SPECIFICATION SHEET IDENTIFICATION Name of Equipment Equipment Code Number Required Capacity Function
Crystallizer T-1 1
6.77
To crystallize Monosodium Glutamate from saturated Monosodium Glutamate solution via adiabatic cooling Batch Vacuum Swenson Surface-Cooled Crystallizer Saturated MSG solution ,MSG crystals DESIGN DATA atm 20-30°C 2.35hrs
Operation Type Material Handled
1 1051.95 / 1.55
Operating Pressure Temperature Residence Time Density
VESSEL DESIGN
Design Pressure Material of Construction Vessel Volume Diameter Height Shell Thickness
SS – SS – 316 316 8.13 2.24 m 5.42 m 4.0 mm
351.29 /ℎ 4.0 mm
Head Thickness Recirculation Rate
COOLING SYSTEM DESIGN
Shell Design
Tube Design Fluid Handled Mass Flow Rate Temperature Number of Tubes Length Outside Diameter Inside Diameter Pitch Clearance
Saturated MSG Fluid Handled Solution 14,988.33 kg/day Mass Flow Rate
180,921.78 kg /day
180°C 219
Temperature Shell Diameter
15°C 374 mm
Baffle Diameter Baffle Spacing
372 mm 149.6 mm
3.66 m 15.88 mm
30°C
12.22 mm 19.84 mm 3.97 mm
PUMP DESIGN Pump Type
Centrifugal Pump
Water
50°C
Power Requirement
0.044 hp
Drawing of the Crystallizer Swenson Surface Cooled Crystallizer
Tube Arrangement
Outside Diameter = 5/8 in = 15.88 mm Using Rotated Square Pitch (From Plant Design and Economics by Peter and Timmershaus)
Tube Pitch, pt = 1.25 Do = 1.25 (15.88 mm) = 19.84 mm Clearance = 0.25 Do = 0.25 (15.88) = 3.97 mm
List of Assumptions
1. 2. 3. 4. 5. 6. 7. 8.
Batch Crystallization process will be employed. 2 batches per day will be used. 20% of the total volume of the feed is allotted as allowance for safety. Using 30% of the conical vessel volume for the extension of the conical vessel on the form of a cylinder to provide for vapor space. SS – 316 will be used as material of construction fo r the vessel design of the crystallizer. Using Double Weld V – butt with efficiency of 0.8 for the welding type. 1 tube pass will be used with a Rotated Square Pitch arrangement. Using 70% pump efficiency for the tube side fluid.
Design Equations: Vessel Design •
Residence Time (Ʈ) ( Ref: ChE Hanbook, 8 th Ed, p. 18 – 47)
° ° ×° 6×× Ʈ
•
•
For Vessel Volume (V) Using 20% allowance for safety factor V vessel = 1.2 × V Feed Vessel Diameter and Height Using H = 1.5D For Conical Vessel, V = 0.230669 × π ×
•
Hydraulic Pressure (P) P = ρgH + 14.7
•
Maximum Stress (S) (Ref: Eq. 4 – 1 of Process Equipment Design by Hesse and Rushton) Sw = Sultimate + Fs + Fm + Fa + Fr
•
•
•
Shell Thickness (ts) (Ref: Eq. 4 – 7 of Process Equipment Design by Hesse and Rushton)
+ 161 2cos
Head Thickness ( (Ref: Eq. 4 – 10 of Process Equipment Design by Hesse and Rushton)
+ 161 2
Circulation Rate (Ref:Handbook of Indutrial Crystallization by Myerson p.134)
1.5∆ Heat Exchanger Design •
Heat Transfer Equation
Richardson)
C. Pump Design •
Power
∆ ∆ (, ,(,) (,,) , ) (, , )
× 3.67×10 (Ref: Equation, 10- 51Perry’s Chemical Engineers’ Handbook, 8th Ed)
•
Circulation Rate
1.5°∆
(Ref: p. 134Handbook of Industrial Crystallization by Myerson)
Vessel Design
From Solubility of MSG Solubility of MSG = 0.10-0.9106 g/mL •
•
Density of MSG crystals = 1618 kg/m3 www.chemicalland21.com/lifescience/foco/MONOSODIUM GLUTAMATE.html MSG liquid density = 680 kg/m3 https://www.merckmillipore.com/INTL/en/product/Sodium-L-glutamatemonohydrate,MDA_CHEM106445?ReferrerURL=https%3A%2F%2Fwww.google.com%2F&bd=1
From Material Balance Basis : 1 day operation Component
Mass (kg/day)
Density (kg/m3)
Volume (m3 /day)
MSG Crystals
3,322.91
1618
2.05
MSG liquid
1,173.59
680
1.73
Water
9,757.40
998.23
9.77
Total
14,253.90
Average Density
13.55
14,13.253.5590kg 1051.95 kg 65.67
Nuclei Population Density ( Ref: Temperature Effects on the Crystallization Kinetics of Size Dependent Systems in a Continuous Mixed Suspensions Mixed Product Removal Crystallizer))
Where:
° ° ./ ∙
ℎ / B° = 1.54x106 crystals / m 3-sec G = 2.4x10-8 m/sec
6.4210 ° 1.2.54410 10− Drawdown Time (Retention Time)
×° 6×× Ʈ ƮRetention Time . 1 / ./ 4√ 1051. 9 5 13 6. 4 210 6 1 1618 Ʈ 2.4108 8445.42sec≈2.35 ℎ
Where:
Operating Time
Number of Batch per Day: 2 Residence Time: 2.35 hours
2. 3 5 hours 2 ℎ × 1 ℎ 4.70 ℎ 1 ,. × 2 ℎ × 1051.95 6.77 ℎ
6.77 Vessel Capacity Using 20% allowance for safety factor,
1.2 () 6.77 Volume of the vessel = 1.2(
) =8.13
Vessel Diameter and Height For Conical Vessel,
1. 5 × × × + × ℎ 0.230699 + × × 0.230699 × × 8.13 8.13 × 0.230699 = 2.24= 17..5 2.34243.36 11.02 (88.13 in)
Extension of the conical vessel in the form of a cylinder is provided for vapor space. Using 30% of the conical vessel volume, Volume of the Vessel Extension
0. 38.132.44
For Cylinder Vessel
2.24 × × 8.13
Total Height
2.06 + 3.36 +2.06 5.42 17.79
Material Specification Material of Construction: Welding Type : Efficiency : Corrosion Allowance :
Hydraulic Pressure
SS316 Double Welded V – Butt 0.80 1/16 inch
+ / 17. 22.14.871+65. 6 7 / 7 9 1 1.55
)
Working Stress For SS – 316 Grade of Steel (Ref: Chemical Engineering Handbook, 8 th Ed., Table 25 – 15,p.25-39)
Tensile Strength: 560 MPa (80,061.11 psi)
. + + + +
(Ref: Process Equipment Design by Hesse and Rushton, p.81) Where; Fm =100% for grade A high tensile strength carbon steel
Fr = 100% for plate thickness of the shell head at any welded
. 100% ℎ 25% 650
joints do not exceed 5/4 in
(Table 4 – 2 of Process Equipment Design by Hesse and Rushton)
Equation 4 – 1 of PED by Hesse and Rushton
. + + + + 81,243.52 ×1.0 ×1.0×1.0×0.25 20310.88 140
Vessel Thickness (Ref: Eq. 4 – 7 of PED by Hesse and Rushton, API – ASME code)
API – ASME CODE: A = ½ of included cone angle =
30
Thickness of the shell is the same with the thickness of the cone
2 + 161 22.81 88.81830.8 + 161 2cos3020310. 0.13 3.302 ≈4.0
Head Thickness (
Using Ellipsoidal Head, (Equation 4 – 10, p.87 of Process Equipment Design by Hesse and Rushton, ASME – UPV code)
2 + 161 22.88180. 88.8122. 3 81 + 161 220310. 0.12 3.16 4
Both shell and head thickness of the vessel is 4.0 mm
Cooling System Design Design Calculations for Heat Exchanger
From Energy Balances Amount of Heat, Q Cooling Water Mass Flow =
= 26,646,159.08kJ 180,921.78 kg
Design Operation: Operation: 2 Batches per Day Residence Time: 2.35 hour Heat Transfer Equation:
∆
Logarithmic Mean Temperature Difference
Temperature in (0C) Temperature out (0C)
Slurry 180 30
Cooling Water 15 50
∆ ∆∆∆ ∆ 5015 ∆ 18030 79. 0 2 18030 ln | 5015 | 1 2.13ℎ 5, 6 69, 3 95. 5 5 26,646,159.08kJ× 2 ℎ 1, 5 74, 8 32. 0 97 5 ℎ ℎ Overall Heat Transfer Coefficient
Overall Heat transfer coefficient of shell and tube heat exchanger wherein Cold fluid =Water and Hot Fluid = Organic Solvent is from 250 to 750
⁄ ∙° 250+750 500 ⁄ ∙° , 2
(Ref: Chemical Engineering Vol. 6, 4 th Ed. By Coulson and Richardson, Table 12.1 p. 637)
Heat Transfer Area
∆ , 5 74, 8 32. 0 97 500 ⁄ ∙°79. 02 39.86 = 429.05
Tube Side Design:
Fluid Handled Mass Flow Rate
:Saturated Solution of MSG :14,253.90 kg/day
Mass Flow Rate
1 × 2.135ℎ 1 ℎ Mass Flow Rate kg/s 14,253.90 × 2ℎ × 0. 8 4 ℎ 3600 Volumetric Flow Rate (GPM)
× 2.135ℎ 1 ℎ 1 0. 2 64 14,253.90 × 21ℎ × × × ℎ 60 1 1 13.34gpm Based on the available standard sizes of tubes used in shell and tube heat exchange,
Using Table 11-12 of Perry’s Chemical Engineers’ Handbook, 8th Ed, and in the assumption of tube outside diameter is 5/8 in outside diameter and 12 ft. tube length. Tube Size and Layout Material of Construction
:
J9290
Outside Diameter
:
5/8 in.
BWG No.
:
15
Inside Diameter
:
0.481 in.
Thickness
:
0.072 in.
Length
:
12 ft.
Number of Tubes
×× 429. 0 5 12 ×× 5 × 1 8 12 219
Pitch Type: Rotated Square Pitch
ℎ, 1.25 1.2558 × 2.514 × 101 19.84 , 0. 25 0.25 58 × 2.514 × 101 3.97
(Reference for the Tube Pitch and Clearance: Chemical Engineering Design by Coulson and Richardson, 4th Ed. Table 12.4)
Pressure Drop (Ref: Equation 12.18 p.666 Chemical Engineering Vol. 6, 4 th Edition by Coulson and Richardson)
Δ8 2
Evaluating for
,
Viscosity of Solution mostly MSG = 56.7 MPa – s (Ref: www.epa.gov/hpv/pubs/sumaaries/;actacid/c13462rd.pdf) Velocity, ut
0. 8 4 ×× ×0.0122 ×1,051.75 ×219 0.0313 4
Reynolds Number
0. 0 122 0. 0 313 1, 0 51. 7 5 × × 0.0000567 ∙
7083 From Fig. 12.24 p. 668 of Chemical Engineering Vol. 6, 4th Ed. By Coulson and Richardson
0.048
Therefore:
Δ8 2
0. 0 313 1051. 9 5 3. 6 576 Δ80.0480.0102 2 Δ70.95 Shell Side Design
Fluid Handled Mass Flow Rate :
: :
Water 180,921.78 kg
Mass Flow Rate
× × . ×
Mass Flow Rate (kg/s) = 180,921.78
=
10.69
Bundle Diameter
0.01588 0.76215, 0.227 (Ref:Equation 12.3 b, p. 648; Chemical Engineering Design, 4th Ed, by Coulson and Richardson) Where: Db =bundle diameter do= tube outside diameter NT = number of tubes For no. of passes =1; Square Rotated Pitch K1 = 0.215 n1 = 2.207 (Ref: Table 12.4, p.649; Chemical Engineering Design, 4th Ed, by Coulson and Richardson)
0.01588 0.219215, 0.366 Shell Diameter
+2 0.366 +20.00397 0.374 =14.72 in
Baffle Diameter and Spacing For pipe shells with shell diameter of 6 to 25 in (152 to 635 mm), equation of Baffle Diameter to be used:
371.9
(in between the range of 152 to 635 mm, therefore, the equation above for
computing Baffle Diameter is suitable)
14.72 161 14.66 0.372
(Ref: Table 12.5, page 651;Chemical Engineering Design, 4 th Ed, Coulson and Richardson)
According to Coulson and Richardson, “the optimum baffle spacing will usually be between 0.3 to 0.5 times the shell diameter.”
Using the average percentage baffle spacing:
0.3+0.2 5 0.40 0.400.374 0.1496
Pressure Drop
∆ 8 2 Where: L= tube length IB= Baffle Spacing For the calculated shell-side Reynold’s number, read the JF from Figure 12.29 (Ref: Equation 12.26, p. 675,Chemical Engineering Design, 4 th Ed, by Coulson and Richardson)
Area for cross flow, As
0. 3 740. 1 496 0.01984 0.015875 0. 0 11 0.01984
Velocity, µ s
10. 6 9 1000 ×0.011 0.956
Evaluating diameter, De,
. 0.785 1.27 [0.0198 0.7850.015875 ]0.0157 0.015875 for
rotated square pitch
(Ref: Equation 12.22, p.672;Chemical Engineering Design, 4 th Ed, by Coulson and Richardson)
Evaluating JF :
⁰
Viscosity of water at 27 C is 0.82 cP. (Ref: Perry’s Chemical Engineerin Handbook, 8th Edition)
×× 0. 9 56 ×0. 0 157 ×1000 8.2×10− ∙ 18,304.53 (Ref: From Fig 12.29, p. 673, Chemical Engineering Design, 4 th Ed, by Coulson and Richardson)
Choose, 25 % Baffle Cut JF= 2.75x10-3
Therefore:
∆ 8 2 1000 0. 9 56 m 0. 3 74 3. 6 576 − ∆ 82.75x10 0.0157 0.1496 2 ∆ 5844.24 A. Pump Design
Δ70.95 ∆ 5844.24
∆ <∆ The pump design will be based on the pressure drop on the shell side. According to Coulson and Richardson, fluid with lowest pressure drop should be allocated to the tube side. Pressure drop to
5844.24 × 2.13ℎ 6. 7 7 × 21ℎ 5 ℎ 1. 44 ℎ ∆ 24 5.56 ∙ 5844. 1,051.95
be used for the pump design is
Capacity
Pressure Head, H
Power
× 3.67×10
(Ref: Perry’s Chemical Engineers’ Handbook, 8th Ed, Equation 10-51)
∙ 5. 4 6 1. 4 4 1, 0 51. 9 5 ℎ 3.67×10×0.70 0.03 0.044 ℎ Available Motor Size is 0.05 hp. Circulation Rate
1.5℃
(Ref: Handbook of Industrial Crystallization by Myerson p. 134)
From Energy Balance:
× 2.13ℎ 26,646,159.08kJ × 21ℎ 5, 6 69, 3 95. 5 5 5 ℎ ℎ From Energy Balance:
4,496.50 10,491.83
0.91
4.18
4,076.53 43,855.85
47, 9 32. 3 8 14,987.33 k℃g 3.198 ℃∙ 5, 6 69, 3 95. 5 5 ℎ 1.5℃3.198 ℃∙ 1,051.95 351.29 ℎ
14,987.33
47,932.38
