This document summarizes a student project to produce 100 tons per year of 1-tetradecene. It outlines the goal, characteristics, manufacturing process, chemical reaction, mass and energy balances, design of equipment like heat exchangers and reactors, simulation results, and process economics. The overall feasibility study examines producing the unsaturated drying oil 1-tetradecene through acetylation of castor oil and determines the necessary feedstock, equipment, utilities, and costs to construct a plant capable of the desired annual production.

1. PRODUCTION OF
1-TETRADECENE
Project taken up by
Aman Kumar & Hazari Akash Khatri
Under the guidance of
Mr. D. Venkatesan

2. INTRODUCTION
 1-tetradecene is an unsaturated fatty oil which is
either natural or synthetic ,when it is applied as a
thin coating it absorb atmospheric oxygen and
polymerize forming a tough elastic layer.
 These oils harden and become completely dry after
being exposed to air over a period of time.

3.  To do a preliminary analysis to determine the
feasibility of constructing a chemical plant to
manufacture 100 tons/annum 1-Tetradecene.
GOAL

4. CHARACTERISTICS OF DRYING OIL:
Physical Characteristics:
 Boiling Point: 312°C at 760.0 mm Hg
 Melting Point: -12° C
 Specific Gravity: 0.96
 Water Solubility: less than 1 mg/ml at 20° C
 Flash Point: 230 ° C
 Density 0.95 g / cm3.
 Auto ignition Temperature: 550 ° C

5. Chemical Characteristics:
 Insoluble in water.
 Can develop heat spontaneously in the air.
 Reacts with acids to liberate heat along with
alcohols and acids.
 Flammable hydrogen is generated by mixing with
alkali metals and hydrides.

6. USES AND APPLICATION
 Paints:
 Automotive Industry.
 Industrial Appliances.
 Pigments.
 Varnishes:
 Protection.
 Highly inflammable.
 Polyurethane, epoxy.

7. Surfactants:
 Stability.
 Adhesive industry.
 Detergent and Soaps:
 Metallic soap.
 Presence of iodine.

8. MANUFACTURING
PROCESS
Processing & Refining of Oil
 ACO Heating.
 Reaction in reactor.
 Effluent quenching.
 Gum filtration.
 Distillation.
 Recycling.

9. CHEMICAL REACTION
Acetylated Castor Oil (ACO), (C16H32O2)
1-Tetradecene, (C14H28)
Acetic Acid (AA), (CH3COOH)
Gum, (C28H56)

10. 1-TETRADECENE PLANT
PROCESS FLOWSHEET
Vesse
l
Furnace
Reactor
Filter
Distillation
Column
Distillation
Column
j
cw
Vessel

11. MATERIAL BALANCE
C16H32O2 → CH3COOH + C14H28
(Acetylated castor oil) (acetic acid) (1-tetradecene)
2C14H28 → C28H56
(1-tetradecene) (1-octadecene)
Production rate = 100tonne/yr of 1-Tetradecene
= 12.6264 kg/hr
Feed required = 148.2228 tonne/yr (ACO)
= 18.715 kg/hr

12. VESSEL
Feed IN
ACO=18.52685 kg/hr
Recycle IN
ACO=2.05865 kg/hr
DO=0.128823 kg/hr
To Reactor OUT
ACO = 20.5865 kg/hr
DO = 0.128823
Total IN = Total OUT = 20.715323 kg/hr
MIXING VESSEL:

13. REACTOR
To Reactor IN
ACO = 20.5865 kg/hr
DO = 0.128823 kg/hr
To Filter
ACO = 2.05865 kg/hr
DO = 12.88278 kg/hr
GUM = 1.43142 kg/hr
AA = 4.34246 kg/hr
REACTOR:
Total IN = Total OUT = 20.71531 kg/hr

14. FILTER
To Filter IN
ACO = 2.05865 kg/hr.
DO = 12.88278 kg/hr.
GUM = 1.43142 kg/hr.
AA = 4.34246 kg/hr.
OUT To Recycle Column
ACO = 2.05865 kg/hr.
DO = 12.88278 kg/hr.
AA = 4.34246 kg/hr.
Gum OUT = 1.43142 kg/hr.
FILTER:
Total IN = Total OUT = 20.71531 kg/hr.

15. ACO RECYCLE COLUMN:
C
O
L
U
M
N
IN To Recycle Column
ACO = 2.05865 kg/hr.
DO = 12.88278 kg/hr.
AA = 4.34246 kg/hr.
Recycle OUT
ACO = 2.05865 kg/hr.
DO = 0.1288278 kg/hr.
OUT To Purification Column 2
AA = 4.34246 kg/hr.
DO = 12.75395 kg/hr.
Total IN = Total OUT = 19.28389 kg/hr.

16. C
O
L
U
M
N
IN To Distillation column 2
AA = 4.34246 kg/hr.
DO = 12.75395 kg/hr.
DO Purification Column:
Product OUT
AA = 4.2990 kg/hr.
DO = 0.127539 kg/hr.
Product OUT
DO = 12.6264 kg/hr.
AA = 0.04342 kg/hr.
Total IN = Total OUT = 17.09641 kg/hr.

17. OverallFeed IN
ACO= 18.52685 kg/hr.
AA = 4.2990 kg/hr.
DO = 0.127539 kg/hr.
DO = 12.6264 kg/hr.
AA = 0.04342 kg/hr.
Gum = 1.43142 kg/hr
OVERALL MASS BALANCE:
Feed IN = Feed OUT
ACO = AA + DO + GUM
18.52685 kg/hr. = 17.528 kg/hr.
BALANCED

18. ENERGY BALANCE
MIXING VESSEL:
VESSEL
FEED
Q = 10412.6593 kj/hr.
Recycle
Q = 2756.506 kj/hr.
OUT to Furnace
Q = 13491.84 kj/hr.
Heat Added
Q = 322.6795 kj/hr.
Total IN = Total OUT = 3491.84 kj/hr.

19. FURNACE
FURNACE:
IN from mixer
Q = 13491.84 kj/hr.
OUT to Reactor
Q = 44026.8397 kj/hr.
Heat added
Q = 30534.99 kj/hr.
Total IN = Total OUT = 44026.8397 kj/hr.

20. REACTOR:
REACTORIN from furnace
Q = 44026.8397 kj/hr.
OUT to Heat Exchanger
Q = 32648.92 kj/hr.
Heat Removed
Q = 11377.9165 kj/hr.
Total IN = Total OUT = 44026.8397 kj/hr.

21. HX 1
HEAT EXCHANGER
IN from Reactor
Q = 29329.679 kj/hr.
Heat removed
Q = 4030.661 kj/hr.
OUT to filter
Q = 25299.017 kj/hr.
Total IN = Total OUT = 29329.679 kj/hr.

22. FILTER:
FILTER
IN From HX1:
Q = 25298.7371 kj/hr.
OUT To Distillation Column:
Q = 23742.9952 kj/hr.
GUM
Q =1555.7426 kj/hr.
Total IN = Total OUT = 2598.7371 kj/hr.

23. ACO RECYCLE COLUMN:
C
O
L
U
M
N
IN from Filter
Q = 23748.9897 kj/hr.
OUT to Distillation column 2
Q = 18217.4713 kj/hr.
Recycle
Q = 4381.288 kj/hr.
Heat removed
Q = 1150.759 kj/hr.
Total IN = Total OUT = 23748.9897 kj/hr.

24. D.O. PURIFICATION COLUMN:
C
O
L
U
M
N
IN from column 1
Q = 18217.4713 kj/hr.
Product (AA 99%)
Q = 4546.98 kj/hr.
Product (DO 99%)
Q = 19738.013 kj/hr.
Heat Added
Q = 6067.526 kj/hr.
Total IN = Total OUT = 24284.998 kj/hr.

25. Heat Removed
Q=-1624.7752 kj/hr.
Heat exchanger 3:
Heat removed
Q = -11599.6613 kj/hr.
Heat exchanger 4:
Heat Removed
Q = -1820.8976 kj/hr.
Heat exchanger 5:
Heat Removed
Q = -803.3663 kj/hr.
.
Heat exchanger 2:

26. OVERALL energy BALANCE:
OverallFeed IN
Q = 10517.8377 kj/hr.
Product OUT -AA(99%)
Q = 2726.086 kj/hr
Product DO(99%)
Q = 8138.352 kj/hr.
GUM
Q = 752.3763 kj/hr.
Total IN = Total OUT = 10517.8377 kj/hr.
BALANCED

27. Heat Exchanger :
 Heat , Q = 4381.288 KJ/hr.
= 1.219 kW
 Logarithmic mean temp. diff. , ∆Tlm = 125.249°C
 Nu = hidi / ki = 3.66 {from O. Levenspiel, Engineering
Flow and Heat Exchange second edition, Equation
(9.23), p 177.}
 Heat transfer coeff. hi = 19.3 w/m2k
 Fouling factor = 500 w/m2k
 Overall heat transfer coeff. ,U = 18.528 W/m2.K
 Area , A = 0.1648 m2
 No. of tubes = 1.14 ≈ 1
DESIGN OF EQUIPMENTS:

28.  Pitch2 = π x ds2 /4 x n
 Ds = 0.1622 m
 Reactor:
 Plug flow reactor.
 PFR consideration L/D = 10m {from do12 ,author-
Joe Shaeiwitz, article no.- ChE 182 .}
 V = π(d2 /4)l
 Volume = 0.01968 m3 {from chemcad}
 Diameter = 0.1358 m
 Length = 1.358 m

29. CHEMCAD SIMULATION:

30. PHASE ENVELOPE:

31. Simulation: 1-tetradecene3A Date: 01/20/2015 Time: 00:08:43
FLOW SUMMARIES:
Stream No. 1 2 3 4
Temp C 25.0000* 44.5475 380.0000 242.4795
Pres kPa 110.0000* 230.0000 230.0000 183.0000
Enth MJ/h -59.847 -136.28 -116.01 -116.01
Vapor mole frac. 0.00000 0.00000 0.00000 0.73925
Total kmol/h 0.0723 0.2231 0.2231 0.2928
Total kg/h 18.5278 76.4422 76.4422 76.4421
Total std L m3/h 0.0210 0.0857 0.0857 0.0869
Total std V m3/h 1.62 5.00 5.00 6.56
Flowrates in kg/h
Acetic Acid 0.0000 0.0000 0.0000 4.3408
1-Tetradecene 0.0000 0.2131 0.2131 13.4095
Hexadecanoic Aci 18.5278 20.6044 20.6044 2.0691
1-octacosene 0.0000 55.6247 55.6247 56.6228
SIMULATION FLOW SUMMARIES:

32. Stream No. 5 6 7 8
Temp C 175.0000 175.0000 175.0000 344.0000
Pres kPa 148.0000 136.0000 136.0000 154.7495
Enth MJ/h -121.65 -122.81 -0.0069308 -76.432
Vapor mole frac. 0.35152 0.00000 0.00000 0.00000
Total kmol/h 0.2928 0.2928 0.0000 0.1533
Total kg/h 76.4421 76.4395 0.0027 58.9043
Total std L m3/h 0.0869 0.0869 0.0000 0.0658
Total std V m3/h 6.56 6.56 0.00 3.44
Flowrates in kg/h
Acetic Acid 4.3408 4.3402 0.0006 0.0000
1-Tetradecene 13.4095 13.4077 0.0018 0.2127
Hexadecanoic Aci 2.0691 2.0688 0.0003 2.0688
1-octacosene 56.6228 56.6228 0.0000 56.6228

33. Stream No. 9 10 11 12
Temp C 140.7126 125.9374 170.0000 252.0000
Pres kPa 136.0000 125.0000 129.7495 125.0000
Enth MJ/h -46.769 -31.630 -77.668 -11.265
Vapor mole frac. 0.00000 0.00000 0.00000 0.00000
Total kmol/h 0.1395 0.0715 0.1533 0.0680
Total kg/h 17.5352 4.2943 58.9043 13.2409
Total std L m3/h 0.0211 0.0041 0.0658 0.0170
Total std V m3/h 3.13 1.60 3.44 1.52
Flowrates in kg/h
Acetic Acid 4.3402 4.2943 0.0000 0.0458
1-Tetradecene 13.1950 0.0000 0.2127 13.1950
Hexadecanoic Aci 0.0000 0.0000 2.0688 0.0000
1-octacosene 0.0000 0.0000 56.6228 0.0000

34. Simulation: dryingoil Date: 01/19/2015 Time:
17:24:26
Overall Mass Balance kmol/h kg/h
Input Output Input Output
Acetic Acid 0.000 0.072 0.000 4.341
1-Tetradecene 0.000 0.067 0.000 13.197
Hexadecanoic Aci 0.072 0.000 18.528 0.000
1-octacosene 0.000 0.000 0.000 0.000
Total 0.072 0.139 18.528 17.538
Overall Energy Balance MJ/h
Input Output
Feed Streams -59.8468
Product Streams -51.529
Total Heating 36.478
Total Cooling -28.228
Power Added 0
Power Generated 0
Total -51.5962 -51.5293

35.  Total purchased cost (TPC) = 26.66 lacs
 Total Direct fixed cost (TDFC) = 22.331 lacs
 Total indirect fixed cost (TIFC) = 14.7845 lacs
 Working Capital (WC) = 5% of (TPC+TDFC+TIFC)
= 3.18878 lacs
 Total fixed cost investment (TFCI) = TPC+TDFC .
. +TIFC+WC
= 66.964 lacs
Variable cost:
 Direct production cost(DPC) = 88.9336 lacs
 Utilities (cooling water, fuel, electricity)=2.523 lacs
PROCESS ECONOMICS:

36.  Total operating cost(TOC) = 27.42 lacs
 Maintenance = 1.5 lacs
 Supervision & labour cost = 5% of TOC
= 1.371 lacs
Depreciation:
Plant life = 10 years
Salvage = 10% of TPC
= 2.66 lacs
Straight line depreciation = 2.399 lacs
Building = 3% of TFCI
= 0.9 lacs
TOTAL Depreciation = 2.489 lacs

37.  Local Tax = 3% of TFCI
= 2.01 lacs
 Insurance = 0.67 lacs
 Plant overhead = 50% of (TPC+Maintenance+ Supervision)
= 15.1455 lacs
General Expenses:
 Administrative Cost = 1.5 lacs
 Distribution & marketing cost = 100 lacs
 R&D cost (5% of TOC) = 1.371 lacs
TOTAL General cost = 102.861 lacs

38. Total Variable Cost (TVC) :
TVC = TDC + Utilities + Labour cost + Maintenance
+Supervision
= 121.7375 lacs
Total Investment = TVC + TFCI + Taxes
= 203.847 lacs
Product Value:
 Sales price(DO) = 101 Rs/kg
 Sales Price (AA) = 180 Rs/kg
 TOTAL Product Value = 162.9164 lacs

39. Profit before Tax = Total earning + TVC + Depreciation
= 43.6679 lacs
 TAX Rate = 40%
 Profit after TAX (PAT)= 26.2 lacs
 Pay Back Period = Total investment/PAT
= 7.78 years

40. PLANT LOCATION:
Requirements for selecting location:
 Available raw material at fare expenses.
 Cheap land.
 Lower installation cost.
 Transport.
 Availability of labour.
 Utilities like electricity,water, etc.
 Available Medical help.
 Favourable Climatic Condition.
PLANT LOCATION AND LAYOUT:

41. PLANT LAYOUT:
Economic Consideration:
 Construction and Operation cost.
 Process requirements.
 Convenience of operation.
 Maintenance.
 High safety.
 Future expansion.
 Modular construction.

43. Material safety data sheet:
1. Substance Name:
 1-TETRADECENE.
2. Chemical Nature:
 Low toxicity.
 Less soluble (at 20°C).
 Degrades in soil & water.
SAFetY & HEALTH ASPECTS:

44. 3. Possible Hazard:
 Animals:
o Skin Irritation on inhalation or dosage.
o High dosage cause kidney damage.
 Humans:
o Minimal concern on inhalation .
4. First aid measures:
 General advice: Move out of dangerous area.
 If inhaled: Keep patient calm, move to fresh air,
. summon medical help.
 On skin contact: Wash thoroughly with soap and
. . water.
 If swallowed: Keep respiratory tract clear. Do
. NOT induce vomiting.

45. 5. Fire fighting measures:
 Unsuitable extinguishing media:
 Use high volume water jet.
 Special protective equipment:
 Wear self contained breathing apparatus.
 Further information:
 Use extinguishing measures that are appropriate
to local circumstances.

46. REFERENCES
 Ashokan K., Chemical process calculation, lecture notes, 1st Edition,
Universities press India pvt. Ltd., 2008.
 Babu B.V., process plant simulation, 1st Edition, oxford university press,
2004.
 Bharat Bhatt I. and Shuchen Thakore B., Stoichiometry, 5th Edition, Tata
McGraw Hill, 2010.
 Deshmukh L.M., Industrial Safety Management, 3rd Edition, Tata
McGraw Hill, New Delhi, 2008.
 Gupta C.B., Management theory and practice, 14th Edition, Sultan
chand, sons, 2009.
 Levenspiel O., Chemical reaction Engineering, 3rd Edition, McGraw Hill,
1998.
 Luyben William L., Process Modeling Simulation and Control for
Chemical Engineers, 2nd Edition, McGraw Hill, 1990.
 Perry R.H., “Chemical Engineer” Handbook, 8th Edition, McGraw-Hill,
2008.
 Seader J.D., Henley Ernest J., Seperation process principles, 2nd
Edition, Wiley India pvt. Ltd., 2006.
 Smith J.M., Chemical kinetics and Reactor Design, 2nd Edition, McGraw
Hill, 2004.

47. THANK YOU