332002475-ASSG-3-Joels

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1. Water Pump Table 1. Water Pump (P-100) Specifications Equipment Specification Equipment code P-100 Pump Type Centrifugal Pump Function Pump water to NaOH storage for mixture Operation Continuous Material Cast Iron Operation Data Flow rate 51.6 Kg/hr Differential Pressure 100 kPa Differential Head 9.46 m NPSH 1.86 m Efficiency 60 % Break Horse Power 3.43 Hp Fuids Conditions Composition 100% Water Temperature 30 0 C Density 995.2 Kg/m 3 (Source : Author’s Personal Data, 2016) 2. NaOH Pump Table 2. NaOH Pump (P-101) Specifications Equipment Specification Equipment code P-101 Pump Type Centrifugal Pump Function Pump NaOH from storage to filter Operation Continuous Material Stainless Steel Operation Data Flow rate 1250 Kg/hr Differential Pressure 900 kPa Differential Head 66.96 m NPSH 5.05 m Efficiency 60 % Break Horse Power 587.09 Hp Fuids Conditions Composition 50% Water ; 50% NaOH

Temperature 30 0 C Density 1278 Kg/m 3 (Source : Author’s Personal Data, 2016) 3. HCl Pump Table 3. HCl Pump (P-102) Specifications Equipment Specification Equipment code P-102 Pump Type Centrifugal Pump Function Pump HCl from storage to mixer Operation Continuous Material Stainless Steel Operation Data Flow rate 83.33 Kg/hr Differential Pressure 100 kPa Differential Head 10.09 m NPSH 0.21 m Efficiency 60 % Break Horse Power 6.77 Hp Fuids Conditions Composition 50% Water ; 50% HCl Temperature 30 0 C Density 1447 Kg/m 3 (Source : Author’s Personal Data, 2016) 4. NaOH Recycle Pump Table 4. NaOH Recycle Pump (P-103) Specifications Equipment Specification Equipment code P-103 Pump Type Centrifugal Pump Function Pump NaOH recycle from filter to storage Operation Continuous Material Stainless Steel Operation Data Flow rate 4.167 Kg/hr Differential Pressure 200 kPa Differential Head 16.01m NPSH 6.71 m Efficiency 60 %

Break Horse Power 0.47 Hp Fuids Conditions Composition 50% Water ; 50% NaOH Temperature 35 0 C Density 1271 Kg/m 3 (Source : Author’s Personal Data, 2016) 5. HNO 3 Pump Table 5. HNO 3 Pump (P-104) Specifications Equipment Specification Equipment code P-104 Pump Type Centrifugal Pump Function Pump HNO 3 from storage to Leacher Operation Continuous Material Stainless Steel Operation Data Flow rate 62.5 Kg/hr Differential Pressure 100 kPa Differential Head 5.75m NPSH 4.91 m Efficiency 60 % Break Horse Power 2.52 Hp Fuids Conditions Composition 100% HNO 3 Temperature 30 0 C Density 1492 Kg/m 3 (Source : Author’s Personal Data, 2016)

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PUMP We selected centrifugal pump as our type of pump in our plant because the fluid viscosity that will be transfered is low and there is no high temperature of mixture in our plant. We used formula from Fluids Mechanical for Chemical Engineering by Noel De Nevers 2 nd ed . This pumping section we also determine the piping size for each flow by considering, flow, pressure, and temperature. First we input all of our data, mass flow, density, pressure difference, temperature, pipe diameter, and lenght of pipe in the spreadsheet. Then the spreadsheet will show the result for friction loss in pipe ,total head ,NPSHa , and actual horse power. In sizing pump, we assume that all the pump efficiency is 60% ∆ P = P at liquid surface suction − P at destination Then we can calculate friction loss in pipe for turbulent. F = 4 f ∆ x.V 2 g. D .2 with f is friction factor that can be seen in Fanning Diagram. Total head can be calculated with this formula after we get friction factor. which is subscript s for the suction area and d for the discharge area. NPSH is calculated by many factor. The most important variable here is the length t of pipe itself, equivalent length of valve and bending. NPSH a =− H f − H s + 2.31 Patm − Pvap SG Where P atm is atmospheric pressure, P vap is vapor pressure of water at 75 0 F, and SG is specific gravity. Hf is the friction loss that we calculated before. BHP (Break Horse Power) is calculated by this formula. P pump ( hp ) = SG .q ( US gal min ) .total head ( ft ) 3960 .η In this case, we will asume :  No fitting

 Elevated height only 1 m wich is different from discharge pump to inlet tank  Length of pipe 10 m  Pump efficiency (η) = 60 % Table A.1. Pump Summarize Calculation Pump Q (Kg/hr) Temperature ( 0 C) Density (Kg/m 3 ) Delta P (Kpa) Diameter of pipe (inch) Total Head (m) NPSH (M) Estimated Efficiency (%) Break Horse Power (BHP) P-100 51.6 30 995.2 100 5 9.47 1.86 60 3.43 P-101 1250 30 1278 900 15 66.96 5.05 60 587.09 P-102 83.33 30 1447 100 5 10.09 0.21 60 6.77 P-103 4.167 35 1271 200 3 16.01 6.71 60 0.47 P-104 62.5 30 1492 100 5 5.75 4.91 60 2.52

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Leaching Unit Amount of needed tank Flow rate into tank is 397.9 kg/hr, to gain the volume we could divide the mass rate with total density. Q = m ρ = 397.9 kg h 1400 kg / m 3 = 0.284 m 3 / h Diameter and height of mixer tank Comparison of high tank with tank diameter (Hs: D) = 1.5:1. The volume will be represented by using ellipsoidal shape, the diameter and height of tank could be calculated. Vs = 1 4 π D 2 x Hs = 1 4 π 1.5 D 3 Cover and pedestal tank of ellipsoidal shape with major to minor axis ratio of 2:1, so high head is H h = 1 6 D (Walas, 1990). Cover and pedestal tank of ellipsoidal shape with major to minor axis ratio of 2:1, so high head isolume of the cover is V h ellipsoidal = 1 4 π D 2 x H h x 2 = 1 4 π D 2 x 1 6 Dx 2 = 1 12 π D 3 Tank volume is V t = V s + V h = 1 4 π 1.5 D 3 + 1 12 π D 3 = 11 24 π D 3 Tank diameter is D = 3 √ 24 V t 11 π = 3 √ 24 x 0.284 m 3 11 π = 0.58 m Height of cylinder is H s = 1.5D = 0.87 m Height of cover ellipsoidal is H h = 1/6 D = 1/6 * 0.58 = 0.097 m Height tank is H t = H s + (2 x H h ) = 0.87 m + (2 x 0.097) m = 1.06 m Pressure design P h = ρgh = 1400 kg m 3 x 9.81 x 1.06 = 14612 Pa = 0.14 atm

Assumptions for pressure safety factor = 15 % Design pressure is Pdesign = 1.15 x ( 1 + 0.14 ) = 1.31 atm = 19.25 psi Thick of wall and head Material choosen is stainless steel because condition of the solution strong acid HNO 3 . Avoiding corrosion, stainless steel used for this case. Thick of wall Assumption of corrosion factor is © = 0.0042 in/year Allowable working stress is (S) = 16250 lb/in2 (Walas, 1990) Assumptions connection efficiency is (E) = 0.85 Planned of tool age (A) = 30 years Thick of cylinder is d = P x R SE − 0.6 P +( C x A ) 19.25 psi x 11.42 ∈ ¿ ( 16250 lb ¿ 2 x 0.85 )− 0.6 ( 19.25 psi ) +( 0.0042 ¿ year x 30 year ) d = ¿ d = 0.14 ∈ ¿ 3.6 mm Thick of wall head (cap) Assumption of corrosion factor is © = 0.0042 in/year Allowable working stress is (S) = 16250 lb/in2 (Walas, 1990) Assumptions connection efficiency is (E) = 0.85 Planned of tool age (A) = 30 years Thick of head is d h = P x Di 2 SE − 0.2 P +( C x A ) 19.25 psi x 22.83 ∈ ¿ ( 2 x 16250 lb ¿ 2 x 0.85 )− 0.2 ( 19.25 psi ) +( 0.0042 ¿ year x 30 year ) d = ¿ d = 0.12 ∈ ¿ 3.05 mm Agitator There are many factors affecting the selection of agitator, such as mixing pattern (axial, radial), capacity of vessel, density and viscosity of fluid viscosity. Three basic types of impeller, such as:  Flat blade (Rushton) turbines (suitable for shear controlled processes).

 Propeller and pitched blade turbines (suitable for bulk fluid mixing).  Anchor and Helical ribbon agitators 90 (suitable for highly viscous fluids) The selection type of turbine is selected impeller blade turbine with inclined 45˚. Figure 1 . Pitched Blade Turbine ( Source : Perry, 2008)

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