ALIRAN FLUIDA - LAMPIRAN
10
LAMPIRAN a. Perhitungan T outlet pada kondisi mula-mula Inlet Large a) Bilangan Reynold Re = Dvρ μ = 0 , 1016 m 0,4 m / s 1000 kgm −3 0 , 0008 kg / ms =50800 b) Bilangan Prandl Pr = Cpμ k ¿ 4216 J/ kgK 0 , 0008 kg / ms 0 , 677 W / mK ¿ 4 , 982 c) Bilangan Nusselt Nu=0 , 023Re d 0,8 Pr n ¿ 0 , 023 ( 50800 ) 0,8 ( 4 , 982 ) 0,4 =254 , 198 d) Menghitung koefisien transfer panas (h) Nu = hd k h = Nu k d h inletl arge = 254 , 198 × 0 , 677 W / m . K 0 , 1016 m h inletl arge = 1693 , 819 W / m 2 . K Inlet Small a) bilangan Reynold
-
Upload
adha-ningrum -
Category
Documents
-
view
215 -
download
0
description
Laporan praktikum aliran fluida
Transcript of ALIRAN FLUIDA - LAMPIRAN
LAMPIRAN
a. Perhitungan T outlet pada kondisi mula-mula
Inlet Largea) Bilangan Reynold
Re =Dv ρ
μ
=0 ,1016m 0,4 m/ s 1000kgm−3
0 ,0008 kg/ms=50800
b) Bilangan Prandl
Pr=Cpμk
¿4216 J /kgK 0 ,0008kg /ms0 ,677W /mK
¿4 ,982c) Bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(50800 )0,8( 4 ,982)0,4
=254 ,198d)
Menghitung koefisien transfer panas (h)
Nu=h dk
h = Nu kd
hinletl arg e =254 ,198 × 0 ,677 W /m .K0 ,1016 m
hinletl arg e = 1693 ,819 W /m2 .K
Inlet Smalla) bilangan Reynold
Re
=Dv ρμ
=0 ,0254m 1,2m /s 1000kgm−3
0 ,0008kg /ms=38100
b)
Bilangan Prandtl
Pr=Cpμk
¿4216 J /kgK 0 ,0008kg /ms0 ,677W /mK
¿4 ,982c)
bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(38100 )0,8( 4 ,982 )0,3
=172 ,064d)
Menghitung koefisien transfer panas (h)
Nu=h dk
h = Nu kd
hinletsmall =172 ,064 × 0 ,677 W /m .K0 ,0254 m
hinletsmall = 4586 ,12 W /m2 .K
Menghitung Toutlet dengan persamaan neraca panas
Q1 = Q2
h inletlarg e . A dT inletl arg e = hinletsmall A dT inletsmall
h inletlarg e π d inletlarg e . L (T out−T inlelarg e )= hinletsmall π d inletsmall L (T inletsmall−T out )(1693 ,819W /m2 .K × 0 ,1016 m × (T out−293 ,15 )K ) =(4586 ,12W /m2. K × 0 ,0254 m × (313 ,15−T out )K )(172 ,092T out ) −(50448 ,77 ) = (36478 ,044−116 ,487T out )
288 ,579 T out = 86926 ,814T out = 301 ,224 K
b.Perhitungan T outlet saat T hotfluid menjadi 675 K
Inlet Large
Inlet Largee) Bilangan Reynold
Re =Dv ρ
μ
=0 ,1016m 0,4 m/ s 1000kgm−3
0 ,0008 kg/ms=50800
f) Bilangan Prandl
Pr=Cpμk
¿4216 J /kgK 0 ,0008kg /ms0 ,677W /mK
¿4 ,982g) Bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(50800 )0,8( 4 ,982)0,4
=254 ,198h)
Menghitung koefisien transfer panas (h)
Nu=h dk
h = Nu kd
hinletl arg e =254 ,198 × 0 ,677 W /m .K0 ,1016 m
hinletl arg e = 1693 ,819 W /m2 .K
Maka:
Q1
L=hπ d (Tout−Tinlarge)
Q1
L=1693,819 x 3,14 x0,1016 (Tout−293,15 )
Q1=305,949Tout−89689,205
Inlet Smalla) bilangan Reynold
Re
=Dv ρμ
=0 ,0254m 1,2m /s 1000kgm−3
0 ,0008kg /ms=38100
b)
Bilangan Prandtl
Pr=Cpμk
¿4216 J /kgK 0 ,0008kg /ms0 ,677W /mK
¿4 ,982c)
bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(38100 )0,8( 4 ,982 )0,3
=172 ,064
d)
Menghitung koefisien transfer panas (h)
Nu=h dk
h = Nu kd
hinletsmall =172 ,064 × 0 ,677 W /m .K0 ,0254 m
hinletsmall = 4586 ,12 W /m2 .K
Maka:
Q2
L=hπ d (Tinsmall−Tout )
Q2
L=4586,12 x3,14 x 0 ,0254 (675−Tout )
Q2=139788,83−207,0946Tout
Menghitung Toutlet dengan persamaan neraca panas
Q1 = Q2
hinletl arg e . A dT inletlarg e = hinletsmall A dT inletsmall
hinletl arg e π d inletlarg e . L (T out−T inlelarg e )= hinletsmall π d inletsmall L (T inletsmall−T out )305 ,949 T out−89689 ,205=139788 ,83−207 ,0946T out
513 ,0436 T out = 229478 ,035T out = 447 ,2875 K
c. Perhitungan T outlet pada saat turbulent intensity menjadi 27%
Inlet Largea) Bilangan Reynold
Re =Dv ρ
μ
=0 ,1016m 0,4 m/ s 1000kgm−3
0 ,0008 kg/ms=50800
b) Bilangan Prandl
Pr=Cpμk
¿4216 J /kgK 0 ,0008kg /ms0 ,677W /mK
¿4 ,982c) Bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(50800 )0,8( 4 ,982)0,4
=254 ,198d)
Menghitung koefisien transfer panas (h)
Nu=h dk
h = Nu kd
hinletl arg e =254 ,198 × 0 ,677 W /m .K0 ,1016 m
hinletl arg e = 1693 ,819 W /m2 .K
Inlet Smalle) bilangan Reynold
Re
=Dv ρμ
=0 ,0254m 1,2m /s 1000kgm−3
0 ,0008kg /ms=38100
f)
Bilangan Prandtl
Pr=Cpμk
¿4216 J /kgK 0 ,0008kg /ms0 ,677W /mK
¿4 ,982
g)
bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(38100 )0,8( 4 ,982 )0,3
=172 ,064h)
Menghitung koefisien transfer panas (h)
Nu=h dk
h = Nu kd
hinletsmall =172 ,064 × 0 ,677 W /m .K0 ,0254 m
hinletsmall = 4586 ,12 W /m2 .K
Menghitung Toutlet dengan persamaan neraca panas
Q1 = Q2
h inletlarg e . A dT inletl arg e = hinletsmall A dT inletsmall
h inletlarg e π d inletlarg e . L (T out−T inlelarg e )= hinletsmall π d inletsmall L (T inletsmall−T out )(1693 ,819W /m2 .K × 0 ,1016 m × (T out−293 ,15 )K ) =(4586 ,12W /m2. K × 0 ,0254 m × (313 ,15−T out )K )(172 ,092T out ) −(50448 ,77 ) = (36478 ,044−116 ,487T out )
288 ,579 T out = 86926 ,814T out = 301 ,224 K
d. Perhitungan T outlet pada kondisi mula-mula saat densitas dan viskositas menjadi
8000 kg/m3 dan 0,0072 kg/ms
Inlet Largea) bilangan Reynold
Re =Dv ρ
μ
=0 ,1016m 0,4m /s 8000kgm−3
0 ,0072kg /ms¿45155 ,56
b)
bilangan Prandtl
Pr=Cpμk
¿4216 J /kgK 0 ,0072kg /ms0 ,677W /mK
¿44 ,8378c)
bilangan Nusselt
Nu=0 ,023Red0,8 Prn
¿0 ,023( 45155 ,56 )0,8 (44 ,83781 )0,4
=557 ,3841
d)
Menghitung koefisien transfer panas (h)
Nu =h dk
h = Nu kd
hinletl arg e =557 ,3841 × 0 ,677 W /m . K0 ,1016 m
hinletl arg e = 3714 ,065 W /m2 . K
Maka:
Q1
L=hπ d (Tout−Tinlarge)
Q1
L=3714,065 x 3,14 x0,1016 (Tout−293,15 )
Q1=670,8614 Tout−196663,006
Inlet Small
a) bilangan Reynold
Re =Dv ρ
μ
=0 ,0254 m 0,4m / s 8000 kgm−3
0 ,0072 kg /ms¿33866 ,67
b)
bilangan Prandtl
Pr=Cpμk
¿4216 J /kgK 0 ,0072kg /ms0 ,677W /mK
¿44 ,8378c)
bilangan Nusselt
Nu=0 ,023 Red0,8 Prn
¿0 ,023(33866 ,67 )0,8( 44 ,83781 )0,4
=302 ,7186d)
Menghitung koefisien transfer panas (h)
Nu =h dk
h = Nu kd
hinletl arg e =302 ,7186 × 0 ,677 W /m . K0 ,0254 m
hinletl arg e = 8068 ,524 W /m2 . K
Maka:
Q2
L=hπ d (Tinsmall−Tout )
Q2
L=8068,524 x3,14 x 0,0254 (313,15−Tout )
Q2=114095,84−364,3488Tout
Menghitung Toutlet dengan persamaan neraca panas
Q1 = Q2
hinletl arg e . A dT inletlarg e = hinletsmall A dT inletsmall
hinletl arg e π d inletlarg e . L (T out−T inlelarg e )= hinletsmall π d inletsmall L (T inletsmall−T out )670 ,8614 T out−196663 ,006=114095 ,84−364 ,3488Tout
1035 ,2102 T out = 310758 ,8419T out = 300 ,189 K
