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BAB IIINERACA MASSA
1. Neraca massa reaktorreaksiNaNO3 + H2SO4 ---------> NaHSO4 + HNO3
basis = 100 kg NaNO3BM NaNO3 = 85 kg/kgmolReaktan :NaNO3 masuk reaktor
komponen kadar (%) massa (kg) masuk (kmol)NaNO3 98 98 1.1529411765
H2O 2 2 0.0235294118Total 100 100 1.1764705882
konversi 97 %NaNO3 reaksi = 1.1411764706NaNO3 sisa = 0.0352941176 = 3
H2SO4 yang diumpankan BM H2SO4= 98H2SO4 masuk = 1.1764705882 kmol
= 115.29411765 kgH2SO4 reaksi = 1.1411764706 kmol
111.83529412 kgH2SO4 sisa = 3.4588235294 kgkadar H2SO4 = 93 %kada air dalam H2SO4 = 7 %H2O dalam H2SO4 = 8.0705882353 kg
produk:NaHSO4 hasil = 1.1411764706 kmol BM NaHSO4=
= 136.92976471 kgHNO3 hasil = 1.1411764706 kmol BM HNO3=
= 71.894117647 kgH2OH2O Total dalam reaktor = H2O dalam NaNO3 + H2O dalam H2SO4
= 2 + = 10.070588235 kg
asumsi H2O dalam either cake = 10 %1.0070588235 kg
H2O keluar reaktor = 9.0635294118 kg
NERACA MASSA REAKTOR
Komponen Masuk KeluarKe Separator either cake
HNO3 71.894117647NaNO3 100 3H2SO4 115.294117647 3.4588235294NaHSO4 136.92976471H2O 10.0705882353 9.0635294118 1.0070588235
Total 225.364705882 80.957647059 144.39564706225.3532941176
2. Neraca Massa di Kondensor Komposisi bahan masuk kondensor
komponen kg kmolHNO3 71.8941176471 1.1411764706H2O 9.0635294118 0.5035294118
1.6447058824
HNO3 terdekomposisireaksi
4HNO3 --------> 2H2O + 4NO2 +O2
asumsi HNO3 terdekomposisi sebesar = 10 % = 7.1894117647 = 0.1141176471
HNO3 sisa = HNO3 cair - HNO3 terdekomposisi = 64.7047058824 kg
HNO3 reaksi = 0.1141176471 kmolH2O terbentuk = 0.0570588235 kmol
1.0270588235 kg
NO2 terbentuk = 0.1141176471 kmol BM NO2 = = 5.2494117647
O2 terbentuk = 0.0285294118 kmol BM O2 = = 0.9129411765 kg
H2O uap = H2O uap + H2O terbentuk
= 10.0905882353 kg
neraca massa di kondensorkomponen masuk keluarHNO3 71.8941176471 64.704705882H2O 9.0635294118 10.090588235O2 0.9129411765NO2 5.2494117647
komponen A B C DH2O 29.8605 -3.15E+03 -7.30E+00 2.42E-09HNO3 71.7653 -4.38E+03 -2.28E+01 -4.60E-03
28.5884 -2.47E+03 -7.351 2.80E-10P operasi 1 atmT opersi 98 C 371.15 KP parsial 760 mmHgV/L 0.9 trial
log P P mmHg KH2O 2.8494143204 706.99170829 0.9302522477HNO3 1.3930384393 24.719429263 0.0325255648
Liq Vap BMH2O 384.814559904 322.17714838 63 706.99170829
0.5442985475 0.4557014525 1HNO3 24.0163970714 0.7030321917 18 24.719429263
0.9715595298 0.0284404702 1
0.0292730083 0.8707269917
0.837227023
30.75414391
kg
kg/kgmol
119.99
63
8.0705882353
kgkmol
46 kg/kmol
32 kg/kmol
E Tmin Tmax1.81E-06 273.16 647.131.19E-05 231.55 376.1
2.74E+06
liq34.290808491
17.48807153651.778880028
BAB IIIPERHITUNGAN NERACA MASSA
Kapasitas Natrium Nitrat direncanakan = 32,000 ton/tahunJumlah hari kerja = 1 tahun = 330Jumlah waktu kerja perhari = 1 hari = 24
Kapasitas produksi Ethylene Glycol = 32,000x
1000xtahun ton
= 4040 kg/jam
Basis = 1000 kg HNO3
Raw material NaNO3 = 1420 kgH2SO4 = 1638 kgYield = 95%
Penentuan kebutuhan umpan bahan bakuNaNO3 = 4040
x 1420= 5737.3737373737 kg/jam
1000
H2SO4 = 4040x 1638
= 6618.1818181818 kg/jam1000
Menghitung konversi reaksi
Yield = produkx 100% feed utama
feed utama = produkx 100%Yield
Feed utama = kapas produksix 100%Yield
= 4253.0568846358 Kg
limiting reaktan mula - mula = feed utama = 4253.056884636 Kg
limiting reaktan mula - mula - limiting reaktan yang bereaksi = 100% - yield
limiting reaktan yang bereaksi = limiting reaktan mula - mula + yield -100%
= 4253.0568846358 + 95% - 100% = 4253.0068846358 kmol/jam
konversi reaksi = limiting reaktan yang bereaksi x 100% limiting reaktan mula - mula
= 4253.0068846358 kmol/jamx 100%4253.0568846358 kmol/jam
= 0.9999882438
Bahan Baku
Bahan Kadar % ms BM n (kmol) massa (kg/) H2O totalH2SO4 98% 98.07754 66.129494906 6485.818181818 533.9797979798 kg/jamH2O 2% 18.01534 7.3472738435 132.3636363636 29.6402842233 kmol
6618.181818182
Bahan Kadar % ms BM n (kmol) massa (kg/)NaNO3 93% 84.9947 62.7775329021 5335.757575758H2O 7% 18.01534 22.2930103798 401.6161616162
5737.373737374
(sumber : N K Patel)
reaksiNaNO3 + H2SO4 ---------> NaHSO4 + HNO3
1. ReaktorFungsi: Sebagai tempat bereaksi natrium nitrat dan asam sulfat
M4Keterangan :
M1 M1 : Aliran NaNO3 masuk reaktorM2 : Aliran H2SO4 masuk reaktor
M2 M3 : Aliran keluar reaktor (Neither Cake)M4 : Aliran keluar reaktor (ke Separator)
M3
Berat AtomH = 1.00797 Na = 22.9898C = 12.01115 N = 14.0067O = 15.9994 S = 32.064
Basis perhitungan = 1000 kg/jam NaNO3Perbandingan mol NaNO3/H2SO4 = 1 / 1Konversi reaksi = 99.9988%Excess H2SO4 = 0%
1.1. Aliran komponen masuk reaktor
KomponenBM M1 M2
Jumlahkg/kg mol kmol/jam kmol/jamNaNO3 84.9947 11.7654 11.7654394921H2SO4 98.0775 11.7654 11.7654394921H2O 18.0153 22.2930 7.3473 29.6402842233Total 34.0584 19.1127 23.5309
konversi = 99.99882%
reaksi NaNO3 + H2SO4 ---------> NaHSO4 + HNO3M 11.7654 11.7654 0.0000 0R 11.7653 11.7653 11.7653 11.7653011747S 0.0001 0.0001 11.7653 11.7653011747
= (-f) * ni limiting reactanvi limiting reactan
KomponenReaksi
Masuk Keluar
Vi ni in ni outNaNO3 -1 11.7653011747 11.7654 0.0001383174H2SO4 -1 11.7653011747 11.7654 0.0001383174HNO3 1 11.7653011747 0 11.7653011747
NaHSO4 1 11.7653011747 0 11.7653011747total = 23.5309 23.5309
ASUMSIKadar air yang keluar M4 90% total H2O
1.2. neraca massa pada reaktor
Komponen BMMasuk Keluar
w in M1 w in M2 w out M4 w out M3NaNO3 84.9947 1000 0 0 0.01175625H2SO4 98.0775 0 1153.93 0 0.013565835HNO3 63.01287 0 0 741.3653934298 0NaHSO4 120.05937 0 0 0 1412.5346468901H2O 18.01534 401.6161616162 132.3636363636 480.5818181818 53.397979798
TOTAL 1401.6161616162 1286.2889987686 1221.947211612 1465.95794877312687.9051603848 2687.9051603848
2. SeparatorFungsi: Sebagai tempat pemisahsn asam nitrat fase liquid dan asam nitrat fase gas
M6 Keterangan:M4 : Aliran masuk Separator (HNO3) M5 : Aliran keluar Separator (fase liquid)
M4 M6: Aliran keluar separator (fase uap)
M5
Berat AtomH = 1.00797 Na = 22.9898C = 12.01115 N = 14.0067O = 15.9994 S = 32.064
ASUMSIEfisiensi Separator = 70%Fase uap keluar separator = 30%
2.1. Neraca mol separator
KomponenBM Masuk Keluarkg/kg mol kmol M4 kmol M5 kmol M6
HNO3 63.0129 11.7653 8.2357 3.5296H2O 18.01534 26.676255801 18.6734 8.0029
TOTAL 38.4416 26.9091 11.5325
2.2 Neraca massa pada Separator
KomponenBM Masuk Keluarkg/kg mol kg M4 kg M5 kg M6
HNO3 63.0129 741.3654 518.9558 222.4096H2O 18.01534 480.5818181818 336.4072727273 144.1745454545
TOTAL 1221.9472 855.3630 366.58421221.9472 1221.9472
M6 vap M5 liq0.6067082001 0.60670820010.3932917999 0.3932917999
1 1
M5 (liquid) 0.7M6 (vapour) 0.3
38.4416 1
Total massa bahan masuk Sparator = 1221.9472 KgTerdiri dari : HNO3 = 741.3654 Kg
H2O = 480.5818181818 Kg
= + L x . XL741.3654 = 0 + L 0,7741.3654 = 0.7 L
L = 1059.0934 Kg
2.3. Jumlah air yang teruapkan :V = F - LV = 1221.9472 - 1059.0934V = 162.8538 Kg
3. AbsorberFungsi: Sebagai tempat pemisahsn asam nitrat fase liquid dan asam nitrat fase gas
M7Keterangan:M6 : Aliran masuk Absorber (HNO3) M7 : Aliran H2O masuk absorberM8 : Aliran keluar Absorber (fase liquid)
F x . XF V x . XV
Absorber
Separator
M6 M8
ASUMSIProduk Absorber 50% HNO3
M1 = 60.67%V1 = 366.5842M2 = 50%
M1 . V1 = M2 . V2V2 = 444.8192360579
3.1. neraca massa pada absorber
KomponenBM Masuk Keluar
kg/kg mol kg M6 kg M7 kg M8 KadarHNO3 63.0129 222.4096 0 222.4096 50%H2O 18.0153 144.1745 78.2351 222.4096 50%
TOTAL 366.5842 78.2350725744 444.8192444.8192 444.8192
4. AkumulatorTotal produk = Produk dari Separator + Produk Absorber
4.1. Neraca massa pada akumulator
KomponenBM Masuk Keluar
kg/kg mol kg M8 kg M7 kg M8HNO3 0.7000 222.4096 518.9558 741.3654 0.5702011191H2O 0.3000 222.4096 336.4073 558.8169 0.4297988809
TOTAL 444.8192 855.3630481281 1300.1823 1.0000
Absorber
harijam
1x
1330 24
Aliran masuk Separator (HNO3) Aliran keluar Separator (fase liquid)Aliran keluar separator (fase uap)
reaksi :NaNO3 + H2SO4 ---------> NaHSO4 + HNO3
KomponenReaksi
Masuk Keluar
Vi ni in ni outNaNO3 -1 11.7653011747 11.7654394921 0.0001383174H2SO4 -1 11.7653011747 11.7654394921 0.0001383174HNO3 1 11.7653011747 0 11.7653011747NaHSO4 1 11.7653011747 0 11.7653011747H2O 29.6402842233 29.6402842233
1. Neraca Panas pada reaktor
a. menghitung Hbahan masuk fase liquid
Cp = a + b(T) + c(T)^2 +d(T)^3Komponen mol Hf Hf
AMasuk kmol Kj/gmol Kj/kmolNaNO3 11.7654394921 -173.23 -173230 110H2SO4 11.7654394921 -811.32 -811320 139.1
bahan keluar fase gas
Cp = a +b(T) + c(T^2) + d(T^3) + e/(T^2)Komponen mol Hf Hf
AKeluar kmol Kj/ gmol Kj/kmolHNO3 11.7653011747 -134.31 -134310 19.63229
NaHSO4 11.7653011747 -262.2 -262200 223.515NaNO3 0.0001383174 -173.23 -173230 110H2SO4 0.0001383174 -811.32 -811320 139.1
Q = H = H keluar - H masuk = 3040274704.98556 Kjoule
b. Menghitung panas yang dibutuhkanCp coal = 0.37 cal/g T= 15 - 90 1 cal =
1.54808 joule/g
( sumber data : himelblau Appendix E )
(sumber : Chase, 1998)
Cp coal = 0.45 cal/g T= 200 1 cal =1.8828 joule/g
T1 = 25 = 298.15
T2 = 200 = 473.15
Hcoal = m . Cp . T = m x 0.37 x = 64.750 m kJ/ kg
Hc = m . Cp . T= m x 0.45 x= 78.750 m kJ/ kg
Hsensibel == 0.0 m kJ/ kg
Qloss = 5% Hcoal= 3.238 m kJ/ kg
Qin = QoutHs + Hsensibel = Hc + Q loss
64.750 m kJ/kg = 78.75064.750 m kJ/kg = 81.988
Neraca energiH bahan masuk + Qin
-9624806.017 + 64.750-17.238
mSehingga :Q in = -11420321226.8493 kJ/hariQ out = -14460595931.8349 kJ/hari
Suhu bahan yang masuk dinaikkan hingga suhu 200 oC dengan menggunakan coal
OCOK
OCOK
m . Cp . (Ts - Tlar)
mm
BAB IVNERACA PANAS
B C D
0 0 0 25 2001.559E-01 0 0 25 200
B C D E
1.54E+02 -1.16E+02 3.29E+01 -2.49E-01 25-9.53E-03 -3.41E-05 1.58E-08 0 25
0 0 0 0 251.559E-01 0 0 0 25
4.184 joule
T1 OC T2 OC
T1 OC
4.184 joule
(Geankoplis, hal 963)
T = 25 - 200175
T = 25 - 200175
78.750 m kJ/ kg 3.23881.988 m kJ/ kg
= H bahan keluar + Qout= 3030649898.968 + 81.99= 3040274704.986= -176375617.403 kg
-11429946032.8666-11429946032.8666
+
H masuk H totalKj/Kmol Kj
110 -2036832.884874166382.5 -7587973.13244237TOTAL -9624806.01731637
H keluar H totalKj/kmol Kj
200 257988506.27104 3033732278.27906200 220.6325840781 -3082266.15919562200 110 -23.945516603200 166382.5 -89.206109139
TOTAL 3030649898.96824
H = 3040274704.98556
T2 OC
m kJ/ kg
81.99 m
BAB VSPESIFIKASI ALAT
Spesifikasi : Alat Sparator (Reri Aringga / 1314902)
Direncanakanbahan konstruksi = SA 240 grade C Type 347F allowable = 18750Tipe pengelasan = single welding butt join, E = 0.85Faktor korosi [C] = 1 / 16jumlah sparator = 1Temperatur (T) = 95Tekanan (P) = 32.7921 atm
a. menentukan volume separator 1 lbm =bahan fase gasbahan masuk = 1221.947212 kg/jam =densitas = 1.41 =rate volumetrik = bahan masuk =
density =
waktu operasi = 0.5 jamvolume gas = 2843.237172 x
= 2843.237172volume separatorvolume separator = volume gas
= 2843.237172
b. menentukan dimensi separator =volume separator = volume silinder +
= x4
= x4
2843.2371715 = 1.740828571 = 1633.266605
di = 11.77367181 ftdi = 141.2854971 in
c. menghitung tebal silinder
tebal silinder (ts) = Pi.di + C2(fE-0.6Pi)
OC
kg/m3
ft3/jamft3
ft3
di2
di2
ft3 di3di3 ft3
= 0.207940305 = 3.327044882 = 3
16 16do = di + 2tsdo = 141.6604971 indo = 11.80492149 ft
dari brownell tabel 5.7 hal 90 di dapatkan do = 144 inicr = 8.75r = 132ts = 7 / 16 =di baru = do baru - 2ts
= 143.125 in = 11.926962154 ft
d. menghitung tinggi silinderTinggi silinder (Ls) = 2 x di
= 286.25 in = 23.85392431 ft
e. menghitung dimensi tutup atas dan tutup bawahbentuk tutup atas dan bawah adalah standart dished, sehingga :tebal tutup (tha/b) = 0.885 x pi.di + C
2(fE-0.6Pi) = 0.192890504 = 3.086248061 = 3
16 16tinggi tutup (ha/b) = 0.169 x di
= 88.594375 in = 7.382864583 ft
f. menghitung tinggi sparatorTinggi sparator = tinggi silinder + tinggi tutup atas
= 286.25 + 0.1875 = 375.031875 in = 31.25265625 ft
Spesifikasi alat Sparatorfungsi = memisahkan produk fase uap dan liquidjumlah = 1waktu operasi = 1 jambahan konstruksi = CS SA 240 grade C Type 347volume tangki = 2843.23717153Diameter dalam (di) = 143.125 inDiameter luar (do) = 144 inTebal silinder (ts) = 0.4375 in
ft3
Tinggi Silinder (L) = 286.25 inTinggi tangki (H) = 375.031875 inTebal tutup atas (tha) = 3 in
16Tinggi tutup atas (ha) = 88.594375 inTebal tutup bawah (thb) = 3 in
16Tinggi tutup bawah (hb) = 88.594375 in
SPESIFIKASI ALAT
= 0.0625
0.45359 kg 3.2808 ft 39.37 in1 ft 12.000121921 in
2693.9465412 lb/jam0.947492727
2693.9465412 lb/jam0.947492727
2843.2371715
1 jam
3.14285714292xtutup standart dished
x Ls +
x 2di +
1m =
lb/ft3
lb/ft3ft3/jam
2(0.0847 di3)
2(0.0847 di3)
= 0.1875
0.4375
0.1875
tinggi tutup atas + tinggi tutup bawah + 88.594375
memisahkan produk fase uap dan liquid
CS SA 240 grade C Type 347
DATA eksport import international dari zauba.comimport eksport
Jan-12 100088 730493Feb-12 200020 746460Mar-12 220564 991595Apr-12 240244 727742
May-12 162244 775863Jun-12 360149 771846Jul-12 120151 864013
Aug-12 120579 860343Sep-12 480325 879044Oct-12 260240 866382Nov-12 180223 815897Dec-12 301125 1204801Jan-13 400213 626098Feb-13 160316 941410Mar-13 300794 1467436Apr-13 40470 898594
May-13 342625 1114596Jun-13 2451 791188Jul-13 930 1234772
Aug-13 100147 1202624Sep-13 300172 1003989Oct-13 260131 763219Nov-13 282863 769033Dec-13 296 1671000Jan-14 240815 1077121Feb-14 140156 1430369Mar-14 201530 1843392Apr-14 766 1317584
May-14 360073 1188837Jun-14 180547 1129053Jul-14 300440 1836658
Aug-14 340192 1600868Sep-14 100197 1307024Oct-14 240336 1054072
2012 2745952 102344792013 2191408 124839592014 2105052 13784978
tahun201020112012
M1 =M3 =
DATA Eksport Indonesia
Nitric Acid
DATA Import IndonesiaNitric Acid
Table Import by Month, Year 2008
Bulan/Month Nilai/Value (US $) Berat/Weight (KG)
9 608 052 713 8 348 821 589
9 842 865 892 8 975 081 428
Maret/March 10 276 652 560 8 407 307 563April/April 11 646 708 019 9 332 487 726
Mei/May 11 664 174 699 8 763 040 882Juni/June 12 110 556 910 8 681 091 282
Juli/July 12 869 784 594 8 782 228 964
12 326 249 588 8 317 156 498
11 296 068 452 8 172 480 300
10 732 446 784 7 867 576 749
9 081 376 305 6 894 664 898
7 742 369 708 6 122 404 080T O T A L 129197306224.00 98664341959.00
imporTahun Nilai/Value (US $) Berat/Weight (KG)2008 129197306224.00 98664341959.002009 96829244981.00 91354405895.00
2010 135663284048.00 110701002318.002011 177435555736.00 128221634466.00
2012 191691001109.00 136373421556.00
2013 186628669880.00 141109588134.00
eksporTahun Nilai/Value (US $) Berat/Weight (KG)2008 137020424402.00 355053970205.00 % kenaikan2009 116510026081.00 378999100814.00 -2010 157779103470.00 478846797632.00 -7.408893546
Januari/January
Pebruari/February
Agustus/August
September/September
Oktober/October
Nopember/November
Desember/December
2011 203496620060.00 582219779283.00 21.1775187342012 190031845244.00 600137346950.00 15.8269860082013 182551794701.00 700005037290.00 6.3575753998
3.47293961247.8852252417
zauba% kenaikan
-6.74
26.3521.593.08
16.6414.88
impor ekspor0.1 %kenaikan 16.3
#N/A - #N/A#N/A #N/A #N/A#N/A #N/A #N/A
#N/A#N/A M5 #N/A#N/A
Table Import by Month, Year 2009
Bulan/Month Nilai/Value (US $)
Januari/January 6 600 569 249
Pebruari/February 5 939 043 327Maret/March 6 554 129 163
April/April 6 706 761 999Mei/May 7 641 286 552Juni/June 7 935 474 878
Juli/July 8 683 341 932Agustus/August 9 707 302 686
8 516 603 276Oktober/October 9 430 126 548
Nopember/November 8 814 657 422
Desember/December 10 299 947 949T O T A L 96829244981.00
eksporNilai/Value (US $) Berat/Weight (KG) % kenaikan137020424402.00 355053970205.00 -116510026081.00 378999100814.00 6.7440819195
September/September
157779103470.00 478846797632.00 26.3451012426203496620060.00 582219779283.00 21.5879028871190031845244.00 600137346950.00 3.077457741182551794701.00 700005037290.00 16.6408057835
%kenaikan-
#N/A#N/A#N/A
M3
tahun produksi %kenaikan konsumsi
2010 40000 - #N/A2011 100000 1.5 #N/A2012 100000 0 #N/A
1.5M2 107728.4004 M4 #N/A
Table Import by Month, Year 2010
Berat/Weight (KG) Bulan/Month
6 408 533 613 Januari/January
5 353 812 083 Pebruari/February
5 977 694 304 Maret/March6 805 889 327 April/April7 567 751 961 Mei/May8 208 625 834 Juni/June7 865 271 031 Juli/July8 493 600 211 Agustus/August8 855 612 703 September/September
9 229 601 000 Oktober/October7 715 424 547 Nopember/November
8 872 589 281 Desember/December
91354405895.00 T O T A L
%kenaikan
-#N/A#N/A#N/A
Table Import by Month, Year 2010
Nilai/Value (US $)
9 490 458 938 Berat/Weight (KG)
9 498 139 407 8 244 314 490
10 972 641 400 8 087 892 28911 235 788 469 8 994 268 257
9 980 350 088 9 322 467 21611 760 001 067 8 562 152 39612 625 936 085 10 011 964 48012 171 550 612 9 877 129 572
9 654 127 469 9 643 683 306
12 120 016 599 7 218 710 61213 007 603 335 9 386 386 703
13 146 670 579 10 544 653 530
135663284048.00 10 807 379 467110701002318.00
Table Import by Month, Year 2011
Bulan/Month Nilai/Value (US $) Berat/Weight (KG)
Januari/January 12 558 694 259 9 742 084 622
Pebruari/February 11 749 862 451 9 446 513 223Maret/March 14 486 238 209 10 336 712 208
April/April 14 888 230 483 11 197 018 167Mei/May 14 825 868 915 11 008 941 300Juni/June 15 072 053 394 11 160 604 730
Juli/July 16 207 276 766 11 766 305 270Agustus/August 15 075 369 345 11 021 766 281
September/September 15 169 115 540 10 048 394 239Oktober/October 15 533 378 964 10 411 631 977
Nopember/November 15 393 896 679 10 705 349 201
Desember/December 16 475 570 731 11 376 313 248T O T A L 177435555736.00 128221634466.00
Table Import by Month, Year 2012
Bulan/Month Nilai/Value (US $)
Januari/January 14 554 618 780
Pebruari/February 14 866 785 109Maret/March 16 325 662 478
April/April 16 937 875 721Mei/May 17 036 735 320Juni/June 16 727 521 763
Juli/July 16 354 450 283Agustus/August 13 813 875 810
September/September 15 348 557 469Oktober/October 17 207 931 360
Nopember/November 16 935 009 726
Desember/December 15 581 977 290T O T A L 191691001109.00
Table Import by Month, Year 2013
Berat/Weight (KG) Bulan/Month
9 670 613 447 Januari/January
11 041 167 920 Pebruari/February11 234 783 756 Maret/March11 579 459 958 April/April11 877 761 174 Mei/May12 279 593 528 Juni/June11 541 325 367 Juli/July10 127 266 344 Agustus/August
10 806 825 885 September/September12 379 019 206 Oktober/October
12 498 589 864 Nopember/November
11 337 015 107 Desember/December136373421556.00 T O T A L
Table Import by Month, Year 2013
Nilai/Value (US $) Berat/Weight (KG)
15 450 235 320 11 925 159 622
15 313 286 233 10 904 690 18814 887 075 645 11 018 318 05016 463 468 844 12 210 318 91116 660 559 292 12 610 027 73915 636 019 963 11 925 604 33317 416 991 671 13 229 872 05813 012 045 835 9 897 645 784
15 509 774 940 11 291 921 78915 674 021 743 12 103 233 550
15 149 325 413 11 653 190 043
15 455 864 981 12 339 606 067186628669880.00 141109588134.00
imporTahun Nilai/Value (US $) Berat/Weight (KG) % kenaikan
2008 $ 129,197,306,224.00 98664341959.00 -2009 $ 96,829,244,981.00 91354405895.00 -7.412010 $ 135,663,284,048.00 110701002318.00 21.182011 $ 177,435,555,736.00 128221634466.00 15.832012 $ 191,691,001,109.00 136373421556.00 6.362013 $ 186,628,669,880.00 141109588134.00 3.47
7.89nilai impor pada th 2018M1 = jumlah tahun terakhir x (1+ kenaikan rata -rata)^selisih tahunM1 = 206236907267.29 kg/th
206236907.267294 ton/ th
nilai ekspor pada th 2018M2= 1400572900878.12
1400572900.87812
eksporNilai/Value (US $) Berat/Weight (KG) % kenaikan $ 137,020,424,402.00 355053970205.00 - $ 116,510,026,081.00 378999100814.00 6.74 $ 157,779,103,470.00 478846797632.00 26.35 $ 203,496,620,060.00 582219779283.00 21.59 $ 190,031,845,244.00 600137346950.00 3.08 $ 182,551,794,701.00 700005037290.00 16.64
14.88
M1 = jumlah tahun terakhir x (1+ kenaikan rata -rata)^selisih tahun
2006 1,365,894.002007 1,988,765.00 0.45601708482008 2,598,076.00 0.30637657042009 3,847,890.00 0.4810536722010 5,538,655.00 0.43940055462011 6,988,943.00 0.261848409
0.3889392582pangkat 2
pangkat 3 pangkat 22010 3.9141066E+014 Err:5022011 3.9160549E+014 Err:5022012 3.9180032E+014 Err:5022013 3.9199515E+014 Err:5022014 3.9218998E+014 Err:5022015 3.9238481E+014 Err:502 12016 3.9257964E+014 Err:502 pangkat 3 -16048.532017 3.9277447E+014 Err:5022018 3.9296930E+014 Err:502 pangkat 3 -16048.532019 3.9316413E+014 Err:502
pangkat 2 Err:502
Err:502
2005 2006 2007 2008 2009 2010 2011 20120.00
1,000,000.00
2,000,000.00
3,000,000.00
4,000,000.00
5,000,000.00
6,000,000.00
7,000,000.00
8,000,000.00
f(x) = 151123.232171669x^2 - 605918745.662213x + 607349044022.922R = 0.9966004187
2 3 496851527 -2E+011 1.3064E+014
96851527 -2E+011 1.3064E+014
Err:502 Err:502
Err:502 Err:502 Err:502
2005 2006 2007 2008 2009 2010 2011 20120.00
1,000,000.00
2,000,000.00
3,000,000.00
4,000,000.00
5,000,000.00
6,000,000.00
7,000,000.00
8,000,000.00
f(x) = 151123.232171669x^2 - 605918745.662213x + 607349044022.922R = 0.9966004187
Nermas nitric acidneraca massa (tingkat reaksi)neraca panasspesifikasi sparatordata ekspor impor% kenaikanimpor bps