II. Fluid properties at calorific temperature

Viscosity:

76 °API gasoline, μ_g =0.2cp (0.484 lb.ft ^-1.h^-1 )

46 °API kerosene, μ_k =1.6 cp (3.872 lb.ft^-1.h^-1 )

Density:

ρ_g =685 kg.m^-3 (42.7 lb.ft^-3 )

ρ_k =800 kg.m^-3 (49.8 lb.ft^-3 )

Thermal conductivity:

k_g =0.075 Btu h^-1 ft^-1 °F^-1

k_k=0.083 Btu h^-1 ft^-1 °F^-1

Specific heat capacity:

C_g = 0.57 Btu lb^-1 ft^-1

C_k = 0.48 Btu lb^-1 ft^-1

Specific gravity:

S_g = 0.685

S_k = 0.80

III. Energy balance

Type heat exchanger: Assume no heat loss to the surrounding

=3240000 Btu/h

⇒150000×0.48×(120-75)= ×0.57×(160-120)

⇒ = 142105 lb h^-1

IV. Calculation of heat transfer area and tube numbers

Iteration #1:

The first iteration is started assuming 1 shell pass and 2 tube passes shell and tube exchanger with following dimensions and considerations.

• 1'' OD tubes ( d_o) (14 BWG) on 1¼'' square pitch ( P T )

• Outer diameter of tube= 1''

• Tube length ( L_t)=16'

• Tube ID ( d_i ) = 0.834''

• Fluid arrangement: Kerosene is placed in tube side because it has the higher fouling tendency

The log mean temperature correction factor (F_T) for 1-2 shell and tube exchanger :

where, ;

= 42.75°F