Perhitungan : Fluida Panasm

T1 = 52oC = 125,6oF T3 = 47,8oC = 118,04oF Fluida Panasm

T6 = 24,8oC = 76,64oF T4 = 29,4oC = 84,92oF

Neraca PanasFluida Panas = Fluida dingin Fluida Panas

Trata-rata =

Interpolasi cp =

Q = m x cp x T =

Fluida dingin

Trata-rata =

Interpolasi cp =

W =

Dingin (oF)Panas (oF)Rata-Rata

84,92T.tinggi125,640,68T2

76,64T. rendah118,0441,4T1

-0,72T2-T1

TLMTD =

Perpindahan Panas pada Inner Pipe Flow area ( ap )D = 0,402 in = 0,0335 ftAp =

Kecepatan massaGp =

Bilangan Reynold = 0,6 x 2,42 = 1,452 Re, p =

Dari grafik didapat JH = 50Pada 121,82oF; Cp = 0,9994 ; k = 0,3725

hi = JH Viskositas dari fluida < 1 cp maka diasumsikan 1hi = 50 x hio = hi x

Perpindahan Panas pada Annulus Flow area ( aa )D2 = 0,75 in = 0,0625 ftD1 = 0,652 in = 0,0543 ftaa =

Diameter Ekivalen

De=

Kecepatan massaGp =

Bilangan Reynold = 0,94 x 2,42 = 2,2748

Re, a = Dari grafik didapat JH = 12Pada 80,78oF; Cp = 0,999 ; k = 0,3535 ho = JH ho = 12 x

Clean Overall Coefficient ( Uc )Uc=

Koefisien Panas Keseluruhan ( UD )

Rd = faktor pengotorDari tabel 12 modul perpindahan panas Rd=0,001 = 269,6128 = 0,3604

Pressure Drop pada Inner PipeRe,p = 13860,8939

f =

g = 32,174

Pressure Drop pada AnnulusDe = ( D2- D1) = ( 0,0625-0,0543)ft = 0,0082 ft

Rea =

Re < 2100 maka aliran laminer, pers. faktor gesekan :

f =

g = 32,174

= 0,1854 ft