Page 111 - APPLIED PROCESS DESIGN FOR CHEMICAL AND PETROCHEMICAL PLANTS, Volume 1, 3rd Edition

Fluid Flow 95

Table 2-9
Brine Pipe Friction Multiples
For Use With Water Friction Data, Figure 2-24
I BRINE TEMPERATURE, °F
Specific
BRINE Gravity 0 10 20 30 40 50 60 70
1.10 ... 1.23 1.20 1.18 1.16 I 1.14 I 1.13 1.12
Sodium Chloride .. ............ 1.15 1.43 1.33 1.29 1.26 1.24 1.22 1.21 1.20
1.20 1.53 1.44 1.38 1.3!5 1.32 1.30 1.28 1.27
- -----
1.05 . . . ... 1.15 1.12 1.10 1.08 1.07 1.06
1.10 ... 1.28 1.23 1.20 1.18 1.16 1.14 1.12
1.15 1.41 1.35 1.31 1.28 1.25 1.22 1.21 1.20
Calcium Chloride ........... .. ---- . ..
1.20 1.49 l.43 1.39 1.36 1.33 1.30 1.28 1.27
1.25 1.56 1.53 1.49 1.45 1.42 1.40 1.38 1.37
1.30 1.65 1.61 1.58 1.55 1.52 1.50 1.49 1.48
I i I
-
NOTE: To find brine friction loss, multiply loss from Fig. 2-10 by multiplier from above Table.
By permission, Crocker, S., Piping Handbook, McGraw-Hill Book Co.

Charge Nquid
Gate valve Flow orifice
2 psi 2 psi Preheater Preheat er
1777 ''' ,777 10 psi 12 psi
Charge pump
22 psi

To vent control system

Head = 15 psi (static)

Dlattllation column Fired healer 85 psi
Figure 2-26. Establishing control valve estimated pressure drop.

Control valve pressure drop: properly estimating the valve pressure drop. From Shin-
sky [10),
�Pc= 0.05 Ps + 50 = 0.05 (192) + 50 = 59.6 psi
GPM = a'(c,') � PJSpG--;- (2- 66)
�
Use this as estimated control valve pressure drop for
the system design.
where a' = fractional opening of control valve, generally
assume 60% == 0.60
The Direct Design of a Control Vafoe C's, == standard valve coefficient from manufacturer's
catalog
This does not require the system balance as outlined in 6Pc = pre�sure drop across valve, psi
A through C above; however, without first preparing a SpGr = specific gravity of fluid, relative to water at
pressure balance, the designer cannot be confident of same temperature