive a high agitation performance of lime in the water because the pH is the highest value and the pH reading is increased fro m 100 rp m to 200 rp m wh ich is suitable with the agitation of p rototype because the homogeneous agitation is showing at 200 rp m. The 200 rp m shows the best agitation index because it ma kes a h igh pH reading and also a high homogeneous motion of the water. At the same speed (i.e. 200 rp m) the saturated solution is produced by adding a quantity of lime and keep it long time in the tank after that the agitator is run at varying speed. The speed of 200 rp m gives the best suspensions of the lime solid mo lecules and homogeneous suspensions solid particles for all position in the tank.

Numerical Result
4.2.1. Impelle r FEM of impeller using ANSYS11 as a logical solution of static and parametric optimization to obtain the optimal volume of impeller for a ma ximu m performance and high agitation process index.
The output as shown in

Shaft
For the static analysis the ma ximu m stress is 120 Pa and ma ximu m deflection is 0.02 mm wh ich is safe as shown in

Discussion
It has been simu lated that the internal container shape and impeller blade thickness would be subjected to the fluid force and power transmission force. Experimental work and FEM have been applied to calculate the optimal shape of the internal container and optimal thickness of the impeller blade. The experimental work has been done to express the internal container shape in the agitation efficiency. The internal container intakes (suction and discharge) has been changed the shape and express the result by pH reading. Fo r all experimental investigations, by repeating the lap test with new shape of internal container intakes (suction and discharge), it has been found that the optimal shape design of internal container intakes (suction and discharge) is the full intake area because it gives the high flow rate. For all experimental investigation, by repeating the lap test with new impeller angle and size, it has been found that the optimal impeller angle is 45 degree because it gives the high suction and discharge of flow through the internal container. It has been figured out that the optima l d imensions of impeller are when the gap between the impeller t ip and the internal container surface is minimu m because it forces the flow to mot ion in the axial flow direction and no more flow can escape between the impeller and internal container. The normalized principal stress which has been calculated by ANSYS11 during the change of impeller blade thickness, has been used to express the change in the impeller blade thickness with the stress. For all the dimensions investigated, by repeating the optimization loop many t imes, in each loop the impeller b lade thickness is changed and the stress in the root of impeller is calculated until the optimal impeller blade thickness to get the minimu m vo lu me of impeller. It has been shown that the impeller blade thickness can be minimized to 2.9 mm to carry out the allowable stress, and the volume of impeller blade was minimized to 46% fro m the original volume.

Conclusions
The experimental work and FEM ANSYS11 package with optimization technique have been used to investigate the parametric and shape optimizat ion of the differential agitator to maximize its performance. The investigations have been made for the two types of agitators, i.e. normal agitator and differential agitator. These investigations have shown that in the normal agitator the experimental test can not completed due to high vortex in the fluid which starts highly fro m 150 rpm speed of the impeller. Norma l ag itator cause vortex in the center of the liquid the matter that enforces the manufacturers to put Baffles inside the agitating tanks that leads to agitator defect like bubbles, cavitations and lowering the agitating efficiency. The differential agitator avoids the vortex forming in the liquid and gives a high homogeneous motion of the liquid due to transferring the vortex fro m the outer tank to internal container. The optimal shape of the internal container is the full open suction and discharge intakes. The optimal location of impeller is 130mm fro m the top for upper impeller and 130mm fro m bottom for lower impeller. The optimal impeller is 4BPT 45 impeller. In addition, the optimal speed for the prototype is 200 rp m because it gives the high ag itation index p H and ho mogenous motion of the liquid.