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Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

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ECONOMICAL RECOVERY OF ETHYL ACETATE AND TETRAHYDROFURAN FROM THE PRODUCTION OF CEFUROXIME ACID V.RAGHUNATH 11707203026 N.SESHA GOPALAN 11707203038 TERNAL GUIDE : S.JENISHEXTERNAL GUIDE : SATI
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Page 1: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ECONOMICAL RECOVERY OF ETHYL ACETATE AND TETRAHYDROFURAN

FROM THE PRODUCTION OF CEFUROXIME ACID

V.RAGHUNATH 11707203026N.SESHA GOPALAN 11707203038

INTERNAL GUIDE : S.JENISH EXTERNAL GUIDE : SATISH

Page 2: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ABOUT ORCHID CHEMICALS & PHARMACEUTICALS LTD.• Orchid Chemicals & Pharmaceuticals Ltd (Orchid) was established

in 1992 as a 100% Export Oriented Unit (EOU). Commencing operations in 1994, Orchid has achieved amazing and consistent growth, quantitatively and qualitatively to emerge among the Top-15 companies in the Indian pharmaceutical industry in a short span of fifteen years of operations.

• Orchid has an established end-to-end connected infrastructure for drug discovery and development. Orchid has two manufacturing sites for APIs (at Alathur near Chennai and at Aurangabad, near Mumbai) and three manufacturing sites for Dosage forms (at Irungattukottai and Alathur in Chennai), besides a world-class R&D centre (at Sholinganallur, Chennai).

• In Alathur, Separation of complex solvent mixtures, residual from production processes, are done in order to get single high purity fractions to be reused or to be sold with economical benefit.

Page 3: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

Multipurpose solvent recovery plantMixture Pre-treatment plant

Page 4: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ABSTRACT

• Recovery of complex solvent mixtures in the production of pharmaceutical components is very complicated.

• This is due to the presence of TDS and solvents mixtures having the tendency to form azeotropes.

• Ethyl Acetate and TetraHydroFuran, are the by-products during the production of cefuroxime acid.

• The solvents are recycled & recovered in order to get single high purity fractions to be reused or to be sold with economical benefit.

• Several operations like distillation, flashing, dehydration are involved here.

• The percentage recovery & percentage loss for every operation involved is studied and estimated.

Page 5: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ETHYL ACETATE

• Ethyl acetate is the ester of ethanol and acetic acid; it is manufactured on a large scale for use as a solvent.

• CAS No: 141-78-6 • Properties Molecular formula : C4H8O2 • Molar mass : 88.105 g/mol • Appearance : colorless liquid • Density : 0.897 g/cm³, • Melting point : −83.6 °C, 190 K, -118 °F• Boiling point : 77.1 °C, 350 K, 171 °F• Solubility in water : 8.3 g/100 mL (20 °C)• Refractive index (nD) : 1.3720 • Viscosity : 0.426 cP at 25 °C• Vapour density: 3.04• Vapour pressure: 100 mm Hg at 27 C • Flash point: -4 C

Page 6: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

TETRAHYDROFURAN

• IUPAC name : Oxolane• CAS No.: 109-99-9 • Molecular formula : C4H8O • Molar mass : 72.11 g/mol • Appearance : colorless liquid • Density : 0.8892 g/cm3 (g/mL) @ 20 °C,• Melting point : −108.4 °C (164.75 K)• Boiling point : 66 °C (339.15 K)• Solubility in water Miscible Viscosity : 0.48 cP at 25 °C• Vapor Density (Air=1): 2.5 • Vapor Pressure (mm Hg): 129 @ 20C (68F) • Evaporation Rate (BuAc=1): 8.0 • Flash point : −14 °C

Page 7: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RECOVERY PROCESS

REMOVAL OF TDS EA AND THF ENRICHMENT RECOVERY OF EA RECOVERY OF THF

Page 8: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

PROCESS DESCRIPTION

• REMOVAL OF TDS FLASHING • EA AND THF ENRICHMENT DISTILLATION • RECOVERY OF EA

DEHYDRATION USING CaCl2 DISTILLATION (THF REMOVAL)• RECOVERY OF THF DISTILLATION (EA REMOVAL) DEHYDRATION USING NaOH DISTILLATION (ANHYDROUS THF RECOVERY)

Page 9: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

NOMENCLATURE

EA = Ethyl Acetate THF = Tetrahydrofuran OI = Other Impurities MC = Moisture Content F = Feed R = Residue T = Top Product B = Bottom Product V = Vent CaCl2 = Calcium Chloride CAS = Chemical Abstract Service

Page 10: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

MASS BALANCE

Page 11: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

STUDY Calculation of amount of Feed, Top product, Bottom

Product/Residue in every operation. Analysis of Composition of the above, in terms of Percentage. The major components to be separated are Ethyl Acetete &

TetraHydroFuran and other components are termed as Other Impurities.

The composition is analysed through chromatography, The peak value is noted.

The amount of EA, THF, OI & MC in Feed, Top product, Bottom Product/Residue in every operation is calculated.

Loss in flashing/dehydration is mainly by residue. Loss in distillation is mainly attributed to loss by vent owing

to the fact that the column is closed & continuous. The percentage recovery of THF & EA for every process is

calculated The percentage loss of THF & EA for every process is

calculated

Page 12: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

TDS REMOVAL

FLASHING

TOP TEMP.=80 OC

BOTTOM TEMP.=100 OC

TOP PRODUCT = 7150 LEA = 52 %THF = 43.5 %OI = 4.5 %MC = 4 %MOTHER LIQUOR = 7530 L

EA = 51 %THF = 43 %OI = 6 %MC = 4 %

RESIDUE = 380 L

Page 13: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

MASS BALANCEF = T + RFxf = Txt + Rxr

% of EA in Residue :7530*(51/100) = 7150*(52/100) + 380*(x/100)3840.3 = 3718 + 3.8xx = 32.18%

% of THF in residue :7530*(43/100) = 7150*(43.5/100) + 380*(x/100)3237.9 = 3110.25 + 3.8xx = 33.59%

% of OI in residue :7530*(6/100) = 7150*(4.5/100) + 380*(x/100)451.80 = 321.75 + 3.8xx = 34.22%

Page 14: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTEA THF OI MC

MOTHER LIQUOR ( FEED)

3840.30 3237.9 451.80 301.20

TOP PRODUCT 3718 3110.25 321.75 286

RESIDUE 122.3 127.65 130.35 15.2

Percentage of recovery of EA = ((3718/3840.3)*100) = 96.8%Percentage of recovery of THF = ((3110.25/3237.9)*100) = 96.05%

Percentage of loss of EA in residue = ((122.3/3840.3)*100) = 3.18%Percentage of loss of THF in residue = ((127.65/3237.9)*100) = 3.94%

Page 15: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA AND THF ENRICHMENT

CONTINOUS COLUMN

TOP TEMP.=64.5 OCBOTTOM

TEMP.=70OC

TOP PRODUCT = 2281.25 LEA = 3.5 %THF = 92.65 %OI = 3.85 %MC = 4 %

BOTTOM PRODUCT = 4372.91 LEA = 78 %THF = 19.2 %OI = 2.8 %MC = 3.6 %

FEED = 7150 LEA = 52 %THF = 43.5 %OI = 4.5%MC = 4 %

Page 16: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

MASS BALANCEF = T + B + VFxf = Txt + Bxb + Vxv

% of EA lost by vent7150*(52/100) = 2281.5*(3.5/100)+4372.91*(78/100) +

495.86*(x/100)x = 45.889%

% of THF lost by vent7150*(43.5/100) = 2281.5*(92.65/100)+4372.91*(19.2/100) +

495.86*(x/100)x = 31.622%

% of OI lost by vent7150*(4.5/100) = 2281.5*(3.85/100)+4372.91*(2.8/100) +

495.86*(x/100)x = 22.484%

Page 17: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTEA THF OI MC

FEED 3718 3110.25 321.75 286

TOP PRODUCT 79.84 2113.57 87.82 91.25

BOTTOM PRODUCT 3410.61 839.85 122.44 157.42

VENT 227.55 156.83 111.49 37.33

Percentage of recovery of EA = ((3490.45/3718)*100) = 93.83%Percentage of recovery of THF = ((2953.16/3110.25)*100) = 94.94%

Percentage of loss of EA by vent = ((227.55/3718)*100) = 6.12%Percentage of loss of THF by vent = ((157.09/3110.25)*100) = 5.05%

Page 18: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA ENRICHMENT

Page 19: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RECOVERY OF ETHYL ACETATE DEHYDRATION USING CACL2

DEHYDRATION USING CaCl2

PRODUCT = 8950 LEA = 80 %THF = 15.2 %OI = 4.8 %MC = 1.35 %

RESIDUE = 549.35 L + 415.65 L (MC)

FEED = 9500 L + 532 L (MC)CACL2 = 390 LEA = 78.5 %THF = 1.15 %OI = 6.8%MC = 5.6 %

Page 20: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

MASS BALANCEF = T + RFxf = Txt + Rxr

% of EA in Residue :9500*(78.2/100) = 8950*(80/100) + 549.35*(x/100)7429 = 7160 + 5.49xx = 48.99%

% of THF in residue :9500*(1.15/100) = 8950*(15.2/100) + 549.35*(x/100)1425 = 1360.4 + 5.49xx = 11.76%

% of OI in residue :9500*(6.8/100) = 8950*(4.8/100) + 549.35*(x/100)646 = 429.6 + 5.49xx = 39.415%

Page 21: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA THF OI MC

FEED 7429 1425 646 532

PRODUCT 7160 1360.4 429.6 116.35

RESIDUE 269 64.6 216.4 415.65

RESULT

Percentage of recovery of EA = ((7160/7429)*100) = 96.37%

Percentage of loss of EA in residue = ((269/7429)*100) = 3.62%

Page 22: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RECOVERY OF ETHYL ACETATE DISTILLATION (THF REMOVAL)

DISTILLATION COLUMN

TOP TEMP.=64.5 OC

BOTTOM TEMP.=70.4 OC

TOP PRODUCT = 1691 L + 40.58 (MC) LEA = 7.1 %THF = 78.5 %OI = 14.4 %MC = 2.4 %

BOTTOM PRODUCT = 6809 L + 7.48 (MC) LEA = 99.46 %THF = 0.20 %OI = 0.33 %MC = 0.11 %

FEED = 8950 L + 116.35 (MC) LEA = 80 %THF = 15.2 %OI = 4.8%MC = 1.35 %

Page 23: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

MASS BALANCEF = T + B + VFxf = Txt + Bxb + Vxv

% of EA lost by vent8950*(80/100) = 1691*(7.1/100)+6809*(99.46/100) + 450.71*(x/100)x = 59.39%

% of THF lost by vent8950*(15.2/100) = 1691*(78.5/100)+6809*(19.2/100) + 450.71

*(x/100)x = 4.29%

% of OI lost by vent8950*(4.8/100) = 1691*(14.4/100)+6809*(0.33/100) + 450.71*(x/100)x = 36.30%

Page 24: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULT

EA THF OI MC

FEED 7160 1360.4 429.6 116.35

TOP PRODUCT 120.06 1327.43 243.5 40.5

BOTTOM PRODUCT 6772.23 13.61 22.46 7.48

VENT 267.71 19.36 163.34 68.37

Percentage of recovery of EA = ((6892.29/7160)*100) = 96.26%

Percentage of loss of EA = ((267.71/7160)*100) = 3.73%

Page 25: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

THF ENRICHMENT

Page 26: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RECOVERY OF TETRAHYDROFURAN DISTILLATION - (EA REMOVAL)

DISTILLATION COLUMN

TOP TEMP.=64OC

BOTTOM TEMP.=70OC

BOTTOM PRODUCT = 4030 LEA = 8.17 %THF = 89.80 %OI = 2.03 %MC = 3.5 %

TOP PRODUCT = 12660 LEA = 0.02 %THF = 99.28 %OI = 0.7 %MC = 5 %

FEED = 17593 LEA = 2.13 %THF = 96.76 %OI = 1.11 %MC = 6.3 %

Page 27: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

F = T + B + VFxf = Txt + Bxb + Vxv

% of EA lost by vent17593*(2.13/100) = 12600*(0.02/100)+4030*(8.17/100) +

902.03*(x/100)x = 59.39%

% of THF lost by vent17593*(96.76/100) = 12600*(99.28/100)+4030*(89.80/100) +

902.03*(x/100)x = 92.48%

% of OI lost by vent17593*(1.11/100) = 12600*(0.7/100)+4030*(2.03/100) +

902.03*(x/100)x = 2.75%

MASS BALANCE

Page 28: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULT

EA THF OI MC

FEED 374.73 17022 195.28 1108.359

TOP PRODUCT 2.53 12568.84 88.62 633

BOTTOM PRODUCT 329.25 3618.94 81.80 141.05

VENT 42.95 834.22 24.86 334.309

Percentage of recovery of THF= ((16187.78/17022)*100) = 95.09%

Percentage of loss of THF = ((834.22/17022)*100) = 4.9%

Page 29: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RECOVERY OF TETRAHYDROFURAN DEHYDRATION USING CAUSTICS

DEHYDRATION USING

CAUSTICS FLAKES

RESIDUE = 500.61 L

FEED = 12660 LEA = 0.035 %THF = 99.28 %OI = 0.69 %MC = 4 %

TOP PRODUCT = 12160 LEA = 0.02 %THF = 99.33 %OI = 0.45 %MC = 0.25 %

Page 30: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

F = T + RFxf = Txt + Rxr

% of EA in Residue :12660*(0.035/100) = 12160*(0.02/100) + 500.61*(x/100)4.43 = 2.43 + 5.00xx = 0.4%

% of THF in residue :12660*(0.035/100) = 12160*(0.02/100) + 500.61*(x/100) 12568.8 = 12078.5 + 5.00xx = 98.06%

% of OI in residue :12660*(0.035/100) = 12160*(0.02/100) + 500.61*(x/100) 87.35 = 79.04 + 5.00xx = 1.662%

MASS BALANCE

Page 31: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTEA THF OI MC

FEED 374.73 17022 195.28 1108.359

TOP PRODUCT 2.53 12568.84 88.62 633

BOTTOM PRODUCT 329.25 3618.94 81.80 141.05

Percentage of recovery of THF= ((12078.5/12660)*100) = 96.09%

Percentage of loss of THF = ((490.3/12660)*100) = 3.9%

Page 32: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RECOVERY OF TETRAHYDROFURAN DISTILLATION (THF RECOVERY)

TOP PRODUCT = 575.42 LEA = 0.1 %THF = 96.2 %OI = 0.7 %MC = 3.4%

BOTTOM PRODUCT = 7200 L (ANHYDROUS THF)EA = 0.017 %THF = 99.74 %OI = 0.243 %MC = 0.04 %

DISTILLATION COLUMN

TOP TEMP.=63OC

BOTTOM TEMP.=68OC

FEED = 8165.4 LEA = 0.02 %THF = 99.33 %OI = 0.65 %MC = 0.5 %

Page 33: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

F = T + B + VFxf = Txt + Bxb + Vxv

% of EA lost by vent8165.1*(0.02/100) = 575.42*(0.1/100)+7200*(0.017/100) +

407.73*(x/100)x = 0.076%

% of THF lost by vent8165.1*(99.3/100) = 575.42*(96.2/100)+7200*(99.74/100) +

407.73*(x/100)x = 92.18%

% of OI lost by vent8165.1*(0.65/100) = 575.42*(0.7/100)+7200*(0.243/100) +

407.73*(x/100)x = 7.7389%

MASS BALANCE

Page 34: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULT

EA THF OI MC

FEED 1.63 8110.69 53.07 40.82

BOTTOM PRODUCT 1.224 7181.28 17.496 19.56

TOP PRODUCT 0.09 553.55 4.02 2.88

Percentage of recovery of THF= ((7734.83/8110.69)*100) = 95.36%

Percentage of loss of THF = ((375.86/8110.69)*100) = 4.6%

Page 35: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCE

Page 36: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

STUDY Calculation of amount of Feed, Top product, Bottom

Product/Residue in every operation. Analysis of Composition of the above, in terms of

Percentage. The energy supplied initially calculated. The energy out with the product is also calculated. The difference between the energy in and energy

out is the energy lost. Energy loss is due to 3 reasons Barebody losses,

Insulation losses, Natural condensation.

Page 37: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

TDS REMOVAL

TOP TEMP = 83.2 C

BOTTOM TEMP =

84.5

84.5 - 35

83.2 - 55

83.2 - 50

6969.76 Kg

EA - 51% = 3417.86THF - 43% = 2881.73MC - 4% = 301.20

EA - 52% = 2987.4THF - 43.5% = 2499.1MC - 4% = 239.38

EA - 52% = 341.3THF - 43.5% = 285.51MC - 4% = 38.59

Page 38: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCEmλ+mCpΔT

ENERGY IN:

Qf = (6294.59*0.5*49.5) + (3417.86*87.6) + (2881.73*98) + (268.068*19.5) + (268.08*540)

Qf = 895755.014 KCal

ENERGY OUT:

Qc1 = (5486.5*0.5*28.2) + (2987.4*87.6) + (2499.1*98) + (239.38*28) + (239.38*540)

Qc1 = 719983.406 KCal

Qc2 = (626.81*0.5*33.2) + (341.30*87.6) + (285.51*98) + (38.54*33.2) + (38.54*540)

Qc2 = 90402.64 KCal

Qc1 +Qc2 = 810386.1 KCal

Page 39: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTQf – (Qc1 + Qc2) = 85368.91 Kcal

The net loss in flashing stage is 85368.91 Kcal

Page 40: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA – THF ENRICHMENT

TOP TEMP.=64.5 OC

CONTINOUS COLUMN

BOTTOM TEMP.=70OC

77.8 - 35

78 -

55

79 -

77

55 -

35

64 - 55

64 - 50

Page 41: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCEmλ+mCpΔT

ENERGY IN:

Qf = (1152*0.5*42.8) + (599.04*87.6) + (501.12*98) + (48*1*42.8) + (48*540)

Qf = 154170.6 KCal

Qr = (4369.92*0.5*7.2) + (152.32*87.6) + (4048.7*98) + (182.08*7.2) + (182.08*540)

Qr = 525449.32 Kcal

Qi = Qf+ Qr = 679619.38 KCal

Page 42: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCE

ENERGY OUT:

Qc1 = (4320*0.5*9) + (151.5*87.6) + (4002.4*98) + (180*9) + (180*540)

Qc1 = 523740.3 KCal

Qc2 = (480*0.5*14) + (16.8*87.6) + (444.72*98) + (120*14) + (120*540)

Qc2 = 59494.24 KCal

Qc3 = (430.08*0.5*20) + (17.92*20)

Qc3 = 8960 KCal

Qphe = (966*0.5*23) + (36.072*23)

Qphe = 11938.6 KCal

Qo = Qc1 +Qc2 +Qc3 +Qphe = 604133.196 KCal

Page 43: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTQi – Qo = 75486.184 Kcal

The net loss in EA & THF enrichment is 75486.184 Kcal

Page 44: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA ENRICHMENT

Page 45: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

THF REMOVAL

TOP TEMP.=68 OC

CONTINOUS COLUMN

BOTTOM TEMP.=80OC

78 - 35

80 -

55

80 -

72

55 -

35

68 - 55

68 - 50

Page 46: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCEmλ+mCpΔT

ENERGY IN:

Qf = (1183*0.5*43) + (947.4*87.6) + (179.93*98) + (16.2*43) + (116.2*540)

Qf = 135521.68 KCal

Qr = (4694.56*0.5*8) + (333.31*87.6) + (3685.22*98) + (115.44*8) + (115.44*540)

Qr = 472388.876 Kcal

Qi = Qf+ Qr = 607910.566 KCal

Page 47: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCE

ENERGY OUT:

Qc1 = (4392*0.5*13) + (311.8*87.6) + (3447.92*98) + (1108*1*13) + (108*540)

Qc1 = 453462.24 KCal

Qc2 = (448*0.5*18) + (34.64*87.6) + (351.68*98) + (12*18) + (12*540)

Qc2 = 48227.10 KCal

Qc3 = (185.44*0.5*20) + (4.56*20)

Qc3 = 1945.6 KCal

Qphe = (2746.98*0.5*25) + (3.02*25)

Qphe = 34412.75 KCal

Qo = Qc1 +Qc2 +Qc3 +Qphe = 538047.69 KCal

Page 48: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTQi – Qo = 69862.56 Kcal

The net loss in THF removal is 69862.56 Kcal

Page 49: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

THF ENRICHMENT

Page 50: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA REMOVAL

TOP TEMP.=63.5 OC

CONTINOUS COLUMN

BOTTOM TEMP.=69.2OC

71 - 35

69.2 - 55

71 -

63

55 -

35

63.8 - 55

68.3 - 50

Page 51: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCEmλ+mCpΔT

ENERGY IN:

Qf = (1124.4*0.5*36) + (23.94*87.6) + (1087.96*98) + (75.6*43) + (75.6*540)

Qf = 172426.42 KCal

Qr = (3800*0.5*8) + (76*87.6) + (3772.64*98) + (200*8) + (200*540)

Qr = 494585.2 Kcal

Qi = Qf+ Qr = 667011.716 KCal

Page 52: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCE

ENERGY OUT:

Qc1 = (4275*0.5*8.8) + (0.85*87.6) + (4244.22*98) + (225*8.8) + (225*540)

Qc1 = 558078.02 KCal

Qc2 = (475*0.5*13.8) + (0.09*87.6) + (471.58*98) + (25*13.8) + (25*540)

Qc2 = 63345.224 KCal

Qc3 = (950*0.5*20) + (50*20)

Qc3 = 10500 KCal

Qphe = (579*0.5*14.2) + (21*14.2)

Qphe = 4409.1 KCal

Qo = Qc1 +Qc2 +Qc3 +Qphe = 636332.34 KCal

Page 53: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTQi – Qo = 30679.370 Kcal

The net loss in THF removal is 30679.370Kcal

Page 54: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ANHYDROUS THF RECOVERY

TOP TEMP.=65.3 OC

CONTINOUS COLUMN

BOTTOM TEMP.=70OC

66 - 35

70 - 55

78 -

63

55 -

35

65.33 - 55

65.33 - 50

Page 55: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCEmλ+mCpΔT

ENERGY IN:

Qf = (1194*0.5*31) + (0.23*87.6) + (1186*98) + (6*31) + (6*540)

Qf = 138181.1 KCal

Qr = (3960*0.5*8) + (3.96*87.6) + (3812.07*98) + (139.4*8) + (139.4*540)

Qr = 466163.356 Kcal

Qi = Qf+ Qr = 604344.456 KCal

Page 56: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ENERGY BALANCE

ENERGY OUT:

Qc1 = (4347*0.5*10.3) + (4181.81*98) + (4.37*87.6) + (153*10.3) + (153*540)

Qc1 = 516780.5 KCal

Qc2 = (483*0.5*15.3) + (464.64*98) + (1.48*87.6) + (17*540) + (17*15.3)

Qc2 = 58711.8 KCal

Qc3 = (72.45*0.5*20) + (2.55*20)

Qc3 = 775.5 KCal

Qphe = (1199.28*0.5*15) + (0.72*15)

Qphe = 9005.4 KCal

Qo = Qc1 +Qc2 +Qc3 +Qphe = 585273.2 KCal

Page 57: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

RESULTQi – Qo = 19071.2 Kcal

The net loss in THF removal is 19071.2 KCal

Page 58: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

POWER CONSUMPTION

Page 59: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

STUDY Power consumption in the recovery process is

mainly due to the usage of agitator in the flashing and dehydration process.

The power consumed is determined by finding the capacity of the motor used for agitation.

From the motor capacity, the power consumed for the specific batch is found out.

Page 60: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

REMOVAL OF TDS Motor capacity = 22 KW Motor error = 0.75 Batch timing = 10 Hrs Cost per unit = 4.12 Rs.

22 KW * 0.75 = 16.5 KW

Batch Timing = 10 Hr

16.5*10 = 165 KW/Hr

Cost = 165 * 4.12

Cost = 679.8 Rs.

Page 61: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

CACL2 DEHYDRATION Motor capacity = 22 KW Motor error = 0.75 Batch timing = 10 Hrs Cost per unit = 4.12 Rs.

22 KW * 0.75 = 16.5 KW

Batch Timing = 10 Hr

16.5*10 = 165 KW/Hr

Cost = 165 * 4.12

Cost = 679.8 Rs.

Page 62: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

NAOH DEHYDRATION Motor capacity = 22 KW Motor error = 0.75 Batch timing = 15 Hrs Cost per unit = 4.12 Rs.

22 KW * 0.75 = 16.5 KW

Batch Timing = 15 Hr

16.5*15 = 247.5 KW/Hr

Cost = 247.5 * 4.12

Cost = 1019.7 Rs.

Page 63: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

COST ESTIMATION

Page 64: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

STUDY The cost is estimated by evaluating the cost

of steam, cooling water and power consumed by the agitator.

The cost incurred by every process is studied.

The cost of all the process is evaluated to find the money spent for the entire recovery process per batch.

Page 65: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

TDS REMOVAL Mass of steam = 1658.8 Kg Cold water (condensor 1) = 238.08 Kg Cold water (condensor 2) = 29.89 Kg

Cost of steam = 1658.8 * 1.160.6 = 1925.2032 RsCold water (condensor 1) = 238.08 * 9.6 = 2285.65

Rs.Cold water (condensor 2) = 29.89 * 0.96 = 28.694 Rs.

Power consumed = 679.8 Rs.

Total cost = 4919.3472 Rs.

Page 66: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA & THF ENRICHMENT Mass of steam = 1260 Kg Cold water (condensor 1) = 180.10 Kg Cold water (condensor 2) = 19.67 Kg

Cost of steam = 1260 * 1.1606 = 1496.4 RsCold water (condensor 1) = 180.10 * 9.6 =

1728.96 Rs.Cold water (condensor 2) = 19.67 * 0.96 =

18.8832 Rs.

Total cost = 3244.2432 Rs.

Page 67: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA ENRICHMENT

Page 68: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

CACL2 DEHYDRATION

Power consumption cost= 679.8 Rs.

Total Cost = 679.8 Rs.

Page 69: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

THF REMOVAL Mass of steam = 1125 Kg Cold water (condensor 1) = 161.9 Kg Cold water (condensor 2) = 15.94 Kg

Cost of steam = 1125 * 1.1606 = 1305.675 RsCold water (condensor 1) = 161.9 * 9.6 =

1554.24 Rs.Cold water (condensor 2) = 15.94 * 0.96 =

15.3024 Rs.

Total cost = 2875.22 Rs.

Page 70: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

THF ENRICHMENT

Page 71: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

EA REMOVAL Mass of steam = 1250 Kg Cold water (condensor 1) = 189.47 Kg Cold water (condensor 2) = 20.94 Kg

Cost of steam = 1250 * 1.1606 = 1450.75 RsCold water (condensor 1) = 189.47 * 9.6 =

1818.912 Rs.Cold water (condensor 2) = 20.94 * 0.96 =

20.1024 Rs.

Total cost = 3289.76 Rs.

Page 72: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

NAOH DEHYDRATIONPower consumption Cost = 1019.7 Rs.

Total Cost = 1019.7 Rs.

Page 73: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

ANHYDROUS THF RECOVERY

Mass of steam = 1120 Kg Cold water (condensor 1) = 174.17 Kg Cold water (condensor 2) = 19.41 Kg

Cost of steam = 1120 * 1.1606 = 1299.87 Rs.Cold water (condensor 1) = 174.17 * 9.6 =

1672.032 Rs.Cold water (condensor 2) = 19.41 * 0.96 =

19.6336 Rs.

Total cost = 2991.536 Rs.

Page 74: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

TOTAL COSTPROCESS COST (Rs.)

FLASHING 4919.3472

EA & THF ENRICHMENT 3244.2432

CACL2 DEHYDRATION 679.8

THF REMOVAL 2875.22

EA REMOVAL 3289.76

NAOH DEHDYRATION 1019.7

ANHYDROUS THF REC. 2991.536

TOTAL 19019.6058

Page 75: Economical Recovery of Ethyl Acetate and Tetrahydrofuran From1

THANK YOU


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