Batch Still Volume Operating pressure
6000 lts 760 mmHg
Feed Composition Component Methanol Water
%w/w 11% 89% 100%
Properties of solvents Component
Sp.gr
MW
Methanol Water
0.78 1.00
32 18
Latent heat Kcal/kg 263 540
Loading factor for Structured packing Heating Medium Saturated pressure Saturated Temperature Latent heat Cost of Steam
Antonie Coefficient A B C 8.08
1582.27
239.73
8.07
1730.63
233.43
1.5 m/s (kg/Cu.M)0.5 Steam 2 bar (g) 142 °C 512 kcal/kg 0.9 Rs/kg
Main Condenser Cooling medium Inlet temperature Outlet temperature Percentage of operating load Cost of cooling water (Rs/TR)
Cooling water 6 °C 11 °C 85 %
Vent Condenser Chilling medium Inlet temperature Outlet temperature Percentage of average operating load Cost of cooling water (Rs/TR)
Chilled brine -5 °C -3 °C 15 %
Cost of Electricity
4.5 Rs/unit
Avg. Specific gravity of Methanol-Water feed mixture Feed Quantity Component Methanol Water
5854.8 kgs wf 0.110 0.890 1.000
mass (kg) Mol. Wt 644 32 5211 18 5855
Moles 20.1 289.5 309.6
Recovery of Methanol as % of total Methanol in feed Distillate Quantity Component Methanol Water
% w/w 1 0.01 1.000
% w/w 0.080 0.920 1.000
mol.fr 0.07 0.93 1.00 30 % 194 Kgs
mass (kg) Mol. Wt 193.2 32 1.0 18 194.2
Moles 6.0 0.1 6.1
Bottom residue Quantity Component Methanol Water
0.98
mass (kg) Mol. Wt 450.8 32 5209.8 18 5660.6
5661 Kgs Moles 14.1 289.4 303.5
Bubble Point calculation for distillate Operating pressure of the column Bubble temperature Antonie Coefficient Component mol. Fr x A B C Methanol 0.99 8.08 1582.27 239.73 Water 0.01 8.07 1730.63 233.43 1.00 Relative volatility of Methanol over water Bubble Point Calculation for feed Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.07 8.08 1582.27 239.73 Water 0.93 8.07 1730.63 233.43 1.00 Relative volatility of IPA over water Bubble Point Calculation for final residue Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.046 8.08 1582.27 239.73 Water 0.954 8.07 1730.63 233.43 1.000 Relative volatility of Methanol over water
mol.fr 0.99 0.01 1.00
mol.fr 0.046 0.954 1.000
760 mmHg 64.74 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 765.8 0.9987 184.96 0.0022 1.00 4.14
760 mmHg 95.77 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 2315.89 0.198 651.82 0.802 1.00 3.55
760 mmHg 96.93 °C Vap. Pr mol. Fr mmHg y=Psat*x/P 2404.73 0.147 680.29 0.854 1.000 3.53
mass kgs 6.34 14.43 20.77
mass fr. w/w 0.31 0.69 1.00
Average relative volatility, Alp
3.83
For a Total Condenser system Nmin+1 = log(xDl/xDh)(xBh/xBl)/log(Alphaavg) Minimum no. of trays, N
6 5
Minimum reflux ratio (L/D)min = (1/(Alp-1))((xlD/xlB)-Alp(xhD/xhB))
4.39
Actual
(L/D)-(L/D)min
N-Nmin
Theoritical
Add Feed
with 50%
Reflux ratio
L/D+1
N+1
N
Total N
packing eff.
Str. Packing
Random Pak
5.3
0.14
0.485
10
11
22
7.5
13.4
18.0
0.72
0.140
6
7
13
4.5
8.0
Note :
Packing Height (M)
1. For Structured packing, Packed ht is calculated considering 4 no. of theoritical stages per mtr of Packing. Hpacking=N50% eff*4 2. For Random Packing, 1" Pall ring is considered and height of packing is calculated considering HETP=1 (Ref. Ludwig Page no. 212, Table 9-36). HETP =HETPEst*1.5 and Hpaking=HETPAct*Ntotal Act 3. Use gilliland plot for entering values in (N-Nmin)/(N+1). Ref. Ludwig Vol-2 Page11 Fig 8-14
Column diameter calculation Option-1 : Considering MellaPak Structured Packing Reflux ratio L/D Internal reflux ratio L/V=R/(R+1) Average molecular weight of Distillate Duration of Batch distillation Average rate of distillation collection Molar flow rate of distillate Liquid flowrate Molar flow rate mass flowrate Vapour flowrate Molar flowrate Mass flowrate Column operating pressure Vapour density Density of Liquid Packing Loading Factor F Column Cross Sectional Area Diameter of the column
5.3 0.84 32 kg/kmol 0.72 hrs 270 kg/hr 8.45 kmol/hr 45 Kmol/hr 1421 kgs/hr 53 Kmol/hr 1691 kgs/hr 760 mmHg 1.15 kg/Cu.M 781.10 kg/Cu.M 1.50 m/s(kg/M3)1/2 0.292 Sq. M 0.609 M
Reboiler Heat Load Calculation Boil-up rate Latent heat of boiling liquid Heat Load of Reboiler Quantity of Steam required at 2 kg/cm2 (g) Total Steam consumption for I fractionation
1690.9 kgs/hr 264.4 Kcal/kg 491746.0 Kcals/hr 960.4 kgs/hr 691.5 kgs/batch
Condenser Load Latent heat of condensing Methanol-water mix
264.4
0.39 kgs/s 0.47 kgs/s 0.07 lb/Cu ft 48.76 lb/Cu ft
Condenser load Cooling water circulation rate at 6°C temp. diff
447041.8 Kcals/hr 147.8 TR 74.5 Cu. M/hr
Avg. Specific gravity of Methanol-Water feed mixture Feed Quantity Component Methanol Water
5660.62 kgs wf 0.080 0.920 1.000
mass (kg) Mol. Wt 451 32 5210 18 5661
Moles 14.1 289.4 303.5
Recovery of Methanol as % of total Methanol in feed Distillate Quantity Component Methanol Water
% w/w 0.99 0.02 1.000
% w/w 0.041 0.959 1.000
mol.fr 0.05 0.95 1.00 50 % 229 Kgs
mass (kg) Mol. Wt 225.4 32 3.4 18 228.8
Moles 7.0 0.2 7.2
Bottom residue Quantity Component Methanol Water
0.98
mass (kg) Mol. Wt 225.4 32 5206.4 18 5431.8
5432 Kgs Moles 7.0 289.2 296.3
Bubble Point calculation for distillate Operating pressure of the column Bubble temperature Antonie Coefficient Component mol. Fr x A B C Methanol 0.97 8.08 1582.27 239.73 Water 0.03 8.07 1730.63 233.43 1.00 Relative volatility of Methanol over water Bubble Point Calculation for feed Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.05 8.08 1582.27 239.73 Water 0.95 8.07 1730.63 233.43 1.00 Relative volatility of IPA over water Bubble Point Calculation for final residue Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.024 8.08 1582.27 239.73 Water 0.976 8.07 1730.63 233.43 1.000 Relative volatility of Methanol over water
mol.fr 0.97 0.03 1.00
mol.fr 0.024 0.976 1.000
760 mmHg 65.06 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 775.44 0.9934 187.62 0.0065 1.00 4.13
760 mmHg 96.93 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 2404.05 0.147 680.07 0.853 1.00 3.53
760 mmHg 98.38 °C Vap. Pr mol. Fr mmHg y=Psat*x/P 2518.83 0.079 717.07 0.921 1.000 3.51
mass kgs 4.70 15.36 20.06
mass fr. w/w 0.23 0.77 1.00
Average relative volatility, Alp
3.81
For a Total Condenser system Nmin+1 = log(xDl/xDh)(xBh/xBl)/log(Alphaavg) Minimum no. of trays, N
5 4
Minimum reflux ratio (L/D)min = (1/(Alp-1))((xlD/xlB)-Alp(xhD/xhB))
8.31
Actual
(L/D)-(L/D)min
N-Nmin
Theoritical
Add Feed
with 50%
Reflux ratio
L/D+1
N+1
N
Total N
packing eff.
Str. Packing
Random Pak
10.0
0.15
0.480
10
11
21
7.0
12.6
18.0
0.51
0.180
6
7
13
4.5
8.0
Note :
Packing Height (M)
1. For Structured packing, Packed ht is calculated considering 4 no. of theoritical stages per mtr of Packing. Hpacking=N50% eff*4 2. For Random Packing, 1" Pall ring is considered and height of packing is calculated considering HETP=1 (Ref. Ludwig Page no. 212, Table 9-36). HETP =HETPEst*1.5 and Hpaking=HETPAct*Ntotal Act 3. Use gilliland plot for entering values in (N-Nmin)/(N+1). Ref. Ludwig Vol-2 Page11 Fig 8-14
Column diameter calculation Option-1 : Considering MellaPak Structured Packing Reflux ratio L/D Internal reflux ratio L/V=R/(R+1) Average molecular weight of Distillate Duration of Batch distillation Average rate of distillation collection Molar flow rate of distillate Liquid flowrate Molar flow rate mass flowrate Vapour flowrate Molar flowrate Mass flowrate Column operating pressure Vapour density Density of Liquid Packing Loading Factor F Column Cross Sectional Area Diameter of the column
10.0 0.91 32 kg/kmol 1.48 hrs 154 kg/hr 4.85 kmol/hr 48 Kmol/hr 1537 kgs/hr 53 Kmol/hr 1691 kgs/hr 760 mmHg 1.15 kg/Cu.M 783.30 kg/Cu.M 1.50 m/s(kg/M3)1/2 0.292 Sq. M 0.610 M
Reboiler Heat Load Calculation Boil-up rate Latent heat of boiling liquid Heat Load of Reboiler Quantity of Steam required at 2 kg/cm2 (g) Total Steam consumption for II fractionation
1691.3 kgs/hr 267.2 Kcal/kg 497026.2 Kcals/hr 970.8 kgs/hr 1441.4 kgs/batch
Condenser Load Latent heat of condensing Methanol-water mix
267.2
0.43 kgs/s 0.47 kgs/s 0.07 lb/Cu ft 48.90 lb/Cu ft
Condenser load Cooling water circulation rate at 6°C temp. diff
451842.0 Kcals/hr 149.4 TR 75.3 Cu. M/hr
Avg. Specific gravity of Methanol-Water feed mixture Feed Quantity Component Methanol Water
5432 kgs wf 0.041 0.959 1.000
mass (kg) Mol. Wt 225 32 5206 18 5432
Moles 7.0 289.2 296.3
Recovery of Methanol as % of total Methanol in feed Distillate Quantity Component Methanol Water
% w/w 0.95 0.05 1.000
% w/w 0.021 0.979 1.000
mol.fr 0.02 0.98 1.00 50 % 119 Kgs
mass (kg) Mol. Wt 112.7 32 5.9 18 118.6
Moles 3.5 0.3 3.9
Bottom residue Quantity Component Methanol Water
0.99
mass (kg) Mol. Wt 112.7 32 5200.4 18 5313.1
5313 Kgs Moles 3.5 288.9 292.4
Bubble Point calculation for distillate Operating pressure of the column Bubble temperature Antonie Coefficient Component mol. Fr x A B C Methanol 0.91 8.08 1582.27 239.73 Water 0.09 8.07 1730.63 233.43 1.00 Relative volatility of Methanol over water Bubble Point Calculation for feed Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.02 8.08 1582.27 239.73 Water 0.98 8.07 1730.63 233.43 1.00 Relative volatility of IPA over water Bubble Point Calculation for final residue Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.012 8.08 1582.27 239.73 Water 0.988 8.07 1730.63 233.43 1.000 Relative volatility of Methanol over water
mol.fr 0.91 0.09 1.00
mol.fr 0.012 0.988 1.000
760 mmHg 66.26 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 812.79 0.9780 197.96 0.0223 1.00 4.11
760 mmHg 98.4 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 2519.98 0.079 717.44 0.922 1.00 3.51
760 mmHg 99.17 °C Vap. Pr mol. Fr mmHg y=Psat*x/P 2582.51 0.041 737.69 0.959 1.000 3.50
mass kgs 2.52 16.59 19.11
mass fr. w/w 0.13 0.87 1.00
Average relative volatility, Alp
3.79
For a Total Condenser system Nmin+1 = log(xDl/xDh)(xBh/xBl)/log(Alphaavg) Minimum no. of trays, N
5 4
Minimum reflux ratio (L/D)min = (1/(Alp-1))((xlD/xlB)-Alp(xhD/xhB))
15.33
Actual
(L/D)-(L/D)min
N-Nmin
Theoritical
Add Feed
with 50%
Reflux ratio
L/D+1
N+1
N
Total N
packing eff.
Str. Packing
Random Pak
18.4
0.16
0.485
9
10
20
6.6
11.8
35.0
0.55
0.230
6
7
13
4.4
7.9
Note :
Packing Height (M)
1. For Structured packing, Packed ht is calculated considering 4 no. of theoritical stages per mtr of Packing. Hpacking=N50% eff*4 2. For Random Packing, 1" Pall ring is considered and height of packing is calculated considering HETP=1 (Ref. Ludwig Page no. 212, Table 9-36). HETP =HETPEst*1.5 and Hpaking=HETPAct*Ntotal Act 3. Use gilliland plot for entering values in (N-Nmin)/(N+1). Ref. Ludwig Vol-2 Page11 Fig 8-14
Column diameter calculation Option-1 : Considering MellaPak Structured Packing Reflux ratio L/D Internal reflux ratio L/V=R/(R+1) Average molecular weight of Distillate Duration of Batch distillation Average rate of distillation collection Molar flow rate of distillate Liquid flowrate Molar flow rate mass flowrate Vapour flowrate Molar flowrate Mass flowrate Column operating pressure Vapour density Density of Liquid Packing Loading Factor F Column Cross Sectional Area Diameter of the column
18.4 0.95 31 kg/kmol 1.37 hrs 86 kg/hr 2.76 kmol/hr 51 Kmol/hr 1589 kgs/hr 54 Kmol/hr 1676 kgs/hr 760 mmHg 1.13 kg/Cu.M 791.00 kg/Cu.M 1.50 m/s(kg/M3)1/2 0.293 Sq. M 0.610 M
Reboiler Heat Load Calculation Boil-up rate Latent heat of boiling liquid Heat Load of Reboiler Quantity of Steam required at 2 kg/cm2 (g) Total Steam consumption for III fractionation
1675.5 kgs/hr 276.9 Kcal/kg 510261.6 Kcals/hr 996.6 kgs/hr 1368.3 kgs/batch
Condenser Load Latent heat of condensing Methanol-water mix
276.9
0.44 kgs/s 0.47 kgs/s 0.07 lb/Cu ft 49.38 lb/Cu ft
Condenser load Cooling water circulation rate at 6°C temp. diff
463874.2 Kcals/hr 153.4 TR 77.3 Cu. M/hr
Avg. Specific gravity of Methanol-Water feed mixture Feed Quantity Component Methanol Water
1.00
5313 kgs wf 0.021 0.979 1.000
mass (kg) Mol. Wt 113 32 5200 18 5313
Moles 3.5 288.9 292.4
mol.fr 0.01 0.99 1.00
Recovery of Methanol as % of total Methanol in feed
35 %
Distillate Quantity
44 Kgs
Component Methanol Water
% w/w 0.9 0.1 1.000
mass (kg) Mol. Wt 39.4 32 4.4 18 43.8
Moles 1.2 0.2 1.5
Bottom residue Quantity Component Methanol Water
% w/w 0.014 0.986 1.000
mass (kg) Mol. Wt 73.3 32 5196.1 18 5269.3
5269 Kgs Moles 2.3 288.7 291.0
Bubble Point calculation for distillate Operating pressure of the column Bubble temperature Antonie Coefficient Component mol. Fr x A B C Methanol 0.84 8.08 1582.27 239.73 Water 0.16 8.07 1730.63 233.43 1.00 Relative volatility of Methanol over water Bubble Point Calculation for feed Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.01 8.08 1582.27 239.73 Water 0.99 8.07 1730.63 233.43 1.00 Relative volatility of IPA over water Bubble Point Calculation for final residue Operating pressure of the column Assumed temperature mol. Fr Antonie Coefficient Component x A B C Methanol 0.008 8.08 1582.27 239.73 Water 0.992 8.07 1730.63 233.43 1.000 Relative volatility of Methanol over water
mol.fr 0.84 0.16 1.00
mol.fr 0.008 0.992 1.000
760 mmHg 67.96 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 867.96 0.9537 213.35 0.0463 1.00 4.07
760 mmHg 99.17 °C Vap. Pr mol. Fr y=P *x/P mmHg sat 2582.57 0.041 737.71 0.959 1.00 3.50
760 mmHg 99.45 °C Vap. Pr mol. Fr mmHg y=Psat*x/P 2605.88 0.027 745.28 0.973 1.000 3.50
mass mass fr. kgs w/w 1.31 0.07 17.26 0.93 18.57 1.00
Average relative volatility, Alp
3.77
For a Total Condenser system Nmin+1 = log(xDl/xDh)(xBh/xBl)/log(Alphaavg) Minimum no. of trays, N
5 4
Minimum reflux ratio (L/D)min = (1/(Alp-1))((xlD/xlB)-Alp(xhD/xhB))
21.44
Actual
(L/D)-(L/D)min
N-Nmin
Theoritical
Add Feed
with 50%
Reflux ratio
L/D+1
N+1
N
Total N
packing eff.
Str. Packing
Random Pak
25.7
0.16
0.485
8
9
19
6.3
11.3
40.0
0.45
0.280
6
7
14
4.5
8.1
Note :
Packing Height (M)
1. For Structured packing, Packed ht is calculated considering 4 no. of theoritical stages per mtr of Packing. Hpacking=N50% eff*4 2. For Random Packing, 1" Pall ring is considered and height of packing is calculated considering HETP=1 (Ref. Ludwig Page no. 212, Table 9-36). HETP =HETPEst*1.5 and Hpaking=HETPAct*Ntotal Act 3. Use gilliland plot for entering values in (N-Nmin)/(N+1). Ref. Ludwig Vol-2 Page11 Fig 8-14
Column diameter calculation Option-1 : Considering MellaPak Structured Packing Reflux ratio L/D Internal reflux ratio L/V=R/(R+1) Average molecular weight of Distillate Duration of Batch distillation Average rate of distillation collection Molar flow rate of distillate Liquid flowrate Molar flow rate mass flowrate Vapour flowrate Molar flowrate Mass flowrate Column operating pressure Vapour density Density of Liquid Packing Loading Factor F Column Cross Sectional Area Diameter of the column
25.7 0.96 31 kg/kmol 0.71 hrs 62 kg/hr 2.02 kmol/hr 52 Kmol/hr 1593 kgs/hr 54 Kmol/hr 1655 kgs/hr 760 mmHg 1.09 kg/Cu.M 802.00 kg/Cu.M 1.50 m/s(kg/M3)1/2 0.293 Sq. M 0.611 M
Reboiler Heat Load Calculation Boil-up rate Latent heat of boiling liquid Heat Load of Reboiler Quantity of Steam required at 2 kg/cm2 (g) Total Steam consumption for IV fractionation
1655.4 kgs/hr 290.7 Kcal/kg 529341.6 Kcals/hr 1033.9 kgs/hr 731.8 kgs/batch
Condenser Load Latent heat of condensing Methanol-water mix
290.7
0.44 kgs/s 0.46 kgs/s 0.07 lb/Cu ft 50.07 lb/Cu ft
Condenser load Cooling water circulation rate at 6°C temp. diff
481219.6 Kcals/hr 159.1 TR 80.2 Cu. M/hr
COD REDUCTION CALCULATION FOR METHANOL STREAM CH3 - OH
+
MW 32 Moles 1 Kgs 32 On 1mg of Acetone basis : mg 1
1.5O2
CO2
32 1.5 48
44 1 44
18 2 36
1.5
1.38
1.13
+
2H2O
Basis : 1 kg of effluent.
Solvent Content in effluent COD of effluent
Initial 11% w/w 110000 mg/l 165000 mg/l
Percentage reduction in COD Cost Saving due to COD Reduction Oxygen requirement Quantity of effluent per month Quantity of Oygen required per month Air equivalent to oxygen Equivalent operating hrs of compressors Motor Power of compressor Power consumption Per month Per year Cost saving (Rs/Annum) Reduction in effluent per batch 0.12 Effluent reduction per annum Saving due to effluent reduction per annum
Final 1.39% w/w 13902.8 mg/l 20854.2 mg/l 87.4 %
0.17 kg/l 75.60 KL 13076.91 Kgs ### Cu. m/month 138.38 hrs 10 hp 1057 kW hr 12687.09 kW hr 58360.61 731.86 L ### L Rs. 88525.81
COST SAVING DUE TO METHANOL RECOVERY
Fractionation details
Feed
Distillate
Bottoms
Qty (kgs) Purity %
Qty (kgs) Purity %
Duration (hrs)
Reflux Steam Con. Vap. flow Liq. flow ratio (kg/hr) rate (kg/hr) rate (kg/hr)
Qty (kgs)
Purity
I Fractionation
5854.8
11.00%
194.2
99.5%
5660.6
8.0%
0.72
5.3
960
1691
1421
II Fractionation
5660.6
7.96%
228.8
98.5%
5431.8
4.1%
1.48
10.0
971
1691
1537
III Fractionation
5431.8
4.15%
118.6
95.0%
5313.1
2.1%
1.37
18.4
997
1676
1589
IV Fractionation
5313.1
2.12%
43.8
90.0%
5269.3
1.4%
0.71
25.7
1034
1655
1593
585.5
4.29
990
Cost due to steam ConsumptionSteam Consumption Cost of steam generation
1.25 Rs/kg
Cost of Power
Steam
Duration
(kgs/hr)
(hrs)
Total Steam (kgs)
I Fractionation
960
0.72
692
864
Pump-2
5
0.00
100%
0.00
0.0
II Fractionation
971
1.48
1441
1802
Pump-3
5
0.05
100%
0.19
0.9
III Fractionation
997
1.37
1368
1710
Pump-4
5
0.08
100%
0.31
1.4
IV Fractionation
1034
0.71
732
915
Pump-5
5
0.00
100%
0.00
0.0
5291
Pump-6
7.5
8.00
100%
45.84
210.9
52.07
239.5
Particulars
Steam Cost (Rs)
Total Steam Cost per recovery batch (Rs)
Pump No. Pump-1
4.6 Rs/unit
Installed Duratio operating hp n (hrs) load 5 1.50 100%
4233
Power Power cons. hp Cost (Rs) 5.73 26.4
Cost due to Chilled water usage Cost of Chilled Water
Particulars
4.9 Rs/kg
Chilling Duration Load (TR) (hrs)
Total TR
Cost
(kgs)
(Rs)
Cost due to operation of Agitator
Agitator prime mover power Duration of operation
I Fractionation
125.7
0.72
90
443
Operating load
II Fractionation
127.0
1.48
189
924
Power consumption
III Fractionation
130.4
1.37
179
877
IV Fractionation
135.3
0.71
96
469
Total Chilling Cost per recovery batch (Rs)
Cost of operating agitator (Rs)
2714
Particulars
10.3 Rs/kg
Chilling Duration Load (TR) (hrs)
Total TR
Cost
(kgs)
(Rs)
I Fractionation
22.2
0.72
16
164
II Fractionation
22.4
1.48
33
343
III Fractionation
23.0
1.37
32
325
IV Fractionation
23.9
0.71
17
174
Total Chilling Cost per recovery batch (Rs)
1007
Cost saving due to Solvent recovery
Particulars
Rec. Sol
Rate
Savings
Kgs
Rs/kg
(Rs)
Utilization
I Fractionation
194.2
18
3,495 Substitute for Incinerator fuel
II Fractionation
228.8
18
4,119 Substitute for Incinerator fuel
III Fractionation
118.6
15
1,780 make up for brine solution
IV Fractionation
43.8
8
Total Saving (Rs/batch)
351 will be sold as spent solvent 9,745
Cost advantage due to recovery (Rs/distillation batch) Savings due to solvent recovery (Rs/Annum)
10 hrs 100% 96 units 439 148
Cost due to Chilled brine usage Cost of Chilled brine
12.5 hp
54 8,215
