Panas Pembentukan Inlet Steam Digester [PDF]

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= 0,8952967 kmol x 2846,591 kkal/kmol.K x (10)K = 25485,435 kkal -Ekstraktif T1 = T2 = Q



25°C = 298K (reference) 35°C = 308K = n x cp x ΔT = 27,580235 kmol x 18,02 kkal/kmol.K x (10)k=K = 4969,9584 kkal



-Air T1 = T2 = Q



25°C = 298K (reference) 35°C = 308K = n x cp x ΔT = 726,5 kmol x 5,4 kkal/kmol.K x (10)k=K = 39230,73 kkal



2. Panas Pembentukan Inlet Steam Digester -LP-Steam P = 3,6 bar m = 2790 kg h = 588,56 kkal/kg (Entalpi pada tekanan 3,6 bar) Q = mxh = 2790 kg x 588,56 kkal/kg = 1642082,4 kkal -MP-Steam P = 12 bar m = 4020 kg h = 798,11 kkal/kg (Entalpi pada tekanan 12 bar) Q = mxh = 4020 kg x 798,11 kkal/kg = 3208402,2 kkal 3. Panas Pembentukan Inlet White Liquor (ΔH f) -NaOH (ΔHf) Q = n x ΔHf = 2080,8 kmol x -112,2 kkal/kmol = -233442,7 kkal -Na2S (ΔHf) Q = n x ΔHf = 644,27 kmol x -89,8 kkal/kmol = -57855,15 kkal



-Na2CO3 (ΔHf) Q = n x ΔHf = 222,23 kmol x -269,46 kkal/kmol = -59881,13 kkal Panas Sensibel Inlet White Liquor Digester -NaOH T1 = 25°C = 298K (reference) T2 = 90°C = 363K Q = n x cp x ΔT = 2080,78 kmol x 11,275 kkal/kmol.K x (65)K = 1524951,6 kkal -Na2S T1 = 25°C = 298K (reference) T2 = 90°C = 363K Q = n x cp x ΔT = 644,27 kmol x 15,475 kkal/kmol.K x (65)K = 648051,73 kkal -Na2CO3 T1 = 25°C = 298K (reference) T2 = 90°C = 363K Q = n x cp x ΔT = 222,23 kmol x 24,747 kkal/kmol.K x (65)K = 357463,41 kkal Neraca Panas Input Tabel 6. Neraca Panas Input Digester



Komponen Chip (S1) -Selulosa -Lignin -Ekstraktif -Air LP-Steam (S2) MP-Steam (S3) White Liqour (S4) -NaOH -Na2S -Na2CO3



Input Panas Sensibel Panas Pembentukkan (kkal) (kkal) -69103,09057 -4040,29495 -629250,7907 -49546,959 1642082,4 3208402,2



72549,89937 25485,4353 4969,9584 39230,73



-233442,7082 -57855,14667 -59881,12981



1524951,643 648051,7333 357463,4111



TotaL



6420067,29



Panas Output 1. Panas Sensibel Outlet Reject Chip Digester (ΔHf) -Selulosa (ΔHf) Q = n x ΔH f = 0,0082 kmol x -387589,6 kkal/kmol = -3196,513 kkal -Lignin (ΔHf) Q = n x ΔH f = 0,0414139 kmol x -4512,8 kkal/kmol = -189,8926 kkal -Esktraktif (ΔHf) Q = n x ΔH f = 1,2757835 kmol x -22815,28 kkal/kmol = -29107,36 kkal -Air (ΔHf) Q = n x ΔH f = 33,6056 kmol x -68,2 kkal/kmol = -2291,902 kkal Panas Sensibel Outlet Reject Chip Digester - Selulosa T1 = 25°C = 298K (reference) T2 = 126,8°C = 399,8K Q = n x cp x ΔT = 0,0082472 kmol x 40692,227 kkal/kmol x (102)K = 34163,599 kkal -Lignin T1 = 25°C = 298K (reference) T2 = 126,8°C = 399,8K Q = n x cp x ΔT = 0,0414139 kmol x 2846,591 kkal/kmol x (102)K = 12001,039 kkal -Ekstraktif T1 = 25°C = 298K (reference) T2 = 126,8°C = 399,8K Q = n x cp x ΔT = 1,2757835 kmol x 18,02 kkal/kmol x (102)K = 2340,3432 kkal -Air T1 = 25°C = 298K (reference) T2 = 126,8°C = 399,8K



Q



=



n x cp x ΔT = 33,6056 kmol x 5,4 kkal/kmol x (102)K = -18473,67 kkal



2. Panas Sensibel Outlet Reject Chip Digester -Selulosa (ΔHf) Q = n x ΔH f = 0,1834621 kmol x -387589,6 kkal/kmol = -71107,99 kkal -Lignin (ΔHf) Q = n x ΔH f = 0,1646335 kmol x -4512,8 kkal/kmol = -742,9579 kkal -Esktraktif (ΔHf) Q = n x ΔH f = 1,0165957 kmol x -22815,28 kkal/kmol = -23193,92 kkal -NaOH (ΔHf) Q = n x ΔH f = 45,063146 kmol x -112,19 kkal/kmol = -5055,634 kkal -Na2S (ΔHf) Q = n x ΔH f = 66,048744 kmol x -89, 8 kkal/kmol = -5931,177 kkal -Na2CO3 (ΔHf) Q = n x ΔH f = 87,486692 kmol x -269,5 kkal/kmol = -23574,16 kkal -Air (ΔHf) Q = n x ΔH f = 528,06499 kmol x -68,2 kkal/kmol = -36014,03 kkal Panas Sensibel Outlep Pulp Digester - Selulosa T1 = 25°C = 298K (reference) T2 = 92,9°C = 365,9K Q = n x cp x ΔT = 0,1834621 kmol x 40692,227 kkal/kmol.K x (68)K = 506906,11 kkal



-Lignin T1 = T2 = Q



25°C = 298K (reference) 92,9°C = 365,9K = n x cp x ΔT = 0,1646335 kmol x 2846,591 kkal/kmol.K x (68)K = 31820,936 kkal



-Ekstraktif T1 = 25°C = 298K (reference) T2 = 92,9°C = 365,9K Q = n x cp x ΔT = 1,0165957 kmol x 18,02 kkal/kmol.K x (68)K = 1243,8638 kkal - NaOH T1 = 25°C = 298K (reference) T2 = 92,9°C = 365,9K Q = n x cp x ΔT = 45,063146 kmol x 11,275 kkal/kmol.K x (68)K = 506906,11 kkal -Na2S T1 = 25°C = 298K (reference) T2 = 92,9°C = 365,9K Q = n x cp x ΔT = 66,048744 kmol x 15,475 kkal/kmol.K x (68)K = 69400,883 kkal -Na2CO3 T1 = 25°C = 298K (reference) T2 = 92,9°C = 365,9K Q = n x cp x ΔT = 87,486692 kmol x 24,747 kkal/kmol.K x (68)K = 147005,75 kkal -Air T1 = 25°C = 298K (reference) T2 = 92,9°C = 365,9K Q = n x cp x ΔT = 528,06499 kmol x 5,4 kkal/kmol.K x (68)K = 193620,31 kkal 3. Panas Pembentukan Outlet Black Liquor Digester (ΔH f) -Senyawa Organik (ΔH f) Q = n x ΔH f = 0,0816666 kmol x -27328,08 kkal/kmol = -2231,79 kkal



-NaOH (ΔHf) Q = n x ΔH f = 2035,7169 kmol = -228387,1 kkal -Na2S (ΔHf) Q = n x ΔH f = 578,21792 kmol = -51923,97 kkal -Na2CO3 (ΔHf) Q = n x ΔH f = 134,73972 kmol = -36306,97 kkal -Air (ΔHf) Q = n x ΔH f = 543,15774 kmol = -37043,36 kkal



x -112,19 kkal/kmol



x -89,8 kkal/kmol



x -269,46 kkal/kmol



x -68,2 kkal/kmol



Panas Sensibel Outlet Black Liquor Digester -Senyawa Organik T1 = 25°C = 298K (reference) T2 = 155°C = 428K Q = n x cp x ΔT = 0,0816666 kmol x 2864,61 kkal/kmol.K x (130)K = 30412,567 kkal -NaOH T1 = 25°C = 298K (reference) T2 = 155°C = 428K Q = n x cp x ΔT = 2035,7169 kmol x 11,275 kkal/kmol.K x (130)K = 2983852 kkal -Na2S T1 = 25°C = 298K (reference) T2 = 155°C = 428K Q = n x cp x ΔT = 578,21792 kmol x 15,475 kkal/kmol.K x (130)K = 30412,567 kkal -Na2CO3 T1 = 25°C = 298K (reference) T2 = 155°C = 428K Q = n x cp x ΔT = 134,73972 kmol x 24,747 kkal/kmol.K x (130)K = 433472,51 kkal



-Air T1 = T2 = Q



25°C = 298K (reference) 155°C = 428K = n x cp x ΔT = 543,15774 kmol x 5,4 kkal/kmol.K x (130)K = 381296,73 kkal Neraca Panas Output



Tabel 7. Neraca Panas Output Digester



Output Panas Sensibel Panas Pembentukkan (kkal) (kkal)



Komponen Reject Chip (S5) -Selulosa -Lignin -Ekstraktif -Air Pulp (S6) -Selulosa -Lignin -Ekstraktif -NaOH -Na2S -Na2CO3 -Air Black Liqour (S7) -Senyawa Organik -NaOH -Na2S -Na2CO3 -Air



-3196,513149 -186,8925952 -29107,35844 -2291,90192



34163,59907 12001,0393 2340,343235 18473,67043



-71107,99035 -742,9578794 -23193,91568 -5055,634367 -5931,177242 -23574,16402 -36014,03243



506906,1056 31820,93617 1243,863809 34499,10546 69400,88324 147005,752 193620,3098



-2231,790086 -228387,0738 -51923,96942 -36306,96579 -37043,35798



30412,56707 2983851,979 1163229,905 433472,5107 381296,7347



Panas Hilang (Heat Loss) Panas yang hilang = = Heat Loss (Qloss) = Effisiensi Thermal = = =



(Qin)-Panas yang keluar (6420067,29)+(5487443,609) 932623,68 kkal (Qout)/(Qin) x 100% 5487443,609/6420067,29 x 100% 84,473100%



Total



5487443,609



ADT/day Brown Stock = CM RPM x cm Fil ADT/rpm/day = 8,4rpm x 162,3 ADT/rpm/day = 1348,47 ADT/day



ADT Brown Stock x 0,9 Blow Line Consistency = day 24 x blow flow x 100 = 



1348,47 x 0,9 = 11,46896 24 x 441 x 100



Calculated Variables



ADT Solid Volume



= day



Brown Stock x 0,9 24



=



1348,9



ADT x 0,9 day = 50,57813 24



50,57813 50,57813 kg = kg = 91,1317 = solid 0,555 l l =



91,1317 85,4220 x 100 = x 100 Digester yield 46



= 198m3/h Flow to Digester



= Solid Volume + Top Downflow = 198 + 62 = 262m3h



Top Downflow



= Upper Cook Extr – Upper Cook Upflow = 186 – 0 = 62m3h



Upper Extraction



= 186m3h



Upper Cook



= 0m3h



Upper Zone



= Upper Extraction – Upper Cook = 186 – 0 = 186m3h



Upper Cook Upflow = WL to Lower Cook + Cold Blow to Lower + Wash to Lower Cook – Lower Cook Downflow = 95,4 +65 + 0 – 37,79 = 123m 3h



Lower Cook



= 551m3h



WL to Lower Cook



= 95,4m3h



Cold Blow to Lower = 65m3h Wash to Lower Cook = 0m3h Lower Zone



= Lower Cook – WL to Lower Cook – Cold Blow to Lower – Wash to Lower Cook = 551 – 95,4 – 65 – 0 = 391m 3h



Lower Cook Downflow = Main Extraction – Wash upflow to Extrac – WL to Main – CB to Main Circ = 0 – (-44)-6,1 – 0 = 38m 3h Main Extrac



= 0m3h



Main Circ



= 93m3h



WL to Main



= 6,1m3h



CB to Main Circ



= 0m 3h



Main Extrac = Main Extrac + Main Circ – WL to Main – CB to = 0 + 93 – 6,1 – 0 = 87m 3h Wash Upflow to Extr = Cold Blow to Bottom – Liquid in Blow + CB to Wash Circ – (Wash Extraction – Wash to Lower Cook) = 512 – 243 + 0 – (313 – 0) -44m 3h Wash Zone



= Wash Extraction = 313m 3h



Bottom Upflow



= Cold Blow to Bottom – Liquid in Blow



Blow Flow



= 441m 3h



Liquid in Blow



= Blow Flow – Solid Volume = 441 – 198 = 243m3h



Cold Blow to OD



= 130m3h



Cold Blow to Nozzle = 354m3h CB to Side Dilution



= Cold Blow to Bottom – Cold Blow to Nozzle – Cold Blow to OD = 512 – 354 – 130 = 28m 3h



CB to Wash Circ



= 0m3/h



Cold Blow to Bottom = Total Filtrat – Diffuser Inlet Dilution – Cold Blow to Lower – Cold Blow to MUL – CB to Wash Circ – CB to Main Circ = 591 – 14 – 65 – 0 – 0 – 0 = 512m 3/h Diffuser Inlet Dilution = 14m3/h Liquor in Chips



= (1 – Solid) x Solid Volume = (1 – 0,555) x 198 = 88m 3/h



Net to Wash Zone = Solid Volume – Wash Upflow to Extr = 198 – (-44) = 242m3/h