BAB V Neraca (117-135) G21 T58

118

BAB VNERACA MASSA DAN PANAS5.1 Neraca MassaBasis : 1 Jam OperasiBahan Masuk : 587.961,69kg/jamArabian Light Crude (ALC)5.1.1 Neraca Massa pada desalter 11V-12Hasil perhitungan neraca massa Desalter 11V-12 disajikan pada tabel 22 di bawah ini :Tabel 22. Neraca Massa pada Desalter 11V-12No.KomponenInput (kg)Output (kg)

1.

2.3.

4.

Crude oil Minyak Air GaramWash waterCrude oil Minyak AirDesalter Effluent Water Mg (OH)2 HCl Effluent Water 587.311,66 646,763,2617.062,08--

-------

587.311,66645,52

1,992,5117.062,08

Total605.023,76605.023,76

5.1.2 Neraca Massa pada Desalter 11V-16

Hasil perhitungan neraca massa Desalter 11V-16 disajikan pada tabel 23 di bawah ini :Tabel 23. Neraca massa pada desalter 11V-16No.KomponenInput (kg)Output (kg)

1.

2.3.Crude oil Minyak AirWash waterEffluent Water587.311,66645,5216.416,56-587.311,66--17.062,08

Total604.373,74604.373,74

5.1.3 Neraca massa pada Preflash Drum 11V-15Hasil perhitungan neraca massa Preflash Drum 11V-15 disajikan pada tabel 24 di bawah ini :Tabel 24. Neraca Massa pada Preflash Drum 11V-15No.KomponenInput (kg)Output (kg)

1.

2.3.Crude oil Naphta& Gas Kerosene LGO HGO Long residu Overhead Vapour to 11C-1Crude oil Naphta& Gas Kerosene LGO HGO Long residu 98.668,3677.525,1449.334,18103.366,85258.417,13-

---------121.859,02

78.196,0461.439,7539.098,0281.919,66204.799,17

Total587.311,66587.311,66

5.1.4 Neraca Massa pada Furnace 11F-1 Hasil perhitungan neraca massa Furnace 11F-1 disajikan pada tabel 25 di bawah ini :Tabel 25. Neraca Massa pada Furnace 11F-1NoKomponenInput (kg)Output (kg)

1.Crude Oil

Naphta& Gas78.196,04-

Kerosene61.439,75-

LGO39.098,02-

HGO81.919,66-

Long residu204.799,17-

2.Fuel Oil2136,67-

3.Udara

O28337,18-

N227.609,43-

4.Crude Oil

Naphta-78.196,04

Kerosene-61.439,75

LGO-39.098,02

HGO-81.919,66

Long residu-204.799,17

5.Flue Gas

CO2-6.815,97

H2O-2.499,92

6.Diatomoc Gas

N2-27.609,43

O2-1.157,96

Total503.535,92503.535,92

5.1.5 Neraca Massa pada Kolom Fraksinasi 11C-1Hasil perhitungan neraca massa Kolom Fraksinasi 11C-1 disajikan pada tabel 26 di bawah ini :Tabel 26.Neraca massa pada Kolom Fraksinasi 11C-1No.KomponenInput (kg)Output (kg)

1.

2345678910111213141516Feed (crude Oil)Naphta& GasKeroseneLGOHGOLong ResiduTop ReflukHot UCRCold UCROVHD ex 11V-15OVHD ex 11C-6Hot LCRCold LCROVHD ex 11C-4OVHD ex 11C-2 LP steamOVHD Vapour (top produk)KeroseneLGOHGOLong residu78.196,0461.439,7539.098,0281.919,66204.799,1736.528,7556.317,92272.612,5121.859,0218.632,83182.586,25378.357,0811.772,5814292,666138,33--------------------143.737,62413.165,96614.547,77112.314,06280.785,15

Total1.564.550,561.564.550,56

5.1.6 Neraca Massa pada Overhead Accumulator 11V-1Hasil perhitungan neraca massa Overhead Accumulator 11V-1 disajikan pada tabel 27 di bawah ini :Tabel 27. Neraca Massa pada Overhead Accumulator 11V-1No.KomponenInput (kg)Output (kg)

1.2.3.4.5.OVHD Vapor ex C-1Off gas to SRUTop refluk to C-1NaphtaWater to SWS143.737,62-----2.903,3336.528,7596.226,678.078,87

Total143.737,62143.737,62

5.1.7 Neraca Massa pada Coaleser 11S-1Hasil perhitungan neraca massa Coalescer 11S-1 disajikan pada tabel 28 di bawah ini :Tabel 28. Neraca Massa pada Coaleser 11S-1No.KomponenInput (kg)Output (kg)

1.2.Produk Naphta from 11V-1Naphta to NHT96.226,67--96.226,67

Total96.226,6796.226,67

5.1.8 Neraca massa pada Kerosene Stripper 11C-6Hasil perhitungan neraca massa Kerosene Stripper 11C-6 disajikan pada tabel 29 di bawah ini :Tabel 29. Neraca Massa pada Kerosene Stripper 11C-6No.KomponenInput (kg)Output (kg)

1.2.3.Produk Kerosene 11C-1OVHD Vapor Kerosene to Kero Merox84.235,54---18.632,83 65.602,71

Total84.235,54 84.235,54

5.1.9 Neraca Massa pada LGO Stripper dan Drier 11C-4 dan 11C-5Hasil perhitungan neraca massa LGO Stripper 11C-4 dan Drier 11C-5disajikan pada tabel 30 di bawah ini :

Tabel 30. Neraca Massa pada LGO Stripper dan Drier 11C-4 dan 11C-5No.KomponenInput (kg)Output (kg)

1.

2.

LGO StripperProduk LGO from 11C-1LP steamOVHD VapourLGO to 11C-5LGO Drier LGO from 11C-4Ejector 11J1ALGO to storage53.604,44390,83--

42.222,69-----11.772,58 42.222,69

-353,6241.869,07

Total96.217,9696.217,96

5.1.10 Neraca massa pada HGO Stripper 11C-2Hasil perhitungan neraca massa HGO Stripper 11C-2 disajikan pada tabel 31 di bawah ini :Tabel 31. Neraca Massa pada HGO Stripper 11C-2No.KomponenInput (kg)Output (kg)

1.2.3.4.Produk HGO from 11C-1LP steamOVHD Vapor HGO to 11C-3112.314,061.940,62----14.292,6599.962,03

Total114.260,68114.260,68

5.1.11 Neraca massa pada HGO Drier 11C-3Hasil perhitungan neraca massa HGO Drier 11C-3 disajikan pada tabel 32 di bawah ini :Tabel 32. Neraca Massa pada HGO Drier 11 C-3No.KomponenInput (kg)Output (kg)

1.2.3.Produk HGO from 11C-2Ejector 11J1AHGO to storage99.960,03---37,2999.924,74

Total99.960,0399.960,03

5.1.12 Neraca Massa Keseluruhan (Overall)Neraca massa overall disajikan pada tabel 33 di bawah ini :Tabel 33. Neraca Massa Keseluruhan (Overall)KodeKomponenMassa Bahan

Input (kg)Output (kg)

F1Crude Oil

- ALC587.961,69-

F3Desalter 11V-12 Effluent water

- Mg(OH)Cl-1,99

- HCl-2,51

- Effluent Water-17.062,08

F5Wash water ke Desalter 11V-1616.416,56

-

F9Udara ke Furnace

- O28.337,18-

- N227.609,43-

F10Fuel Oil ke Furnace 2.136,67-

F11Flue Gas keluar Furnace-

- CO2-6.815,97

- H2O-2.499,92

- Diatomic Gas

N2-27.609,43

O2-1.157,96

F14LP Steam ke kolom 11C16.138,33-

F19Produk Long Residue-280.785,15

F20Off gas keluar 11V-1 ke SRU-2.903,33

F21H2O keluar 11V-1-8.078,87

F24Produk Naphta-96.226,67

F28Produk Kerosene-65.602,71

F31LP Steam ke LGO Stripper 11C-4390,83-

F34Ejector LGO Drier 11C-5-353,62

F35Produk LGO-41.869,07

F36LP Steam ke HGO Stripper 11C-21940,62-

F38Ejector HGO Drier 11C-3-37,29

F40Produk HGO -99.924,74

Total650.931,31650.931,31

Perhitungan efisiensi produksi :Losses massa = total massa crude masuk total massa produk keluar = (587.961,69 584.408,34)kg = 3553,35 kg

= 99,39 %

BLOK DIAGRAMGambar. 20

5.2 Neraca PanasBasis : 1 jam operasiSatuan Laju alir = kkal5.2.1 Neraca Panas pada Heat Exchanger 11E-20Tabel 34.Neraca panas pada 11E-20No.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas HGO Produk ExchangerKehilangan Panas13.064.982,088.326.530,98-16.331.227,594.995.918,5964.366,88

Total21.391.513,0621.391.513,06

5.2.2 Neraca Panas pada Heat Exchanger 11E-1Tabel 35. Neraca panas pada 11E-1No.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas UCR ExchangerKehilangan Panas16.331.227,5928.016.721,2-24.496.841,3919.687.425,7163.681,704

Total44.347.948,7944.347.948,79

5.2.3 Neraca Panas pada Heat Exchanger 11E-2Tabel 36. Neraca panas pada 11E-2No.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas Kerosene Produk ExchangerKehilangan Panas13.064.982,088.746.471,12-14.698.104,845.466.544,451.646.803,91

Total21.811.453,221.811.453,2

5.2.4 Neraca Panas padaHeat Exchanger11E-21Tabel 37. Neraca Panas pada 11E-21No.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas LGO Produk ExchangerKehilangan Panas13.064.982,085.981.166,63-14.698.104,843.401.055,54946.988,33

Total19.046.148,7119.046.148,71

5.2.5 Neraca Panas pada Heat Exchanger 11E-4Tabel 38. Neraca Panas pada 11E-4No.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas LCRKehilangan Panas32.662.455,1942.036.996,54-37.561.823,4634.680.522,162.457.106,083

Total74.699.451,7174.699.451.71

5.2.6 Neraca Panas pada Heat Exchanger 11E-22 A/BTabel 39. Neraca Panas pada 11E-22A/BNo.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas Long residuKehilangan Panas37.561.823,4627.296.816,23-42.461.191,7521.057.543,951.339.904

Total64.858.639,764.858.639,7

5.2.7 Neraca Panas pada Desalter 11V-12Tabel 40. Neraca Panas pada Desalter 11V-12No.KomponenInput (kkal)Output (kkal)

1.

2.3.

4.

5.Panas Crude Oil masuk - crude oil - H2O - MgCl2Panas H2O masukPanas Crude Oil Keluar - crude oil - H2ODesalter Effluent water keluar - H2O - Mg(OH)2 - HCl - Panas reaksi pelarutan garamPanas yang hilang42.414.485,9230.327,3364,52792.673,01

--

--------

40.782.933,2529.987,93

825.926,1868,2561,02226,061.598.348,09

Total43.237.550,7843.237.550,78

5.2.8 Neraca Panas pada Desalter 11V-16Tabel 41. Neraca Panas pada Desalter 11V-16No.KomponenInput (kkal)Output (kkal)

1.

2.3.4.Panas Crude Oil - crude oil - H2OPanas H2O (wash water) masukPanas H2O (wash water) keluarPanas yang hilang40.782.933,2567.818,331.724.723,79--40.782.933,25--1.792.542,120

Total42.575.475,3742.575.475,37

5.2.9 Neraca Panas pada Heat Exchanger 11E-5A/BTabel 42. Neraca Panas pada 11E-5A/BNo.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas Long residu ExchangerKehilangan Panas20.391.466,63 29.636.543,33-25.285.418,6224.177.180,09565.411,25

Total50.028.009,9650.028.009,96


1.2.3.Panas Crude Oil Panas Long residu ExchangerKehilangan Panas25.285.418,63 33.536.088,5-28.548.053,2929.636.543,33636.910,51

Total58.821.507,1358.821.507,13

5.2.11 Neraca Panas pada Heat Exchanger 11E-24 A/BTabel 44. Neraca Panas pada 11E-24A/BNo.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas HGO ExchangerKehilangan Panas20.391.466,6318.873.470,21-29.363.711,968.326.530,981.574.693,89

Total39.264.936,8439.264.936,84


1.2.3.Panas Crude Oil Panas LCR ExchangerKehilangan Panas58.727.423,92 57.800.870,25-66.884.010,3346.240.696,213.403.587,7

Total116.528.294,2116.528.294,2

5.2.13 Neraca Panas pada Heat Exchanger 11E-7Tabel 46.Neraca Panas pada 11E-7No.KomponenInput (kkal)Output (kkal)

1.2.3.Panas Crude Oil Panas Residu ExchangerKehilangan Panas66.884.010,33 52.253.905,3875.040.597,21 42.894.996,961.202.321,5

Total119.137.915,7119.137.915,7

5.2.14 Neraca Panas pada Preflash Drum 11V-15Tabel 47.Neraca Panas pada Preflash Drum 11V-15No.KomponenInput (kkal)Output (kkal)

1.2.3.4.Panas Crude OilPanas OVHD VaporPanas Preflash crudeKehilangan Panas75.040.597,21----22.000.921,29 53.006.506,3333.169,59

Total75.040.597,2175.040.597,21


1.2.3.Panas Crude Oil Panas Long ResidueKehilangan Panas53.006.506,33 59.273.086,67-60.763.556,08 49.134.269,212.381.767,7

Total112.279.593112.279.593

5.2.16 Neraca Panas pada Furnace 11F-1Tabel 49. Neraca Panas pada Furnace 11F-1No.KomponenInput (kkal)Output (kkal)

1.2.

3.4.5.

6.Panas Crude Oil masukPanas Fuel Oil Masuk - Net Heating Value Fuel Oil - Sensible Heat Content Fuel OilPanas Udara masukPanas Crude Oil keluarPanas Flue gas keluar - CO2 - H2O - Diatomic Gas (N2 dan O2)Kehilangan Panas60.763.556,08

21.903.212,21166.611,4312.979.901,38-

-----

---93.084.596,54

470.370,04385.829,171.647.117,75225.367,6

Total95.813.281,195.813.281,1

5.2.17 Neraca Panas pada Crude Splitter 11C-1Tabel 50. Neraca Panas pada Kolom fraksinasi 11C-1No.KomponenInput (kkal)Output (kkal)

1.Feed

Panas Overhead 11V-1522.000.921,29-

Panas Crude dari 11F-193.084.596,54-

Panas LP Steam3.643.550,65-

Panas Top refluk1.319.009,68-

Panas Hot UCR6.257.147,48-

Panas Overhead ex. 11C-63.415.801,11-

Panas Hot LCR29.921.950,45-



Panas Cold UCR20.444.634,39-

Panas Cold LCR34.680.522,15-

2.Produk

Panas Overhead Vapor-20.760.778,08

Panas Kerosene-37.871.132,61

Panas LGO-83.641.448,75

Panas HGO-19.029.780,44

Panas Long residu-58.493.177,63

3.Kehilangan Panas-950.516,5

Total220.746.834220.746.834

5.2.18 Neraca Panas pada Overhead Accumulator 11V-1Tabel 51.Neraca Panas pada Overhead Accumulator 11V-1No.KomponenInput (kkal)Output (kkal)

1.2.3.4.5.6.OVHD Vapor Ex 11C-1Top Refluks Destilat to 11C-1 Off Gas to SRUNaptha to 11S-1Water to SWSKehilangan Panas5.190.194,52-----1.319.009,68354.829,233.207.351,13 88.341,16220.663,33

Total5.190.194,525.190.194,52

5.2.19 Neraca Panas pada Coalescer 11S-1Tabel 52.Neraca Panas pada Coalescer 11S-1No.KomponenInput (kkal)Output (kkal)

1.

2.

Feed - Panas Naphta from 11V-1Produk - Panas Naphta to NHT3.207.351,13--

3.207.351,13

Total3.207.351,133.207.351,13

5.2.20 Neraca Panas pada Kerosene Stripper 11C-6Tabel53.Neraca Panas pada Kerosene Stripper 11C-6No.KomponenInput (kkal)Output (kkal)

1.

2.

3.Feed - Panas Produk Kerosene 11C-1 - Panas Kerosene dari ReboilerProduk - Panas Overhead Vapor - Panas Kerosene ke Kero Merox - Panas Kerosene ke ReboilerKehilangan Panas8.890.963,019.839.780,02

------

3.364.046,558.746.471,136.559.853,3560.372

Total18.730.743,0318.730.743,03

5.2.21 Neraca Panas pada LGO Stripper 11C-4Tabel 54.Neraca Panas pada LGO Stripper 11C-4No.KomponenInput (kkal)Output (kkal)

1.

2.

3.Feed - Panas Produk LGO 11C-1 - Panas Stripping SteamProduk - Panas OVHD Vapor - Panas LGOKehilangan Panas8.337.936,61 239.674,13-----

2.452.464,53 6.098.444,4226.701,8

Total8.577.610,74 8.577.610,74

5.2.22 Neraca Panas pada LGO Drier 11C-5Tabel 55.Neraca Panas pada LGO Drier 11C-5No.KomponenInput (kkal)Output (kkal)

1.

2.

3.Feed - Panas LGO Produk - Panas sistem ejector - Panas LGO to StorageKehilangan Panas3.518.333,32

----

230.272,673.256.275,4831.785,16

Total3.518.333,323.518.333,32

5.2.23 Neraca Panas pada HGO Stripper 11C-2Tabel 56.Neraca Panas pada HGO Stripper 11C-2No.KomponenInput (kkal)Output (kkal)

1.

2.

3.Feed - Panas Produk HGO C-1 - Panas Stripping SteamProduk - Panas OVHD Vapor - Panas HGOKehilangan Panas21.837.452,97 1.190.066,03

-----

3.453.960,25 18.880.514,07693.044,68

Total23.027.51923.027.519

5.2.24 Neraca Panas pada HGO Drier 11C-3Tabel 57.Neraca Panas pada HGO Drier 11C-3No.KomponenInput (kkal)Output (kkal)

1.

2.

3.Feed - Panas HGO Produk - Panas sistem ejector - Panas Produk HGO Kehilangan Panas8.607.294,304----

24.348,92 8.048.979,95533.965,43

Total8.607.294,3048.607.294,304

5.2.25 Neraca Panas Keseluruhan (Overall)Tabel 58.Neraca Panas Keseluruhan (Overall)NoAlatInputOutputKehilanganPanas

1Heat Exchanger 11E-20 Panas Crude Oil Panas HGO Produk Exchanger13.064.982,088.326.530,9816.331.227,594.995.918,5964.366,88

2Heat Exchanger 11E-1 Panas Crude Oil Panas UCR Exchanger16.331.227,5928.016.721,2

24.496.841,3919.687.425,7163.681,7

3Heat Exchanger 11E-2 Panas Crude Oil Panas Kerosene Produk Exchanger13.064.982,088.746.471,1214.698.104,845.466.544,451.646.803,91

4Heat Exchanger 11E-21 Panas Crude Oil Panas LGO Produk Exchanger13.064.982,085.981.166,6314.698.104,843.401.055,54946.988,33

5Heat Exchanger 11E-4 Panas Crude Oil Panas LCR32.662.455,1942.036.996,5437.561.823,4634.680.522,162.457.106,083

6Heat Exchanger 11E-22 A/B Panas Crude Oil Panas Long residu

37.561.823,4627.296.816,23

42.461.191,7521.057.543,95

1.339.904

7Desalter 11V-12 Panas Crude Oil masuk - crude oil - H2O - MgCl2 Panas H2O masuk Panas Crude Oil Keluar - crude oil - H2O Desalter Effluent water keluar - H2O - Mg(OH)2 - HCl- Panas reaksi pelarutan garam

42.414.485,9230.327,3364,52792.673,01

40.782.933,2529.987,93

825.926,1868,2561,02226,06

1.598.348,09

8Desalter 11V-16 Panas Crude Oil crude oil H2O Panas H2O (wash water) masuk Panas H2O (wash water) keluar

40.782.933,2567.818,331.724.723,79

-

40.782.933,25--

1.792.542,120

9Heat Exchanger 11E-5 A/B Panas Crude Oil Panas Long residu Exchanger

20.391.466,63 29.636.543,33

25.285.418,6224.177.180,09

565.411,25

10Heat Exchanger 11E-23 Panas Crude Oil Panas Long residu Exchanger25.285.418,63 33.536.088,528.548.053,2929.636.543,33636.910,51

11Heat Exchanger 11E-24 A/B Panas Crude Oil Panas HGO Exchanger

20.391.466,6318.873.470,21

29.363.711,968.326.530,98

1.574.693,89

12Heat Exchanger 11E-6 Panas Crude Oil Panas LCR Exchanger58.727.423,92 57.800.870,2566.884.010,3346.240.696,213.403.587,7

13Heat Exchanger 11E-7 Panas Crude Oil Panas Residu Exchanger66.884.010,33 52.253.905,3875.040.597,21 42.894.996,961.202.321,5

14Preflash Drum 11V-15 Panas Crude Oil Panas OVHD Vapor Panas Preflash crude75.040.597,21---22.000.921,29 53.006.506,3333.169,59

15Heat Exchanger 11E-25 Panas Crude Oil Panas Long Residue53.006.506,33 59.273.086,6760.763.556,08 49.134.269,212.381.767,7

16Furnace 11F-1 Panas Crude Oil masuk Panas Fuel Oil Masuk Net Heating Value Fuel Oil Sensible Heat Content Fuel Oil Panas Udara masuk Panas Crude Oil keluar Panas Flue gas keluar CO2 H2O Diatomic Gas (N2 dan O2)60.763.556,08

21.903.212,21

166.611,43

12.979.901,38-

-

----

-

-

-93.084.596,54

470.370,04385.829,171.647.117,75

225.367,6

17Kolom Fraksinasi 11C-1

Feed

Panas Overhead 11V-1522.000.921,29-

Panas Crude dari 11F-193.084.596,54-

Panas LP Steam3.643.550,65-

Panas Top refluk1.319.009,68-

Panas Hot UCR6.257.147,48-


Panas Hot LCR29.921.950,45-

Panas Overhead ex. 11C-42.485.164,05-950.516,5


Panas Cold UCR20.444.634,39-

Panas Cold LCR34.680.522,15-

Produk

Panas Overhead Vapor-20.760.778,08

Panas Kerosene-37.871.132,61

Panas LGO-83.641.448,75

Panas HGO-19.029.780,44

Panas Long residu-58.493.177,63

18Overhead Accumulator 11V-1 OVHD Vapor Ex 11C-1 Top Refluks to 11C-1 Off Gas to SRU Naptha to 11S-1 Water to SWS

5.190.194,52

----

-

1.319.009,68354.829,233.207.351,13 88.341,16220.663,33

19Coalescer 11S-1 Feed Panas Naphta from 11V-1 Produk Panas Naphta to NHT

3.207.351,13

-

-

3.207.351,13-

20Kerosene Stripper 11C- 6 Feed Panas Produk Kerosene 11C-1 Panas Kerosene dari Reboiler Produk Panas Overhead Vapor Panas Kerosene ke Kero Merox Panas Kerosene ke Reboiler

8.890.963,01

9.839.780,02

-

-

-

-

-

3.364.046,55

8.746.471,13

6.559.853,3560.372

21LGO Stripper 11C-4 Feed Panas Produk LGO 11C-1 Panas Stripping Steam Produk Panas OVHD Vapor Panas LGO

8.337.936,61

239.674,13

--

-

-

2.452.464,536.098.444,42

26.701,8

22LGO Drier 11C-5 Feed Panas LGO Produk Panas sistem ejector Panas LGO to Storage

3.518.333,32

-

-

-

230.272,67

3.256.275,4831.785,16

23HGO Stripper 11C-2 Feed Panas Produk HGO C-1 Panas Stripping Steam Produk Panas OVHD Vapor Panas HGO

21.837.452,97

1.190.066,03

--

-

-

3.453.960,25 18.880.514,07693.044,68

24

HGO Drier 11C-3 Feed Panas HGO Produk Panas sistem ejector Panas Produk HGO

8.607.294,304

-

-

-

24.348,92

8.048.979,95533.965,43

Jumlah1.290.488.196,501.269.730.718,8720.757.477,63

Total1.290.488.196,501.290.488.196,50

% Panas yang hilang= x 100 %= x 100%= 1,61 %BLOK DIAGRAMGambar. 21117

Documents

BAB V Neraca (117-135) G21 T58