perhitungan evaporator

Stasiun Penguapan EvaporatorEvaluasi evaporator (Quadruple Effect)

Dara Operasional laporan periode VIII (01 - 15 September 2015) PG BungamayangKapasitas Pabrik = 85538.3 =

336 =NM%Tebu = 109.48

Brix NM = 11.5Berat Jenis NM = 1.0422

NE % Tebu = 104.776Brix NE = 11.29 %Brix NK = 62.965 %

Tekanan UBE = 0.7 Kg/cm3.g ==

T UBE = 116.086163241 steam tableP UN4 = 64 cmHg (g)

= 12 cmHg (abs) =T UN4 = 55.3359535202 oC (steam table)

Pressure drop = 117.2 cmHg

Distribusi Tekanan tiap badan evaporatorkoefisien tekanan diambil dari hugot 579 untuk Qadruple yaitu 11/40; 10,3/40; 9,7/40; 9/40BP1 96.97 CmHgBP2 66.791 CmHgBP3 38.37 CmHgBP4 12 CmHg abs

Uap Tekanan T UapUbe 1.7 116.086163241UN1 1.2759210526 107.2882320004UN2 0.8788289474 96.7026424408UN3 0.5048684211 82.2377280517UN4 0.1578947368 55.3359535202

atmCp = 1 -Cp = 0.93226

Desain Bleeding untuk memanasi nira1. UN1

- Vacum Pan (VP)(Hugot 589)= 120= 30.5493928571- JH1juice after heater 1

T awal

oC

kkal/kg.oC

T akhirHeat Coef

Heating Media TPanas laten

bleeding steam use

-JH2Juice after heater 2

T awalT akhirHeat Coef

Heating Media TPanas laten

bleeding steam use

-JH DiffuserJuice after Heater 1

T awalT akhirHeat coef

Heating MediaTPanas laten

Bleeding steam use (UN1)

total vapor bleeding UN1(y) =2. UN2

-JH1Juice after Heater 1

T awalT akhir

Heating MediaTPanas laten

Bleeding steam use

Total Vapor Bleeding UN2(z) =

W = UN1 + UN2 + UN3 + UN4 .(i)UN1 = y +x UN2 = z + x UN3 = UN4 = xW = ((y + x)+(z + x)+x+x) = y + z + 4x

W = (1-br NE/ bx NK) G .. (ii)W = 218909.409508656W = 218.9094095087 ton uap air /jamx = 46.4206513762UN1 = y +x = 79.3717315455 ton uap air/jamUN2 = x + z = 46.6963752107 ton uap air/jamUN3 = UN4 = x = 46.4206513762 ton uap air/jamtotal evaporasi 218.9094095087perhitungan nilai brixMasuk BP1 = (b0) 11.29Masuk BP2 = (b1) 11.29 x

Masuk BP3 = (b2) 11.29 x

Masuk BP4 = (b3) 11.29 x

Keluar BP4 = (b4) 11.29 x

brix rata - ratab1= 13.6813374687b2= 18.7404147771b3= 26.6803017553b4= 47.4587244469

Perhitungan Boiling Point Rise (E BPR = 2b/(100 - t) (Hugot 497)BP Brix rata-rata suhu uap1 13.6813374687 107.28823200042 18.7404147771 96.70264244083 26.6803017553 82.23772805174 47.4587244469 55.3359535202

C

Perhitungan koefisien penggunaan spesifik dengan desain formula (Hugot 572)c = 0.001(100-brix rata-rata)*(Temp vapour -54)c1 = 5.3591945727c2 = 4.3301796296c3 = 3.130944858c4 = 1.4836462506

Perhitungan Luas Pemanas, Si = q/(cp.T)S1 =

5.3591945727 xS2 =

4.3301796296 xS3 =

3.130944858 x

S4 =1.4836462506 x

dari perhitungan di atas dapat digunakan perstandaran luas pemanas yang ada

BP

1

234

LP totalSetiap hari dilakukan cleaning 1 unit evaporator, sehingga dalam 10 hari rata-rata LP Cleaning didekati denganrata-rata sebagai berikutLP rata-rata = LP Total - LP rata-rata cleaning persiklus =

AP keseluruhan (total)AP = Jumlah air yang diuapkan

Luas pemanastotal air yang diuapkan = 218909.409508656Total Si 14040angka penguapan = 218909.409508656 =

14040Perhitungan angka penguapan tiap badan evaporatorEVA brix analisa Nira in

(kg/jam)NE 11.29BP 1 16.07 266736.932BP 2 21.41 187365.201BP 3 31.95 140668.825BP 4 62.965 94248.174Total

Neraca massaBP Input

I Gnira = 266736.932- Brik nira

- Air nira

total = 266736.932II 187365.200621138

- Brik nira- Air nira

total = 187365III G nira = 140668.825410412


total = 140668.825410412IV G nira = 94248.1740342115


total = 94248.1740

Menghitung Q lostHeat loss

1AVariabel Tube DindingBahan Stainless steel Stainless steelPanjang (m) 2.5 10.5Kond. Termal 0.1078 0.1078Ai 2041.314 156.9372Ao 2226.888 157.66254Do 0.036 4.782Di 0.033 4.76tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001

Menghitung Hi menghitung HoFlowrate 266,737 TjuiceKs 0.1078 TwR tube Outside 0.018 TbR tube inside 0.0165 delta Tviskositas nira 0.001054 Tf

cross sec. area 0.00101736 roG 262185393.731488 miuNre 8955098837.12862 kbrix nira i 13.6813374687 NprCp nira 0.9179119752 BNpr 0.0089747609 LNu 513682.021766491 ghi 3076384.55257932 Ngr

a, NGr >10^9m, NGr >10^9Nuho

2AVariabel Tube DindingBahan Stainless steel Stainless steelPanjang (m) 2.5 10.5Kond. Termal 0.1078 0.1078Ai 1499.3814 156.9372Ao 1635.6888 157.66254Do 0.036 4.782Di 0.033 4.76tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001

Menghitung Hi menghitung HoFlowrate 266,737 TjuiceKs 0.1078 TwR tube Outside 0.018 TbR tube inside 0.0165 delta Tviskositas nira 0.001054 Tfcross sec. area 0.00101736 roG 262,185,394 miuNre 8955098837.12862 kbrix nira i 13.6813374687 NprCp nira 0.9179119752 BNpr 0.0089747609 LNu 513682.021766491 ghi 3076384.55257932 Ngr

a, NGr >10^9m, NGr >10^9Nu

ho

Heat lost untuk pipaBP1Variabel pipa insulatorBahan Stainless steel silika boldPanjang (m) 15 15Kond. Termal 0.1078 0.1078Ai 35.325 47.1Ao 35.9844 49.455Do 0.764 1.05Di 0.75 1tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001

Menghitung Hi menghitung HoFlowrate 266,737 TjuiceKs 0.1078 TwR tube Outside 0.382 TbR tube inside 0.375 delta Tviskositas nira 0.001054 Tfcross sec. area 0.45820136 roG 582,139 miuNre 421968008.032239 kbrix nira i 13.6813374687 NprCp nira 0.9179119752 BNpr 0.0089747609 LNu 44592.4855211553 ghi 12583.9527203679 Ngr


BP2Variabel pipa insulatorBahan Stainless steel Stainless steelPanjang (m) 15 15Kond. Termal 0.1078 0.1078Ai 35.325 47.1

Ao 35.9844 49.455Do 0.764 1.05Di 0.75 1tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001



BP3Variabel pipa insulatorBahan Stainless steel Stainless steelPanjang (m) 15 15Kond. Termal 0.1078 0.1078Ai 35.325 47.1Ao 35.9844 49.455Do 0.764 1.05Di 0.75 1tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001

Menghitung Hi menghitung HoFlowrate 140,669 TjuiceKs 0.1078 Tw

R tube Outside 0.382 TbR tube inside 0.375 delta Tviskositas nira 0.001054 Tfcross sec. area 0.45820136 roG 307,002 miuNre 222532903.743444 kbrix nira i 26.6803017553 NprCp nira 0.8399181895 BNpr 0.0082121871 LNu 25947.6937967754 ghi 7322.41201909 Ngr


BP4Variabel pipa insulatorBahan Stainless steel Stainless steelPanjang (m) 15 15Kond. Termal 0.1078 0.1078Ai 35.325 47.1Ao 35.9844 49.455Do 0.764 1.05Di 0.75 1tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001



Panas yang hilangNo. BP Qlost eva (kcal)

1 I 13826.26045046652 II 4106.64338199083 III 5509.02373661934 IV 9627.6397651958

Neraca panasTref =

No. BP Input

1 IV Nira-Gnira-Cpnira-TniraUN3-G Un3-Hv

total 33892902.2302 III Nira

-Gnira-Cpnira-TniraUN2-G Un2-Hv

total 40605225.2283 II Nira

-Gnira-Cpnira-TniraUN1-G Un1-Hv

total 48210812.4484 I Nira

-Gnira-Cpnira-TniraUbe-G ube-Hv

total 79480855.470

neraca energi 28,099,503.48 529.0658136504

Perhitungan Steam EkonomiSteam Ekonomi : V1 + V2 + V3 +V4 =S

254.5782738095 ton/jam254578.273809524 kg/jam

1.7 atm129.2 cmHg

0.1578947368 atm

Delta T r (laten heat) Hv529.0658136504 645.4742053219

8.7979312406 534.8038712349 642.311746654110.5855895595 517.5999038078 614.45724086614.4649143891 511.6842294084 593.973535770126.9017745316 566.4340621892 621.7904208853

kkal/kg0.006 *b (Brix NE)

kg uap/ton tebu 254.5782738095 TCH*Ton uap/jam 30549.3928571429

JH Quadkg/hour 27871.2294166667C 70

oC

C 780.931

UN1C 107.2882320004KJ/kg 534.8038712349kg/hour 426.9666332773ton/hour 0.4269666333

kg/hour 27871.2294166667C 78C 105

0.931UN1

C 107.2882320004KJ/kg 534.8038712349kg/hour 1441.012387311ton/hour 1.4410123873

kg/hour 27871.2294166667C 70C 80

0.931UN1

C 107.2882320004KJ/kg 534.8038712349kg/hour 533.7082915967ton/hour 0.5337082916

32.9510801693 ton uap/jam

JH Quadkg/hour 27871.2294166667C 65C 70

UN2C 96.7026424408KJ/kg 517.5999038078kg/hour 275.7238345257ton/hour 0.2757238345

0.2757238345 ton uap/jam

, maka :

ton uap air/ jam

1.04776 x 254.5782738095266.7369321667 - 79.3717315455

1.04776 x 254.5782738095187.3652006211 - 46.6963752107

1.04776 x 254.5782738095140.6688254104 - 46.4206513762

1.04776 x 254.578273809594.2481740342 - 46.4206513762

Ton Nira (C) 90BPR Titik didih nira hl

0.3169960485 107.6052280489 116.40839167150.4612481032 97.1638905441 107.50787541910.7277799116 82.9655079634 96.85733705821.8065311109 57.1424846311 82.2893063617C kcal/kg

79371.73154552848.7979312406 x 1

79371.731545528410.5855895595 x 1

79371.731545528414.4649143891 x 1

79371.731545528426.9017745316 x 1

Total = 7156.1826479944

Luas Pemanas lapanganA B

2000 20001500 20001500 15001200 15001200 1200

15600Setiap hari dilakukan cleaning 1 unit evaporator, sehingga dalam 10 hari rata-rata LP Cleaning didekati dengan

15600 -

kg uap air/jam

15.5918382841

Nira Out Uap dihasilkan LP (kg/jam) (kguap/jam) (m2)

187365.201 79371.732 7110.000140668.825 46696.375 2610.000

94248.174 46420.651 2310.00047827.523 46420.651 2010.000

218909.410 14040.000

Input Output G nira = (brix in/brix out) x Gnira input

kg/jam Gnira = 187365.20062113830115 - Brik nira

m2

kg uap/jamm2

236622 - Air niraair yang diuapkan = 79371.7315455283

total = 266736.932kg/jam G nira = 140668.825410412

30115 - Brik nira157251 - Air nira

air yang diuapkan = 46696.3752107263total = 187365

kg/jam G nira = 94248.174034211530115 - Brik nira

110554 - Air niraair yang diuapkan = 46420.6513762005total = 140668.825410412

kg/jam G nira = 47827.52265801130115 - Brik nira64134 - Air nira

air yang diuapkan = 46420.6513762005total = 94248.1740342115

Insulator 1Silikal bold

10.50.2308164.85

166.49855.05

5

menghitung Qlost107.61 Tjuice 107.61

76 Tb 4040 AiT 2041.31436 teb. Dinding 0.022

0 tebal silika 0.05

1.0712 AlnD 157.29959127610.00002017 AlnS 165.6728830756

0.0266 K stainls 0.10780.0006960257 ksilika 0.23080.0172413793 hi 3076384.55257932

10.5 ho 1.60553967919.8 Ri 1.59239044846E-010

19860849099027.1 Rd 0.00064870360.13 Rs 0.00065381180.33 Ro 0.0037408357

288.6349904324 Qlost 3490.77964247961.6055396791

Insulator 1Silikal

10.50.2308164.85

166.49855.05

5


76 Tb 4040 AiT 1499.381436 teb. Dinding 0.022

0 tebal silika 0.051.0712 AlnD 157.2995912761

0.00002017 AlnS 165.67288307560.0266 K stainls 0.1078

0.0006960257 ksilika 0.23080.0172413793 hi 3076384.55257932

10.5 ho 1.60553967919.8 Ri 2.16794000240E-010

19860849099027.1 Rd 0.00064870360.13 Rs 0.00065381180.33 Ro 0.0037408357

288.6349904324 Qlost 3490.7796026427

1.6055396791


76 Tb 4040 AiT 35.32536 tebal silika 0.05

0 Alns 48.26792531011.0712 ksilika 0.1078

0.00002017 hi 12583.95272036790.0266 ho 10.4086464285

0.0006960257 Alnpipa 35.65368372850.0172413793 Rinside pipa 2.24957642241E-006

15 Rinsulator 0.00480465959.8 Rluar isolasi 0.0019426544

57903350142936.1 Rpipa 0.00182127230.13 Qlost 2054.08535027970.33

410.86762217910.4086464285



0 Alns 48.26792531011.0712 ksilika 0.1078

0.00002017 hi 9380.66280096050.0266 ho 10.2937771191



57903350142936.1 Rpipa 0.00182127230.13 Qlost 1215.05814806650.33

406.33330733410.2937771191


76 Tb 40

40 AiT 35.32536 tebal silika 0.05

0 Alns 48.26792531011.0712 ksilika 0.1078

0.00002017 hi 7322.412019090.0266 ho 10.1080671879

0.0006368853 Alnpipa 35.65368372850.0172413793 Rinside pipa 0.000003866


57903350142936.1 Rpipa 0.00182127230.13 Qlost 1645.19358211950.33

399.002652152810.1080671879



0 Alns 48.26792531011.0712 ksilika 0.1078

0.00002017 hi 5037.95225821830.0266 ho 9.5860687674



57903350142936.1 Rpipa 0.0018212723

0.13 Qlost 2954.27383943930.33

378.39745134479.5860687674

Qlost pipa (kcal) Qlost total (kcal)2054.0853502797 15880.34580074621215.0581480665 5321.70153005721645.1935821195 7154.21731873882954.2738394393 12581.9136046351

0Input output

6320263.800 Nira 1528407.34594248.174 -Gnira 47827.523

0.808 -Cpnira 0.55982.966 -Tnira 57.142

27572638.431 UN4 28863916.35746420.651 -Gun4 46420.651

593.974 -hv 621.790Kond 3819923.203-Gkond 46420.651-hl 82.289Qlost 12581.914Quncond -331926.588

33892902.23011912299.357 Nira 6320263.800

140668.825 -Gnira 94248.1740.872 -Cpnira 0.808

97.164 -Tnira 82.96628692925.870 UN3 27572638.431

46696.375 -Gun3 46420.651614.457 -hv 593.974

Kond 4496180.677-Gkond 46420.651

-hl 96.857Qlost 7154.217Quncond 2208988.103

40605225.22818217182.124 Nira 11912299.357

187365.201 -Gnira 140668.8250.904 -Cpnira 0.872

107.605 -Tnira 97.16429993630.324 UN2 28692925.870

46696.375 -Gun2 46696.375642.312 -hv 614.457

Kond 5020228.089-Gkond 46696.375-hl 107.508Qlost 5321.702Quncond 2580037.430

48210812.44828099503.479 Nira 18217182.124

266736.932 -Gnira 187365.2010.932 -Cpnira 0.904

113.000 -Tnira 107.60551381351.991 UN1 50981395.524

79602.487 -Gun1 79371.732645.474 -hv 642.312

Kond 9266397.476-Gkond 79602.487-hl 116.408Qlost 15880.346Quncond 1000000.000

79480855.470

+ 645.4742053219 m529.0658136504 m

m

218,909.41 = 2.75 79,602.49

hl116.4083916715107.5078754191

96.857337058282.289306361755.3563586961

1

= 16.0726749374

= 21.4081546169

= 31.9524488938

= 62.965

delta T17.605228048910.441337504814.198382580725.8230233323

= 1683.3939669395

= 1731.5892912487

= 1752.5667514874

m2

m2

m2

= 1988.6326383187

1560 = 1404014040

AP efisiensi(kg uap/jam m2)

11.163 47%17.891 75%20.096 84%23.095 96%15.592 65%

Output G nira = (brix in/brix out) x Gnira input

kg/jam30115

m2

157251kg uap air/jam

kg/jam30115

110554kg uap air/jam

kg/jam3011564134

kg uap air/jam

kg/jam3011517713

kg uap air/jam

1B, 2BVariabel TubeBahan Stainless steelPanjang (m) 2Kond. Termal 0.1078Ai 3999.732Ao 4363.344Do 0.036Di 0.033tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001

Menghitung HiFlowrate 266,737 Ks 0.1078R tube Outside 0.018R tube inside 0.0165viskositas nira 0.001054

cross sec. area 0.00101736G 262185393.731488Nre 8955098837.12862brix nira i 13.6813374687Cp nira 0.9179119752Npr 0.0089747609Nu 513682.021766491hi 3076384.55257932

3A, 3BVariabel TubeBahan Stainless steelPanjang (m) 2.5Kond. Termal 0.1078Ai 2998.7628Ao 3271.3776Do 0.036Di 0.033tebal pipa (m) = 0.014Tebal isolasi (m) = 0.05tebal dinding(m) = 0.022tebal tube (m) = 0.001

Menghitung HiFlowrate 187,365 Ks 0.1078R tube Outside 0.018R tube inside 0.0165viskositas nira 0.001054cross sec. area 0.00101736G 184168043.387924Nre 6290369603.3826brix nira i 18.7404147771Cp nira 0.8875575113Npr 0.0086779742Nu 382922.436231642hi 2293279.92365395

output/total (%)

0.045

0.852

0.113

0.000-0.010

0.156

0.679

0.111

0.0000.054

0.247

0.595

0.104

0.0000.054

0.229

0.641

0.117

0.0000.013

1015880.346

= 70,214,457.99 += 42,114,954.51 = 79,602.49 kguap/jam

47%75%84%96%

ap total

15.591838284124

65%

P172.2525

129.282700657989.047343092151.155792763215.9986842105

Perhitungan kebutuhan uap bekas untuk BP I

T Nira Encer = 113AsumsiUBE x panas laten UBE =UBE x 529.0658136504 =

UBE =

V.Hv T1 + 0.051355591.84310998 + S 529 1355591.84310998 + S 502.6125229679

S

Line AEvaporator Satuan I Aluas pemanas m2 2000Diameter dinding m 4.76tebal dinding m 0.022

F.cf.(T1 - Tf) + S.(),Ts =

tinggi evaporator m 10.5diameter tube m 0.033tebal tube m 0.001jumlah tube 7880

Line BEvaporator Satuan I Bluas pemanas m2 2000

Diameter dinding m 4.76tebal dinding m 0.022tinggi evaporator m 10.5

diameter tube m 0.033tebal tube m 0.001jumlah tube 9650

Dinding Insulator 1Stainless steel Silikal

10.5 10.50.1078 0.2308

324.0951 329.7325.54578 332.997

4.937 5.054.915 5

menghitung HoTjuice 107.61Tw 76Tb 40delta T 36Tf 0

ro 1.0712miu 0.00002017k 0.0266Npr 0.0006960257B 0.0172413793L 10.5g 9.8Ngr 19860849099027.1a, NGr >10^9 0.13m, NGr >10^9 0.33Nu 288.6349904324ho 1.5551328227


10.5 10.50.1078 0.2308

313.8744 329.7315.32508 332.997

4.782 5.054.76 5

menghitung HoTjuice 97.16Tw 76Tb 40delta T 36Tf 0ro 1.0712miu 0.00002017k 0.0266Npr 0.0006730088B 0.0172413793L 10.5g 9.8Ngr 19860849099027.1a, NGr >10^9 0.13m, NGr >10^9 0.33Nu 285.4496288919

ho 1.5878210223

116.4083916715 m

brix nira densitas6 1.01997 1.02388 1.02799 1.0320

10 1.036111 1.040212 1.044313 1.048514 1.052715 1.0569

t

P T 116.09198.53 120 107.29

232.1 125 96.7082.24

143.27 110 55.34169.06 115

101.33 100108.78 102

60.11 8662.49 87

15.74 5516.51 56

oC

UN1 x Panas Laten UN179371.7315455284 534.803871234980232.5688070567 kg/jam

= 42448309.2971691 + 0.05 (S 529.07= 42448309.2971691= 81758.2443258846 kg/s= 294329.679573185 ton/jam

II A III A IV A VA1500 1500 1200 1200.004.76 4.76 4.76 4.76

0.022 0.022 0.022 0.022

( S.(),Ts)

10.5 10.5 10.5 10.50.033 0.033 0.033 0.0330.001 0.001 0.001 0.0015788 5788 5788 5788.00

II B III B IV B VB2000 1500 1500 1200.00

4.76 4.76 4.76 4.760.022 0.022 0.022 0.022

10.5 10.5 10.5 10.5

0.033 0.033 0.033 0.0330.001 0.001 0.001 0.0019650 5788 5788 5788.00

4AVariabelBahanPanjang (m)Kond. TermalAiAoDoDitebal pipa (m) =Tebal isolasi (m) =tebal dinding(m) =tebal tube (m) =

menghitung Qlost Menghitung HiTjuice 107.61 FlowrateTb 40 KsAiT 3999.732 R tube Outsideteb. Dinding 0.022 R tube insidetebal silika 0.05 viskositas nira

AlnD 324.8199000927 cross sec. areaAlnS 331.3457661511 GK stainls 0.1078 Nreksilika 0.2308 brix nira ihi 3076384.55257932 Cp niraho 1.5551328227 NprRi 8.12696679655E-011 NuRd 0.0003141458 hiRs 0.0003269059Ro 0.0019310441Qlost 6844.7012053442

4BVariabelBahanPanjang (m)Kond. TermalAiAoDoDitebal pipa (m) =Tebal isolasi (m) =tebal dinding(m) =tebal tube (m) =

menghitung Qlost Menghitung HiTjuice 97.16 FlowrateTb 40 KsAiT 2998.7628 R tube Outsideteb. Dinding 0.022 R tube insidetebal silika 0.05 viskositas niraAlnD 314.5991825521 cross sec. areaAlnS 331.3457661511 GK stainls 0.1078 Nreksilika 0.2308 brix nira ihi 2293279.92365395 Cp niraho 1.5878210223 NprRi 1.45412190320E-010 NuRd 0.0003243518 hiRs 0.0003269059Ro 0.00189129Qlost 4106.6433819908

t hv hl

120 2706.3 503.71125 2713.5 524.99

110 2691.5 461.3115 2699 482.48

100 2576 419.1102 2579.1 427.5

86 2489.7 360.187 2490.9 364.3

55 2601 230.256 2602.7 234.4

Tube Dinding Insulator 1Stainless steel Stainless steel Silikal

2 10.5 10.50.1078 0.1078 0.2308

1199.50512 156.9372 164.851308.55104 157.66254 166.4985

0.036 4.782 5.050.033 4.76 50.014

0.050.0220.001

menghitung Ho 140,669 Tjuice 82.97

0.1078 Tw 760.018 Tb 40

0.0165 delta T 360.001054 Tf 0

0.00101736 ro 1.0712138268484.519159 miu 0.000020174722642734.99975 k 0.0266

26.6803017553 Npr 0.00063688530.8399181895 B 0.01724137930.0082121871 L 10.5

298903.809777143 g 9.81790101.70522089 Ngr 19860849099027.1

a, NGr >10^9 0.13m, NGr >10^9 0.33Nu 280.2998349587ho 1.5591751589


2.5 10.5 10.50.1078 0.1078 0.2308

1499.3814 156.9372 164.851635.6888 157.66254 166.4985

0.036 4.782 5.050.033 4.76 50.014

0.050.0220.001


0.1078 Tw 760.018 Tb 40

0.0165 delta T 360.001054 Tf 0

0.00101736 ro 1.0712138268484.519159 miu 0.000020174722642734.99975 k 0.0266

26.6803017553 Npr 0.00063688530.8399181895 B 0.01724137930.0082121871 L 10.5

298903.809777143 g 9.81790101.70522089 Ngr 19860849099027.1

a, NGr >10^9 0.13m, NGr >10^9 0.33Nu 280.2998349587

ho 1.5591751589

5A, 5BVariabelBahanPanjang (m)Kond. TermalAiAoDoDitebal pipa (m) =Tebal isolasi (m) =tebal dinding(m) =tebal tube (m) =

menghitung Qlost Menghitung HiTjuice 82.97 FlowrateTb 40 KsAiT 1199.50512 R tube Outsideteb. Dinding 0.022 R tube insidetebal silika 0.05 viskositas nira

AlnD 157.2995912761 cross sec. areaAlnS 165.6728830756 GK stainls 0.1078 Nreksilika 0.2308 brix nira ihi 1790101.70522089 Cp niraho 1.5591751589 NprRi 4.65714958740E-010 NuRd 0.0006487036 hiRs 0.0006538118Ro 0.0038520753Qlost 2754.5118434228

menghitung QlostTjuice 82.97Tb 40AiT 1499.3814teb. Dinding 0.022tebal silika 0.05AlnD 157.2995912761AlnS 165.6728830756K stainls 0.1078ksilika 0.2308hi 1790101.70522089ho 1.5591751589Ri 3.72571966992E-010Rd 0.0006487036Rs 0.0006538118Ro 0.0038520753Qlost 2754.5118931965


2 10.5 10.50.1078 0.1078 0.2308

2399.01024 313.8744 329.72617.10208 315.32508 332.997

0.036 4.782 5.050.033 4.76 50.014

0.050.0220.001


0.1078 Tw 760.018 Tb 40

0.0165 delta T 360.001054 Tf 0

0.00101736 ro 1.071292639944.5960246 miu 0.000020173164172680.69913 k 0.0266

47.4587244469 Npr 0.00054235130.7152476533 B 0.01724137930.0069932377 L 10.5

205651.241630617 g 9.81231622.43598781 Ngr 19860849099027.1

a, NGr >10^9 0.13m, NGr >10^9 0.33Nu 265.8246570253ho 1.4786566033

menghitung QlostTjuice 57.14Tb 40AiT 2399.01024teb. Dinding 0.022tebal silika 0.05

AlnD 314.5991825521AlnS 331.3457661511K stainls 0.1078ksilika 0.2308hi 1231622.43598781ho 1.4786566033Ri 3.38446717690E-010Rd 0.0003243518Rs 0.0003269059Ro 0.0020309178Qlost 9627.6397651958

BP2Variabel Tube Dinding Insulator 1Bahan Stainless steel Stainless steel SilikalPanjang (m) 2.5 10.5 10.5Kond. Terma 0.1078 0.1078 0.2308Ai 1499.3814 313.8744 329.7Ao 1635.6888 315.32508 332.997Do 0.036 4.782 5.05Di 0.033 4.76 5

Menghitung Hi menghitung HoFlowrate 187,365 Tjuice 102.33Ks 0.1078 Tw 76Diameter tu 0.036 Tb 40viskositas n 0.001215 delta T 36cross sec. a 0.00101736 Tf 0G 184168043.387924 ro 1.0712Nre 5456830915.19775 miu 0.0000199brix nira i 21.1379053877 k 0.0266Cp nira 0.8731725677 Npr 0.0006532381Npr 0.0098414162 B 0.0172413793

Nu 356398.084990881 L 10.5hi 1067214.26561158 g 9.8

Ngr 20403442822209.5a, NGr >10^9 0.13m, NGr >10^9 0.33Nu 285.1800199769ho 0.7224560506

BP3Variabel TubeBahan Stainless steelPanjang (m) 2Kond. Terma 0.1078Ai 1199.50512Ao 1308.55104Do 0.036Di 0.032

menghitung Qlost Menghitung HiTjuice 102.33 Flowrate 140,669 Tb 40 Ks 0.1078AiT 1499.3814 Diameter tu 0.036teb. Dinding 0.022 viskositas n 0.001545tebal silika 0.05 cross sec. a 0.00101736AlnD 314.5991825521 G 138268484.519159AlnS 331.3457661511 Nre 3221789930.54352K stainls 0.1078 brix nira i 45.21ksilika 0.2308 Cp nira 0.72874hi 1067214.26561158 Npr 0.010444372

ho 0.7224560506 Nu 238489.346612693Ri 0.000000003 hi 714143.099023564Rd 0.0003243518Rs 0.0003269059Ro 0.0041566958Qlost 2346.5920581531


10.5 10.50.1078 0.2308

313.8744 329.7315.32508 332.997

4.782 5.054.76 5

menghitung Ho menghitung QlostTjuice 86.91 Tjuice 86.91Tw 76 Tb 40Tb 40 AiT 1199.50512delta T 36 teb. Dinding 0.014Tf 58 tebal silika 0.05ro 1.0712 AlnD 314.5991825521miu 0.0000199 AlnS 331.3457661511k 0.0266 K stainls 0.1078Npr 0.0005451852 ksilika 0.2308B 0.0172413793 hi 714143.099023564

L 10.5 ho 0.6806084959g 9.8 Ri 4.461273623257E-009Ngr 20403442822209.5 Rd 0.0003243518a, NGr >10^9 0.13 Rs 0.0003269059m, NGr >10^9 0.33 Ro 0.0044122724Nu 268.6612483633 Qlost 2228.1496324998ho 0.6806084959

BP4Variabel Tube Dinding Insulator 1Bahan Stainless stStainless stSilikalPanjang (m) 2 10.5 10.5Kond. Terma 0.1078 0.1078 0.2308Ai 1199.5051 313.8744 329.7Ao 1308.551 315.32508 332.997Do 0.036 4.782 5.05Di 0.032 4.76 5

Menghitung Hi menghitung Ho menghitung QlostFlowrate 94,248 Tjuice 57.30 Tjuice 57.30Ks 0.1078 Tw 76 Tb 40Diameter tu 0.036 Tb 40 AiT 1199.5051viskositas n 0.001974 delta T 36 teb. Dinding 0.014cross sec. a 0.0010174 Tf 58 tebal silika 0.05G 92639945 ro 1.0712 AlnD 314.59918Nre 1.69E+009 miu 0.0000199 AlnS 331.34577brix nira i 49.539299 k 0.0266 K stainls 0.1078Cp nira 0.7027642 Npr 0.0005258 ksilika 0.2308Npr 0.0128688 B 0.0172414 hi 456803

Nu 152550.17 L 10.5 ho 0.6725051hi 456803 g 9.8 Ri 6.97E-009

Ngr 2.04E+013 Rd 0.0003244a, NGr >10 0.13 Rs 0.0003269m, NGr >1 0.33 Ro 0.0044654Nu 265.46254 Qlost 2204.9966ho 0.6725051

Sheet1

perhitungan evaporator

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