Sentrifugasi

LAPORAN PRAKTIKUM OPERASI TEKNIK KIMIA-1
ROTARY DRUM VACUUM FILTER
OLEH:
POLITEKNIK NEGERI BANDUNG
D-IV TEKNIK KIMIA PRODUKSI BERSIH
2019
I.
TUJUAN PRAKTIKUM
Setelah melakukan praktikum ini, kami diharapkan dapat:
1. Memahami pengoperasian rotary drum filter, mulai dari prosedur start
up, operasi normal, sampai shut down.
2. Mengamati karakter proses operasi filtrasi kontinyu memakai alat rotary
drum filter.
3. Mendapatkan
hubungan
antar
variabel
yang
mempengaruhi
pengoperasian rotary drum filter dengan persamaan karakteristik yang
telah tersedia di literatur.
4. Mencari konstanta karakteristik untuk operasi ini dengan pengolahan
data praktikum.
II.
TABEL DATA PENGAMATAN
a. Kondisi Alat
-
Keliling drum (K) = 1,5857 m
-
Lebar screen (L): 40,4 cm = 0,404 m
-
Filter area = K x L = 0,641 m2
-
Panjang busur drum yang tercelup ke dalam slurry (K’) = 0,4857 m
-
Fraksi drum yang tercelup = K’/K = 0,4857 m/1,6014 m = 0,3063 m
-
Panjang dead zone (Ldz) = 0,14 m
-
Tekanan Operasi (-∆𝑃) = -0,8 bar = 80000 Pascal
-
1 cm tinggi filtrat (H filtrat) setara dengan volume filtrat (V) = 2,28
Liter = 2,28 x 10-3 m3
b. Hubungan antara Volume Filtrat dengan Time Cycle
Run
1
2
3
4
5
Skala
10
20
30
40
50
Periode
19,4
17,6
27,28
27,3
27,1
Nomor
H Filtrat
Data
(m)
1
0
0
20,13
14,46
5,87
17,11
28,07
2
0,02
4,56 x 10-3
24,84
41,47
17,36
36,13
62,63
3
0,04
9,12 x 10-3
27,84
70,45
36,23
50,59
84,60
4
0,06
13,68 x 10-3
37,84
92,9
63,69
65.65
108,14
5
0,08
18,24 x 10-3
65,84
178,55
89,68
82,69
68,89
6
0,1
22,8 x 10-3
68,84
141
114,22
99,36
147,66
V filtrat (m)
Waktu Pengisian Tangki Filtrat (S)
Rata-rata
c. Hubungan antara Tebal Cake dengan Periode Putaran
RUN
Waktu pelepasan
cake pada detik ke-
1
2
3
4
5
19,14
17,6
19,41
18,85
18,26
100
138
134,63
122,2
166,41
80,86
120,4
115,22
103,35
148,15
2,592
4,776
5,019
4,597
5,980
2,701
4,832
5,102
4,653
6,067
1070
1070
1040
1030
1040
0,00025
0,00045
0,00050
0,00045
0,00055
Waktu pelepsan
cake pada 10 cm
filtrat (tp,s)
Waktu Percobaaan
(tp, detik)
Massa Total Cake
(M1, kg)
Massa Total Cake +
Air (M2, kg)
Massa Jenis Cake
(kg/m3)
Volume Total Cake
(Vcake, m3)
Rata-rata
d. Karakter Filtrat
RUN
1
2
3
4
5
Rata-rata
tfiltrat (𝑠)
0,99
0,98
0,92
0,73
0,59
0,842
1070
1070
1040
1030
1040
1050
m (gram)
V (ml)
𝜌 (𝑘𝑔/
𝑚 3)
e. Penentuan Cs
Berat cawan penguap kosong = 41,2 gram
Berat basah slurry + cawan penguap = 42,7 gram
Berat basah slurry = 1,5 g = 0,0015
Berat kering slurry + cawan penguap = 41,6 gram
Berat kering slurry = 0,4 gram = 0,0004 kg
Cx =
𝒃𝒆𝒓𝒂𝒕 𝒔𝒐𝒍𝒊𝒅
𝒃𝒆𝒓𝒂𝒕 𝒔𝒍𝒖𝒓𝒓𝒚
=
𝟎,𝟎𝟎𝟎𝟒 𝒌𝒈
𝟎,𝟎𝟎𝟏𝟓 𝒌𝒈
= 𝟎, 𝟐𝟔𝟕
Berat basah cake + cawan penguap = 41,8 gram
Berat basah cake = 2,1 g = 0,0021 kg
Berat kering cake + cawan penguap = 40,4 gram
Berat kering cake = 0,7 gram = 0,0007 kg
𝒃𝒆𝒓𝒂𝒕 𝒃𝒂𝒔𝒂𝒉 𝒄𝒂𝒌𝒆
m = 𝒃𝒆𝒓𝒂𝒕 𝒌𝒆𝒓𝒊𝒏𝒈 𝒄𝒂𝒌𝒆 =
III.
𝟎,𝟎𝟎𝟐𝟏 𝒌𝒈
𝟎,𝟎𝟎𝟎𝟕 𝒌𝒈
=𝟑
Pengolahan Data

Keliling drum (K) = 1,5857 m

Lebar Screen = 40,5 cm = 0,404 m

Filter Area = K x L = 0,641 m2

Panjang busur drum yg tercelup kedalam slurry (K’) = 0,4857 m

Fraksi drum yang tercelup = K’ / K = 0,3063

Massa Jenis Cake
𝜌cake = (1-𝜀) 𝜌air
𝜀=
𝑚2−𝑚1
𝑚1
 Run 1
𝑚2−𝑚1
𝜌cake = (1-
𝑚1
) 𝜌air
2,701−2,592
𝜌cake = (1-
2,592
) 997 kg/m3 = 955,126 kg/m3
 Run 2
𝑚2−𝑚1
𝜌cake = (1-
𝑚1
) 𝜌air
4,832−4,776
𝜌cake = (1-
) 997 kg/m3 = 985,036 kg/m3
4,776
 Run 3
𝑚2−𝑚1
𝜌cake = (1-
𝑚1
) 𝜌air
5,102−5,019
𝜌cake = (1-
5,019
) 997 kg/m3 = 980,051 kg/m3
 Run 4
𝑚2−𝑚1
𝜌cake = (1-
𝑚1
) 𝜌air
4,653−4,597
𝜌cake = (1-
4,597
) 997 kg/m3 = 985,036 kg/m3
 Run 5
𝑚2−𝑚1
𝜌cake = (1-
𝑚1
) 𝜌air
6,067−5,980
𝜌cake = (1-

5,980
) 997 kg/m3 = 982,045 kg/m3
Volume Total Cake (V cake)
V cake =
𝑚 𝑐𝑎𝑘𝑒
𝜌 𝑐𝑎𝑘𝑒
 Run 1
V cake =
𝑚 𝑐𝑎𝑘𝑒
𝜌 𝑐𝑎𝑘𝑒
=
2,592𝑘𝑔
𝑘𝑔
𝑚3
955,126
= 2,714 𝑥 10-3 m3
 Run 2
V cake =
𝑚 𝑐𝑎𝑘𝑒
𝜌 𝑐𝑎𝑘𝑒
4,776 𝑘𝑔
= 985,036 𝑘𝑔/𝑚3 = 4,849 𝑥 10-3 m3
 Run 3
V cake =
𝑚 𝑐𝑎𝑘𝑒
𝜌 𝑐𝑎𝑘𝑒
5,019𝑘𝑔
= 980,051
𝑘𝑔/𝑚3
= 5,121 𝑥 10-3 m3
 Run 4
𝑚 𝑐𝑎𝑘𝑒
V cake =
𝜌 𝑐𝑎𝑘𝑒
4,597 𝑘𝑔
= 985,036 𝑘𝑔/𝑚3 = 4,667 𝑥 10-3 m3
 Run 5
𝑚 𝑐𝑎𝑘𝑒
V cake =

𝜌 𝑐𝑎𝑘𝑒
5,980 𝑘𝑔
= 982,045 𝑘𝑔/𝑚3 = 6,089 𝑥 10-3 m3
Viskositas
tfiltrat rata-rata =
0,99+0,98+0,92+0,73+0,59
5
= 0,842 𝑠
tair = 0,26 s
η air = 0,899 cp
𝜌air = 997 kg/m3
η filtrat =
η air . ρ filtrat . t filtrat
𝜌 𝑎𝑖𝑟. 𝑡 𝑎𝑖𝑟
η filtrat =

0,899 𝑐𝑝 . 1050
𝑘𝑔
997
𝑚3
0,842 𝑠
.0,26 𝑠
= 3,066 cp
Penentuan Cs
Cx =
𝒃𝒆𝒓𝒂𝒕 𝒔𝒐𝒍𝒊𝒅
𝒃𝒆𝒓𝒂𝒕 𝒔𝒍𝒖𝒓𝒓𝒚
=
𝟎,𝟎𝟎𝟎𝟒 𝒌𝒈
𝟎,𝟎𝟎𝟏𝟓 𝒌𝒈
𝒃𝒆𝒓𝒂𝒕 𝒃𝒂𝒔𝒂𝒉 𝒄𝒂𝒌𝒆
m = 𝒃𝒆𝒓𝒂𝒕 𝒌𝒆𝒓𝒊𝒏𝒈 𝒄𝒂𝒌𝒆 =
𝜌.𝐶𝑥
Cs = 1−𝑚.𝐶𝑥 =

𝑘𝑔
.
𝑚3
806,74
= 𝟎, 𝟐𝟔𝟕
𝟎,𝟎𝟎𝟐𝟏 𝒌𝒈
𝟎,𝟎𝟎𝟎𝟕 𝒌𝒈
𝑘𝑔
𝑥
𝑚3
0,6820
1−1,0579 𝑥 0,6820
=𝟑
= 1975,4850 kg/m3
Penentuan Z
Z=(
Z=(
Φ=
2.𝑓.(−∆𝑃)
𝜇 . 𝐶𝑠
)
2 . 0,3063 . ( 80000 𝑘𝑔/𝑚𝑠2)
0.003066
𝑉
𝐴 . 𝑡𝑐
1
Φ2 = (𝛼)(
𝑘𝑔
.
𝑚𝑠
=[
1975,4850𝑘𝑔/𝑚3
2.𝑓. (−∆𝑃)
𝑡𝑐 . 𝜇 . 𝛼 . 𝐶𝑠
2.𝑓. (−∆𝑃)
𝜇 . 𝐶𝑠
1
)(𝑡𝑐)
]1/2
) = 8091.352 𝑚3/kg.s

Penentuan flow rate (Φ)
𝑉
Φ = 𝐴.
𝑡𝑐
 Run 1
Φ =
0,0228 𝑚3
= 5,170 x 10-4 m/s
0,6406 𝑚2 𝑥 68.84 𝑠
 Run 2
Φ =
0,0228 𝑚3
0,6404 𝑚2 . 141 𝑠
= 2,525 x 10-4 m/s
 Run 3
Φ =
0,0228 𝑚3
0,6404 𝑚2 . 114,22 𝑠
= 3,117 x 10-4 m/s
 Run 4
Φ =
0,0228 𝑚3
0,6404 𝑚2 . 99.36 𝑠
= 3,583 x 10-4 m/s
 Run 5
Φ =
0,0228 𝑚3
0,6404 𝑚2 . 147,66 𝑠
= 2,411 x 10-4 m/s
 Rata-rata
Φ = 3.890 x 10-4

Penentuan 𝜶
1𝑥𝑍
𝛼=
Φ x tc
 Run 1
𝛼=
8091.352 m3/kg. s
= 227347,242 𝑚/𝑘𝑔
(5,170 x 10 − 4 𝑚/𝑠)2 𝑥 68.84 𝑠
 Run 2
𝛼=
8091.352 m3/kg. s
= 227269,209 𝑚/𝑘𝑔
( 2,525 x 10 − 4 𝑚/𝑠)2 𝑥 141 𝑠
 Run 3
𝛼=
8091.352 m3/kg. s
= 227270,013 𝑚/𝑘𝑔
(3,117 x 10 − 4 𝑚/𝑠)2 𝑥 114,22 𝑠
 Run 4
𝛼=
8091.352 m3/kg. s
= 227280,776 𝑚/𝑘𝑔
(3,583 x 10 − 4 𝑚/𝑠)2 𝑥 99,36 𝑠
 Run 5
𝛼=
8091.352 m3/kg. s
= 227279,900 𝑚/𝑘𝑔
(2,411 x 10 − 4 𝑚/𝑠)2 𝑥 147,66 𝑠
 Rata-rata
𝛼=

Nilai Tebal Cake
∆𝐿 𝑐𝑎𝑘𝑒 =
𝑉𝑐𝑎𝑘𝑒
𝐿−𝐿𝑑𝑧
𝐴.(
)
𝐿
𝑥
𝑡𝑐
𝑡𝑝
L = Lebar Screen = 0,404 m
Ldz = panjang dead zone = 0,14 m
 Run 1
∆𝐿 𝑐𝑎𝑘𝑒 =
2,714 𝑥 10−3 m3
0,404−0,14
)
0,404
0,6406 𝑚2.(
𝑥
68.84 𝑠
𝑡𝑝
 Run 2
∆𝐿 𝑐𝑎𝑘𝑒 =
4,849 𝑥 10−3 m3
0,404−0,14
0,6406 𝑚2.(
)
0,404
𝑥
141 𝑠
𝑡𝑝
 Run 3
∆𝐿 𝑐𝑎𝑘𝑒 =
5,121 𝑥 10−3 m3
0,404−0,14
)
0,404
0,6406 𝑚2.(
𝑥
114,22 𝑠
𝑡𝑝
 Run 4
∆𝐿 𝑐𝑎𝑘𝑒 =
4,667 𝑥 10−3 m3
0,404−0,14
)
0,404
0,6406 𝑚2.(
𝑥
99,36 𝑠
𝑡𝑝
 Run 5
∆𝐿 𝑐𝑎𝑘𝑒 =
 Rata-rata
6,089 𝑥 10−3 m3
0,404−0,14
0,6406 𝑚2.(
)
0,404
𝑥
147,66 𝑠
𝑡𝑝