Korean Chemical Engineering Research
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(2) o Jk÷ ÒM« ´ , )éÑ Yfà_Ñ lÄ« Ñ æ( :Ê À´ Ñw( Äo Jk
(3) ÒM « íê 3/ Í Q)Ês f8Gñ ÆJ¯ Yfà_¯ åfÆ à_Ñ lÄO ) Ñw( Qu Dê Yf lÄÑ @÷2 éfÑ ¬g Æ G. Ñw( ¡¤CÆõ lÄO Î, HYSYSõ «ÄK QjS«Ë ê ,Ê 2/ Í Q)ÊÑ 9g 18% Ñw( QÝÁêÍ À{s <Ik 2/ ÍQ)ÊÑ 9g f´Pé ¤2 Íæ(O 3Í( f\ Æ ÆQ« Ê Î / ÒMFts j Æ QO ¤ À2 ßYs äÊ À. Abstract − Though a fully thermally coupled distillation column-an energy efficient distillation system-consumes less energy, it is not widely implemented in practice due to its operational difficulty. A 3-column distillation system having improved operability is proposed here, and its energy saving performance and application related issues are investigated from the implementation result to a practical hexane process. When an energy integration is employed, the proposed system requires 18% less energy than a conventional 2-column system, which is found from the HYSYS simulation. Though more control loops than the 2-column system are required, the proposed system has better controllability of product compositions and the pressure control of the system is easier. Key words: Distillation, Ternary Separation, Energy-Efficient Distillation, Hexane Process. 1.. g «. ùJk³2 Yê Q)Ês ÄGñ Ñw( QÝÁêõ K( K OÑf\ Æ ÆQs j O ¤ À´ K gÆõ f8G Ê « Q)Ê ¡¤ f´ Ds Q×K õgÍ è,æÉ[10]. ~ ~- Í/s MhÍ =³ ÒMG
(4) / ÍË o Í ÍÍ ËÑ [Gj æ[11], MhÍ ÆÊÑ 2 M Ñw(õ ÄG, )éÑ / ùòHJ ÁSo « J « ê. «6K « J¯ Í Ëo Ñw( ÁS« o Í Q )Ê G÷³ <s À2 ùÞY Í/ / UZÆ ~¯Q K G. Fig. 1 ùÞY Í/o ÍË« Í ÍÍ Ëê K K gƳ æ´ À, )éÑ /ÁS« 4 Ñw( Ä
(5) « ,Ê 2/ Q)ÊÝ Jo ßYs Í(Ê À. «6K YÑ ô8Gñ Í ÍÍ Ëê K K Í s Í(Ê ,Ê 2/ Q)Êê 97K gÆõ Í, Fig. 2 3/. ¬z~ ÎÑ ~ HYís ~-G2 ùÞY Í/(fully o ,Ê 2/ Í Q)ÊÝ Jo Ñw(õ 9G(O / ÒM« ,Ê Q)Ê Ý ´ , )éÑ °o lÄ« 4) «P´(( :Ê À. « 6K éfõ gG, .Gñ / ÒMörs íGs2 Qo õ g[1-6]Ë« ¤}æ´ f. « éf g ñ [ örk³, ÒMs j G, .Gñ / gÆõ JQ¾ ¡K õg[7-9] è,ê à À. âÑ «6K õg ³hk³ ùÞY Í/ ?/s & z~k³ ~OGñ ~Oê / « í0«o Lk
(6) 3 thermally coupled distillation column, FTCDC). † To. whom correspondence should be addressed. E-mail: [email protected]. 39.
(7) 40. 6Közä. s ÄG2 «K2 / UZÆ ~¯õ ùÞY Í/ Æ ~¯Q ³Gj OË, .W«. 0 Jk³ 2, Í/« 3 ~ HYí ~-Ñ «ÄæÉ( O, UZ Æ ~¯Í Í ÍÍ Ëê2 UM¾ í . àü´ SG
(8) , 2/ Í Q)Êo ò0 àÑ HYê OÑ9Y ~ éHY ço 9ÍòJ ê_« ¯Wæ´ À, )é Ñ 9« J«[1]. 6÷ 2/ Q)ÊÑ MI-/s zÍG
(9) o Í/ ÁSs ÷ 2 ùÞY Í/ê K K Æ ~¯õ Í ,. 9´ zÍê /« 3/ Q)Ê ÒMÑ f´Pé ¤õ 6 -(O, f´PéË « õ« UM¾ ~-æ, )éÑ § Í ( f\ Æ f´Í ùÞY Í/ Æ f´Ý . á õgÑ2 3 ~ HYí ~-õ .Gñ í
(10) ê ÍQ)Ê s f8GÊ «õ Yf ßÑ ÄG2 å fÆà_Ñ lÄG ñ Ds Æ G ÄÑ @,2 éfYÑ îg ~g Ý ÊÉ K. ÄG2 ÍQ)Êo ,Ê ùÞY Í/ê K K ÍËs Í(2 3/ ÍQ)Ê« D Íõ .g HYSYS QjS«Ës ÄG. 2.. Fig. 1. A schematic diagram of a fully thermally coupled distillation column.. ·» o. á õg 3/ ÍQ)Ê gÆ2 ,Ê ùÞY Í/s , ák³ g æÉ, )éÑ ùÞY Í/s ÏI ªGÊ «õ à 3k³ 3/ ÍQ)Ês ªK. ùÞY Í/o Fig. 1Ñ ÷ ÷ À2 aIF MI- /ê ?/k³ g æ´ À. & / UZ Æ « ~ª Í ÍÍ Ëê K K =õ Í0 ), Í/ ùòHJ¯ ÁS« « J»s à3k³ K ªör [12, 13]s ÄG
(11) ùÞY Í/s ªO ¤ Àk÷ ñ,2 í 0 ¤(Rs «ÄK ªR ªrs ÄGñ {ê ç« gÆ ªõ G. ùÞY Í/ ªÑ Ý2 àQ ç« UZÆ « Í ÍÍ Ëê K K Æ ~¯õ Í, MI- /o Yf/ Ñ2 »s ¤ Ç. MhÍ ÆÊo «·J¯ ÎÑ K_æ Y f³ ò0Í àæ
(12) MI-/ zQ GzÑ ,Q U 9 S« ³ íj æ³ K í ÍËk³ MZõ ,O ¤ Ç, )é«. 6÷ ñ,2 ª sõ .Gñ ò0 à Æ ê ò0 Æ « çÊ Í_G
(13) ò0 àQ HY« ³´÷( :k³ o /ÁS« »´,. 6³ Table 1Ñ ÷ ò0 Æ Ñ [K à Æ s OË, .g à Æ « ò0 Æ ê çÊ Í_GÊ ò0 àÝ K . UZ Æ o { í0¤(³z ªO ¤ À. «6K ª örk³ MI- / o . >( UZÆ s ªK. xn, i = ( V2yn + 1, i – Fzi γ1, i ) ⁄ L2 II. Fig. 2. A schematic diagram of a 3-column distillation system.. Q)Êo Ñw( Ä
(14) « Jk
(15) / ÒM« Ä«K ßYs 5 ¤Í À. «6K 3/ Q)Êo I9Y ~ê Ê9Y ~ & z~k³ ÷2 MI- /s Í(Ê Àk I9Y ~o z/k³ «GÊ Ê9Y ~o Gz/k³ «K. MI- / ¤@¤ C43× C1 2005 2 . II. (1). ñ, Uê , K
(16) o ª Q)Ê ¬Aèõ «ÄGñ ªK M K
(17) [14] 1.5 õ ÄGk, ÙPK Í_s JÄG. Yf K
(18) o ñ, ÄK à« 4v ¤ À(O ª sõ .g 0 ª,Cs ÄG. R (1)Ñ ,Æ o HYSYS )«}«) ²¶è õ «ÄK Peng-RobinsonRk³ z gG. á õg ò0Ñ ¯Wê 19í g ~Ñ ¬K ª« ÑG( :, )éÑ, ñ,2 ?® ~O >Gñ.
(19) ÑM( 3u Í/. 41. Table 1. Flow rates of feed and products of FTCDC and 3-column systems of hexane process in kmol/h Component. Feed. (Light) n-butane i-butane n-pentane i-pentane Cyclopentane 2,2-methylbutane 2-methylpentane (Intermediate) 3-methylpentane n-hexane 1-hexene Methylcyclopentane (Heavy) Cyclohexane Benzene n-heptane 2-methylhexane 3-methylhexane Methylcyclohexane Cycloheptane Toluene Total. Overhead. FTCDC Bottom. 0.0000 0.0000 0.0000 0.0000 0.0000 0.0002 0.6217. 3.0316 0.6518 26.040 13.479 1.4812 0.2666 7.2507. 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0015. 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.3318. 5.0856 21.182 0.0099 2.6959. 3.3096 2.1110 0.0077 0.1196. 0.0145 1.3207 0.0000 0.6783. 1.7302 17.789 0.0021 1.9189. 3.4113 1.7340 0.0082 0.0984. 0.0158 1.6676 0.0000 0.6138. 1.6586 17.780 0.0017 1.9837. 1.7874 1.2541 8.0516 1.6330 1.3632 1.2355 1.1786 0.7385. 0.0043 0.0773 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000. 1.4605 0.3239 8.0278 1.5957 1.3395 1.2301 1.1789 0.7382. 0.3136 0.8580 0.0224 0.0341 0.0218 0.0051 0.0000 0.0004. 0.0017 0.0648 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000. 1.2397 0.2946 8.0205 1.5810 1.3309 1.2284 1.1785 0.7379. 0.5459 0.8948 0.0311 0.0520 0.0323 0.0071 0.0001 0.0006. 98.750. 57.519. 17.910. 23.318. 57.520. 17.910. 23.320. (2). ³K örk³ MI-/ Gz , Æ o ò0Æ Ñ QÊ Gñ { í0¤(³z ªê. ñ,2 zQ íj U ZÆ ¬UÑ ,Æ « »´,. yn + 1, i = ( L3x n – 1, i – Fzi γ2, i ) ⁄ L3. (3). ?/ OÑ9Y f\ @ z(Fig. 1Ñ NPQ NR «)Ñ 2 R (1)ê K Gj (4). s ÄGñ U Æ s ªGÊ MI- / ê õæ2 ?/ z õ(NR)o MI- / M ê Æ ó«Í ÍDK Ê4t G, )éÑ MJd ª« 1®G³ {ê ç o IJRs ÄGñ ªK. Min ∑ ( x n, i – xm, i Fzi γ1, i ) II. m, n. i. Side. 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0022. α B – αC β = ----------------αA – αC. xn, i = ( V4 yn + 1, i + Fz iγ3, i ) ⁄ L4. 3-column Bottom. 3.0320 0.6518 26.051 13.484 1.4818 0.2664 6.9219. 1,i. II. Overhead. 3.0316 0.6517 26.040 13.479 1.4812 0.2666 7.5840. ÄG2) I9Y HYíÑ 3Í(, OÑ9Y HYíÑ 1Í (, Ê9Y HYíÑ 5Í(õ Í o aO Ò¶ ªÑ. ÄG. ñ, ª¤ γ 2 i ~« MI- /Ñ ?/ zõ s 0g «æ2 MZ à
(20) Ñ ¬K 9«, ÊéË[14] Ñ _ê OÑ9Y ~ MJ~-9 β³z ªæ´ ,. õ Ë´ I9Y ~ AÑ ¬g2 1, OÑ9Y ~ BÑ ¬g 2 β«Ê Ê9Y ~ CÑ ¬g2 0« ê. MJ~-92 { Rê ç« ªê.. II. Side. (5). ñ, GSÉ mo MI- / ò0 à z dDõ ÷ Ê GSÉ no ?/ OÑ9Yf\ @ z dDõ ÷ . ³ dDÍ _ æ
(21) , z õ(NR)Ñ UZ Æ o { í0¤(Rk³z gg,. xNR, i = ( V4y NR + 1, i + V2 y1, i – Fziγ4, i ) ⁄ L. (6). xn, i = ( Vyn + 1, i–F ziγ4, i ) ⁄ L. (7). yn, i = ( L5 xn–1, i + F zi γ5, i ) ⁄ V5. (8). Min ∑ ( xn, i – xm, i )Fzi γ2, i. (9). II. -Ê õ(NR)Ñ ?/ M z>( UÆ o zf\ Æ s OÇO )>( { Rk³ K ªK. ?/ GzÑ zQ K Gj OÑ9Yf\ @(NP) Gzò(Fig. 1 NPQ NS «)Ñ s ÄGÊ Gz õ(NS) _o { IJRs ÄGñ MJd ªs G II. m, n. i. ñ, GSÉ mo MI- / ò0 à Gz dDõ ÷ Ê GSÉ no ?/ OÑ9Yf\ @ Gz dDõ ÷ . Gz õ(NS) Æ o yNS, i = ( L5x NS–1, i + L3xNT2, i + F zi γ6, i ) ⁄ V. (10). yn, i = ( Lxn –1, i – F ziγ6, i ) ⁄ V. (11). II. Q ç« ªGÊ Q ?/ MGzÑ2 {Rs ÄGñ Gzf\ Æ « »´0 )>( ªR ªs äÞK. Korean Chem. Eng. Res., Vol. 43, No. 1, February, 2005.
(22) 6Közä. 42. Table 2. Tray numbers from structural design and operating conditions for 3-column, the FTCDC and 2-column systems of hexane process. Tray numbers are counted from top Name. Prefract.. 3-coumn Upper. Lower. Prefract.. Main. 1st. 2nd. 29 10. 46 17. 20 11. 29 11. 66 32 11 57. 25 11. 70 44. 98.75 71.00 27.75. 71.00 57.52 13.48. 27.75 9.840 17.91. 98.75. 98.75 57.53 41.22. 41.22 23.32 17.90. 34.00 99.74 3.121. 73.00 123.5 3.636. 61.00 65.93 2.108. 25.00 94.00. 132.3 175.7 5.382. 74.39 89.92 2.892. Structural Number of trays Feed/side product Interlinking stages Operating Feed(kmol/h) Overhead(kmol/h) Bottom(kmol/h) Side(kmol/h) Reflux(kmol/h) Vapor boilup(kmol/h) Heat duty(GJ/h). FTCDC. « ê ç« í0¤(õ ÄGñ ªRk³ Î Ñ UZ. õ ªGÊ ªê ¤³z MI- /ê ?/ ¤, ò0 à(NF) .j, OÑ9Y f\ @(NP) Ú z(NR) Q Gzõ(NS)s <4 ¤ À. Yf/ Î à U Z Í ò0 Q í³ ªQ ª sõ .Gñ çÊ Í_GÊ ªG, )éÑ Ý_« 1®G. á õgÑ 2 »´, MI-/ ¤Ñ 0 ª,Cs JÄGñ 1.7s Ü K às ÄG. «Rj »o ê2 ùÞY Í/ gÆ« «õ à3k³ 3/ Q)Ê gÆõ »s ¤ À. \ Q)Ê MI- /o ç, )éÑ ço às ÄO ¤ À. 3/ Q)Ê z/o ùÞY Í/ ?/Ñ OÑ9Y f\ @ z z~Ñ g¢æ, Gz/o ?/ Gz z~Ñ g¢ê. 6÷ HYSYS QjS«Ë ê_Ñ uÑ ¤ Æ_« ÀÉk MZ ¤2 ³G. Table 2Ñ ùÞY Í/ ªêQ 3/ ÍQ)Ê ªêÍ _-æ´ À. «Rj 3/ Í Q)Ê gÆÉ0Í »´(
(23) , ?´, f\ Æ s @O ¤ À2 Í/ ÒMÆQ, Uê , K
(24) ç o ÆÊ ¡¤Ëo HYSYS QjS«Ës 0g gO ¤ À. Qj S«Ë ê2 Table 2Ñ ÷ ÷ À. HYSYS QjS«ËÑ Í Q)Ê gÆõ ½tGÊ ÒM¡¤õ ¡dQÿ
(25) Table 1Ñ ?´, 3Í( f\ ê Æ « »´0 )>( äÞ ªK. 3.. û @`. 2-column. 57.52 17.91 23.32 134.1 169.3 5.449. ÄG2 o ùòHJ¯ ÁSs Í((O, ÒM ´sÞo ùÞY Í/ YfJ¯ lÄs fKGñ f. «6K ÒM ís .Gñ 3/ ÍQ)Ês f8GÊ « Q)Ê Ds Ñw( ®
(26) s 9GGñ ÍGÊÉ K. «6K Í2 ,Ê 2/ Q) Êê ùÞY Í/s 9GGñ YQGÊ 3/ Í Q)Ê Y f lÄQ @÷2 éfYs ]GÊÉ K. åà_Ñ ¬g, 3/ Q)Ê gÆJ¯ ª2 Table 2Ñ ÷ ÷ À2 aIF ùÞY Í/ ª ê³z KæÉ. í · uÑ ¤_« ÀÉ(O, & Q)Ê gÆ2 K G. 3/ Q )Ê z/o ùÞY Í/Ñ ?/ z z~(OÑ9Y f \@ ,C)ê K GÊ, Q K Gj Gz/o ùÞY Í/ ?/ Gz z~ê K G. & Q)ÊÑ MI- /o ³G . Fig. 2 3/ Q)Ês HYSYS³ QjS«Ë G, .Gñ g K à_Í Fig. 3ê ç. « =ê ço 3/ Q)Ê / U Z Æ ~¯õ =k³ ÷ a« Fig. 4«. ñ, o ,D 2 MI- / Æ ~¯«Ê, + ,D2 z / Æ ~¯, x , D2 Gz /Ñ Æ ~¯õ ÎÎ ÷ . o ,DÑ Öñ À 2 UQ Lo z /ê Gz /Ñ àæ2 ÎÎ ò0Æ s ÷ . D2 I9Y f\, S2 OÑ9Y f\, B2 Ê9Y f\s ÎÎ ,QK. F³ ,,ê ò0 Æ ê UQ L« ³ Ñ À {s ?IO 1®Í À2) « ®gÆQo Í/ ª Kõ s fKGñ /ÁSs IGQÿ2 ?®¯« ê. ùÞY Í/ . å à_o òKõ _fG2 F Í/Ñ »´(2 I9Y ÷é õ ò0³ Gñ Ê ås »2 à_«. « à_ f \s MÜ f\k³ ¶kG, .g2 Kz dYís fMG2 à _« Íæ´ ,. Table 1 ò0 Æ Ú 3Í( f\ 2 Yfà_Ñ »o É0«. ÆJ¯ à_Ñ îK õg³2 ÷é _Íà_Ñ Ñw( QuÑ ¬g õg[15, 16]ê à À(O, å à_ Ñw( QuÑ ¬g2 4) õgæ( :I. 4.. ûG Z +{. ùÞY Í/« ,Ê 2/ Q)ÊÑ 9Gñ Jo Ñw(õ. ¤@¤ C43× C1 2005 2 . Fig. 3. A HYSYS flow diagram of 3-column distillation system..
(27) ÑM( 3u Í/. 43. Fig. 6. A HYSYS flow diagram of 3-column distillation system with heat integration.. Fig. 4. Liquid composition profile of hexane process in 3-column system. The symbols U and L indicate feed compositions of upper and lower main columns, respectively.. Fig. 5. Liquid composition profile of hexane process in a fully thermally coupled distillation column.. Î, Fig. 5Ñ Æ ~¯Í ÷ ÷ À. ñ, L22 ?/Ñ MI - /k³ « æ2 U Æ «, LB2 MI- / GÑ ? /k³ «æ2 U Æ «. «Ë 3Í( Æ Ëo 3/ Q)Ê ê2 - )s «P( :4 ùÞY Í/ gÆ ªõ Kõ Gj K. ùÞY Í/ Î2 MI- /ê ?/ «Ñ ö í0«« ³´÷, )éÑ «Ë Æ «Ñ )s «X 1 ®Í Ç. Fig. 4Q 5õ 9GG
(28) & Q)Ê H& Í ÍÍ. Ëê K K ÍËs Í2s < ¤ ÀÊ «2 «Ë Q) Ê ÁS« 2 as Gj K. åà_ ÒMÑ îK HYSYS QjS«Ë êÍ Table 2Ñ ÷ ÷ À. 9´ 3Í( ñ Q)Ê« ?´, Æ ço f\ s @K O(¶, Ñw( H
(29) « Î, í. ùÞY Í / Î2 ,Ê 2/ Q)ÊÑ 9g 34% Ñw( QÝÁêÍ Àk÷ 3/ Q)Êo 2/ Q)ÊÑ 9g 1¾s 7%
(30) Qo Ñw. (õ ®gK. «2 OÑ (JK MI- / ò0Q f\ Æ . « ) ÆQÑ ñ Í/ ª fuÑ g @0 é fY«. 6÷ 3/ Q)Ê Gz / ÒMFts 0.1,F 9Q ÿ
(31) Gz/ -Î,Ñ ¡¤ê ùs z/ é9,Ñ lÄ O ¤ À2 gÆÍ ÍDG. «6K ¡ Q)Ê à_s HYSYS à_³ Ê K a« Fig. 6«. =ÑQ ç« Gz/ -Î ,Q z/ é9,õ 1í ùGh,³ g GÊ zÇK ù
(32) o Í Íù,õ jGñ gG. «6K gÆ2 2/ Q)Ê Ñ 9g ÞÛK gÆ«(O 3Í( f\ Æ s ÎÎ ÆQG ,Í Ê 2/ Q)ÊÑ 9g 18% Ñw( QÝÁêõ »s ¤ À. 2/ Q)Ê Î2 f1/ é9, 5Í f2/ -Î, 5Ý wå , )éÑ ¨K ùY« ÍDG. Ñw( 9 Ä O 4n¶ 99Äs 9GG, .Gñ f8ê 3/ ÍQ) Ê 99Äs ]I¥³ g~Gñ Table 3Ñ ÷ Ék ,Ê 2/ Q)Êê 9GGñ uÑ Jo 9Ä« ®ös < ¤ À. 99Ä ªo ÊéË[17]Ñ fQê örk³ ªK ê «. 3/ ÍQ)Êo MI-/ ÒM ÆQÑ ¶ Ñw( Ä
(33) « ¡dG³ MI- /Ñ z Ú Gzf\ ~-
(34) ê h Í
(35) Ñ ñ Ñw( ®
(36) s ªK êõ Table 4Ñ _-G. ñ, < ¤ À2 àQ ç« MI-/ z³ 70%õ ~-O ) -Ê hÍ9õ 0.5³ O ) Íß Jo Ñw(õ ÄWs < ¤ À. á õgÑ »o ªêõ 2/ ÍöRs ÄG2 Yf ßÑ ¤Q 9GG
(37) Yfà_Ñ2 f1/Ñ 36, f2/ Ñ 100s ÄG2) 9g á õg ê2 MI-/« 29, z/« 46, Gz/« 20«³ ¤Í 95«. 6÷ ñ , ªê ào « J¯ /ÁSs Ís Ϋ Yfà_Ñ 70% /ÁSs ÊsG
(38) Yfà_Ñ ¤Í »´2s Table 3. Investment costs of proposed 3-column and conventional 2-column systems in thousand dollars. Column Tray Condenser Reboiler Subtotal Total. Prefr. 151.3 14.3 145.7 107.0 418.3. 3-column Upper 224.6 23.6 146.4 69.3 463.9 1126.2. Lower 77.6 5.8 91.5 69.1 244.00. 2-column 1st 2nd 181.6 290.2 19.2 32.0 208.9 141.3 152.4 101.8 562.1 565.3 1127.4. Korean Chem. Eng. Res., Vol. 43, No. 1, February, 2005.
(39) 6Közä. 44. Table 4. Comparison of energy requirements for different operating conditions of upper split rate and reflux flow in prefractionator. Units are in GJ/h Upper split (kmol/h) 67 69 71 73 75 Reflux ratio 0.45 0.50 0.55 0.60. Prefr.. Upper. Lower. Total. 2.99 3.06 3.12 3.19 3.25. 4.65 3.56 3.64 3.81 4.03. 2.23 2.17 2.11 2.05 1.99. 9.87 8.79 8.87 9.05 9.27. 2.97 3.07 3.17 3.27. 3.69 3.54 3.45 3.45. 2.17 2.17 2.17 2.17. 8.83 8.78 8.79 8.89. < ¤ ÀÊ «2 á õg ª,C« JQWs ÷ . f8ê 3/ Q)Ê f´ D« ùÞY Í/Ñ 9g ÒM D« íös <4Ý, .Gñ zf\ K
(40) , z/ ,à
(41) Ú Gz/ , à
(42) ¡dÑ ñ zf\ OÑ f\ Ú. Gzf\ ?® ~Ñ ¬K ªs Fig. 7Ñ ÷ É. = zù 3í =o zf\ K
(43) ¡dÑ ñ zf\ S!Æ , OÑf\ å Æ , Gzf\ ÿ! Æ s ÎÎ ÷ OÑùo z/ ,à
(44) Ñ ¬K ªs, Gzù o Gz/ ,à
(45) Ñ ¬K s ÷ . =Ñ < ¤ À2 àQ ç« z/Ñ ¡dÍ ?´s ) Gz/ f\Æ o s ç( :k «Yo Gz/Ñ ¡dÍ ?´s )Ñ K÷ Í(³ z/ f\Æ « s ç( :2. z/ Ñ ,à
(46) s ÆQGñ OÑf\ Æ s ÆQO ¤ Àk zf\ K
(47) ê ,à
(48) s ÞYJk³ ÆQGñ zf\ Æ s ÆQO ¤ À{s < ¤ ÀÊ Gzf\ Æ o Gz/ ,à
(49) s ÆQGñ j f´O ¤ À{s Ýñ?Ê À. 6÷ ùÞY Í/ Î Fig. 8Ñ ÷ àQ ç« 1í /Ñ 3Í( f\« @æ, )éÑ hÍ
(50) Ñ ¬K 3Í( f\ ª « QÑ ÷ ÷ OÑf\ K
(51) ¡dÑ ¬K ªÑ OÑf\ê Gzf\ Æ ¡dÍ QÑ ÷ ÷, )éÑ 3 Í( f\ Æ f´õ QÑ G,Í kÎ ´sÞs Ýñ?Ê À . «6K êõ ÊsO ) 3/ ÍQ)Ê« ùÞY . Fig. 7. The responses of overhead, side draw and bottom product specifications with step changes of overhead product and vapor boilup rates in upper column and vapor boilup rate in lower column of 3-column system for hexane process. Top three figures are of overhead product flow, middle three are of vapor boilup rate in upper column and the bottom three are of vapor boilup rate in lower column.. ¤@¤ C43× C1 2005 2 .
(52) ÑM( 3u Í/. 45. Fig. 8. The responses of overhead, side draw and bottom product specifications with step changes of reflux, vapor boilup and side draw rates in the FTCDC for hexane process. Top three figures are of reflux flow rate, middle three are of vapor boilup rate and the bottom three are of side draw rate.. Í/Ñ 9g f\ \0î-Í Þs < ¤ À. 3/ Í Q)Êo ,Ê 2/ ÍQ)ÊÑ 9Gñ /« f´ Pé ¤Í 4í
(53) 1®G í¢ 15,0006 9Ä(Âh ª+f´Q)Ê¡ è_9Ä)s Ý8O ) u 60,0006 99Ä« Íê . 6÷ 3/ ÍQ)Ê Ñw( QÝ9Ä« õÑ 88,0006 »s Ý8O ) Í9Äo u 8íö ÒM9Ä QÝk³ ¡¤O ¤ À{s < ¤ À. ùÞY Í/ o ÁSê o Ñw( ®2 ß ,¬ÉË Ñj - <s Àk÷, ÆÊ ´sÞ« / Yf lÄÑ Q o fus Íf. í· ,Ê 2/ Q)ÊÝ 3/ Q)ÊÑ / « G÷
(54) Q, )éÑ
(55) Ï Qo f´Péõ ®gG(O, 3Í( f\ Æ f´2 ùÞY Í/ Æ f´Ý Ä«G. K, 3/ Q)ÊÑ 3, / ÒM Fto ÎÎ ³ ÆQO ¤ À, )éÑ O ùYÑ K Ñw( ¡¤Í ÍDG(O, ù ÞY Í/Ñ2 MI- /ê ?/ « ö ~ý õ ) éÑ / Fts »¬³ ÆQG, ´ , )éÑ Q)Ê Ñ Ñw(õ ¡¤Gñ é ÄG,Í ÍDG. 3/ Q)Êo 3,. /s ÎÎ ñ Ftk³ ÒMG, )éÑ / ¤ ó«Ñ ñ / j gÆÑ fK« Çk÷ ùÞY Í/ Î2 MI-/ ¤)J .j _s JQGj G( :k
(56) ?/ê ö , U « s O ¤ Ç2 éfÍ À. 5.. û «. Ñw( Qu Í Q)ʯ ùÞY Í/ o ÒM s í G, .Gñ 3, Í/s ÄGñ 3Í( f\s @G2 à _s f8GÊ Yf ßÑ ÄG2 å fÆà_Ñ lÄG s ) Ds Æ G. ò0Q f\ Æ ÑÑ ) s 1 ®³ G, )éÑ 3/ ÍQ)Ê ªÑ fK« À´ ùÞY Í/ê ço /ÁSo »´(( :k÷ Q)Ê Ñ Ñw( ¡¤ Í ÍDGñ «õ lÄO Î ,Ê 2/ Q)ÊÑ 9g 18% Ñw( QÝÁêõ »s ¤ À. 3/ Q)Êo 3, Í/s Î Î ÒMG, )éÑ 3Í( f\ Æ ÆQ« Ê ÎÎ ÒMF t _« Ò ßYs Í(Ê À. Korean Chem. Eng. Res., Vol. 43, No. 1, February, 2005.
(57) 46. [ ÷. 6Közä. á õg2 2004¸ KhH¬,é (ò(KRF-2004-002D00093)k³ ¤}æÉk, «Ñ Ý Ã?n.. ÷ô{S D. : overhead product. B F. : bottom product : flow rate of feed [kmol/h]. L NF. : liquid flow rate [kmol/h] : feed tray number. NP NR. : side draw tray number : location of upper interlinking tray. NS S. : location of lower interlinking tray : side draw. V x. : vapor flow rate [kmol/h] : liquid composition [mol fraction]. y z. : vapor composition [mol fraction] : feed composition [mol fraction]. bóÛ II. : prefractionator. ãóÛ A. : lightest component. B C. : intermediate component : heaviest component. i m. : component : tray number. n. : tray number. +÷¿ï SÛ. α. : relative volatility. β γ. : intermediate component split ratio defined in Eq. (2) : transport ratio. +S 1. Triantafyllou, C. and Smith, R., “The Design and Optimisation of Fully Thermally Coupled Distillation Columns,” Trans. IChemE, Part A, 70(2), 118-132(1992). 2. Wolff, E. A. and Skogestad, S., “Operation of Integrated Three-. ¤@¤ C43× C1 2005 2 . Product (Petlyuk) Distillation Columns,” Ind. Eng. Chem. Res., 34(6), 2094-2103(1995). 3. Halvorsen, I. J. and Skogestad, S., “Optimizing Control of Petlyuk Distillation: Understanding the Steady-State Behavior,” Computers chem. Engng., 21(S1), S249-S254(1997). 4. Abdul Mutalib, M. I. and Smith, R., “Operation and Control of Dividing Wall Distillation Columns, Part 1: Degrees of Freedom and Dynamic Simulation,” Trans. IChemE, Part A, 76(3), 308-318 (1998). 5. Abdul Mutalib, M. I., Zeglam, A. O. and Smith, R., “Operation and Control of Dividing Wall Distillation Columns, Part 2: Simulation and Pilot Plant Studies using Temperature Control,” Trans. IChemE, Part A, 76(3), 319-334(1998). 6. Kim, Y. H., “Structural Design and Operation of a Fully Thermally Coupled Distillation Column,” Chem. Eng. J., 85(2), 289301 (2002). 7. Agrawal, R., “More Operable Fully Thermally Coupled Distillation Column Configurations for Multicomponent Distillation,” Trans. Inst. Chem. Eng., Part A, 77(6), 543-553(1999). 8. Agrawal, R., “Multieffect Distillation for Thermally Coupled Configurations,” AIChE J., 46(11), 2211-2224(2000). 9. Agrawal, R., “Thermally Coupled Distillation with Reduced Number of Intercolumn Vapor Transfers,” AIChE J., 46(11), 2198-2210(2000). 10. Kim, Y. H., “An Alternative Structure of a Fully Thermally Coupled Distillation Column for Improved Operability,” J. Chem. Eng., Japan, 36(12), 1503-1509(2003). 11. Widagdo, S. and Seider, W. D., “Azeotropic Distillation,” AIChE J., 42(1), 96-130(1996). 12. Kim, Y. H., “Structural Design of Extended Fully Thermally Coupled Distillation Columns,” Ind. Eng. Chem. Res., 40(11), 2460-2466(2001). 13. Kim, Y. H., “Rigorous Design of Extended Fully Thermally Coupled Distillation Columns,” Chem. Eng. J., 89(1), 89-99(2002). 14. Fidkowski, Z. and Krolikowski, L., “Thermally Coupled System of Distillation Columns: Optimization Procedure,” AIChE J., 32(14), 537-546(1986). 15. Lee, J. C., Yeo, Y. K., Song, K. H. and Kim, I. W., “Operating Strategies and Optimum Feed Tray Locations of the Fractionation Unit of BTX Plants for Energy Conservation,” Korean J. Chem. Eng., 18(4), 428-431(2001). 16. Lee, J. Y., Kim, Y. H. and Hwang, K. S., “Application of a Fully Thermally Coupled Distillation Column for Fractionation Process in Naphtha Reforming Plant,” Chem. Eng. Process., 43(4), 495-501(2004). 17. Douglas, J. M., Conceptual Design of Chemical Processes, McGraw-Hill, New York, NY(1988)..
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