Simulation and Experimental System Terner Aseton-Butanol-Ethanol with Batch Distillation

Transcription

1 Strengthenng Basc Scences and Technology for Industral Sustanablty Smulaton and Expermental System Terner Aseton-Butanol-Ethanol wth Batch Dstllaton N Ketut Sar Departement of Chemcal Engneerng, Industral Technolog Faculty UPN Veteran East Java E-mal: sar_ketut@yahoo.com ABSTRACT Result of Aseton-Butanol-Ethanol (ABE) terner system smulaton (ABE) n the form of temperature profle, lquda composton profle and vapour n bottom utlzed as reference n ABE terner system experment, wth komparas result of ABE terner system experment and smulaton wll know how far devaton obtaned. For the dssocaton of ABE terner system done by research smulatonly before done by research expermentally, so that n determnaton of research varable can more drectonal and expense of cheaper research. Smulaton of ABE terner system by batch dstllaton use rgorous method, model DAEs and Matlab Ianguage. Result of from ABE terner system smulaton later then comparaton use Metanol-Ethanol-Propanol (MEP) terner system whch formng homolog deret. Usage of MEP terner system n ABE terner system comparaton, because MEP terner system mxture predcton form zeotropk mxture. Result of smulaton n the form of temperature profle, lquda composton profle and vapor composton profle functon of tme dmensonless () ether n bottom and also[n dstlate. Is afterwards done by ABE terner system experment wth operatng pressure 1 atmospher, ABE mxture volume 350 ml, ABE feed composton :, 0.1, 0.1 ( mole fracton) and : 0, 1, 2,3. Result of ABE terner system smulaton comparaton wth MEP terner system come near result whch same and show zeotropk mxture. Result of experment and smulaton n the form of temperature profle, lquda composton profle and vapor composton profle tme dmensonless functon ether n bottom and also n dstlate show result come near s samely. So that ABE terner system smulaton after comparaton wth MEP terner system can wear by reference n ABE terner system experment Keyword : tme dmensonless,batch dstllaton, eksperment, smulaton, zeotropk 1. INTRODUCTION In the chemcal ndustry, the fermentaton process s one way to get a chemcal compound wth the help of mcroorgansms, fermentaton products enter the next stage of separaton. At ths stage t s very mportant to produce a product wth a certan purty, one of the tools commonly used n the separaton process s a batch dstllaton column. Separaton process n the ndustry generally and the separaton of multcomponent separaton rarely bnary, therefore t s mportant to revew the multcomponent batch dstllaton. Desgn of mult-component batch dstllaton s generally obtaned by performng smulatons, n order to obtan smulaton results are close to the actual state of the requred thermodynamc data are accurate. In the process of separaton, thermodynamc data of the most domnant nfluence on the process performance s the equlbrum phase. One of the modern thermodynamc correlaton n mempersentaskan behavor s not deal mxture UNIQUAC equaton, the approxmate equlbrum ternary and quaternary systems can be done only based on expermental data of bnary systems. Actvty coeffcent models wth UNIQUAC equaton was developed from a bnary mxture, and has advantages for applcatons n mult-component mxture system because t only requres a bnary parameter (does not requre addtonal parameters). But the loss model does not always succeed n predctng the equlbrum multcomponent system that shows a mxture whch s not deal especally for mxtures that have a spouse wth lmted solublty such as butanol-water. To overcome these measurement data needed to accurately balance the bnary system and model parameters estmaton of actvty coeffcent models so that these parameters can be used to estmate the vapor-lqud equlbrum multcomponent systems accurately. From the smulaton results obtaned ternary system, to see the profle of the movement of the composton of lquda on the bottom then drawn n the form of resdue curve maps. From the resdue curve maps the ternary system can be known whether they form a ternary mxture zeotropk or azeotropc mxtures. Of the azeotropc mxture can be dvded nto homogeneous azeotropc mxtures and heterogeneous azeotropc mxtures. For homogeneous azeotropc mxture after separaton of the results obtaned form a sngle phase and azeotropnya pont does not le n Lqud-Lqud-Equlbrum (Mademoselle), whle for heterogeneous azeotropc mxture after separaton of the results obtaned form more than one phase and AII.4-1

2 Strengthenng Basc Scences and Technology for Industral Sustanablty azeotropnya pont s at Mademoselle. Then further developed for mult-component systems, namely n the form of resdue curve maps of homogeneous and heterogeneous azeotropc mxture, the movement of the composton profle n the resdue s formed lquda zeotropk or azeotropc mxtures. Ternary systems such as sopropanol-water-benzene to form a pseudohomogeneous azeotropc mxtures have been studed by Pham and Doherty (1990). Ternary systems such as chloroform-benzene-acetone (Fdkowsk et al. 1993), acetone-heptane-benzene (Henley and Seader, 1998), acetone-water-metyl ethyl ketone (Vllers et al. 2002) and sopropanol-methyl cyclohexane-toluene (Egbewatt and Fletcher 2003) to form a homogeneous azeotropc mxtures. Other ternary systems that form the heterogeneous azeotropc mxtures such as ethanolwater-benzene (Henley and Seader, 1998), ethanolwater-toluene (Henley and Seader, 1998). Other ternary systems such as ntrogen-argon-oxygen mxture wthout formng azeotropc or zeotropk, octane-2- ethoxy ethanol to form ethyl benzene azeotropc bnary system, acetone-chloroform-methanol to form bnary and ternary azeotropc system (Wdagdo and Seder 1996). From the results of prevous research, no one has made a map of resdue curves for ternary mxtures ABE. From the resdue curve maps obtaned and valdated, the valdaton of the topologcal relatons. To valdate the topologcal relatons usng the equaton that already exst n the lterature (Henley and Seader, 1998). To determne whether the program lstng the ternary system smulaton s generally applcable, then valdated based on data from the lterature. Many ternary systems that already exst n the lterature or ournals that can be used for valdaton ABE ternary system, one of the ternary system used s a mxture that forms the ternary system zeotropk the MEP. 2. STRUCTURE OF WRITING At low pressure, the vapor phase so close to the deal gas low pressure lqud vapor equlbrum becomes: y. P γ... (1) x.p Equaton (1) s also known as the modfed Raoult's equaton. The constant of equlbrum between the vapor phase and lqud phase s defned as follows: y γ.p K... (2) x P Iteraton procedure to fnd the temperature of whch s to seek prce bubble uraton temperature of pure component T on P (Prausntz et al., 2001). T B C A - log P... (3) where A, B, C are Antone constants for speces, for all ntal estmates. T x T... (4) For = 1, 2, 3. Prce T as the ntal prce wll be used to determne the urated vapor pressure of a substance to be estmated wth the equaton T Antone.Sedangkan prces were sought by the equaton: B T C... (5) A - log P 1 Then look for the error between the new T wth T the begnnng wth Equaton (6) (T new T T new begnnng ) e γ actvty coeffcents obtaned from: ln = ln C ln C = φ ln x z q 2 ln... (6) R + ln... (7) θ φ m x... (8) φ x 1 ln R =q m m θ τ 1 ln θ τ... (9) m 1 1 θ τ k1 k k z (r q) (r 1)... (10) 2 where the coordnaton number z s set equal to 10. x r φ... (11) m x r 1 q x θ m... (12) 1 q x The parameters r, q s a constant component of the molecular structure based purely on molecular sze and external surface area. For each bnary combnaton n mult-component AII.4-2

3 Strengthenng Basc Scences and Technology for Industral Sustanablty mxtures, there are two parameters that can be adusted r, q: τ u u exp... (13) RT = = 1 Model-Dfferental-Algebrac Equatons (DAEs) for batch dstllaton of ternary system, assumng t does not form a two phase lquda by Doherty and Perkns (1978) as follows: - dx dξ... (14) ( x - y ) W o ξ ln... (15) W Wth a forward-fnte-dfference, Equaton (15) becomes: Tabel 3.3 Parameter UNIQUAC ABE system terner Komponen r q Aseton Butanol Ethanol Source: Prausntz, 2001 Dmana : Aseton (1), Butanol (2), Ethanol (3) u 11 = 0 ; u 12 = -198,659 ; u 13 = 98,75291 u 21 = 453,669 ; u 22 = 0 ; u 23 = -32,707 u 31 = 94,242 ; u 32 = 75,355 ; u 33 = 0 Valdaton of smulaton results wth the ternary system MEP Table 3.4. MEP feed composton x,+1 = x, + (y, x, )... (16) Where the composton of the early lquda on the bottom (x, ) and determned, whle the composton of the vapor (y, ) s calculated usng Equaton BUBL T (Prausntz, 2001). 3. METHODOLOGY To calculate the urated vapor pressure Antone equaton s used, data Antone parameters such as Table 3.2. (Prausntz, 2001), where the temperature (T) n unts of K and urated vapor pressure (PSAT) n unts of Bar. To calculate the actvty coeffcent (γ) usng the UNIQUAC equaton, where the prce of UNIQUAC bnary nteracton parameters (u), the volume of molecular data (r) and molecular surface area (q) Table 3.3, the assumpton z = 10. Sources: Henley and Seader, 1998 To calculate the urated vapor pressure Antone equaton used Table 3.5. Antone parameters MEP Parameter Antone Komponen A B C Metanol Ethanol Propanol Sources: Prausntz, 2001 Table 3.1. ABE feed composton Table 3.2. Antone parameters ABE Parameter Antone Komponen A B C Aseton Butanol Ethanol Source: Prausntz, 2001 Fgure 3.1. Batch dstllaton algorthm AII.4-3

4 Temperatur ( C) Koefsen Aktftas ARTICLES BALI INTERNATIONAL SEMINAR ON SCIENCE AND TECHNOLOGY 2011 Strengthenng Basc Scences and Technology for Industral Sustanablty Fgure 3.2. A set of batch dstllaton equpment Capton: 1. Pot Stll 8. Thermometer 2. Ol batch 9. glasses Measure 3. Heater 10. condenser 4. Thermocouple 11. thermocouple RTD 5. Controller 12. column separator 6. Contactor 13. packed column 7. regulators 7. Regulator 4. RESULTS AND DISCUSSIONS Temperature profle at the bottom shows the results of the approach wth temperatures n the dstllate, because the smple batch dstllaton processes operate n condtons of total reflux. Therefore the temperature profle as Fgure 4.1 smulaton results s the sum of the -component temperature after normalzaton multpled n the bottom component of the composton of lquda-. From Fgure 4.1 shows the temperature profle for Run ABE-1 to Run-6 as a whole rose aganst the dmensonless tme. Ths s because the components are evaporated wth a larger porton s a component of ethanol, so t takes a larger temperature to evaporate the water component that has not evaporated. composton on the nfluence of ethanol actvty coeffcent maxmum at dmensonless tme showed 1.75, after whch profles a constant declne n the end. The bgger the bat nto the water composton showed a steeper slope of declne n temperature, because the composton of the bat nto the water greatly affects the temperature of the mxture of ethanol-water-hcl, the greater the ncomng feed water composton at the hgher temperature of the mxture. For regon 2 the temperature profle rses for all the runs, the greater the ethanol composton n feed entry shows the temperature rse slope s more gentle. Ths s because the composton of the feed nto ethanol greatly affects the temperature of the mxture of ethanol-water-hcl, the greater the ethanol composton n feed mxture nto a temperature become smaller. For regon 3 the temperature profle rses and some constant, for the temperature profle rses mean the separaton of a mxture of ethanol-water-hcl stll exst that have not teruapkan ethanol, whle for constant composton profle ndcates that t s all teruapkan ethanol. The greater the composton of ncomng feed water at the temperature of the mxture the greater and faster the temperature profle constant. For the dmensonless tme of 3.5 the temperature profle has not been constant, so the dmensonless tme requred to obtan a larger constant temperature profle. If a smple batch dstllaton contnued untl the dmensonless tme s very large, then the value wll be the composton of each mxture s negatve, ths s not desred Dmensonless Waktu Dmensonless Waktu Fgure 4.1 Profle of the temperature of the ternary system of ABE for Run-1 to Run-7 Fgure 4.2 Profle of the actvty coeffcent of the ternary system of ABE From Fgure 4.3 shows the composton profle n the bottom lquda, the composton of ethanol shows the composton profle decreases from the ntal composton and the composton of the water showed up from the ntal composton profle. From Fgure 4.2 s dvded nto 3 regons, for regons 1 shows the profle of water actvty coeffcent decreases and the actvty coeffcent of ethanol rses, so does not affect the temperature profle. Fgure 4.2 shows that the larger the ncomng feed water AII.4-4

5 Temperatur ( C) Komposs Lquda d Bottom (fraks mol) Komposs Uap d Bottom (fraks mol) ARTICLES BALI INTERNATIONAL SEMINAR ON SCIENCE AND TECHNOLOGY 2011 Strengthenng Basc Scences and Technology for Industral Sustanablty Dmensonless waktu Fgure 4.3. Lquda composton profles n ternary systems ABE Bottom Run-1 Because ethanol s a component of volatle components whle the water component s non-volatle components, as a smple batch dstllaton process of ethanol component n a larger porton s evaporated and the remanng components of the water. Component of pure water has not been approached wth a dmensonless tme of 3.5; one way to get more pure water component of the ntal composton s to enlarge the composton of the feed water to enter. Fgure 4.4. shows the vapor composton profles at total reflux for a bottom after the composton of ethanol contnues to declne, whle the composton of the water contnues to rse. Ths dsebakan because volatle components were evaporated n a larger porton and the rest are non-volatle components, after a smple batch dstllaton process takes place then the non-volatle components are evaporated n a larger porton. Components of ethanol has not evaporate all at dmensonless tme 3.5; one way to obtan the components of ethanol n the dstllate wth a smaller dmensonless tme s to enlarge the composton of the feed water to enter. Vapor composton profles at the bottom of small composton of ethanol on the feed entry, the greater the total composton of ethanol at reflux, ths s due to a hgh temperature so that the mxture of non-volatle components evaporate more. Vapor composton profles at total reflux for a bottom after the composton of ethanol contnues to declne, whle the composton of the water contnues to rse. Ths dsebakan because volatle components were evaporated n a larger porton and the rest are nonvolatle components, after a batch dstllaton process takes place then the non-volatle components are evaporated n a larger porton. Components of ethanol all teruapkan at dmensonless tme shows the value of 2.25; Run-7 requres a smaller dmensonless tme to obtan a more pure ethanol component of ethanol component of the ntal 1,0 0,9 0,8 0,7 0,6 0,5 0,4 0,3 0,2 0,1 0,0 0,0 0,5 1,0 1,5 2,0 2,5 3,0 3,5 Dmensonless Waktu Fgure 4.4. Vapor composton profles n ternary systems ABE Bottom Run-1 Temperature profle at the bottom shows the results of the approach wth temperatures n the dstllate, because the smple batch dstllaton processes operate n condtons of total reflux. Therefore the temperature profle as Fgure 4.5 smulaton results s the sum of the -component temperature after normalzaton multpled n the bottom component of the composton of the lquda-. From Fgure 4.5 shows the temperature profle for Run MEP-1 to Run-6 as a whole rose aganst the dmensonless tme. Ths s because the components are evaporated wth a larger porton s a component of ethanol, so t takes a larger temperature to evaporate the water component that has not evaporated Dmensonless waktu Fgure 4.5 Profle of the temperature of the ternary system of MEP for Run-1 to Run-6 From Fgure 4.6 s dvded nto 3 regons, for regons 1 shows the profle of water actvty coeffcent decreases and the actvty coeffcent of ethanol rses, so does not affect the temperature profle. Fgure 4.6 shows that the larger the ncomng feed water composton on the nfluence of ethanol actvty coeffcent maxmum at dmensonless tme showed 1.75, after whch profles a constant declne n the end. The bgger the bat nto the water composton showed a steeper slope of declne n temperature, because the composton of ncomng feed water at the temperature of the mxture greatly affects the MEP, the greater the ncomng feed water composton at the hgher temperature of the mxture. For regon 2 the temperature profle rses for all the runs, the greater the ethanol composton n feed AII.4-5

6 Komposs lquda d bottom (fraks mol) Komposs lquda d bottom (fraks mol) Koefsen Aktftas ARTICLES BALI INTERNATIONAL SEMINAR ON SCIENCE AND TECHNOLOGY 2011 Strengthenng Basc Scences and Technology for Industral Sustanablty entry shows the temperature rse slope s more gentle. Ths s because the composton of the feed nto ethanol greatly affects the temperature of the mxture of ethanol-water-hcl, the greater the ethanol composton n feed mxture nto a temperature become smaller. For regon 3 the temperature profle rses and some constant, for the temperature profle rses mean the separaton of a mxture of ethanol MEP stll exst that have not teruapkan, whle for constant composton profle ndcates that t s all teruapkan ethanol. The greater the composton of ncomng feed water at the temperature of the mxture the greater and faster the temperature profle constant. For the dmensonless tme of 3.5 the temperature profle has not been constant, so the dmensonless tme requred to obtan a larger constant temperature profle. If a smple batch dstllaton contnued untl the dmensonless tme s very large, then the value wll be the composton of each mxture s negatve, ths s not desred Dmensonless Waktu Fgure 4.6. Ternary system actvty coeffcent profle MEP From Fgure 4.7 shows the composton profle n the bottom lquda, the composton of ethanol shows the composton profle decreases from the ntal composton and the composton of the water showed up from the ntal composton profle. Because ethanol s a component of volatle components whle the water component s non-volatle components, as a smple batch dstllaton process of ethanol component n a larger porton s evaporated and the remanng components of the water. Component of pure water has not been approached wth a dmensonless tme of 3.5; one way to get more pure water component of the ntal composton s to enlarge the composton of the feed water to enter Dmensonless Waktu Fgure 4.7. Composton profles n the bottom lquda MEP ternary system Run-1 Fgure 4.8. shows the vapor composton profles at total reflux for a bottom after the composton of ethanol contnues to declne, whle the composton of the water contnues to rse. Ths dsebakan because volatle components were evaporated n a larger porton and the rest are non-volatle components, after a smple batch dstllaton process takes place then the non-volatle components are evaporated n a larger porton. Ethanol components have not evaporate all at dmensonless tme 3.5; one way to obtan the components of ethanol n the dstllate wth a smaller dmensonless tme s to enlarge the composton of the feed water to enter. Vapor composton profles at the bottom of small composton of ethanol on the feed entry, the greater the total composton of ethanol at reflux, ths s due to a hgh temperature so that the mxture of non-volatle components evaporate more. Vapor composton profles at total reflux for a bottom after the composton of ethanol contnues to declne, whle the composton of the water contnues to rse. Ths dsebakan because volatle components were evaporated n a larger porton and the rest are nonvolatle components, after a batch dstllaton process takes place then the non-volatle components are evaporated n a larger porton. Components of ethanol all teruapkan at dmensonless tme shows the value of 2.25; Run-7 requres a smaller dmensonless tme to obtan a more pure ethanol component of ethanol component of the ntal Dmensonless Waktu Fgure 4.8. Vapor composton profles n ternary systems bottom MEP Run-1 bl... AII.4-6

7 Strengthenng Basc Scences and Technology for Industral Sustanablty Fgure 4.9 Profle of the temperature of the ternary system of ABE for Run-1, Run-7 smulaton results and expermental Fgure Lquda composton profles n ternary systems bottom ABE-1 Run the smulaton and expermental results 5. CONCLUSION 1. Ethanol-Water temperature profle-hcl as a whole rose aganst the dmensonless tme, except at the begnnng of the process shows the temperature profle decreases, due to the nature of the characterstcs of the mxture. 2. Lquda composton profles of ethanol n the bottom seteleh process shows the composton of a mnmum of ethanol, after the process s complete profle constant composton 3. Ethanol vapor composton profles n the bottom seteleh process showed a maxmum ethanol composton, once the process s complete profle constant composton. 4. Resdue curve map at bottom shows azeotropc mxture, between the smulaton and valdaton results showed that close to the same profle Acknowledgments To the Drectorate General of Hgher Peddkan Mnstry of Natonal Educaton (Drectorate General of Hgher DP2M) Compettve Grant n 2009, whch has funded ths research. 6. REFERENCES [1] Fesser and Fsser, (1963), "Introducton to Chemstry Organc ", Dhwantara, Bandung. [2] Judoamdoo, Mulyono, (1992), "Fermentaton Technology", Raawal Press Jakarta [3] Krk Othmer, "Encyclopedya of Chemcal Technology", Vol. 8, John Wleys nd Sons. Inc. [4] Sardoko, (1991), "Botechnology", Grameda, Jakarta. [5] N. Sar K., Kuswand, Nonot S., Renanto Handogo, (2006), "Comparson of resdue curve maps the ternary system ABE Wth Methanol- Ethanol-1-Propanol", Journal REACTORS, Department of Chemcal Engneerng Dponegoro Semarang, Vol. 13, No. 2. [6] Sar N. K., Kuswand, Nonot S., Renanto Handogo, (2007), "Separaton of Ethanol-Water Bnary Systems and ternary systems ABE Wth Smple Batch Dstllaton", Journal INDUSTRIAL Journal of Scence and Technology, Faculty of Industral Engneerng ITS Surabaya, Vol. 6, 5. [7] Handogo, R., and G. Authorty, (1997), "Experments and Correlatons of Vapor-Lqud equlbra of Acetone-1-Butanol-Ethanol Ternary Mxture", Internatonal Conference on Flud and Thermal Energy Converson, Yogyakarta, Indonesa, p [8] Henley, E. J. and J. D. Seader (1998), "Separaton Process Prncples", p , John Wley & Sons, Inc.., New York. [9] Prausntz, J. M., (2001), "The Propertes of Gases and lquds", ed. 5, p.. A.50 - A. 51, Mc. Graw- Hll, New York. [9] Raylegh, L., (1902), Phl. Mag. [V.], No. 4 (23), p [10] Wdagdo, S. and Warren D. Seder, (1996), "Journal Revew Azeotropc Dstllaton", AIChE J., Vol. 42, No.1, p AII.4-7