Base Case v Optimized Cost Breakdown:

	Base CAse	Optimized Case
Steam	$322,123	$0
Cooling Water	$803,235	$0
Fuel gas	$45,200	$45,200
Electricity	$2,986	$2,986
Total Utilities	$1,173,697	$856,457
Raw Materials
IPA	$13,440,000	$13,440,000
Process Water	$115	$115
Equipment	$1,135,000	$1,184,000
Waste Water	$205,296	$205,296
Labor Cost	$800,000	$800,000
Supervisor/Clerical	$144,000	$144,000
Maintenance	$68,100	$71,040
Supplies	$10,215	$10,656
Laboratory	$120,000	$120,000
Patents	$618,474	$607,033
Depreciation	$113,500	$118,400
Taxes and Insurance	$36,320	$37,888
Overhead	$607,260	$609,024
Administration	$151,815	$152,256
Selling Cost	$2,267,738	$2,225,786
Research	$1,030,790	$1,011,721
Cost of Manufacturing	$20,615,803	$20,234,417
Direct Manufacturing Cost	$16,579,897	$16,254,596
Fixed Manufacturing Cost	$757,080	$765,312
General Manufacturing Expense	$3,450,343	$3,389,763
Total	$20,787,320	$20,409,671

 

Calculations for Double Pipe Heat Exchanger

1. Q= WC(T₁-T₂)=wc(t₂-t₁)
2. LMTD= (T₁-t₂)-(T₂-t₁)

ln (T₁-t₂)/(T₂-t₁)

(3) a_p= p D²

4

4. G= W/a
5. Re= DG/m
6. j_H= (h_iD/k)(cm /k)^(-1/3) (m /m _w)^-0.14
7. h_io= h_i (ID/OD)
8. U= h_ioh_i/ (h_io+h_i)
9. A= Q/(UD t)

 

	Hot Side(annulus)	Cold Side(inner pipe)
W(kgmole/hr)	36.114	58.372
C (kJ/kgmole-c)	76.247	147.76
C (kJ/kg-c)	4.184567	3.209871
T1 ° C	102.0775	30.2667
T2 ° C	45	48.2883
Calculated Q (J/hr)	157167.7	155437.1
Tc ° C	73.53875	39.2775
LMTD	30.15987
Diameter(m)	0.2	0.15
Flow Area(m2)	0.031429	0.017679
Mole Velocity(kgmole/hr/m2)	1149.082	3301.851
Molecular Weight (kg/mole)	18.221	46.033
Mass Velocity(kg/hr/m2)	20937.42	151994.1
mu (viscosity) Cp	0.26824	1.345
mu(kg/m*hr)	0.964892	4.838129
Reynold's number	4339.847	4712.382
conversion from Cp to kg/m-hr	3.597122
k Thermal Cond (kJ/hr-m-k)	2.445156	0.893412
jh	40	50
ho, hi	578.0217	771.4391
hio		641.3168
U	304.0132
A (m2)	17.14121